Thermophysical Properties of Normal Butane

from 135 to 700 K at Pressures to 70 MPa

William M. Haynes and Robert D. Goodwin

Thermophysical Properties Division

National Engineering Laboratory

National Bureau of Standards

Boulder, CO 80303

U.S. DEPARTMENT OF COMMERCE, Malcolm Baldrige, Secretary

NATIONAL BUREAU OF STANDARDS, Ernest Ambler, Director

Issued April 1982
Library of Congress Catalog Card Number: 82-600512

National Bureau of Standards Monograph 169

Nat. Bur. Slanii. (U.S.), Mongr. \W. 197 pages (Apr. 1982) CODEN: NBSMA6

U.S. GOVERNMENT PRINTING OFFICE

WASHINGTON: 1982
Contents

Page

1. Introduction 1 2. Physical Properties and Their Formulation 2

2.1 Fixed-Point Values 2

2.2 Melting Line and Vapor Pressures 3

2.3 The Orthobaric Densities 4

2.4 The Virial Equation 5 2.5 The Equation of State 6

2.6 The Ideal Gas Functions 8

2.7 Thermal Loop Computations 8

2.8 The Heats of Vaporization 9

2.9 Saturated Liquid Enthalpies and Entropies 9

2.10 Dielectric Constants 10

3. Computational Methods 11

3.1 The Homogeneous Domain 11 3.2 The Saturated Liquid 12

3.3 The Compressed Liquid 13

3.4 Fugacity Coefficients 13

3.5 Simplified Computation 13

4. Tests and Conclusions 13

5. Tables of Physical and Thermodynamic Properties 14

5.1 Calculated P-p-T Isochores and Isotherms 14

5.2 The Joule-Thomson Inversion Locus 14

5.3 Thermophysical Properties of the Saturated Liquid ..... 15

5.4 Thermophysical Properties Along Selected Isobars 15

6. Acknowledgments 15

7. References 16

APPENDIX A. Symbols and Units 23

APPENDIX B. Conversion of Units 25

APPENDIX C. Fixed-Point Values for Normal Butane 26

APPENDIX D. Normal Butane Properties Reference Index 27

APPENDIX E. Computer Program 30

i i i
List of Figures

Page

Figure 1. Density-temperature diagram of normal butane 49

Figure 2. P-T locus of P-p-T data for normal butane 50

List of Tables

Table 1. Comparisons of vapor pressure data with eq (2) 51

Table 2. Comparisons of saturated liquid density data with eq (3) . . 54

Table 3. Comparisons of saturated vapor density data with eq (4) . . 57

Table 4. Comparisons of second virial coefficients with eq (5). . . . 59

Table 5. Behavior of coefficients of equation of state for

normal butane (eq (6)) 62

Table 6. Calculated P(p) critical isotherm of normal butane 63

Table 7. Comparisons of experimental P-p-T data of normal butane

with eq (6) 64

Table 8. Comparisons of data for ideal gas functions with eq (7). . . 85

Table 9. Interpolated ideal gas functions from eq (7) 86

Table 10. Comparisons of heat of vaporization data with eq (9) , . . . 87

Table 11. Enthalpies of saturated liquid normal butane from eq (10) . 89

Table 12. Entropies and specific heats of saturated liquid normal

butane from eq ( 1 1

) 90

Table 13. Comparisons of dielectric constant data with eq (12) .... 91

Table 14. Comparisons with saturated liquid specific heats 95

Table 15. Comparisons with C and C data 96

v p

Table 16. Comparisons with velocity of sound data 97

Table 17. Calculated P(T) isochores of normal butane 98

Table 18. Calculated P(p) isotherms of normal butane 113

Table 19. The Joule-Thomson inversion locus for normal butane .... 133

Table 20. Thermophysical properties of saturated liquid normal

butane 134

Table 21, Thermophysical properties of normal butane along isobars . . 136

i V
THERMOPHYSICAL PROPERTIES OF NORMAL BUTANE FROM 135 TO 700 K AT

PRESSURES TO 70 MPa

William M. Haynes and Robert D. Goodwin

Thermophysical Properties Division

National Engineering Laboratory

National Bureau of Standards

Boulder, Colorado 80303

Using a modified version of the nonanalytic equation of state,

thermophysical properties of normal butane are derived from physical

properties data and are tabulated at integral temperatures from 135 to

700 K along isobars at pressures to 70 MPa. These isobar tables, along

with a table for the saturated liquid, give values for densities,

compressibility factors, internal energies, enthalpies, entropies, heat

capacities, fugacities, sound velocities, dielectric constants, and

isochore and isotherm derivatives. Equations, whose coefficients are determined from a least squares fit to selected experimental data, are also presented for vapor pressures, orthobaric liquid and vapor

densities, ideal gas properties, second virial coefficients, dielectric

constants, heats of vaporization, melting pressures, and orthobaric

liquid specific heats, enthalpies, and entropies. Comparisons between

experimental and calculated values for all properties considered here are reported in detail.

Key words: Densities; dielectric constants; enthalpies; entropies;

equation of state; fugacities; internal energies; isobars; isochores;

isotherms; Joule-Thomson inversion; latent heats of vaporization; melting

line; normal butane; orthobaric densities; specific heats; vapor

pressures; velocities of sound.

1 . Introduction

The present work is a revision and extension of a previous provisional

report [28] from this laboratory. Since that report new compressibility

data [35] for normal butane at low temperatures have become available and are incorporated in the work reported here. These new data cover a range from 140 to

300 K at pressures to 35 MPa. As a result of new dielectric constant measurements [35,38] on normal butane, the present work also includes a correlation of

dielectric constant data. The nonanalytic equation of state used here, which is

modified from earlier versions [26-29], is also currently being employed in

correlations for propane [30] and isobutane [31].

1
other correlations on normal butane have been reported by Hanson [34],

Prengle, et al . [57], Canjar, et al. [9], Das and Kuloor [?C], and Das,

et al . [21]. Many new properties data, especially at low temperatures, have

appeared since these correlations were developed.

SI units are used throughout this report in tables and equations. Pressures

3 are given in MPa, densities in kg/m , and temperatures in K. For thermal

properties, the mol is used for amounts of substance. However, all computations

in computer programs (Appendix E) for the present work have been conducted in

units of bar for pressure and mol/L for density.

Symbols and units used in this report and in computations appear in

Appendix A; conversion factors for units are given in Appendix B. Fixed-point

values of normal butane used in this work are reported in Appendix C. A

collection of references for the major physical properties of normal butane,

along with ranges of data, is presented in Appendix D. Appendix E consists of

computer programs used for the calculation of thermophysical properties of normal

butane. In figure 1 is presented the density-temperature diagram for normal

butane.

2. Physical Properties and Their Formulation

In this section, first the fixed-point values selected in present work are presented and their origins are briefly discussed. As the present equation of

state originates on a given liquid-vapor coexistence boundary, the P(T) melting

line, the vapor pressures, and the orthobaric densities are next formulated.

Then the truncated virial equation of state is given because it is used to derive

some needed data. The equation of state description is followed by formulation

of some thermal properties needed for the final computations of a thermodynamic

network. All symbols used in the equations are defined in Appendix A.

2.1 Fixed-Point Values

These values are listed in Appendix C.

(a) The Triple Point. The temperature (T^ = 134.86 K) is adopted from

Das, et al . [21], while the pressure is determined from the vapor pressure

equation (eq (2)). The liquid density is based on consistency with data in

eq (3). Equation (4) for saturated vapor densities is used for calculating the

vapor density.

2
(b) The Boiling Point. The temperature {J^ = 272.638 K) is froin vapor

pressure eq (2) at a pressure of 1 atm = 0.101325 MPa. Liquid and vapor

densities are from eqs (3) and (4).

(c) The Critical Point. The temperature (T^ = 425.16 K) is adopted from

Das, et al. [21] and is in agreement within acceptable limits with the values of

Beattie, et al . [2] and Kay [44]. The density and pressure (p^ = 227.85 kg/n?

(3.92 mol/L) and P^ = 3.7960 MPa) are adopted on the basis of fitting orthobaric

densities, vapor pressures, and P-p-T data and then examining the behavior of the

calculated critical isotherm. The selected values for density and pressure are substantiated by those obtained experimentally from the data of Kay [44],

Beattie, et al . [2] and by those selected in the correlation of Das,

et al. [21].

2.2 Melting Line and Vapor Pressures

(a) The Melting Line. Experimental pressures from about two to ten

kilobars were reported by Reeves, et al . [59] as constants for the Simon eq (1).

In present work using the triple point temperature and pressure from Appendix C,

the relation,

% = Pt ^ Po [(T/T^)^ - 1] . (1)

is obtained, where P^ = 6.7358 x lO"'' MPa, T^ = 134.86 K, P^ = 363.4 MPa, and

c = 2.21.

(b) The Vapor Pressures. Data used for adjusting eq (2) appear in the

first part of table 1. Other data, weighted zero, appear in the continuation of

the table. Values at ID = 40 have been derived via thermal loops, as described

by Goodwin [27], by use of the saturated liquid specific heat data of Aston,

et al . [1] from the triple- to the normal boiling-point; the heat of

vaporization of Aston, et al . [1] at the normal boiling point; the ideal gas

thermofunctions formulated in section 2.6; the virial equation formulated in

section 2.4; and, for the minor contribution of V*dP to AH on the saturated

liquid path, the preliminary vapor pressure and saturated liquid densities

equations were also used. This procedure also has been described by Yarbrough

and Tsai [75].

The argument for eq (2) is T^ e T/T^; then, vapor pressures (P^) in MPa are given by the relation.

3
£n(P^-10) = a/T^ + b + c-T^ + d-T^ + e-T^ + f-(l - T^)^ , (2)

where e = 1.85 and, from least squares analysis,

a = - 9.5092 4729 d = 4.8614 7936

b = 5.2015 3488 e = - 7.5581 8629

c = 10.6409 5231 f = 18.7288 6023

Exponent e was selected for a best fit of P-p-T data under the constraint that,

at the critical point, the slope of the vapor-pressure equation be equal to the

slope of the critical isochore from the equation of state, dP^/dT = (3P/3T)p . The fit of present vapor pressure data is relatively insensitive to values o? e in the range, 1.1 <. e <. 1.95, but the critical point slope is dependent on the

value of £. The value of e = 1.85 is consistent with scaling law equations* The

present slope at the critical point is dP^/dT = 0.064272 MPa/K»

2.3 The Orthobaric Densities

(a) Saturated Liquid Densities. Data in table 2 have been selected for

consistency. Data weighted zero, which appear in the continuation of the table,

are shown for comparison. If the variable for eq (3) is defined by

x(T) E (T^ - T)/(T^ - T^) ,

then the orthobaric liquid densities, p^, are described by

(p^ - P^)/(p^ - P^) = X + (x^ - x) -[a + b-x + c-x^] , (3)

where e = 0.35, and, from least squares analysis,

a = 0.7943 88335 c = -0.0858 29197

b = -0.0010 89476

(b) Saturated Vapor Densities. The following new type of formulation for

saturated vapor densities has been developed for consistency with the equation of

state (eq (5)) to yield a compressibility factor approaching unity in the limit

of low densities, as described earlier [26,29]. Data in table 3 used in the fit

have been selected for internal consistency. Values at ID = 40 are derived from

the vapor-pressure and virial equations. Other data, weighted zero, appear in

the continuation of table 3. The compressibility factor for saturated vapor is

formulated by use of the vapor-pressure equation, such that Z (T) approaches

4
unity as Pq-*0, (hence T^(p) -» 0). Let = (Z^ - 1), where is value of

the compressibility factor at the critical point, and define the arguments

n(T) = P^(T)/P^ , E T/T^ , u(T) e (1 - T^) .

The saturated vapor densities, e P^/(Z^«R*T), then are given by

Z = 1 + A^-n-T^^-fd) , (4)

where

f(T) E 1 + a'u^ + b'u + c*exp[n*(l - 1/u)] ,

e = 0.35, n

= 2.3, and, from least squares analysis, . *

a = -0.8665 77289 c = 4.4986 58942

b = 1 .1203 97967

The next-to-last column in table 3 gives the experimental residuals,

F(Z) E (Z^^p - 1)-t2/[A„.„] ,

used to develop a functional form for f(T).

2.4 The Virial Equation

For the truncated virial equation,

Pv/RT = 1 + B^(T).p^ + . . . , (5a)

the second virial coefficient, B^(T), is dimensionl ess through the use of the

reduced variables, e p/p^ and T^ e T/T^. The following relation,

B^(T) = + B2/T^ + B3/T^ . (5b)

is used to fit the second virial data given in the first part of table 4.

Excluded data, weighted zero, appear at the end of table 4. From least squares

analysis, the following coefficients,

B-| = 0.3703 0532 B^ = -0.6660 5953

B^ = -0.9668 8512

have been determined. The second virial s have been used to synthesize P-p-T

data, to calculate saturated vapor densities via the vapor pressure equation, and

to make thermal loop computations.

5
2.5 The Equation of State

Figure 2 shows the P-T regions covered by P-p-T data of Beattie, et al . [2],

Kay [44], Olds, et al . [51], and Haynes [35]. The data of Sage, et al . [64] are excluded from this figure and are not used in the fit, since they are superseded

by data of Olds, et al . [51]. These P-p-T data for normal butane are also

summarized in Appendix D and table 7. Data from the virial equation along a low

density isochore are included in the fit. Equal weightings of unity have been

given to the data sets [2,35,44,51] used in fit.

The nonanalytic equation of state used here originates on the liquid vapor

coexistence boundary, as described in detail by Goodwin [26,29]. Twelve least

squares coefficients appear in the vapor pressure and orthobaric density

equations. In the equation of state there are four nonlinear parameters and only

three least squares coefficients, as described below. The equation has been

modified from earlier forms [26-29]. For any density (isochore) the coexistence

temperature, T^(p)» is obtained by iteration from eqs (3) and (4) for the

orthobaric densities. The vapor pressure, P^[T^(p)], thus is a function of

density, and the equation of state has the form,

P - P^(p) = p^-R*-[T - T^(p)] + p^R*T^-F(p.T) , (6)

where

• F(p,T) E B(p).$(p,T) + C(p)-f(p,T) . (6a)

The density, p^ = p/p^» is reduced at the critical point, while the constant

R* is defined by R* e (0.0083145) 'p^, MPa/K.

The temperature-dependent functions in (6a) are defined as follows.

$(p,T) = T^.exp[b-(1 - T^/T)] - (T^)^ , (6b) ...

where b e (1 - 3) + (1 - 8)^^^ T^ e T/T^, and (T^) e T^(p)/T^.

y(p.T) = ^(P.T)/I'^(p) - 1 , (6c)

where i|'^(p) is obtained from i|j(p,T) merely by replacing T with T^(p)5 and

^(P.T) = 1 - (03 - a3'^/n)/(l - 1/n) . (6d)

6
The value for 3 was found by trial, while the value for n was determined from

critical region behavior.

a)(p.T) = [1 - 0(p)/T] , (6e)

where g(p) is a locus of temperatures inside the coexistence envelope defined by

e(p) = T^(p) •exp[-a.f(p)] , and (6f)

Hp) = |P^ - ll^/((pJ - 1)^ . ^ r

(Px) = ^t^^c

reduced density at the liquid triple point. The parameter

r a is found by trial

.

The density-dependent coefficients in (6a) are

B(p) E + B2-P^ (6g)

and

C(p) = C^-(p^ - l).(p^ - CQ)-exp[-Y.p^] , (6h)

where Cq and y ai^e to be found by trial.

Parameters and coefficients of eq (6) for normal butane are

a = 1 , 3 = 0.70, Y = 0.14, n = 1 .1

,

B^ = 0.4565 5869 162 = 2.2

B^ = 0.1714 3942 370 = -0.2803 6114 629

Table 5 gives behavior of coefficients B(p), C(p) as a function of density

and table 6 gives behavior along the critical isotherm. (In table 6, the symbol,

Pp f» is defined as the density reduced by the triple point density.) These

r , u tables show that the equation is smooth and well-behaved. Table 7 summarizes

experimental compressibility data and presents deviations of experimental

densities and pressures from values calculated from the equation of state.

Although the data of Sage, et al . [64] are not used in the fit, comparisons with

these data are presented in table 7. These data show systematic differences of

approximately 1 percent when compared in regions of overlap with the results of

Kay [44], Olds, et al . [51], and Haynes [35].

For normal butane, there are four comprehensive sets of liquid and gaseous

compressibility data covering a temperature range from 140 to 600 K at pressures

7
as high as 70 MPa that are internally consistent within a few tenths percent in

regions of overlap. Using these data sets, the present equation yields a slightly better fit than that obtained from a slightly different equation used in

the provisional work [28] for which the low temperature data were not available.

In the earlier work, the single phase results at temperatures less than room temperature were obtained by extrapolation. Thus, a significant improvement has

been made in the P-p-T behavior of normal butane at low temperatures.

It should be noted that the functional form of the equation of state used

here for normal butane has also been used in current work for propane [30] and

isobutane [31]. Identical nonlinear parameters except for insignificant

differences in y. have been obtained for all three fluids in fitting this

equation to available P-p-T data.

2.6 The Ideal Gas Functions

A formulation of the spectroscopic specific heats, C^(T), of Chen,

et al . [12] has been developed. Using x^ = T/lOO,

5 , . C°/R - 4 = exp(-£/x^). £ A. .x^-"" , (7)

where R = 8.31434 J/(mol»K) and

e = 2.37 A3 = 257.279067

A^ = 41.110973 A^ = -170.730596

A2 = -139.304011 Ag = 40.032171

Table 8 shows the fit of data used. In this table, the values for (H°-H°)

0

' ' 0'

and for S are obtained by numerical integration, starting at T = 300 K.

Table 9 gives interpolated values at integral temperatures.

2.7 Thermal Loop Computations

At temperatures from the triple- to the normal boiling-point, new data have

been derived for vapor pressures, saturated vapor densities, and for heats of

vaporization by thermal loop computations for AH and for AS of saturated vapor

and saturated liquid. This procedure described by Goodwin [29], and more generally by Yarbrough and Tsai [75] uses virial eq (5a), ideal gas functions

eq (7), the heat of vaporization of Aston, et al . [1] at the normal boiling

point, and the following new formulation of the specific heats of Aston,

8
et al . [1] for the saturated liquid from the triple- to the normal boiling-point.

Define k^{T) = T/lOO; t^ J/(mol«K), are given byDefine Xq(T) - T/lOO; then the saturated liquid specific heats, C^(T) , in

C (T) = a/x + b + c-x + d»x ^

. (8) ' 0 0 0' ^

'

where, from least squares analysis, the coefficients, in units of J/(mol«K), are

as follov/s:

a = -104.7430 c = -97.2492

b = 284.0264 d = 20.6032

Results for the vapor pressures appear in table 1 at ID = 80, and for the

heats of vaporization in table 10 at ID = 80. Saturated vapor densities from the

thermal loop computations are replaced in table 3 at ID = 40 by derived data from

the fitted vapor-pressure eq (2) and the virial eq (5a).

2.8 The Heats of Vaporization

Table 10 shows the fit of selected data. Those at ID = 80 are derived via

thermal loops (section 2.7). Those at ID = 41 are from the Clapeyron equation.

The formulation of these heat of vaporization (Q^gp) "^ata in kJ/mol uses argument

x(T) = (T^ - T)/(T^ - T^);

= A^-x + (x"^ - x)-[A2 + A3-X + A^-x^] , (9)

where

e = 0.34 A3 = 12.710873

A^ = 28.789248 A^ = -16.533537

A2 = 24.163103

The coefficients have units of kJ/mol . The uncertainty of at least one percent

in Qy^p at the higher temperatures will affect compressed liquid thermofunctions

in this region, since Q^^p is used to compute across the "dome."

2.9 Saturated Liquid Enthalpies and Entropies

Data for saturated liquid enthalpies and entropies have been derived at

temperatures from the triple- to the critical-point by use of the ideal gas

functions, the equation of state, and the formulated heats of vaporization. The

enthalpies then have been formulated, as shown in table 11. Define the

variabl e.

9
X = (T^ - T)/(T^ - T^) ;

then the enthalpies, H(j(T), are described in J/mol by

(H^ - H^)/(H^ H^) = X + (x^- - x)

i = l A.*x

1

i-1

(10)

where e = 0.29, = 0.001 J/mol, = 45399.788 J/mol, and

0.1929 77338

0.3998 98449

-0.0549 93612

-1.0205 68625

kr = 2.8727 89244

Ag = -4.0526 10155

A^ = 2.6963 77850

A„ = -0.6834 38899

The formulation of saturated liquid entropies in J/(mol*l<) is shown in table 12,

Lei

by

Let X E (T^ - T)/(T^ - T^) ; then the entropies, S^(T), are given in J/(mol»l<)

(^a

- V/(^t - = x + (x^ - X)

i = l A.'x

i-1

(11)

where e

A,

0.23, = 133.54372 J/(mol»K)

= 0.08883 44435

= -0.34703 04947

= 0.20937 24392

= 297.64652 J/(mol«K), and

A4 = -0.95683 28496

A. = 0.95799 92545

5 A. = -0.65346 07056

Specific heats along the saturated liquid path follow from the relation,

C^(T) = T*dS^/dT, and are given in the last column of table 12. All of the

above saturated liquid formulations for H^(T), S^(T), and C^(T) are used to

compute thermodynamic properties for compressed liquid states at T < T^.

2.10 Dielectric Constants

Dielectric constants, e, for the saturated vapor of normal butane are estimated from the refractive indices, n, of Sliwinski [67] via e = n'. (These

low density data are in a region for which dispersion effects should be minimal.)

Haynes [35,38] recently has measured e for the saturated liquid at temperatures

from 135-300 K and for the compressed liquid at presures to 35 MPa along

isotherms up to 300 K. These data and their formulation via the

Clausius-Mossotti function.

10
CMF E [(£ - l)/(e + 2)]/p , (12a)

are presented in table 13. The following formulation has been used to fit the

data in table 13 and to calculate e along isobars (table 21) at temperatures

extrapolated up to 450 K, and at pressures up to 70 MPa. Define the variables,

T E T/T and p = p/p.; then, with P in units of MPa, the CI ausi us-Mossotti

3 function, in units of cm /mol , is given by

CMF = + A2-p^ + A3-p^ + A^/T^ + A^-P/IO (12b)

where

A^ = 20.654382 A^ = -0.0392 1649

A, = 0.2512 9317 A. = -0.0116 4552

2 5 A3 = -0.0972 3048

3 The least squares coefficients have units of cm /mol. Data at high pressures

have a diminished v/eighting as seen in table 13. The rms relative deviation for

152 points is 0.083 percent for the CMF and 0.017 percent for the dielectric

constant.

Comparisons with dielectric constant data for liquid normal butane not used

in the fit to eq (12) are not presented in table 13. The dielectric constants

of Thompson and Miller [70] and Luo and Miller [47] at temperatures between 220

and 289 K agree within 0.1 percent with values calculated from eq (12).

3. Computational Methods

The numerical values For E and H in this report are based on the assigned

value, E = 0 at the liquid triple-point, obtained by use of the arbitrary value,

E° = 22644.306 J/mol . Specific heats of Aston, et al . [1] could be integrated

to give the solid at T = 0 as reference state.

3.1 The Homogeneous Domain

The homogeneous domain of figure 1 includes all regions which can be

attained along isotherms starting at zero density without crossing the

vapor-liquid "dome," and without passing very close to the critical point at

T > TcComputations start with ideal gas thermodynamic functions at zero density,

and then continue by integrating numerically along isotherms by use of the

equation of state in the following relations.

11
AE = / [P - T-(9P/aT)]-dp/p^ , (13)

AC^ = - T . / (9^P/9T^).dp/p^ , (14)

AS = R'iln[P°/(pRT)] +

J*

[R - 0P/8T)/p] -dp/p . (15)

Equation (15) is for use with initial entropies in hypothetical ideal gas states

at P° = 1 atm (0.101325 MPa). For all other initial states,

AS = - / (9P/3T)'dp/p^ . (15a)

In each (p,T) state, reached by above integrations, the following are computed,

H = E + P»v , (16)

Cp = + T.(9P/9T)2/(9P/9p)/p^ , (17)

and

= Cp.(9P/9p)/Cy . (18)

3,2 The Saturated Liquid

At temperatures from the triple-point to the critical-point, thermofunctions

for the saturated vapor are obtained via eqs (13) through (16). Then eq (9) for

the heat of vaporization, Qygp» is used to compute

AH = - Q , AS = AH/T , (19)

such that the free energy of vaporization, AG = AH - T»AS, is zero (see

section 2.9). Having obtained H and S for the saturated liquid, E = H - P»v is

computed.

The single-phase specific heat, Cy(p,T), at the saturated liquid boundary,

is obtained from eq (11) using C^(T) = T«dS^/dT and the thermodynamic relation,

Cy(p,T) = C^(T) + T.(9P/9T).(dp^/dT)/p^ , (20)

where p, is density of the saturated liquid. Values for C (p,T) and W(p,T) on

X/ P this boundary follow from eqs (17) and (18). For liquid at the normal boiling

point, the following values have been obtained.

12
= 272.638 K, = 16770.1 J/mol ,

E,^ = 16760.3 J/mol , = 218.485 J/(mol -K)

.

3.3 The Compressed Liquid

Starting vvith above values for E, S, and on the saturated liquid

boundary, eqs (13), (14), and (15a) are used to integrate along isotherms, and

then H, C^, and W are obtained via eqs (16), (17), and (18).

3.4 Fugacity Coefficients

The fugacity coefficients in table 21 were computed along isotherms relative

to properties in hypothetical ideal gas states at a pressure, P° = 1 atm

(0.101325 MPa)

,

(f/P) = (P°/P)-exp [AG/RT] . (21)

For any (P,T) point, the isothermal free energy change is

AG = (H - E°) - - T.(S - S°) , (22)

in which the arbitrary value of E° was added to tabulated values of H(P,T)

such that E(P,T) = 0 for liquid at the triple point.

3.5 Simplified Computation

Given the subroutines of Appendix E, it is necessary first to call

SUBROUTINE PVTDATA, to place constants in common statements. To obtain the

density in mol/L at a given T,K and P,bar, it is necessary merely to write the

instruction DEM = FINDENF(T,P) for single-phase domains. Coexisting densities

are given by the functions DENGASF(T) and/or DENLIQF(T), and the vapor pressure

in bar by PSATF(T)

.

For thermodynamic properties, the subroutine SIMPLE here is an example of

how to use the general subroutine THERMO (see Appendix E).

4. Tests and Conclusions

In the provisional report [28], comparisons were made between enthalpy

- differences from that work and those from the correlation of Das, et al . [21].

Since the results from the present work are approximately equivalent to those

from the earlier report at temperatures above 300 K, these comparisons, along

with some consistency tests, are omitted in this report.

13
It has been a routine procedure to validate equation of state computations

by comparing calculated and experimental specific heats and sound velocities.

For normal butane, there are only a few experimental specific heats and sound

velocities available, most of which are unreliable. Comparisons with available

data are presented in tables 14-16.

In the present work, an isochoric, nonanalytic equation of state has been

developed, based on thermophysical properties data, to compute thermodynamic

properties of normal butane. This equation originates on the liquid-vapor

coexistence boundary; approximately twelve constants are used in the vapor

pressure and orthobaric density equations. The equation, as used here, has only

three least squares coefficients and describes a P(p,T) surface free of

irregularities consistent with the known behavior of specific heats, especially

in the critical region. Four nonlinear parameters appear in the equation.

For normal butane, the equation of state has been developed from

comprehensive and consistent sets of vapor pressure, orthobaric vapor and liquid

density, and compressibility data. In general, the experimental data for these

properties over the range of this work are in relatively good shape except for

low temperature vapor pressures and vapor densities for which values have been

determined from thermal loop computations. However, as mentioned earlier,

accurate specific heat and sound velocity data are needed for comparisons with

computations from the equation of state.

5. Tables of Physical and Thermodynamic Properties

5.1 Calculated P-p-T Isochores and Isotherms

Tables 17 and 18 give a selection of isochores and isotherms computed by

equation of state (6). These are essential to examine behavior of the P(p,T)

surface. They are a useful supplement to the isobars of table 21 for

interpolating P-p-T values and their derivatives.

The tables of isochores show that the isochore curvatures are qualitatively

consistent with a maximum in the specific heat Cy(p,T) at the critical point.

The isotherm tables show that 3P/3p is nonnegative and that pressure increases

monotonical ly with density along isotherms.

5.2 The Joule-Thomson Inversion Locus

Table 19 gives the P-p-T locus of the JT inversion, (3T/9P)|^ = 0,

obtained from equation of state (5) under the condition, T»(3P/3T) = p'(3P/9p).

14
This table has been computed to temperatures well above those of P-p-T data, to

show approach to a maximum in P-T coordinates.

5.3 Thermophysi cal Properties of the Saturated Liquid

Table 20 gives physical and thermodynamic properties of the saturated liquid

computed by methods of section 3. (Properties of the saturated vapor can be

obtained from Table 21 from values given at the coexistence boundary for each

isobar.)

5.4 Thermophysical Properties Along Selected Isobars

Table 21 gives physical and thermodynamic properties on isobars, computed by

methods of section 3. These tables are extrapolated above the maximum

temperature and pressure of P-p-T data used for adjusting the equation of state.

Small discontinuities may be detected at T^ = 425.16 K along isobars at

P > P^ = 3.796 MPa due to a change in the paths of computation (section 3).

The first line of each table refers to freezing liquid on the P(T) melting

line. Each table at P < P contains a blank line for the transition from

c saturated liquid to vapor, as seen by the abrupt decrease of density. Dielectric

constants are extrapolated above maximum experimental temperatures and pressures

(see section 2.10 and table 13), but have not been extrapolated above 450 K.

6. Acknov;l edgments

Many staff members of the Thermophysical Properties Division of the National

Bureau of Standards (NBS) have contributed valuable suggestions, references, and

documents. Robert D. McCarty contributed the essential least-squares program,

providing for constraints. James F. Ely indicated the new numerical integration

procedure, and the simple method for obtaining fugacities. Neil A. Olien and the

Cryogenic Data Center have been of invaluable assistance in supplying references

and in obtaining documents. Special thanks go to Karen A. Bowie for her

diligence and expertise in the preparation of the manuscript and tables for

publication. Finally, we express grateful appreciation for support of this work

by the Gas Research Institute.

15
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16
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19
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22
APPENDIX A. Symbols and Units

Subscripts c and t refer to critical and liquid triple points.

Subscripts g and £ refer to saturated vapor and liquid.

Subscript a refers to liquid-vapor coexistence (usually the liquid).

Subscript r refers to reduced parameter.

Subscript o refers to reference state property.

Subscript m refers to melting line.

Subscript b refers to normal boiling point.

Superscript o refers to ideal gas state property,

expt refers to experimental value,

calc refers to calculated value.

(aP/3T)p isochore derivative, MPa/l(

(3P/3p)j isotherm derivative, MPa»m^/kg

(9^P/8T^)^ isochore curvature, MPa/K^

a,3,Y,ri nonlinear parameters in the equation of state

a,b,c,d,e,f coefficients defined in various equations

Aq ^c

~ ^ saturated vapor density equation

Aj coefficients defined in various equations

b (1 - B) + (1 - 3)^''^ in equation of state

B(p),C(p) density-dependent coefficients in the equation of state

B(T),C(T) second and third virial coefficients

Bp(T),Cp(T) reduced second and third virial coefficients

c exponent in Simon equation

Cy(p,T) molal heat capacity at constant volume, J/(mol»l()

Cp(p,T) molal heat capacity at constant pressure, J/(mol'K)

C^(T) molal heat capacity for saturated liquid, J/(mol»K)

CMF CI ausius-Mossotti function, cm-^/mol

E(p,T) the internal energy, J/mol

E° 22,644.306 J/mol (arbitrary)

e exponent in various equations

e dielectric constant

f/P fugacity/pressure ratio

f(p) used in definition of e(p)

f(T) defined in saturated vapor density equation

F(p,T) defined in the equation of state

F(Z) defined in the saturated vapor density equation

G(p,T) Gibbs free energy, J/mol

H° enthalpy for ideal gas state at T = 0

23
APPENDIX A. (Continued)

H(p,T) the enthalpy, J/mol

J the jou1 e, 1 N 'in JT Joule-Thomson

L the liter, 10"^ n?

mo] 58.1243 grams of normal butane (C^'^ = 12 scale)

'jL)(p,T) defined in the equation of state

P ' pressure, MPa

melting pressure, MPa

P^(T) the vapor pressure, MPa

P^(p) - P^[T^(p)], vapor pressure as a function of density

n(T) Pa(T)/''c

$(p,T) function in the equation of state

^{PiJ) function in the equation of state

Qygp ^^vap' ^^^^ vaporization, J/mol

r(^) ^ the gas constant, 8.3145 J/(mol*K), 0.0083145 MPa'L/(mol 'K)

R* 0. 00831 45 'Pc, MPa/K

p density, kg/m-^

p^ p/Pq, density reduced at the critical point

Pp ^ P/Pf density reduced at the triple point

S(p,T) the entropy, J/(mol'K)

T temperature, K Tq constant

T/Tq, temperature reduced at the critical point

T^(p) liquid-vapor coexistence temperature, K

(T(j) T^(p)/T^, reduced temperature at coexistence for the equation

r of state

e(p) defined locus of temperatures

u(T) defined in various equations

V 1/p, molar volume, m^/kg

W(p,T) the velocity of sound, m/s

x(T) (T^ - T)/(Tc - T^)

Xo(T) T/lOO

Z compressibility factor

The gas constant is increased slightly in value from earlier work in view

of the recent report of Rowlinson and Tildesley [60].

24
APPENDIX B. Conversion of Units

In the following table the molecular weight of normal butane is given by

mol . wt.

and 1 BTU

58.1243 g/mol . Also, 1 cal

IT

1 cal (thermocheinical ) = 4.184 J

= 1 BTU (International Table) = 1055.056 J.

th

To convert from

Pressure, MPa

Volume, m"^

Density, kg/m"^

Molar energy, J/mol

Molar entropy, J/(mol«K)

To

bar

atm

kg/cm^

Ib/inliter (L)

ft^

g/cm^

mol/L

Ib/ft^

MPa»m^/kg

bar»L/mol

calj-u/mol 'th

BTUij/lb

BTUij/(lb-°F)

Multiply by

10.

9.85923

10.1972

145.038

1000.

35.3147

0.001

1 ./(mol . wt .)

0.062428

0.001/(mol . wt.)

0.01

0.239006

0.429923/(mol . >/rt.) 0.238846/(mol . wt.)

25
APPENDIX C. Fixed-Point Values for Normal Butane

Critical Point

?^ = 3.7960 MPa

= 227.85 kg/m3 (3.92 mol/L)

= 425 .16 K

Normal Boiling Point

P = 0.101325 MPa

T = 272.638 K Py = 2.709 kg/m^ (0.04661 mol/L)

p^ = 501 .09 kg/in^ (10.341 mol/L)

Triple Point

P^ = 6.7358 X lO"'' MPa

= 134.86 K

Py = 3.4915 X 10"^ kg/m^ (6.0071 x 10"^ mol/L)

p^ = 735.27 kg/m3 (12.650 mol/L)

26
APPENDIX D.

Melting Line

Reeves [59]

Normal Butane Properties Reference Index

Date Pressure Range, MPa

1964 200 - 1000

Vapor Pressures Date

Seibert [66] 1915

Dana [19] 1926

Delaplace [22] 1937

Sage [64] 1937

Beattie [2] 1939

Aston [1] 1940

Kay [44] 1940

Wackher [74] 1945

Tickner [71] 1951

Connolly [15] 1962

Hi rata [39] 1966

Carruth [11] 1973

Thermal loops (This report) 1982

Saturated Liquid Densities Date

Dana [19] 1926

Coffin [13] 1928

Van der Vet [73] 1937

Sage [64] 1937

Kay [44] 1940

Benoliel [6] 1941

Carney [10] 1942

NGAA [69] 1942

Olds [51] 1944

Foehr [24] 1949

Connolly [14] 1956

Sliwinski [67] 1969

Kahre [42] 1973

McClune [49] 1976

Haynes [36,37] 1976

Orrit [53] 1978

Temperature Range, K 303 - 403

255 - 331

135 - 151

294 - 394

348 - 423

195 - 273

325 - Tc

205 - 279

136 - 196

344 - Tc

333 - 401

135 - 213

Temperature Range, K 273 - 329

239 - 306

283 - 323

294 - 394

325 - T^

213 - 293

228 - 333

227 - 333

311 - 411

293

293 - 298

283 - 368

289 - 328

143 - 173

135 - 300

135 - 275

27
APPENDIX D. (Conti nued)

Saturated Vapor Densities Date Temperature Range, K Dana [19] 1926 281 - 321

Sage [64] 1937 294 - 394

Kay [44] 1940 325 - Tr

Olds [51] 1944 311 - 411

Sliwinski [67] 1969 283 - 368

Virial/vapor pressure equations (This 1982 135 - 270

report)

Virial Coefficients Date Temperature Range, K Sage [64] 1937 311 - 394

Beattie [3] 1939 423 - 573

Kay [44] 1940 311 - 589

Beattie [4] 1942 423 - 573

Olds [51] 1944 311 - 511

Kretshmer [45] 1951 303

Gunn [33] 1958 344 - 511

Connolly [15] 1962 344 - 444

McGlashan [50] 1962 296 - 413

Tripp [72] 1962 283 - 323

Kapallo [43] 1963 244 - 321

Bottomley [8] 1964 273 - 426

Jones [41] 1967 368 - 498

St rein [68] 1971 296 - 498

Bottomlev [7] 1977 316 - 580

Compressibility Data Date Range of T, K Range of P, MPa

Sage [64] 1937 294 - 394 0.1 - 20.7

Beattie [3] 1939 423 - 573 1.5 - 36.3

Kay [44] 1940 311 - 589 0.2 - 8.3

Olds [51] 1944 311 - 511 0.07 - 68.9

Haynes [35] 1981 140 - 300 1.7 - 36.1

Virial equation (This 1982 300 - 700 0.2 - 0.6

report)

28
APPENDIX D Specific Heats Date

Dana [19] 1926

Huffman [40] 1931

Sage [65] 1937

Aston [1] 1940

Dailey [18] 1943

Chen [12] 1975

Heats of Vaporization

Dana [19]

Sage [64]

Das [20]

Das [21]

Thermal loops (This report)

Clapeyron equation (This report)

Sound Velocities

Rao [58]

Dielectric Constants

Sliwinski [67] (index of refraction)

Thompson [70]

Luo [47]

Haynes [35,38]

(Continued)

Type Range of T, K Ca(T) 257 - 294

Ca(T) 140 - 252

Cp(T) 294 - 411

Co(T) 140 - 268

CO(T) 345 - 693

C°(T) Spectroscopic

Date Temperature Range, K 1926 275 - 297

1937 294 - 394

1967 273 - 420

1973 280 - 420

1982 T^ - 270

1982 140 - 420

Date Temperature Range, K 1971 143 - 268

Date Temperature Range, K 1969 283 - 368

1980 228

1981 220 - 289

1981 135 - 303

29
APPENDIX E. Computer Program

PROGRAM NBTHRMB ( INPUT, OUTPUT)

C REVISION OF NBUTANE THERMOFUNCTIONS , RDG/NBS, START MAR. 26, 1981.

COMMON GK,GKK, Bl ,B2 ,B3 ,B4 ,B5 , C1,C2,C3, E1,E2,E3, ER, IX COMMON/l/AL , BE ,GA,DE , EP , ET , DCRT ,TCRT ,PCRT , DGAT ,DTRP ,TTRP , PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDSDT

C0MM0N/4/XBl,XB2, XC1,XC2, XE1,XE2, DXBDR ,DXCDR ,DXEDR

COMMON/6/ TSAT, THETA, PSAT

. COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

COMMON /9/ DNG,EG,HG,SG, CVG,CPG,WG, DPGDT,DPGDD

COMMON/11/ DELS, DELCV

C0MM0N/12/ZCRT,ZCALC,DZDT, ZSAT,DZSDT, ZFX, FRT,DFRTDT

COMMON/21/ TPS(70)

- COMMON/95/ PIS, DIS, DPTIS, DPDIS

COMMON/99/ TI,EZZ, EZ,SZ,CVZ, HZ,CPZ

. DIMENSION HZA(70), SZA(70), PP(99)

DATA (WM=58. 1243) ,(PA=1. 01325) ,(GJ=8. 3145)

1 FORMATdS, 2F10.0)

2 F0RMAT(I5, 3F10.0)

3 F0RMAT(8I10)

5 FORMAT (IX)

9 F0RMAT(8F10.0)

14 FORMATdHl 13X * NBUTANE ISOBAR AT P =* F10.6, 4H MPA / ) 16 FORMAT( 9X1HT 8X3HDEN 9X3HDEN 8X1HZ 5X5HDP/DT 5X5HDP/DD

2 8X1HE 8X1HH 8X1HS 6X2HCV 6X2HCP 9X3HF/P 5X1HW 4X5HDIEL. /

3 9X1HK 6X5HM0L/L 7X5HKG/M3 9X 5X5HMPA/K 1X9HMPA-M3/KG

4 4X5HJ/M0L 4X5HJ/M0L 2X7HJ/M0L/K 1X7HJ/M0L/K 1X7HJ/M0L/K

5 12X 1X5HM/SEC 4X5HC0NST ) 17 FORMATdX F9.3, Ell. 4, E12.5, F9.5, F10.6, F10.5,

1 2F9.1, F9.3, 2F8.2, E12.5, 16, F9.5)

20 F0RMAT(1H116X*TEST IDEAL FNCTNSV17X 3HT,K 7X3HHZA 7X3HSZA ) 21 FORMATdOX F10.2, FlO.l, F10.3)

80 CALL PVTDATA

CALL PEEK $ CALL ISOTHRM

C COMPUTE THERMOFUNCTIONS ON ISOBARS. START ON THE MELTING LINE.

C NOTE, ISOBAR P=PCRT OK, BUT ISOTHERM T=TCRT IS EXCLUDED.

C ISOBARS AT P UNDER PORT TRAVERSE THE DOME.

C NOTE USE OF QVAP ,DATA, TO CROSS THE ,DOME,.

C NOTE USE OF CSAT ,DATA, FOR SPECIFIC HEATS IN COMPRESSED LIQUID.

C NOTE TPS(IK) USED BY COMPRES.

C GET FUGACITIES, F/P, VIA H,S, HZ{T),SZ(T). (J. F.ELY).

C SAVE HZA(70), SZA(70) FROM 90 THRU 700 K. 85 DO 86 J=9,70 $ TI = 10*J $ CALL IDEAL $ HZA(J) = HZ

86 SZA(J) = SZ

C 87 PRINT 20 $ DO 88 J=9,70 $ T = 10*J

C 88 PRINT 21, T, HZA(J), SZA(J)

89 CALL JTLOCUS $ CALL TABLIQ

90 IN = 1 $ NI = 57 $ READ 9, ( PP( I )

, 1 = 1 , NI

)

91 DO 300 I=IN,NI $ IK = I $ LS = 0

92 P = PP(I) $ IF(I.EQ.26) P = PORT

93 PK = P/IO $ PRINT 14, PK $ PRINT 16

100 T = FINDTMF(P) $ CALL COMPRLQ $ V=1/DEN $ IW=W

101 Z = P/DEN/GKK/T $ DIE = DIELF{DEN ,T,P)

102 TI = T $ CALL IDEAL $ GIB = H-EZZ-HZ - T*(S-SZ)

103 XP = EXP(GIB/GJ/T) $ FOP = XP*PA/P $ CALL CON

30
104 PRINT 17, T,DEN,DIS,Z, DPTIS,DPDIS, E,H,S,CV,CP, FOP, IW, DIE

105 IT = T/10 $ IF(P.LT.PCRT) 110,180

C CASES FOR P LESS THAN PORT.

110 TPS(IK) = TS = FINDTSF(P) $ K = L = 0

111 DO 150 J=l,99 $ T = JT = 10*(IT+J)

112 IF{T.LT.TS) 113,117

113 CALL COMPRES $ V = 1/DEN $ IW = W

114 Z = P/DEN/GKK/T $ DIE = DIELF( DEN ,T,P)

M =JT/10 $ GIB = H-EZZ-HZA(M) - T*(S-SZA(M))

XP = EXP(GIB/GJ/T) $ FOP = XP*PA/P % CALL CON

115 PRIUT 17, T,DEN,DIS,Z, DPTIS,DPDIS, E,H,S,CV,CP, FOP, IW, DIE

116 GO TO 150

117 LS = LS + 1 $ IF{LS.EQ.l) 120,130

C CASE FOR SATURATED LIQUID AND VAPOR.

120 T = TS $ CALL COEXIST $ V=1/DEN $ VG=1/DNG $ IW=W $ IWG=Wn

121 Z = P/DEN/GKK/T $ ZG = P/DNG/GKK/T

122 DIEL = DIELF(DEN,T,P) $ DIEG = DIELF(DNG,T,P)

123 TI = T $ CALL IDEAL $ GIB = H-EZZ-HZ - T*(S-SZ)

124 FOP = EXP(GIB/GJ/T)*PA/P $ CALL CON

125 PRINT 17, T,DEN,DIS,Z, DPTIS,DPDIS, E,H,S,CV,CP, FOP, IW, DIEL

126 PRINT 5 $ DIS=DNG*WM $ DPTIS=DPGDT/10 $ DPDIS = DPGDD/IO/WM

127 PRINT 17, T, DNG,DIS,ZG,DPTIS, DPDIS, EG, HG,SG,CVG,CPG, FOP, IWG, DIEG

128 T = JT

C CASES FOR THE HOMOGENEOUS DOMAIN.

130 IF(JT.GT.500) 131,132

131 K = K+1 $ T = JT = JT + 10*K $ IF{ JT .GT .700) 300,132

132 CALL GENIUS $ V=1/DEN $ IW=W $ Z = P/DEN/GKK/T

133 IF(T.GT.450) 134,135

134 DIE = 0 $ GO TO 136

135 DIE = DIELF{DEN,T,P)

136 M =JT/10 $ GIB = H-EZZ-HZA(M) - T*(S-SZA(M))

137 XP = EXP{GIB/GJ/T) $ FOP = XP*PA/P $ CALL CON

141 PRINT 17, T,DEN,DIS,Z, DPTIS, DPDIS, E,H,S,CV,CP, FOP, IW, DIE

150 CONTINUE

C FOR P.GE.PCRT, CASES FOR T.LT.OR.T.GT.TCRT.

180 TPS(IK) = TCRT $ K = L = 0

181 DO 250 J=l,99 $ T = JT = 10*(IT+J)

182 IF(T.LT.TCRT) 190,210

C CASE A FOR T LESS THAN TCRT.

190 CALL COMPRES $ V = 1/DEN $ IW = W

191 Z = P/DEN/GKK/T $ DIE = DIELF(DEN,T,P)

192 M =JT/10 $ GIB = H-EZZ-HZA(M) - T*(S-SZA(M))

193 XP = EXP{GIB/GJ/T) $ FOP = XP*PA/P $ CALL CON

194 PRINT 17, T,DEN,DIS,Z, DPTIS, DPDIS, E,H,S,CV,CP, FOP, IW, DIE

195 GO TO 250

C CASE FOR T ABOVE TCRT, HOMOGENEOUS DOMAIN.

210 IF(JT.GT.500) 211,220

211 K = K+1 $ T = JT = JT + 10*K $ IF(JT.GT.700) 300,220

220 CALL GENIUS $ V=1/DEN $ IW=W $ Z = P/DEN/GKK/T

221 IF(T.GT.450) 222,223

222 DIE = 0 $ GO TO 224

223 DIE = DIELF(DEN,T,P)

224 M =JT/10 $ GIB = H-EZZ-HZA(M) - T*{S-SZA(M))

225 XP = EXP(GIB/GJ/T) $ FOP = XP*PA/P $ CALL CON

31
226 PRINT 17, T,DEM,DIS,Z, DPTIS,DPDIS, E,H,S,CV,CP, FOP, IW, DIE

250 CONTINUE

300 CONTINUE

999 STOP $ END

SUBROUTINE COEXIST

C GIVE^^: T AT COEXISTENCE, GET BOTH VAPOR AND LIQUID FUNCTIONS.

C FOR VAPOR, GET DNG,EG,HG,SG, CVG,CPG,WG, DPGDT,DPGDD, - C FOR LIQUID, GET DEN,E,H,S, CV,CP,CSAT,W. DPDT,DPDD.

C COEXIST CALLED BY COMPRLQ. P NOT USED, MUST NOT CHANGE.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT,TCRT,PCRT, DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT ,D2PDT2 ,DPSDT ,DPMDT ,DPDD ,DPDR ,DTSDR ,DTHDR ,DDSDT

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

C0MM0N/9/DNG,EG,HG,SG, CVG,CPG,WG, DPGDT,DPGDD

COMMON/11/ DELS, DELCV

COMMON/99/ TI,EZZ, EZ,SZ,CVZ, HZ,CPZ

DATA (Q=l. 01325) , (0=0.083145)

1 FORMAT! IHO 9X *T EXCEEDS TCRT IN COEXIST. * / ) 2 IF(T.GT.TCRT) 3,4

3 PRINT 1 $ STOP

4 PS = PSATF(T) $ DNG = DB = DENGASF(T)

5 TI = T $ CALL IDEAL $ M=15 $ DA=L=0

6 EG = EZZ + EZ + EDELF(L,M,T,DA,DB) $ HG = EG + 100*PS/DB

7 SG = SZ + DELS - 100*G*AL0G(Gn*DB/Q)

8 IF(T.EQ.TCRT) 9,11

9 PX = PVTF(T,DB,1) $ DPGDT = DPDT $ DPGDD = DPDD

10 CPG = CVG = WG = 0 $ GO TO 15

11 CVG = CVZ + DELCV $ PX = PVTF(T,DB,1)

12 CPG = CVG + 100*T/DPDD*(DPDT/DB)**2 $ WG = SQRT( WK*CPG*DPDD/CVG)

13 DPGDT = DPDT $ DPGDD = DPDD

C NOW TRAVERSE THE ,DOME, USING QVAP ,DATA,.

15 DEN = DL = DENLIQF(T) $ DDLDT = DDSDT $ QV = QVAPXF{T)

15 H = HG - QV $ S = SG - QV/T $ E = H - 100*PS/DL

C THIS RETURN AT 16+ USED ONLY WHEN CALLING SSATFIT, HSATFIT.

17 IF{T.EQ.TCRT) 18,19

18 PX = PVTF(T,DL,1) $ CP=CV=CSAT=W=0 $ RETURN

19 CSAT = CSATXF(T) $ PX = PVTF(T,DL,1)

22 CV = CSAT + 100*T*DPDT*DDLDT/DL/DL

23 CP = CV + 100*T/DPDD*(DPDT/DL)**2

30 W = SQRT(WK*CP*DPDD/CV) $ RETURN $ END

SUBROUTINE COMPRES

C SAVES COMPUTER TIME INTEGRATING COMPRLIQ AT T.LT.TCRT.

C FOR T = INTEGER MULTIPLES OF 10 K. FIRST ISOBAR USES COMPRLQ.

C FOR SUCCEEDING ISOBARS, START ON PREVIOUS ISOBAR, EXCEPT - C AT TEMPS GE TPS(IK-l) ON PREVIOUS ISOBAR, MUST USE COMPRLQ.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT , TCRT , PORT , DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT, DPDD, DPDR,DTSDR,DTHDR, DDSDT

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV, CP, CSAT, W,WK

COMMON/11/ DELS, DELCV

COMMON/21/ TPS(70)

DIMENSION DK(50) ,EK{50) ,SK{50) ,CK(50)

1 FORMAT! IHO 9X *T G.E. TCRT IN COMPRES. * / ) 2 IF(T.GE.TCRT) 3,4

32
3 PRINT 1 $ STOP

4 J = T/10 $ IF(T - 10*J) 5,6

5 CALL COMPRLQ $ RETURN

6 IF(IK.EQ.IN) 7,9

7 CALL COMPRLQ

8 DK{J)=DEN $ EK(J) = E $ SI<{J)=S $ CK(J)=CV $ RETURN

C INTEGRATE FROM OLD DEN TO NEW DEN ON GIVEN ISOTHERM - C EXCEPT IF T EXCEEDS OLD TMAX , USE COMPRLQ.

9 IF(T.GE.TPS(IK~1)) GO TO 7 10 DA=DK(J) $ DK(J) = DEN = DB = FINDENF{T,P) $ N = 13

11 EK(J) = E = EK(J) + EDELF(1,N,T,DA,DB) $ H = E + 100*P/DB

12 SK{J) = S = SK(J) + DELS $ CK(J) = CV = CK(J) + DELCV

C GET NEW DP/DT, DP/DD, CP, W. 15 PX = PVTF{T,DB,1) $ CP = CV + 100*T/DPDD*(DPDT/DB)**2

30 W = SQRT(WK*CP*DPDD/CV) $ RETURN $ END

SUBROUTINE COMPRLQ

C GIVEN P,T FOR COMPR.LIQ. AT T.LT.TC, GET DEN AND FUNCTIONS.

C REVISED TO USE HSATF, SSATF, CSATXF, BUT NOT COEXIST. TIMESAVER.

C INTEGRATE ALONG ISOTHERM T FROM SATLIQ UP TO POINT (P,T).

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT,TCRT,PCRT, DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT,D2PDT2,0PSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDSDT

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

COMMON/11/ DELS, DELCV

1 FORMAT! IHO 9X *T NOT UNDER TCRT IN COMPRLQ.*/)

2 IF{T.GE.TCRT) 3,4

3 PRINT 1 $ STOP

C GET PSAT, DENLIQ, AND SATLIQ FUNCTIONS FOR START.

4 PS = PSATF(T) $ DL = DENLIQF{T) $ DDLDT = DDSDT

6 HS = HSATF(T) $ ES = HS - 100*PS/DL $ SS = SSATF(T)

C 7 IF(T.GT.340) 8,9

C 8 CVS = CVSATF(T) $ GO TO 10

9 PX=PVTF(T,DL,0) $ CVS = CSATXF{T) + 100*T*DPDT*DDLDT/DL/DL

C INTEGRATE UP TO POINT (P,T).

10 DB = FINDENF(T,P) $ DX = DB - DL $ IF(DX.GT.O) 11,20

11 M = 14 $ E = ES + EDELF(1,M,T,DL,DB)

12 H = E + 100*P/DB $ S = SS + DELS $ CV = CVS + DELCV

13 PX = PVTF{T,DB,1) $ CP = CV + 100n/DPDD*( DPDT/DB)**2

14 W = SQRT(WK*CP*DPDD/CV) $ DEN = DB $ RETURN

20 DEN=DL $ E=ES $ H=HS $ S=SS $ CV=CVS $ PX = PVTF{T,DL,1)

21 CP = CV + 100*T/DPDD*{DPDT/DL)**2 $ W = SQRT( WK*CP*DPDD/CV)

30 RETURN $ END

SUBROUTINE CON

C CONVERT TO SI UNITS FOR P, DEN, DP/DT, DP/DD,

C0MM0N/3/DPDT ,D2PDT2 , DPSDT ,DPMDT , DPDD ,DPDR , DTSDR , DTHDR , DDSDT

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

COMMON/95/ PIS, DIS, DPTIS, DPDIS

DATA (WM = 58.1243)

1 PIS = P/10 $ DIS = DEN*WM

2 DPTIS = DPDT/10 $ DPDIS = DPDD/IO/WM

9 RETURN $ END

FUNCTION CSATXF (T)

33
C NBUTANE SATLIQ CSAT, J/MOL/K.

C CONSTRAINED AT TRIPLE AND CRITICAL POINTS.

C Y # (S-SCRT)/{STRP-SCRT) , X # ( TC-T) /( TC-TT)

.

C Y = X + (XE-X)*(A1 + A2*X + A3*X2 + . . . ).

DIMENSION AS(6)

DATA {NFS=6) ,(ES=0.23) ,(TTRP=134.86) ,{TCRT=425.16)

DATA (STRP = 133. 54372), (SORT = 297.64652)

DATA (AS = 0.08883444348, -0.3470304947, 0.2093724392,

1 -0.9568328496, 0.9579992545, -0.6534607056)

1 FORMATdHO 9X *CSATXF, T.GT.TCRT. * / ) 2 IF(TCRT-T) 3,4,5

3 PRINT 1 $ STOP

4 CSATXF =0 $ RETURN

5 XN=TCRT-TTRP $ X = (TCRT-T)/XN $ DXDT = -1/XN $ SN=STRP-SCRT

6 XE = X**ES $ V = XE -X $ VI = ES*XE/X - 1 7Z1=Z=0 $ DO 9 K=1,NFS $ L=K-1 $ XL= X**L

8 Z = Z + AS(K)*XL $ Zl = Zl + L*AS{K)*XL/X

9 CONTINUE $ DSDT = SN*(1 + V*Z1 + V1*Z)*DXDT

10 CSATXF = T*DSDT $ RETURN $ END

FUNCTION DELTAF(T,D)

C GET (T*DP/DT - D*DP/DD) FOR THE J-T INVERSION CURVE.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT ,TCRT ,PCRT, DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT,D2P0T2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDSDT

1 IF(T-TCRT) 2,4,4

2 DL - DENLIQF(T) $ IF{D-DL) 3,3,4

3 DELTAF = l.OE+100 $ RETURN

4 P = PVTF(T,D,1)

5 DELTAF = ABS (T*DPDT-D*DPDD) $ RETURN $ END

FUNCTION DENGASF(T)

C DESIGNED FOR ZSAT = 1 AT LOW DENSITIES, 5/29/77.

C USE ZSAT # PS/DS/GK/TS WITH VAPOR PRESSURES, AND ZCRT.

C Z = 1 + (ZCRT-1)*PI*F(X)/X/X.

C F(X) # 1 + A1*UE + A2*U + A3*EXP( EGX*{ 1-1/U) )

.

C NOTE ZSMl FOR FUGACTY, NOT IN COMMON HERE.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT ,TCRT , PORT , DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDSDT

C0MM0N/12/ZCRT,ZCALC,DZDT, ZSAT,DZSDT, ZFX, FRT,DFRTDT

DIMENSION AV(3)

DATA (EG=0.35) ,{ EGX=2. 30) ,( GKK=0 .083145

)

DATA(AV = -0.8665772894, 1.120397967, 4.498658942)

1 FORMATdHO 9X *T EXCEEDS TC IN DENGASF. * / ) 2 IF(TCRT-T) 3,4,5

3 PRINT 1 $ STOP

4 DENGASF = DCRT $ DDSDT = l.OE+10 $ RETURN

5 ZN = ZCRT-1 $ PC = PORT $ P = PSATF(T)

6 PI = P/PC $ PIT = DPSDT/PC $ TC = TCRT $ X = T/TC

7 X2 = X*X $ U = 1-X

8 UE = U**EG $ UEl = -EG*UE/U

9 EGXU = EGX*(1-1/U) $ IF(EGXU.LT.-270) 10,11

10 XP = XPl = 0 $ GO TO 12

11 XP = EXP(EGXU) $ XPl = -EGX*XP/U/U

12 F = 1 + AV(1)*UE + AV(2)*U + AV(3)*XP $ ZFX = F

34
13 Fl = AV(1)*UE1 - AV(2) + AV(3)*XP1

15 ZSMl = ZN*PI*F/X2 $ ZSAT = Z = 1 + ZSMl $ ZCALC = Z 16 DZSDT = DZDT = {PI*( F1-2*F/X)/TC + F*PIT)*ZN/X2

17 DENGASF = P/T/Z/GKK

18 DDSDT = (DPSDT - P/T - P*DZDT/Z) /T/Z/GKK $ RETURN $ END

FUNCTION DENLIQF(T)

C NBUTANE SAT. LIQUID DEN, MOL/L, (DCRT=3.92), RDG, I^IAR. 19, 1981.

C DEN = DCRT + YNL*(X + (XE-X)*Y), YNL # DTRP - DCRT.

C Y # Al + A2*X + A3*X2 + A4*X3.

C0MM0N/3/DPDT,D2PDT2, DPSDT, DPMDT,DPDD,DPDR,DTSDR,DTHDR, DDSDT

DIMENSION AW(3)

DATA (EL=0.35) ,(NFL=3)

DATA (TTRP=134.86) ,(TCRT=425.16) ,(DCRT=3.92) ,(DTRP=12.65)

DATA(AW = 0.794388335, -0.001089476, -0.085829197)

1 FORMATdHO 9X *DENLIQF = 0, T EXCEEDS TCRT. * / ) 2 IF(TCRT-T) 3,4,5

3 PRINT 1 S STOP

4 DENLIQF = DCRT $ DDSDT = -l.OE+10 $ RETURN

5 XN=TCRT-TTRP $ X=(TCRT-T)/XN $ X2 = X*X $ DXDT = -1.0/XN

6 XE = X**EL $ U = XE - X $ Ul = EL*XE/X - 1 7Y1-Y=0 $ DO 9 K=1,NFL $ L = K-1 $ XL = X**L

8 Y = Y + AW(K)*XL $ Yl = Yl + AW(K)*L*XL/X

9 CONTINUE $ YNL = DTRP - DCRT

11 DENLIQF = DCRT + YNL*(X + U*Y)

12 DDSDT = YNL*(1 + U*Y1 + U1*Y)*DXDT $ RETURN $ END

FUNCTION DIELF(D,T,P)

C NBUTANE CONSTS., RDG, OCT. 14, 1980, VIA HAYNES DATA.

C CM,RMSPCT = 0.083, E,RMSPCT = 0.017.

C CM = Al + A2*R + A3*R2 + A4/X + A5*PI.

DIMENSION A(5)

DATA (DCRT=3.92) ,{TCRT=425.16)

DATA(A = 20.654382, 0.25129317, -0.097230479,

1 -0.039216489, -0.011645515)

1 R = D/DCRT $ X = T/TCRT $ G = 1/X $ PI = P/100

2 CM = A(l) + A(2)*R + A(3)*R*R + A(4)*G + A{5)*PI

3 Z = CM*D/1000 $ DIELF = (2*Z+1 )/( 1 .0-Z)

5 RETURN $ END

FUNCTION EDELF(L,M,T,DA,DB)

C GET CHANGE OF E, S, CV WITH DENSITY ALONG ISOTHERMS.

C GET EDELF, DELS, DELCV FROM DA TO DB ON ISOTHERM T.

C ROMBERG NUMERICAL INTEGRATION VIA - C CARNAHAN/LUTHER/WILKES, APPLIED NUMERICAL METHODS, P. 90,

C JOHN WILEY AND SONS, INC., N.Y., 1969.

C NOTE, VALUE OF LD CONTROLS CONVERGENCE LIMITS.

C NOTE, NMAX = M, NK = FINAL, TOTAL SUBDIVISIONS OF INTERVAL DX

.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT, TCRT, PORT, DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT,D2PDT2, DPSDT, DPMDT,DPDD,DPDR,DTSDR,DTHDR, DDSDT

COMMON/11/ DELS, DELCV

C0MM0N/12/ZCRT, ZCALC, DZDT, ZSAT, DZSDT, ZFX, FRT,DFRTDT

DIMENSION E(20), S(20), C(20)

DATA (LD=2) ,(DI=0. 00001) , (0=0.083145)

35
1 F0RMAT(1H09X*EDELF L =*I2,5H, N =13, 5H, T = F8.3,6H, DA =E10.4,

1 6H, DB =E10.4, 6H, LD =12//

2 lOX IHN 7X5HEDELF 8X4HDELS 7X5HDELCV ) 2 FORMATdHO 9X 6HEDIF =F10.3, 8H, SDIF =F10.5, 9H, CVDIF =F10.3)

3 F0RMAT(6X 15, F12.3, F12.5, F12.3)

4 FORMATdHO 9X *EOELF NG AT TCRT FOR CV AT DEN NEAR OR GT CP.*/)

C FOR DA=0 AND DB.LE.DI, IDEAL GAS, EDELF=DELS=DELCV=0.

C FOR DA=0 AND DB.GT.DI, START ROMBERG WITH DA = DI, - C TO AVOID INFINITIES IN ORDINATE FUNCTIONS AT DA = 0.

5 NK = 1 $ DM = DCRT/2 $ DZ = 0.98*DCRT

9 ZK = 1.0 - 1/ZCRT $ RK = 100*GnCRT/DCRT

10 IF(L.EQ.O) 11,14

11 IF(DB.LE.DI) 12,13

12 EDELF = DELS = DELCV =0 $ RETURN

13 DA = DI

C GET FIRST TRAPEZOID AREA, E(l) ETC., FROM DA TO DB.

14 DX = DB - DA $ P = PVTF(T,DA,0) $ IF(DA,LT.DM) 16,17

16 EA - RK*(ZK*ZSAT*ZFX + FRT - T*DFRTDT) $ GO TO 18

17 EA = 100*(P-T*DPDT)/DA/DA

18 IF{L.EQ.O) 19,20

19 SA = -RK*DFRTDT $ GO TO 21

20 SA = -100*DPDT/DA/DA

21 CA = -100*T*D2PDT2/DA/DA

22 P = PVTF(T,DB,0) $ IF{DB.LT.DM) 23,24

23 EB = RK*(ZK*ZSAT*ZFX + FRT - T*DFRTDT) $ GO TO 25

24 EB = 100*(P-T*DPDT)/DB/DB

25 IF(L.EQ.O) 26,27

26 SB = -RK*DFRTDT $ GO TO 28

27 SB = -100*DPDT/DB/DB

28 CB = -100*T*D2PDT2/DB/DB

29 E(l)=(EA+EB)*DX/2 $ S(l)=(SA+SB)*DX/2 $ C(l)=(CA+CB)*DX/2

C INTERVAL HALVING, GET E(N+1), ETC.

30 DO 60 N=1,M $ K = N + 1 31 JM = 2**N - 1 $ DXN = DX/2**N $ E(K) = S(K) = C(K) = 0

33 DO 45 J=1,JM,2 $ NK = NK+1 $ DN = DA + J*DXN

34 P = PVTF(T,DN,0) $ IF(DN.LT.DM) 35,36

35 EB = RK*(ZK*ZSAT*ZFX + FRT - T*DFRTDT) $ GO TO 37

36 EB = 100*{P-T*DPDT)/DN/DN

37 IF{L.EQ.O) 38,39

38 SB = -RK*DFRTDT $ GO TO 40

39 SB = -100*DPDT/DN/DN

40 CB = -100*T*D2PDT2/DN/DN

41 E(K) = E(K) + EB $ S(K) = S(K) + SB $ C(K) = C(K) + CB

45 CONTINUE $ E(K) = E{N)/2 + E(K)*DXN

46 S{K) = S(N)/2 + S(K)*DXN $ C(K) = C{N)/2 + C(K)*DXN

C

C TEST FOR CONVERGENCE.

50 ED=ABS{E(K)-E(N)) $ SD=ABS( S(K) -S( N) ) $ CD=ABS(C(K)-C(N)

)

53 IF(ED.LT.0.4/LD) 54,60

54 IF(SD.LT.0.002/LD) 55,60

55 IF(T.EQ. TCRT. AND. DB.GT.DZ) GO TO 57

56 IF(CD.LT.0.04/LD) 57,60

57 EDELF = E{K) $ DELS = S(K) $ DELCV = C(K) $ RETURN

60 CONTINUE $ N = M $ NM = N-1 $ NP = N+1

36
61 PRINT 1, L, N, T, DA, DB, LD

62 PRINT 3, NM,E(NM) ,S(NM) ,C(NM) $ PRINT 3, N ,E( N) , S( N ) ,C( N)

64 PRINT 3, NP,E(NP) ,S{NP) ,C(NP) $ PRINT ?., ED, SD, CD

99 STOP $ END

FUNCTION FIMDENF(T,P)

C ON ISOTHERM T, FIND DEN, MOL/L, TO MINIMIZE (P-PC) VIA EQNSTATE.

C0MM0N/1/AL,BE,GA,0E,EP,ET, DCRT,TCRT,PCRT, DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT,D2PDT2,0PSDT,DPMDT,DPDD,0PDR,DTSDR,DTHDR,D0SDT

DATA (GKK = 0.083145)

41 FORMATdHO 9X *FINDENF = 0, FAILS TO CONVERGE. * / ) 42 FORMATdHO 9X *FINDENF = DCRT, DP/DR ZERO OR NEG. * / ) 43 FORMATdHO 9X *FINDENF = 0, DOUBLE-VALUED AT P = PSAT. * / ) DM = 1.05*DTRP

IF(P.GT.O) 1,35

1 IF(T-TCRT) 2,5,8

2 DG=DENGASF(T) $ DL=DENLIQF(T) $ PS=PSATF(T) $ IF{P-PS) 3,32,4

3 D = DG/2 $ GO TO 11

4 D = (DL+DTRP)/2 $ GO TO 11

5 DG=DL=DCRT $ PS=PCRT $ IF(P-PS) 6,33,7

6 D = DCRT/2 $ GO TO 11

7 D = 2*DCRT $ GO TO 11

8 IF(T.LT. 450.0) 9,10

9 PC = PVTF(T,DCRT,0) $ IF{P-PC) 6,33,7

10 D = DCRT

11 DO 30 J=l,50 $ DP=P-PVTF{T,D,1) $ IF(ABS (DP/P)-1 .OE-7) 31,31,12

12 IF(DPDD.GT.O) 13,34

13 DD = DP/DPDD $ IF(ABS ( DD/D )-l .OE-7 ) 31,31,14

14 D = D + DD $ IF{D.GT.O.O) 16,15

15 D = P/GKK/T $ GO TO 30

16 IF(D.GT.DM) 17,18

17 D = DM $ GO TO 30

18 IF(T-TCRT) 19,24,30

19 IF{P.LT.PS) 20,22

20 IF(D.GT.DG) 21,30

21 D = DG $ GO TO 30

22 IF(D.LT.DL) 23,30

23 D = DL $ GO TO 30

24 IF(P.LT.PCRT) 25,27

25 IF(D.LT.DCRT) 30,26

26 D = DCRT - 0.02 $ GO TO 30

27 IF{D.GT.DCRT) 30,28

28 D = DCRT + 0.02

30 CONTINUE $ PRINT 41 $ STOP

31 FINDENF = D $ RETURN

32 PRINT 43 $ STOP

33 FINDENF = DCRT $ RETURN

34 FINDENF = DCRT $ PRINT 42 $ RETURN

35 FINDENF=DPDT=D2PDT2=0 $ DPDD=GKK*T $ DPDR=DPDD*DTRP

36 RETURN $ END

FUNCTION FINDTMF(P)

C GIVEN P ON THE MELTING LINE, FIND T FOR NBUTANE.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT,TCRT,PCRT, DGAT,DTRP ,TTRP ,PTRP

37
DATA (A=3634.0) ,(E=2.210)

1 X = (P-PTRP)/A + 1 $ FINDTMF = TTRP*X**( 1 .0/E) $ RETURN $ END

FUNCTION FINDTSF(P)

C GIVEN VAPOR PRESSURE P, ITERATE T TO MINIMIZE (P-PC).

C0MM0M/1/AL,BE,GA,DE,EP,ET, DCRT,TCRT,PCRT, DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,0THDR,DDSDT

1 FORMATdHO 9X *FINDTSF = 0, FAILS TO CONVERGE. * / ) 2 FORMATdHO 9X *FINDTSF = 0, P EXCEEDS PCRT. * / ) 3 IF(P-PCRT) 4,11,12

4 T = 300 $ DO 9 J=l,50 $ DP = P - PSATF{T) $ ADP = ABS (DP)

5 IF(ADP/P-1.0E-7) 10,6,6

6 IF(ADP/DPSDT/T-1.0E-7) 10,7,7

7 T = T + DP/DPSDT $ IF(T-TCRT) 9,9,8

8 T = TCRT

9 CONTINUE S PRINT 1 $ STOP

10 FINDTSF = T $ RETURN

11 FIMDTSF = TCRT $ RETURN

12 PRINT 2 $ STOP S END

SUBROUTINE GEMEOUS

C GIVEN P,T FOR THE HOMOGENEOUS DOMAIN - C GET DEN AND FUNCTIONS AT ANY TEMPERATURE.

C0MM0M/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDSDT

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

COMMON/11/ DELS, DELCV

COMMON/99/ TI,EZZ, EZ,SZ,CVZ, HZ,CPZ

DATA (Q=l. 01325) , (0=0.083145)

3 TI = T $ CALL IDEAL $ IF(P.GT.O) 4,10

4 DEN = DB = FINDENF(T,P) $ M = 15 $ DA = L = 0

5 E = EZZ + EZ + EDELF(L,M,T,DA,DB) $ H = E + 100*P/DB

6 S = SZ + DELS - 100*G*AL0G(G*T*DB/Q)

7 CV = CVZ + DELCV $ PX = PVTF(T,DB,1)

8 CP = CV + 100*T/DPDD*(DPDT/DB)**2

q W = SQRT(WK*CP*DPDD/CV) $ RETURN

10 DEN=S=0 $ E = EZZ + EZ $ H = E + 100*G*T S CV=CVZ $ CP=CPZ

12 W = SQRT(WK*CP*G*T/CV) $ RETURN $ END

SUBROUTINE GENIUS

C VALID ONLY FOR THE HOMOGENEOUS DOMAIN.

C SAVES COMPUTER TIME WHEN TABULATING FUNCTIONS ALONG ISOBARS.

C SAVES DEN,E,S,CV ALONG ISOBARS FOR USE IN INTEGRATING TO NEXT

C HIGHER ISOBAR. VALID ONLY FOR MONOTONICALLY INCREASING ISOBAR

C PRESSURES, AND AT TEMPS. T = INTEGER MULTIPLES OF 10 K.

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,0TSDR,DTHDR,DDSDT

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

COMMON/11/ DELS, DELCV

DIMENSION DK(70) ,EK(70) ,SK(70) ,CK{70)

1 FORMATdHO 9X *GENIUS T NOT INTEGRAL. * / ) 2 J = T/10 $ IF(T - 10*J) 3,4

3 CALL GENEOUS $ RETURN

4 IF(IK.EQ.IN) 5,9

5 CALL GENEOUS

6 DK(J) = DEN $ EK(J) = E $ SK(J) = S $ CK(J)=CV $ RETURN

C INTEGRATE FROM OLD DEN UP TO NEW DEN ON GIVEN ISOTHERM.

38
9 DA = DK{J) $ DK(J) = DEN = DB = FIND£MF(T,P) $ M = 14

11 EK(J) = E = EK(J) + EDELF(1,N,T,DA,DB) $ H = E + 100*P/DB

13 SK(J) = S = SK{J) + DELS $ CK{J) = CV = CK(J) + DELCV

C NOW GET NEW DP/DT, DP/DD, CP, W.

15 PX = PVTF(T,DB,1) $ CP = CV + 100*T/DPDD*(DP0T/DB)**2

30 W = SQRTfWK*CP*DPDD/CV) $ RETURN $ END

FUNCTION HSATF(T)

C NBUTANE SATLIQ ENTHALPY, J/MOL.

C DEFINE YH # {H-HC)/( HT-HC) , X # (TC-T)/(TC-TT) , WHEN - C YH = X + (XE-X)*(A1 + A2*X + A3*X2 + . . .)

DIMENSION AH(8)

DATA (NFH=8) ,(EH=0.29) ,(TTRP=134.86) ,(TCRT=425.16)

DATA (HTRP = 0.001),(HCRT = 45399.788)

DATA (AH = 0.1929773377, 0.3998984487, -0.05499361241,

1 -1.020568625, 2.872789244, -4.052610155, 2.696377850,

2 -0.6834388986)

1 FORMATdHO 9X 3HT =F10.5, * IN HSATF(T).*/)

2 IF{T.GT.TCRT) 3,4

3 PRINT 1, T $ STOP

4 X = (TCRT-T)/(TCRT-TTRP) $ IF(X.LE.O) 5,6

5 HSATF = HCRT $ RETURN

6 V = X**EH -X $ FX=X $ DO 7 K=1,NFH

7 FX = FX + V*AH(K)*X**{K-1)

8 HSATF = HCRT - (HCRT-HTRP)*FX $ RETURN $ END

SUBROUTINE IDEAL

C N-BUTANE, VIA DATA OF CHEN ET AL (1975).

C CPZ/R = 4 + (Al + A2/X + A3/X2 + . . )*EXP{-E/X), X # T/IOO.

COMMON/99/ TI,EZZ, EZ,SZ,CVZ, HZ,CPZ

DIMENSION A(5)

DATA (E=2. 37) ,(R=8. 3145 ),(HI=7. 7980) ,(SI=37. 3495)

DATA(A = 41.1109726, -139.304011, 257.297067, -170.730596,

1 40.0321709)

1 NK = 5 $ XI = Tl/lOO $ XP = EXP(-E/XI)

2 CP = 4.0 $ DO 3 K=1,NK

3 CP = CP + A(K)*XP*XI**(1-K)

C NUMERICAL INTEGRATION FOR HZ/R, SZ/R - 5H=S=0 $ N= ABS(TI-300)/4 +4 $ DX = (XI-3)/N

6 DO 10 J=1,N $ X = 3.0 + (J-0.5)*DX $ XP = EXP(-E/X)

7 CPX = 4.0 $ DO 8 K=1,NK

8 CPX = CPX + A(K)*XP*X**(1-K)

9 H = H + CPX*DX $ S = S + CPX*DX/X

10 CONTINUE $ H = (HI*3 + H)/XI $ S = SI + S

C CONVERT TO JOULES, MOLES, KELVINS.

11 HZ = R*TI*H $ EZ = HZ - R*TI $ SZ = R*S

12 CPZ = R*CP $ CVZ = CPZ - R $ RETURN $ END

SUBROUTINE ISOTHRM

C PRINTOUT THE CRITICAL ISOTHERM.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT,TCRT,PCRT , DGAT ,DTRP ,TTRP , PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDSDT

C0MM0N/4/XBl,XB2, XC1,XC2, XE1,XE2, DXBDR ,DXCDR ,DXEDR

COMMON/6/ TSAT, THETA, PSAT

39
DATA (WM = 58.1243)

1 FORMATdHl 14X *THE CRITICAL ISOTHERM, NBUTANE* //

1 5X6HTC,K = F7.2, 12H, 0C,KG/M3 = F9.4, lOH, PC,MPA = F10.7/ 6X

2 *AT THE CP., DPS/DT =*F9.6, 9H, DP/DT =F9.6, * MPA/K.* //

3 5X4HD/DC 9X5HTS/TC 9X5HPS/PC 10X4HP/PC 9X5HDP/DR 4X6H0TS/DR

4 4X6HDTH/DR 4X5HDPS/DR 4X6HDXB/DR 4X6HDXC/DR ) 2 F0RMAT(2X F8.3, 3F14.10, F14.9, 5F10.5)

3 PC = PVTF(TCRT,DCRT,0) $ PCS = PCRT/10 $ DCS = DCRT*WM

DPST = DPSDT/10 $ DPT = DPDT/10

4 PRIMT 1, TCRT, DCS, PCS, DPST, DPT $ DO 8 J=l,41

5 DR = 0.895 + O.OOS^J $ DN = DR*DCRT

6 PR = PVTF(TCRT,DN,1)/PCRT $ DPSDR = DPSDT*DTSDR '

7 TSN = TSAT/TCRT $ PSN = PSAT/PCRT

DPDR = DPDR/10 $ DPSDR = DPSDR/10

8 PRINT 2, DR, TSN,PSN, PR, DPDR, DTSDR,DTHDR, DPSDR, DXBDR,DXEDR

9 RETURN $ END

SUBROUTINE JTLOCUS

€ THE JOULE-THOMSON P-V-T LOCUS FOR HBUTANE.

C DERIVE THE J-T INVERSION CURVE. USE ROUTINE DELTAF(T ,DI )

.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT, TCRT, PORT, DGAT,DTRP,TTRP,PTRP

DIMENSION DK{60) ,DN{60) ,TT{60) ,PP(60)

DATA (A=1 .2275) ,{ B=0. 485) ,(WM=58. 1243)

1 FORMATdHl 16X nHE JOULE-THOMSON INVERSION LOCUS FOR NBUTANE* //

2 17X 3HT,K 8X2HDI 5X5HKG/M3 5X5HP,MPA

3 7X 3HT,K 8X2HDI 5X5HKG/M3 5X5HP,MPA ) 2 FORMATdOX 110, 2F10.1, F10.3, 110, 2F10.1, F10.3)

C SAVE INITIAL, TRIAL DENSITY, DK(I) = DI.

5 TA = 340 $ NP = 52

6 PRINT 1 $ DO 25 1=1, NP $ DX = 0.4

7 T = TA + 10*1 $ X = T/TCRT $ DK(I) = DI = DCRT*EXP{ A-B*X

)

10 IF(T-TCRT) 11,12,12

. 11 DL = DENLIQF(T) $ IF(DI.LT.DL) 23,12

12 SS = DELTAF(T,DI) $ DO 20 IT=1,14

14 D=DI-DX $ SL=DELTAF(T,D) $ D=DI+DX $ SP=DELTAF(T,D)

15 IF(SS-SL) 18,16,16

. 16 IF(SP-SL) 19,17,17

17 SS = SL $ DI = DI - DX $ GO TO 20

18 IF(SS-SP) 20,20,19

19 SS = SP $ DI = DI + DX

20 DX = DX/2 $ TT(I) = T $ DN{I) = DI $ PP(I) = PVTF(T,DI,0)

21 GO TO 25

23 TT(I) = T $ DK(I) = DN(I) = PP(I) = 0

25 CONTINUE $ N = NP/2

26 DO 35 J=1,N $ K = J + N 27 IT = TT(J) $ ITT = TT(K)

28 DKJ = WM*DK(J) $ DNJ = WM*DN(J)

29 DKK = WM*DK(K) $ DNK = WM*DN{K)

30 PPJ = PP(J)/10 $ PPK = PP(K)/10

35 PRINT 2, IT, DKJ, DNJ, PPJ, ITT, DKK , DNK, PPK

40 RETURN $ END

SUBROUTINE PEEK

C EXAMINE BEHAVIOR OF THE PVT COEFFICIENTS.

40
C B{S) # Bl + B2*S2, E(S) # El*( S-l)*( S-ER)*EXP{ -GA*S**IX)

.

C WHERE, R # DEN/DTRP, S # DEN/DCRT.

COMMON GK,GKK, Bl ,B2 ,B3 ,B4 ,85 , C1,C2,C3, E1,E2,E3, ER,IX

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT,TCRT,PCRT, DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,D0S0T

COMMON/6/ TSAT, THETA, PSAT

DATA (WM = 58. 1243), (EX = 1.10)

4 FORMATdHl 14X ^EQUATION OF STATE COEFFS., NBUTANE * //

1 15X 6HTTRP =F7.3, 8H, TRLP =F9.4, 8H, TCRT =F8.3, * K* /

2 15X 6HPTRP =E12.6, 8H, PBLP =F8.6, 8H, PCRT =F9.6, * MPA* /

3 15X 6HDTRP =E11.5, 8H, DLBP =E11.5, 8H, DCRT =E11.5, * KG/M3* /

3 15X 6HDGAT =E11.5, 8H, DGBP =E11.5, * KG/M3* /

3 15X *DPS/DTB,MPA/K =* Ell. 5, *, QVAPB,KJ/MOL =* F7.3//

4 15X 4HIX =12, 6H, EX =F5.2, 6H, ER =F5.2, *, S # DEN/DCRT* /

5 15X 4HAL =F10.7, 6H, BE =F10.7, 6H, GA =F10.7/

6 15X 4HDE =F10.7, 6H, EP =F10.7, 6H, ET =F10.7//

7 15X 4HB1 =F14.11, 6H, B2 =F14.11, 6H, B3 =F14.11/

8 15X 4HC1 =F14.11, 6H, C2 =F14.11, 6H, C3 =F14.11/ ) 5 FORMAT! 15X 4HD/DC 5X4HTSAT 5X5HTHETA 4X6HPS,MPA 9X1HB 9X1HC ) 6 F0RMAT(9X F10.2, 2F10.3, F10.4, 2F10.5)

8 TB=FINDTSF(1. 01325) $ DGB=DENGASF( TB) $ DLB=DENLIQF(TB)

9 QB = TB*DPSDT*(1/DGB - 1/DLB)/10.0

PTR = PTRP/10 $ PBLP = 0.101325 $ PCR = PCRT/10

DTR = DTRP*WM $ DLBI = DLB*WM $ OCR = DCRT*WM

DGA = DGAT*WM S DGBI = DGB*WM $ DPSB = DPSDT/10

10 PRINT 4, TTRP,TB, TCRT, PTR, PBLP, PCR, DTR, DLBI, DCR, DGA, DGBI, DPSB, QB,

1 IX,EX,ER, AL,BE,GA,DE,EP,ET, B1,B2,B3, E1,E2,E3

11 PRINT 5 $ N = 10*DTRP/DCRT + 1 12 DO 20 J=1,N $ S = 0.1*J

13 DN = S*DCRT $ S2=S*S $ SN=S-1 $ SX = S**IX

14 SR = 1 $ IF(ER.GT.O) SR = S-ER

16 B = Bl + B2*S2

17 E = (El + E2*S)*SN*SR*EXP(-GA*SX)

19 TSAT=TS=TSATF(DN) $ TH=THETAF( DN) $ PS=PSATF(TS) $ PIS=PS/10

20 PRINT 6, S, TS,TH,PIS, B,E $ RETURN $ END

FUNCTION PMELTF(T)

C NBUTANE MELTING LINE, BAR, VIA REEVES, SCOTT, AND BABB(JR),

C J. CHEM. PHYS. 40(12), 3662 (1964).

COMMON/l/AL ,BE ,GA,DE ,EP ,ET , DCRT , TCRT, PCRT, DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT ,D2PDT2 ,DPSDT,DPMDT ,DPDD ,DPDR ,DTSDR ,DTHDR ,DDSDT

DATA (A = 3634.0) ,(E = 2.210)

1 X = T/TTRP $ XE = X**E $ PMELTF = PTRP + A*(XE-1)

2 DPMDT = A*E*XE/X/TTRP $ RETURN $ END

FUNCTION PSATF(T)

C NBUTANE VAPOR PRESSURE, BAR, RDG, FEB. 19, 1981. (0CRT=3.92).

C LN(P) = Pl/X + P2 + P3*X + P4*X2 + P5*X3 + P6*( 1-X)**EPP

.

C0MM0N/3/DPDT,D2PDT2,DPSDT, DPMDT, DPDD,DPDR,DTSDR,DTHDR,DDSDT

DIMENSION PJ(6)

DATA (EPP = 1.85)

DATA (TTRP=134.86) ,(TCRT=425.16) ,(DCRT=3.92),(DTRP=12.65)

DATA(PJ = -9.50924729, 5.20153488, 10.64095231,

1 4.86147936, -7.55818629, 18.72886023)

41
1 FORMATdHO 9X *T ABOVE TCRT IN PSATF(T). * / ) 4 X = T/TCRT $ V = 1.0 - X $ IF(V) 7,8,9

7 PRINT 1 $ STOP

8 Z = Zl = 0 $ GO TO 10

9 2= v**EPP $ Zl = -EPP*Z/V

10 PL = PJ(6)*Z $ PLl = PJ(5)*Z1

11 DO 13 K=l,5 $ L = K-2 $ XL = X**L

12 PL = PL + PJ(K)*XL $ PLl = PLl + PJ(K)*L*XL/X

13 CONTINUE $ PSATF = EXP(PL)

15 DPSCT = PL1*PSATF/TCRT $ RETURN $ END

SUBROUTINE PVTDATA

C NBUTANE EOS CONSTANTS, RDG/NBS, FEB. 19, 1981. (DCRT=3.92).

COMMON GK,GKK, 81 ,B2,B3,B4,B5, C1,C2,C3, E1,E2,E3, ER, IX C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT, TCRT, PORT , DGAT,DTRP ,TTRP ,PTRP

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

' C0MM0N/12/ZCRT,ZCALC,DZDT, ZSAT,DZSDT, ZFX, FRT,DFRTDT

COMMON/99/ TI,EZZ, EZ,SZ,CVZ, HZ,CPZ

10 WM = 58.1243 $ TTRP = 134.86 $ TCRT = 425.16

12 DCRT = 3.92 $ DTRP = 12.650

13 PTRP = PSATF(TTRP) $ PORT = PSATF(TCRT)

20 GKK = 0.083145 $ GK = GKK*DCRT $ ZCRT = PCRT/DCRT/GKK/TCRT

21 IX = 2 $ AL = 1.0 $ BE = 0.7 $ GA = 0.14 $ DE = 0

22 EP = 0 $ ER = 2.20 $ ET = 1.1

23 Bl = 0.45555869162 $ B2 = 0.17143942370

24 El =-0.28036114629 $ B3=B4=E2=E3=0

25 DGAT = DENGASF(TTRP) $ WK = 100000/WM $ EZZ = 22644.306

99 RETURN $ END

FUNCTION PVTF(T,D,M)

C NBUTANE EQNSTATE, PVTF = P,BAR. SIMPLIFIED, FEB. 12, 1981.

C NOTE, M=0 RETURNS DP/DT, D2P/DT2. M=l RETURNS ALSO DP/DD.

C P-PSAT = S*GK*(T-TSAT) + S*S*GK*TCRT*F( S ,T) , WHERE - C F(S,T) # B(S)*XBF(S,T) + E( S) *XEF( S ,T) , AND - C B(S) # Bl + B2*S2, E(S) # El*{ S-1 )*{ S-ER)*EXP{ -GA*S**IX)

.

C WHERE, R # DEN/DTRP, S # DEN/DCRT.

COMMON GK,GKK, Bl ,B2 ,B3 ,B4 ,B5 , C1,C2,C3, E1,E2,E3, ER,IX

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT, TCRT, PORT, DGAT , DTRP , TTRP , PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDSDT

C0MM0N/4/XBl,XB2, XC1,XC2, XE1,XE2, DXBDR ,DXCDR ,DXEDR

COMMON/6/ TSAT, THETA, PSAT

C0MM0N/12/ZCRT,ZCALC,DZDT, ZSAT,DZSDT,ZFX , FRT,DFRTDT

1 S = D/DCRT $ S2=S*S $ SN=S-1 $ SR=S-ER $ SX=S**IX

5 GK = DCRT*GKK $ TC = TCRT $ DSDR = DTRP/DCRT

6 RG = S*GK $ GKT = GK*TC

7 TSAT=TS=TSATF(D) $ PSAT=PS=PSATF( TS) $ THETA=THETAF(D)

8 XB = XBF(T,D) $ XE = XEF(T,D)

9 B = B1*S2 + B2*S2*S2

10 XP = EXP(-GA*SX) $ SM = S2*SN*SR $ E = E1*SM*XP

12 F = B*XB + E*XE $ Fl = B*XB1 + E*XE1 $ F2 = B*XB2 + E*XE2

13 PVTF = PS + RG*(T-TS) + GKT*F $ FRT=F/S2 $ DFRTDT=F1/S2/TC

14 DPDT = RG + GK*F1 $ D2PDT2 = GK*F2/TC $ IF{M) 15,30

15 BD = (2*B1 + 4*B2*S2)*S*DSDR

16 XPl = -IX*GA*SX/S $ SMI = (SN+SR)*S2 + 2*S*SN*SR

42
18 ED = E1*(SM*XP1 + SM1)*XP*DSDR

20 Fl = B*DXBDR + BD*XB + E*DXEDR + ED*XE

26 DPDR = (DPSDT-RG)*DTSDR + ( T-TS)*GK*DSDR + GKT*F1

27 DPDD = DPDR/DTRP

30 RETURN $ END

FUNCTION QVAPXF(T)

C QVAP = A1*X + (XE-X)*(A2 + A3*X + A4*X2 + . . ). C X # {TC-T)/(TC-TT), XE # X**E.

DIMENSION AQ(4)

DATA ( NFQ=4 ) , ( EQ=0 . 34 ) , ( TTRP=134 .86 ) , ( TCRT=425 . 16

)

DATA (AQ = 28.789248, 24.163103, 12.710873, -16.533537)

1 FORMATdHO 9X *T EXCEEDS TCRT IN QVAPXF{T). * / ) 2 IF(TCRT-T) 3,4,5

3 PRINT 1 $ STOP

4 QVAPXF = 0 $ RETURN

5 XN = TCRT - TTRP $ X = (TCRT-T)/XN $ XE = X**EQ

6 F = 0 $ DO 7 K=2,NFQ

7 F = F + AQ(K)*X**{K-2)

9 Q = AQ(1)*X + {XE-X)*F

10 QVAPXF = Q*1000 $ RETURN $ END

SUBROUTINE SIMPLE

C FOR ANY GIVEN T,K AND P,MPA, CONVERT TO P,BAR, AND USE SUBROUTINE

C THERMO (OR ENTRIES THEREIN) TO GET THERMOPHYSICAL PROPERTIES.

C THEN CONVERT TO MPA, AND KG/M3 IN PRESENT ROUTINE.

C0MM0N/3/DPDT ,D2PDT2 , DPSDT ,DPMDT , DPDD , DPDR ,DTSDR , DTHDR ,DDSDT

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

COMMON/99/ TI,EZZ, EZ,SZ,CVZ, HZ,CPZ

DATA (R=0. 083145) , {GJ=8. 3145) ,(PA=1. 01325) ,{WM=58. 1243)

14 FORMATdHl 18X *TEST OF THERMO AT P,MPA =* F8.5/

1 19X ^DENSITIES KG/M3, HEATS J/MOL. * / ) 16 F0RMAT(6X4HPMPA 9X1HT 6X3HDEN 8X1HZ 5X5HDP/DT 5X5HDP/DD

1 8X1HE 8X1HH 8X1HS 6X2HCV 6X2HCP 5X1HW 9X3HF/P 5X4HDIEL ) 17 FORMATdX F9.4, F10.3, F9.2, F9.5, F10.5, F10.6, 2F9.1, F9.3,

1 2F8.2, 16, E12.5, F9.5)

C LET US EXAMINE A SUBCRITICAL ISOBAR.

19 PMPA = 3.5

20 P = 10*PMPA $ PRINT 14, PMPA $ PRINT 16

21 DO 90 J=l,39 $ TIK = T = 130 + 10*J

22 CALL THERMO $ IW = W $ Z = P/DEN/R/T

C GET DIEL. CONST., AND FUGACITIES.

25 GIB = H-EZZ-HZ -T*(S-SZ) $ FOP = EXP{GI8/GJ/T)*PA/P

26 IF(T.GT.450) 27,28

27 DIE = 0 $ GO TO 30

28 DIE = DIELF(DEN,T,P)

C CONVERT PRESSURES, DENSITIES, AND DERIVATIVES.

30 PMPA=P/10 $ DEN=DEN*WM $ DPDT=DPDT/10 $ DPDD=DPDD/10/WM

31 DPMDT = DPMDT/10 $ DPSDT = DPSDT/10 $ DDSDT = DDSDT*WM

40 PRINT 17, PMPA, T, DEN, Z, DPDT,DPDD, E,H,S, CV,CP,IW, FOP, DIE

90 CONTINUE $ RETURN $ END

FUNCTION SSATF(T)

C NBUTANE SATLIQ ENTROPY, J/MOL/K.

43
C CONSTRAINED AT TRIPLE AND CRITICAL POINTS.

C Y # (S-SCRT)/(STRP-SCRT) , X # (TC-T)/(TC-TT)

.

C Y = X + (XE-X)*(A1 + A2*X + A3*X2 + . . . ).

DIMENSION AS(6)

DATA (NFS=6) ,(ES=0.23) ,(TTRP=134.86) ,(TCRT=425.16)

DATA (STRP = 133.54372) ,(SCRT = 297.64652)

DATA (AS = 0.08883444348, -0.3470304947, 0.2093724392,

1 -0.9568328496, 0.9579992545, -0.6534607056)

1 FORMATdHO 9X 3HT =F10.5, * IN SSATF(T). * / ) 2 IF{TCRT-T) 3,4,5

3 PRINT 1, T $ STOP

4 SSATF = SCRT $ RETURN

5 YN = STRP-SCRT $ XN = TCRT-TTRP

6 X = {TCRT-T)/XN $ XE = X**ES $ V = XE - X

7 Y = X $ DO 8 K=1,NFS

8 Y = Y + V*AS(K)*X**{K-1)

9 SSATF = SCRT + YN*Y $ RETURN $ END

SUBROUTINE TABLIQ

COMMON/l/AL , BE ,GA ,DE , EP , ET , DCRT .TCPJ ,PCRT , DGAT ,DTRP ,TTRP , PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDSDT

COMMON/5/ TSAT, THETA, PSAT

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

C0MM0N/9/DNG,EG,HG,SG, CVG,CPG,WG, DPGDT,DPGDD

C0MM0N/12/ZCRT,ZCALC,DZDT, ZSAT,DZSDT,ZFX , FRT,DFRTDT

COMMON/99/ TI,EZZ, EZ,SZ,CVZ, HZ,CPZ

DIMENSION DSA(50) ,TSA(60) ,PSA(50) ,DLT(60) ,DPT(50) ,DPD(60)

DATA (0=0.083145) ,(WM=58. 1243)

4 FORMATdHl 13X ^PROPERTIES OF SATURATED LIQUID NBUTANE* //

1 14X IHT IIXIHP 3X5HDEN,L 7X5HDEN,G 5X3HZ,L 5X3HZ,G

2 5X6HDPS/DT 3X6HDDL/DT 3X5HDP/DT 6X5HDP/DD /

3 14X IHK 9X3HMPA 3X5HKG/M3 7X5HKG/M3 16X

4 5X5HMPA/K 2X7HKG/M3/K 3X5HMPA/K 2X9HMPA-M3/KG ) 5 F0RMAT(5XF10.3, E12.5, F8.2, E12.5, 2F8.5, Ell .4,F9.4,F8.4,E11 .4)

11 FORMATdHl 13X ^PROPERTIES OF SATURATED LIQUID NBUTANE * //

1 14X IHT 4X5HQ,VAP 8X1HE 8X1HH 8X1HS

2 6X2HCV 6X2HCS 6X2HCP 6X3HF/P 6X1HW 4X5HDIEL. /

. 3 14X IHK 4X5HJ/M0L 4X5HJ/M0L 4X5HJ/M0L 2X7HJ/M0L/K

4 1X7HJ/M0L/K 1X7HJ/M0L/K 1X7HJ/M0L/K IIX 5HM/SEC 4X5HC0NST ) 12 F0RMAT(5X F10.3, 3F9.1, F9.3, 3F8.2, F9.5, 17, F9.5)

C FOR PAGE ONE OF TABLIQ.

C REPLACE T = 230 BY B.P. AT J = 30.

120 NP = 59 $ PRINT 4

121 DO 150 J=1,NP $ IF(J.EQ.l) 122,123

122 T = TTRP $ GO TO 139

123 IF{J.EQ.29) 124,125

124 T = FINDTSFd. 01325) $ GO TO 139

125 IF(J.EQ.NP) 126,128

126 T = TCRT $ DSA(J)=DG=DL=DCRT $ DLT(J) = DDLDT = 0

127 VG = VL = 1.0/DCRT $ ZG = ZCRT $ GO TO 141

128 T = 130 + 5*J

139 DSA{J) = DL = DENLIQF(T) S DLT(J) = DDLDT = DDSDT

140 DG = DENGASF{T) $ ZG = ZSAT $ VG = 1/DG $ VL = 1/DL

141 TSA(J) =T $ PX = PVTF{T,DL,1) $ DPT(J)=DPDT $ DPD(J)=DPDD

44
147 PSA{J) = PS = PSAT $ Z = PS/DL/G/T

148 PS=PS/10 $ DPSDT=DPSDT/10 $ 0PDT=DP0T/10 $ 0PDD=DPDD/10

149 DL=DL*WM $ DG=DG*WM $ OOLDT=ODLDT*WM $ DPDD = DPOD/WM

150 PRINT 5, T,PS, DL,DG, Z,ZG, DPSDT,DDLDT, DPDT,DPDD

C PAGE 2, TABLIQ. AVOID COEXIST, TIMESAVER.

C USE COEXIST AT ALL TEMPERATURES.

160 PRUJT 11 $ DO 180 J=1,NP $ T = TSA(J) $ P = PSA(J)

161 CALL COEXIST $ DL = DEN $ IW = W

162 DIEL = DIELF(DL,T,P) $ QX = QVAPXF(T)

C GET FUGACITY COEF., (F/P), VIA HZ, SZ, HG, SG.

C NOTE, DI = 0.00001 MOL/L IN EDELF.

170 GIBS = HG-EZZ-HZ - T*(SG-SZ)

171 GO = 100*G $ XP = EXP(GIBS/GJ/T) $ FOP = XP*1.01325/P

172 IF(DNG.LE. 0.00001) FOP = 1.0

180 PRINT 12, T,QX, E,H,S, CV,CSAT,CP, FOP, IW, DIEL

999 RETURN $ END

SUBROUTINE THERMO

C FOR COMPUTATION AT ANY (T,P) POINT.

C ASSUMES AN ISOTHERM IN SINGLE-PHASE ONLY.

C CASES FOR ISOTHERMS BELOW, EQ., ABOVE TCRT,

C GIVEN (T,P), RETURNS DEN, E,H,S, CV,CP,W, DPDT, DPDD.

C ENTRIES BELOW FOR PHASE BOUNDARIES ASSUME A GIVEN ISOBAR P, OR - C ENTRIES BELOW FOR PHASE BOUNDARIES ASSUME A GIVEN ISOTHERM, T.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT, TCRT, PORT, DGAT ,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDSnT

COMMON/8/ IN, IK, P,T,DEN, E,H,S, CV,CP,CSAT, W,WK

COMMON/9/ DNG,EG,HG,SG, CVG,CPG,WG, DPGDT,DPGDD

COMMON/99/ TI,EZZ, EZ,SZ,CVZ, HZ,CPZ

1 FORMATdHO 9X *THERMO, P.GE.PMELT. * / ) 2 FORMATdHO 9X *THERMO DOUBLE-VALUED AT P = PSAT. * / ) 3 FORMATdHO 9X *THERMO, DEN GE. DCRT AT T = TCRT. * / ) 10 IF(T-TCRT) 11,20,25

C SUBCRITICAL ISOTHERMS.

11 PM = PMELTF(T) $ IF(P.GE.PM) 12,13

12 PRINT 1 $ CALL COMPRLQ $ TI=T $ CALL IDEAL $ RETURN

13 PS = PSATF(T) $ IF(P-PS) 14,15,16

14 CALL GENEOUS $ RETURN

15 PRINT 2 $ RETURN

16 CALL COMPRLQ $ TI = T $ CALL IDEAL $ RETURN

C THE CRITICAL ISOTHERM.

20 CALL GENEOUS $ IF(DEN.LT.DCRT) RETURN

21 CP = CV = W = 0 $ PRINT 3 $ RETURN

C ISOTHERMS AT T ABOVE TCRT.

25 CALL GENEOUS $ RETURN

C THERMOM FOR GIVEN ISOBAR AT THE MELTING LINE, GET T. C RETURNS T,DEN, E,H,S, CV,CP,W, DPMDT, DPDT, DPDD.

ENTRY THERMOM

40 T = FINDTMF{P) $ PM = PMELTF(T) $ CALL COMPRLQ

41 TI = T $ CALL IDEAL $ RETURN

C THERMOL FOR GIVEN ISOBAR AT SATURATED LIQUID LINE, GET T. C RETURNS T,DEN, E,H,S, CV ,CP ,CSAT,W, DPSDT,DDSDT, DPDT, DPDD.

ENTRY THERMOL

43 T = FINDTSF(P) $ CALL COEXIST $ RETURN

45
C THERMOV FOR GIVEN ISOBAR AT THE SATURATED VAPOR LINE, GET T. C RETURNS T,DEN, E,H,S, CV,CP,W, DPSDT,DDSDT, DPDT,DPDD.

ENTRY THERMOV

45 T = FINDTSF(P) $ CALL COEXIST $ DEN=DNG $ E=EG $ H=HG $ S=SG

47 CV=CVG $ CP=CPG $ W=WG $ DPDT=DPGDT $ DPDD=DPGDD $ RETURN

C THRMM FOR ISOTHERM AT THE MELTING LINE, GET P. C RETURNS P,DEN, E,H,S, CV,CP,W, DPMDT, DPDT, DPDD.

ENTRY THRMM

50 P = PMELTF(T) $ CALL COMPRLQ $ TI=T $ CALL IDEAL $ RETURN

C THRML FOR ISOTHERM AT SAT. LIQ. LINE, GET P. C RETURNS P,DEN, E,H,S, CV ,CP ,CSAT ,W , DPSDT,DDSDT, DPDT, DPDD.

ENTRY THRML

55 P = PSATF(T) $ CALL COEXIST $ RETURN

C THRMV FOR ISOTHERM AT SAT. VAPOR LINE, GET P.

C RETURNS P,DEN, E,H,S, CV,CP,W, DPSDT,DDSDT, DPDT, DPDD

ENTRY THRMV

60 P = PSATF(T) $ CALL COEXIST

61 DEN=DNG $ E=EG $ H=HG $ S=SG $ CV=CVG

62 CP=CPG $ W=WG $ DPDT=DPGDT $ DPDD=DPGDD

99 RETURN $ END

FUNCTION THETAF{DEN)

C THETA = TSAT*EXP(U(S)).

C LET Q = (S-1)/(ST-1) , WHERE ST = DTRP/DCRT, THEN - C IF S < 1, U = AL*Q**3, IF S > 1, U = -AL*Q**3

,

COMMON/l/AL , BE ,GA ,DE i EP , ET , DCRT ,f CRT , PORT , DGAT ,'dTRP , TTRP , PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT, DPMDT, DPDD, DPDR,DTSDR,DTHDR,DOSDT

COMMON/6/ TSAT, THETA, PSAT

1 S = DEN/DCRT $ DSDR = DTRP/DCRT $ C = DSDR-1

2 Q = (S-l)/C $ Q2 = Q*Q $ U = AL*Q*Q2

3 Ul = AL*3*Q2*DSDR/C $ IF{Q) 5,9,4

4 U = -U $ Ul = -Ul

5 XP = EXP(U) $ THETAF = TSAT*XP

6 DTHDR = (TSAT*U1 + DTSDR)*XP $ RETURN

9 THETAF = TCRT $ DTHDR =0 $ RETURN $ END

FUNCTION TSATF(DEN)

C ITERATE T TO MINIMIZE (DEN-DCALC) VIA DENGASF(T), DENLIQF(T).

C IF ITERATION FAILS, PRINTOUT ONCE ONLY AND STOP AT K = 2.

COMMON/l/AL, BE, GA,DE,EP,ET, DCRT, TCRT, PORT, DGAT ,DTRP , TTRP , PTRP

C0MM0N/3/DPDT ,D2PDT2 ,DPSDT , DPMDT , DPDD ,DPDR ,DTSDR , DTHDR ,DDSDT

DATA (Q=2.0) ,(FN=6. 3890561)

C NOTE, FN # EXP{Q) - 1.0.

1 FORMATdHl 14X *TSATF(DEN) FAILS AT DEN =* E15.7//

1 15X 5HDCALC 13X2HDD 10X5HDDSDT 13X2HDT 12X3HT,K ) 2 F0RMAT(5X 5E15.7)

3 K = 0 $ D = DEN

4 S = D/DCRT $ YN = TCRT/TTRP-1 $ IF(D-DCRT) 5,30,6

5 ST=DGAT/DCRT $ F=ALOG(S)/ALOG{ ST)*( (1-S)/(1-ST) )**2 $ GO TO 7 6 ST=DTRP/DCRT $ U=( ( S-l)/( ST-1) )**3 $ F=( EXP(Q*U)-1)/FN

7 T = TCRT/(YN*F+1)

8 DO 20 J=l,50 $ IF(D-DCRT) 9,30,10

9 DC = DENGASF(T) $ GO TO 11

10 DC = DENLIQF(T)

46
11 DD = D - DC $ IF(ABS(DD/D) .LT.l.OE-7) 25,12

12 DT = DD/DDSDT $ IF(ABS(DT/T) .LT.l .OE-7) 25,13

13 T = T + DT $ IF(T) 14,14,15

14 T = TTRP $ GO TO 18

15 IF(T.LT.TCRT) 18,16

16 T = TCRT - 0.05

18 IF(l<.EQ.l) PRIMT 2, DC, DD, DDSOT, DT, T

20 CONTINUE $ K = K+1 $ IF(K.NE.l) STOP

21 PRINT 1, DEN $ GO TO 4

25 TSATF = T $ DTSDR = DTRP/DDSDT $ RETURN

30 TSATF = TCRT $ DTSDR = 0 $ RETURN $ END

FUNCTION XBF{T,D)

C XBF(R,T) # (X**BE)*EXP(A*(1-TS/T)) - XS**BE, WHERE - C X # T/TC, XS # TS/TC, A # (1-BE) + SQRT(l-BE),

C XBF = U*EXP(A*V) - US, U # X**B, US # XS**B, V # (1-TS/T).

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT, TCRT, PORT, DGAT,DTRP ,TTRP ,PTRP

C0MM0N/3/DPDT ,D2PDT2 ,DPSDT ,DPMDT ,DPDD ,DPDR, DTSDR ,OTHOR ,DDSDT

C0MM0N/4/XBl,XB2, XC1,XC2, XE1,XE2, DXBDR,DXCDR ,DXEDR

COMMON /6/ TSAT, THETA, PSAT

1 B = BE $ BN = 1-B $ A = BN + SQRT(BN)

2 TC=TCRT $ TS=TSAT $ X=T/TC $ XS=TS/TC $ XS1=DTSDR/TC

3 U = X**B $ Ul = B*U/X $ U2 = -BN*U1/X

4 US = XS**B $ USl = B*US*XS1/XS

5 V = 1-TS/T $ VIR = -DTSDR/T $ VIX = TS/T/X $ V2X = -2*V1X/X

6 P = EXP(A*V) $ PI = A*P $ P2 = A*P1

7 PIR = P1*V1R $ PIX = P1*V1X $ P2X = P1*V2X + P2*V1X*V1X

8 XBF = U^P - US $ XBl = U*P1X + U1*P

9 XB2 = U*P2X + 2*U1*P1X + U2*P $ DXBDR = U*P1R - USl

10 RETURN S END

FUNCTION XEF(T,D)

C ULTRA REVISION, MARCH 29, 1981.

C XEF = H(R,T)/HS(R) - 1.0,

C H(R,T) # 1 - {W-WE/E)/1-1/E) , E = ET.

C X#T/TC, F#TS/T, W#(1-TH/T), WE#W**E

C A = DE, B = 1-A, C = EP, E = ET.

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT,TCRT,PCRT, DGAT,DTRP,TTRP,PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,DPDD,nPDR, DTSDR, DTHDR,DDSDT

C0MM0N/4/XBl,XB2, XC1,XC2, XE1,XE2, DXBDR ,DXCDR,DXEDR

COMMON/6/ TSAT, THETA, PSAT

1 E = ET S EK = E/(E-1) $ TC = TCRT

2 TS = TSAT $ TH = THETA $ X = T/TC

3 W = 1.0 - TH/T $ IF(W) 30,30,4

4 CONTINUE

5 WIR = -DTHDR/T $ WIX = TH/T/X $ W2X = -2*W1X/X

6 WE = W**E $ WEI = E*WE/W $ WEIR = WE1*W1R

7 WEIX = WEI^WIX $ WE2X = WE1*W2X + { E-1 )*WE1*W1X*W1X/W

8 H = 1 - EK*{W-WE/E) $ HIR = -EK*( WIR-WEIR/E)

9 HIX = -EK*(W1X-WE1X/E) $ H2X = -EK*{ W2X-WE2X/E)

10 WS = 1.0 - TH/TS $ IF(WS) 11,11,12

11 HS = 1 $ HSl = 0 $ GO TO 16

12 WSl = (TH*DTSDR/TS - DTHDR)/TS

13 WSE = WS**E $ WSEl = E*WSE*WS1/WS

47
14 HS = 1 - EK*{WS-WSE/E) $ HSl = -EK*( WSl-WSEl/E)

16 U = 1.0/HS $ UlR = -U*HS1/HS

17 P = H*U $ DXEDR = H*U1R + 'rllR*U 18 XEl = H1X*U $ XE2 = H2X*U $ XEF = P -- 1 $ RETURN

30 XEF = XEl = XE2 = DXEDR =0 $ RETURN $ END

48
o

O0h-(OIO^COC>JTooooooooo oooooooo

49
100 200 300 400 500 600

Temperature, K

Figure 2. P-T locus of P-p-T data for normal butane.

50
Table 1, Comparisons of vapor pressure data with eq (2). Data sources and ID numbers : (UAston, (2)8eattie, ( 10)Dana , (19)Kay, (29)Sage, (35)Wackher,

(37)Connol ly. (95)Seibert, (96)Carruth

,

(97)Hirata, (98)Tickner, (99)De laplace, (40)Thermal

Loops.

ID Weight Temp. T/Tc P(j( expt) Pg ( ca 1 c

)

Di ff

.

dPa/dT

K MPa MPa % MPa/K

40 1.000 134.860 .31720 .67437E-06 .67358E-06 .12 .128E-06

40 1 .000 140.000 .32929 . 17216E-05 . 17210E-05 .03 .301E-06

40 1.000 145.000 .34105 .39908E-05 .39917E-05 -.02 .646E-06

40 1.000 150.000 ,35281 .86893E-05 .86943E-05 -.06 .130E-05

40 1 .000 155.000 .36457 .17884E-04 . 17897E-04 -.07 .249E-05

40 1 .000 160.000 .37633 .34986E-04 .35012E-04 -.07 .453E-05

40 1 .000 165.000 .38809 .65366E-04 .6541 lE-04 -.07 .789E-05

40 1.000 170.000 .39985 .1 1714E-03 .1 1721E-03 -.05 .132E-04

40 1.000 175.000 .41161 .20212E-03 .20220E-03 -.04 .213E-04

40 1.000 180.000 .42337 .33690E-03 .33697E-03 -.02 .333E-04

40 1.000 185.000 .43513 .5441 1E-03 .5441 1E-03 -.00 .505E-04

40 1.000 190.000 .44689 .85368E-03 .85357E-03 .01 .745E-04

40 1 .000 195.000 .45865 .13044E-02 .13040E-02 .03 .107E-03

1 1 .000 195.107 .45890 .13200E-02 .13155E-02 .34 .108E-03

40 1.000 200.000 .47041 . 19449E-02 .19442E-02 .04 .151E-03

40 1.000 205.000 .48217 .28356E-02 .28345E-02 .04 .208E-03

40 1.000 210.000 .49393 .40497E-02 .40479E-02 .04 .281E-03

1 1.000 212.668 .50021 .48340E-02 .48572E-02 -.48 .327E-03

40 1.000 215.000 .50569 .56740E-02 .56716E-02 .04 .372E-03

40 1.000 220.000 .51745 .78102E-02 .78075E-02 .03 .486E-03

40 1 .000 225.000 .52921 .10576E-01 .10574E-01 .03 .625E-03

1 1 .000 226.276 .53221 .1 141 lE-01 .11396E-01 .13 .565E-03

40 1.000 230.000 .54097 .14106E-01 .14104 E-01 .01 .792E-03

40 1 .000 235.000 .55273 .18550E-01 .18550E-01 .00 .992E-03

1 1 .000 235.822 .55467 .19409E-01 .19379E-01 .15 . 103E-02

40 1.000 240.000 .55449 .24076E-01 .24079E-01 -.01 .123E-02

40 1 .000 245.000 .57625 . 30869 E-01 .30877E-01 -.03 .150E-02

1 1 .000 246.51

1

.57981 .33268E-01 .3321 1E-01 .17 .159E-02

40 1 .000 250.000 .58801 .39131E-01 .39147E-01 -.04 . 182E-02

40 1 .000 255.000 ,59977 .49080E-01 .49 106 E-01 -.05 .218E-02

1 1.000 256.204 .60261 .51832E-01 .51782E-01 . 10 .227E-02

40 1 .000 260.000 .611 53 .60950E-01 .60989E-01 -.06 .259E-02

1 1 .000 262.267 .61 687 .67106E-01 .67078E-0

1

.04 .279E-02

40 1 .000 265.000 .62329 .74991 E-01 .75047E-01 -.07 .305E-02

1 1.000 266.789 .62750 .80656E-01 .80655E-01 .00 .322E-02

40 1 .000 270.000 .63506 .91469E-01 .91543E-01 -.08 .356E-02

1 1 .000 270.397 .63599 .92943E-01 .92966E-0

1

-.02 .360E-02

1 1 .000 272.027 .63982 .98952E-01 .98989E-01 -.04 .379E-02

1 1 .000 272.806 .64 165 .10193E+00 .10197E+00 -.05 .388E-02

29 1 .000 294.260 .69212 .21580E+00 .21562E-K)0 .08 .691E-02

29 1 .000 327.590 .77051 .55660E+00 .5 5724 E+OO -.11 .141 E-01 97 1 .000 333.130 .78354 .64017E+00 .63961 E+OO .09 . 156E-01

97 1 .000 336.420 .79128 .69357E+00 ,69259E+00 .14 . 166E-01

19 1.000 336.480 .79142 .68950E+00 .69359E+00 -.59 . 166E-01

97 1 .000 340.940 .80191 .76916E+00 .77056E+00 -.18 .179E-01

97 1.000 343.070 .80692 .80878E+00 .80946E+00 -.08 . 186E-01

29 1.000 344.260 .80972 .83420E+00 .83180E+00 .29 .190E-01

97 1.000 344.710 .81078 .83836E+00 .84037E+00 -.24 . 191E-01

19 1.000 345.650 .81299 .86180E+00 .85848E+00 .39 .194E-01

2 1.000 348.140 .81884 .90790E+00 .90782E+00 .01 .202E-01

97 1 .000 348.660 .82007 .91476E+00 .9 1838 E+OO -.39 .204 E-01 97 1 .000 348.990 .82084 .92571 E+OO .92513E+00 .06 .205E-01

97 1 .000 352.640 .82943 .99917E+00 .10022E+01 -.30 .217E-01

19 1 .000 353.870 .83232 .10342E+01 .10292E+01 .48 .222E-01

97 1 .000 355.080 .83517 .10550E+01 .10563E+01 -.12 .226 E-01 97 1.000 357.020 .83973 .10981E+01 .1 1008E+01 -.25 .233E-01

97 1 .000 359.020 .84444 .n475E+01 .1 1481E+01 -.05 .240 E-01 29 1.000 360.930 .84893 .12024E+01 .1 1946E+01 .65 .247E-01

97 1.000 361.140 .84942 .1 1995E+01 .11998E+01 -.03 .248 E-01

19 1.000 361.210 .84959 .12066E+01 .12016E+01 .42 .248E-01

97 1.000 363.450 .85485 .12579E+01 .12581 E+01 -.02 .257E-01

97 1.000 365.700 .86015 .13144E+01 .13169E+01 -.19 .266E-01

97 1.000 366.620 .86231 .13399E+01 .13415E+01 -.12 .269E-01

97 1.000 367.850 .86520 .13746E+01 .13749E+01 -.02 .274E-01

19 1.000 367.980 .86551 .13790E+01 .13785E+01 .04 .275E-01

51
Table 1. (Continued).

Data sources and ID numbers : (l)Aston, (2)3eattie, ( 10)Dana1, (19)Kay, (29)Sage, (35)Wackher,

\5 1

)

uonno I I

y

, (yD)beiDerT, \ yo / uarruTri

,

(97)Hirata, (98)Tickner, (99) De 1 ap lace , (40)Thermal

Loops

.

ID Weight Temp. T/Tc Pg( expt) Pij(calc) Di f f

.

dPrr/dT K MPa MPa t MPa/K

97 1 .000 359.620 .86937 . 14225E+01 . 14240E+01 -. 1

1

.281 E-01

2 1 .000 373. 1 40 .87765 .15290E+01 .15256E+01 .22 .296E-01

97 1 .000 373.580 .87868 .15385E+01 .15386E+01 -.01 .298E-01

19 1 .000 373.980 .87962 .15513E+01 .15506E+01 .05 .299E-01

97 1 .000 375 .040 .8821

1

.15785E+01 .15826 E+01 -.25 .304 E-01 97 1 .000 377.240 .88729 . 16505E+01 . 16505E+01 -.00 .314E-01

19 1 .000 379 .430 .89244 . 17237E+01 . 17202 E+01 .20 .323 E-01

19 1 .000 384.710 .90486 .18961E+01 . 18974E+01 -.07 .348 E-01

97 1 .000 385.710 .90721 .19319E+01 .19324 E+01 -.03 .353 E-01

19 1.000 389.370 .91582 . 20684 E+01 .20648E+01 .17 .371 E-01 97 1.000 391 .010 .91968 .21239E+01 .21263E+01 -. 12 .379E-01

97 1 .000 396.090 .93163 .23251E+01 .23259E+01 -.03 .407E-01

2 1 .000 398, 140 .93645 .24207E+01 .24104 E+01 .43 .418E-01

97 1 .000 401 .300 .94388 .25465E+01 .25455E+01 .04 .437E-01

2 1 .000 423. 140 .99525 .36730E+01 ,36696 E+01 .09 .612E-01

10 0.000 255.030 .59984 .49620E-01 .49171E-01 .91 .218E-02

10 0.000 260.490 .61269 .62230E-01 ,62266E-01 -.06 .263 E-02

10 0.000 271 .350 .63823 .97540E-01 ,96451E-01 1.13 .371 E-02

10 0.000 272.960 .64202 .10172E+00 .10257E+00 -.83 .389 E-02

10 0.000 272.960 .64202 .10230E+00 . 10257E+00 -.26 .389 E-02

10 0.000 283.420 .66662 .15040E+00 .15007 E+00 .22 .523 E-02

10 0.000 290.530 .68346 .19330E-K)0 .19130E+00 1 .04 .631 E-02

10 0.000 29 1 . 9 1

0

.68659 .19520E+00 .19984 E+00 -2.32 .652 E-02

10 0.000 298.690 .70254 .25000E+00 .24794E+00 .83 .769E-02

10 0.000 304.860 .71705 .30320E+00 .29894 E+00 1 .42 .886E-02

10 0.000 31 0.280 .72980 .35210E+00 ,3499&E+00 .61 .998E-02

10 0.000 314.420 .73953 . 39690 E+00 ,39313E+00 .96 .109E-01

10 0.000 322.080 .75755 .48140E+00 ,48338E+00 -.41 . 127E-01

10 0.000 TOO r\Ci r\ 322.080 .75755 .48640E+00 ,48338E+00 .62 . 1 27 E-0

1

10 0.000 322. 1 50 .75771 .48930E+00 ,48427E+00 1 .04 . 127E-01

10 0.000 330. 100 .7764

1

.59080E+00 ,593 52 E+00 -.46 .148E-01

10 0.000 330. 100 .77641 .59770E+O0 ,59352E+00 .70 .148E-01

10 0.000 330.630 .77766 .60010E+00 ,60140E+00 -.22 .149E-01

10 0.000 330.630 .77766 .60480E+00 ,60140E+00 .57 .149E-01

19 0.000 325.040 .76451 .51710E+00 ,52209 E+00 -.96 .135E-01

29 0.000 310.930 .73132 .35180E-K)0 ,35649E+00 -1.31 .101E-01

35 0.000 205.450 .48323 .31300E-02 . 29293 E-02 6.85 .214E-03

35 0.000 213. 150 .50134 .56700E-02 ,50169E-02 13.02 .336E-03

35 0.000 228. 1 50 .53662 .13280E-01 .12699E-01 4.57 .727E-03

35 0.000 241 .850 .56884 .27650E-01 ,26436E-01 4.59 .132E-02

35 0.000 250.450 .58907 .41450E-01 ,39970E-01 3.70 .185E-02

35 0.000 255.450 .60083 .51260E-01 ,50093E-01 2.33 .221 E-02

35 0.000 261 .850 .61589 .66390E-01 .65923E-01 ,71 .275 E-02

35 0.000 266.050 .62576 .78570E-01 ,78300E-01 .35 .315E-02

35 0.000 273. 150 .64246 .10338 E+00 .10331 E+00 ,06 .392E-02

35 0.000 278.750 .65564 .12732E+00 .12713E+00 .15 .460E-02

37 0.000 344.260 .80972 .83086E+00 .83180E+00 -.11 .190E-01

37 0.000 360.930 .84893 .1 1946E+01 .1 1946E+01 -.00 .247E-01

37 0.000 377.590 .8881

1

.16638 E+01 .16615E+01 .14 .315E-01

37 0.000 394.260 .92732 .22575E+01 .22524E+01 .23 .397 E-01

37 0.000 406.870 .95698 .28 037 E+01 .2798 5 E+01 .18 .472E-01

37 0.000 410.930 .96653 .300T3E+01 .29959E+01 .18 .501 E-01 37 0.000 425. 120 .99991 .3784 5 E+01 .37934 E+01 -.24 .642 E-01 95 0.000 303. 150 .71303 .34000E+00 .28408E+00 19.68 .853E-02

95 0.000 313. 150 .73655 .44660E+00 .37949E+00 17.69 .106E-01

95 0.000 323. 150 .76007 .57330E+O0 .49712E+00 15.33 .130E-01

95 0.000 333. 150 .78359 .71990E+00 .63992E+00 12.50 .156E-01

95 0.000 343.150 .8071

1

.89330E+00 .81095E+00 10.16 .186E-01

95 0.000 363. 150 .85415 .14265E+01 .12505E+01 14.08 .256E-01

95 0.000 373. 150 .87767 .16665E+01 ,15259E+01 9.22 .296E-01

95 0.000 383. 150 .901 19 . 19598E+01 ,18437 E+01 6.30 .341 E-01 95 0.000 393.150 .92471 .24131 E+01 ,22087E+01 9.25 .391 E-01

95 0.000 403.150 .9482_ .27464E+01 .26274 E+01 4.53 .448 E-01 96 0.000 135.430 .31854 .90230E-06 .75036E-06 20.25 . (41E-06

52
Table 1. (Cont i nued )

.

Data sources and ID numbers: (l)Aston, (2)Beattie, (lO)Oana, ( 19)l<ay, (29)Sage, (35)Wackher,

(37)Connol ly, (95)Seibert, (96)Carruth, (97)Hirata, (98)Tickner, ( 99) De I ap I ace , (40)Thermal

Loops.

ID Weight Temp, T/Tc P„(expt) Prf(calc) Di ff. dPg/dT

K MPa MPa % MPa/K

96 0.000 137. 730 .32395 . 10800E-05 . 1 1483E-05 -5 .95 .208E-06

96 0.000 138.930 .32677 . 14490E-05 . M248E-05 1 .70 .254E-06

96 0.000 146. 320 .344 15 . 51 320E-05 .493 1 1 E-05 4.08 .78 1 E-06

96 0.000 148. 100 .34834 .678 1 OE-05 .651 32t-05 A 11 4.11 . lOOE-05

96 0.000 1 54.840 .36419 . 18450E-04 . 17503E-04 5. 4

1

. 244 E-05

96 0.000 1 59.790 .37583 .32260E-04 .3407 1 E-04 -5.32 .442E-05

96 0.000 171 .430 .40321 . 12590E-03 . 13750E-03 -8.44 . 1 52 E-04

96 0.000 184.090 .43299 .4do50E-03 .49978t-03 -2.64 .469 b-U4

96 0.000 1 94 .650 .45783 . 12420E-02 . 1 25d9E-02 -1 .97 . 105E-03

96 0.000 196.710 .46267 . 1 5390E-02 . 1 4988t-02 2.68 .121E-03

96 0.000 205.270 .48281 .31320E-02 .28910E-02 8.33 .21 1 E-03

96 0.000 209.280 .49224 .37740E-02 .38501 E-02 -1 .98 .269E-03

96 0.000 212.900 .50075 .49480E-02 .49335E-02 .29 .331 E-03

98 0.000 135.850 .31953 .66660E-06 .81 196E-06 -17.90 . 152E-06

98 0.000 139.950 .32917 . 1 3330E-05 . 17060E-05 -21 .86 .299E-06

98 0.000 144.250 .33928 .26660E-05 .35332E-05 -24.54 .578E-06

98 0.000 149.950 .35269 .66660E-05 .86294E-05 -22.75 . 129E-05

98 0.000 1 54.750 .36398 . 13330E-04 . 17284E-04 -22.88 .241 E-05

98 0.000 1 59.850 .37598 .26660E-04 .34338 E-04 -22.36 .445E-05

98 0.000 166.950 .39268 .66660E-04 .82509E-04 -19.21 .969E-05

98 0.000 172.850 .40655 . 13330E-03 . 16065E-03 -17.02 . 174 E-04

98 0.000 179.250 .42161 .26660E-03 .31277E-03 -14.76 .312E-04

98 0.000 188.450 .44324 .66660E-03 .74455E-03 -10.47 .663E-04

98 0.000 195.850 .46065 . 13330E-02 . 1 3979E-02 -4.64 . 1 14E-03

99 0.000 135. 1 50 .31788 . 17330E-05 .71 170E-06 143.50 . 135E-06

99 0.000 1 36. 1 50 .32023 .20000E-05 .85875E-06 132.90 . 160E-06

99 0.000 137. 150 .32258 .22660E-05 . 10330 E-05 1 19.36 . 189E-06

99 0.000 138. 150 .32494 .25730E-05 . 12390E-05 107.67 .223E-06

99 0.000 139. 150 .32729 .30000E-05 . 14816E-05 102.48 .263 E-06

99 0.000 140.150 .32964 .39060E-05 .17667E-05 121.09 .308E-06

99 0.000 142.150 .33434 .45330E-05 .24913E-05 81 .95 .421 E-06

99 0.000 143.150 .33670 .53330E-05 .29465E-05 80.99 .491 E-06

99 0.000 144.150 .33905 .62000E-05 .34758E-05 78.38 .570 E-06 u.uuu • /ZUUvJt:-U-5 /D.UO .DDUt-(JD

99 0.000 146.150 .34375 .83330E-05 .47998E-05 73.51 .763 E-06

99 0.000 147.150 .34610 .96790E-05 .56196E-05 72.24 .879E-06

99 0.000 148.150 .34846 .11332E-04 .65636E-05 72.65 .101 E-05

99 0.000 149.150 .35081 .14000E-04 .76483E-05 83.05 .1 16E-05

99 0.000 150.150 .35316 .17065E-04 .88917E-05 91 .92 . 133E-05

99 0.000 151.150 .35551 .19865E-04 .10314E-04 92.60 . 152E-05

Number of data points used in fit = 80; rms pressure deviation = 0.189^.

53
Table 2. Comparisons of saturated liquid density data with eq (3).

Data sources and ID numbers: (2)Carney, (7)Coffin, (8)Connolly, (lO)Dana, (15)Foehr,

( 17)Benol iel , (18)Kahre, (19)Kay, (25)0lds, (29)Sage, ( 32) S I i w i nsk i , (33)NGAA, (90)Haynes,

(91)0rrit, (92)McClune, (93)Van der Vet.

1 n1 U we 1 y nT Temp • (T^ T\/<T PiU"no n c 1 "t" \/ i> 1 I y

( expt) U 1 T T . /Ha. /HT

IS

rrw~» mo 1 / 1 1 / L

k -1 /fii3 IN J/ flM p Ky/ ^ m-^»is 1

90 1 AAA 1 .000 1 T C; A"7 K

1 35.0 ID .yyyzo 1 O CO "7"^ C 11 /35.3

/

It. c; A~7 Ayl .04 C\A A \ - .944 1 O 1 1 AAA 1 .000 1 "^Q A^ 1

1 JO .04 1 • yoyu4 1 1 c^QR

1 Z • 0^0 AQ ! DZ %/Li A"^ Q/l ICS 90 1 AAA 1 .000 1 yi A A~7 c 140.0/3 A O O A >1 .yo.d04 /30.OD Ay! .04 Ayl OT -•y4^3

n 1 1 AAA 1 .000 1 /I o A/1 n 1 4z .04y .y /5/4 I Z • DDZ "700 A O /<CO .4Z /zo .49 A 1 -.01 CiA 1 Q -. y4 1

8

no92 1 AAA 1 .000 1 ^ "Z 1 CA 1 43. 1 PO at i A A

• 9 /144 1 Z. 31

4

"70"7

1 Z 1 ,5o 1 Z 1 .40 A 1 -.01 - Ayl 1 c

. y4 1

5

An90 1 AAA 1 .000 ^ A c A"? c; 145.0/3 •yoHo

1

1 O ACi'~>

1 z •4yz ~70(^ AO izo* oy /z 0-? A^ .00 - Qyl 1 A . y4 1

0

91 1 AAA 1 .000 14/. loo AC cyt "7 •y554

/

1 z .44

1

"70 "Z 11 iZ5» 1

1

/z J .1)9 AA .00 -.y404 Ayl Ayl 92 1 .000 148 . 1 50 .95422 1 2»435 722 .76 "7-1 O 1 u. AA .00 - . 94 04

90 1 .000 1 50.075 .94759 1 2»409 72 1 . 28 720.94 .05 -.9401

92 1 .000 1 53. 1 50 .93700 12 .357 ~7 1 O OO 718.22 T 1 0 AC 71 0 .05 AO .02 -.9397

91 1 .000 1 53.204 A"Z O 11 z»354 ~7 1 O A y1 / 1 0 .04 T 1 0 AA / 1 0 .00 A 1 .01 A "ZA "7 - .9597

90 1 .000 1 55.075 .93037 12 .330 716.67 7 1 6 .24 .06 -.9395

92 1 .000 1 58. 1 50 .91977 1 2.276 71 3.53 71 3.36 .02 -.9394

91 1 .000 ICO COT 1 58 . 587 A 1 O OT •91827 1 o ^cc T 1 O Ayl/ 1 ^.94 "7 1 '> r\A/ 1 2 . 94 A A -.00 -.9394

90 1 .000 160.075 .91314 1 2.248 71 1 . 93 71 1 .55 .05 -.9394

92 1 .000 163. 1 50 .90255 1 2 . 1 96 708.87 708.65 .03 -.9395

91 1 .000 164.010 : .89959 1 2. 179 707.91 707.85 .01 -.9395

90 1 .000 165.075 .89592 12. 163 705.99 706.85 .02 -.9396

92 1 .000 1 68. 1 50 .88533 12.116 704.25 703.96 .04 -.9400

9

1

1 .000 169. 522 .88050 12.092 702.8

1

702.67 .02 -.9402

90 1 .000 170.075 .87869 12.084 702.37 702. 15 .03 -.9403

92 1 .000 173. 150 .86810 12.035 599. 55 699.26 .04 -.9409

91 1 .000 174.925 .85198 1 2.003 597.59 597.59 .01 - . 94 1

4

91 1 .000 180.442 .84298 1 1.915 692.52 692.39 .02 -.9431

91 1 .000 186.368 .82257 1 1 .8 17 686.88 585.79 .01 -.9456

9

1

1 .000 1 O 1 "70 C\ 191 •789 .80390 1 1 .728 68 1 .66 68 1 .66 -.00 - . 94 84

91 1 .000 1 97.248 .78509 1 1 .636 676.35 676.47 -.02 -.9519

91 1 AAA 1 .000 Z04 • ZOO "7^ A O yl . /60o4 11 coo 1 1 . 522 009.08 569.75 A 1 -.01 -.9572

y 1

1 AAA 1 . 000 ZUo •ZZ /

"7 A "70 "7

1 1 .458 665.96 665.98 AA -.00 -.9606

O 1 y 11 AAA 1 .000 Z 1 ^» o4o "70"7AO

» 1 z. lyz 1 1 T^O 1

1

»5oZ A yi o DOO .4^ /CCA C/C D00.5D AO -•Oz -.9061

y 1

1 AAA 1 .000 O 1 TCI Z 1 9»353 "7 AO A C

. 70895 1 1 OT 1 11.2/1 £ C C 1 yi 655. 14 ^ C C 0*7 655. 23 A 1 -•01 A~700 -,'9 IZZ

y 1

1 AAA 1 .000 ZZ4%^ /O C O A£ A .68960 11 1 "7 yi 11.1/4 64y .45 C A C\ ~7 C 649.75 A^ ".04 A~7 A 1 -.y /91 33 1 .000 226.820 .68322 1 1 . 143 647.70 647.93 -.04 -. 98 1

6

yu 1 AAA 1 .000 O'ZA AAA Z30.000 "700*7 mOiZZ/ 11 A A

1

1 1 .091 a A A cc D44 .00 a A A OA d44 .oU AO -•Oz -.yaoo

A 1 y 1 1 AAA 1 .000 O'Z T TA 1 z33.3y

1

^C^f\ CA .DD05y 1 1 .034 CLA 1 "^C 04 1 .35 yr ^ 1 yl c 04 1 .45 no -•Uz QO 1 A -. yy 1

0

Z"Z 1 AAA 1 .000 O C Q "7A Z35.0 /O a coAc .o5Z05 1 A AAO 1 o.yy-i CKO AA 638. yo XZQ AO 638. yy A 1 -.01 -.yy48 A Ayl Q 55 1 . 000 238 .650 .64247 1 0.942 636. 00 636.22 A"2 -.03 -.9993

A 1 y 11 AAA 1 .000 24 1 . 557 .63245 1 0.892 633.07 633.31 -.04 1 A A yi "Z -1 .0043

91 1 .000 247.21

5

.61 297 10.793 627.35 627.50 -.04 -1 .0146

33 1 .000 247.760 . 6 11 09 1 0.791 627.20 627.04 .03 -1 .0157

91 1 .000 252.249 .59553 10.702 522.05 622.46 -.07 -1 .0246

33 1 .000 255.370 .58488 10.662 51 9.70 519.26 .07 -1 .0312

33 1 .000 255.430 .58467 10.558 519.50 619. 19 .05 - 1 . 03 1

4

91 1 .000 258.254 .57494 1 0.597 61 5.95 615.27 -.05 -1 .0377

91 1 .000 263.785 .55589 10.496 6 1 0 . 09 6 1 0 . 50 -.07 -1 .0508

33 1 .000 266.480 .54661 10.464 608.20 607.66 .09 -1 .0576

91 1 .000 269.401 .53654 10.393 604. 1

1

604 . 56 -.07 -1 .0652

91 1 . 000 274.973 .51735 10.289 598.05 598.58 -.09 -1 .0808

33 1.000 277. 150 .50985 10.259 596.30 596.22 .01 -1 .0873

32 1 .000 283.200 .48901 1 0. 145 589.67 589.58 .01 -1 . 1064

90 1 .000 288.706 .47004 10.033 583.13 583.44 -.05 -1 .1253

33 1 .000 288.710 .47003 10.047 584.00 583.44 . 10 -1 .1253

90 1 .000 290.000 .46559 10.007 581 .63 581 .98 -.06 -1 .1299

32 1.000 293.190 .45460 9.949 578.28 578.36 -.01 -1.1418

33 1 .000 299.820 .43176 9.822 570.90 570.70 .04 -1 .1685

90 1.000 300.000 .431 14 9.810 570.22 570.49 -.05 -1 . 1693

32 1 .000 303.150 .42029 9.752 566.82 566.79 .01 -1 .1829

33 1.000 310.930 .39349 9.597 557.80 557.44 .06 -1.2197

25 1.000 310.930 .39349 9.585 557.16 557.44 -.05 -1.2197

32 1.000 313.120 .38595 9.545 554.78 554.76 .00 -1.2309

33 1 .000 322.040 .35522 9.363 544 . 20 543.56 .12 -1.2809

32 1.000 323.120 .35150 9.327 542.13 542.17 -.01 -1.2875

32 1.000 333.110 .31709 9.102 529.06 528.99 .01 -1 .3547

54
Table 2. (Continued),

Data sources and ID numbers: (2)Carney, (7)Coffin, (8)Connolly, (lO)Dana, (15)Foehr,

( 17)Benol iel , (18)Kahre, (19)Kay, (25)0lds, (29)Sage, (3:-? ) S I i wi nski , (33)NGAA, (90)Haynes,

(91 )Orr it. ( 92) McO 1 une p (93)Van der Vet.

1

D

Weight Temp. ( rc-T)/( Ic-Tt) Dens 1 ty ( expt) Dens 1 ty ( ca 1 c

)

U 1 T T • ^A- / A'V apj_/a 1 K mol/L kg/in3 kg/m3 % kg/(m3.K)

33 1 .000 333. 1 50 .31695 9. 108 529.40 528.93 .09 -1 .3550

32 1 .000 343.080 .28274 8.863 515.18 5 1 5 . 09 .02 -1 .4354

25 1 .000 344.260 .27868 8.833 51 3.4

1

51 3.39 .00 -1 .4450

32 1 .000 353.090 .24826 8.606 500.24 500. 24 -.00 -1 .5348

32 1 .000 363. 1 10 .21374 8.330 484.20 484.26 -.01 -1 .6603

32 1 .000 368. 100 .19656 8. 186 475.82 475.79 .01 -1 .7360

25 1 .000 377.590 .16386 7.899 459. 1

1

458.51 .13 -1 .91 48

25 1 .000 410.930 .04902 6.405 372.26 373.21 -.25 -3.8043

2 0.000 227.594 .68055 11.131 647.00 647. 17 -.03 -.9825

2 0.000 233 . 1 50 .66142 1 1 . 038 64 1 .50 54 1 .69 -.01 -.9906

2 0.000 238.706 .64228 1 0.944 635. 10 635. 15 -.01 -.9994

2 0.000 244.261 .6231

5

10.849 530.60 530. 59 .00 - 1 . 009

1

2 0.000 249.817 .60401 10.755 525. 10 524 .95 .02 -1 .0197

2 0.000 255.372 .58487 10.662 619.70 61 9. 25 .07 - 1 . 03 1

3

2 0.000 266.483 .54660 1 0.464 508.20 607.55 .09 -1 .0576

2 0.000 277. 150 .50985 1 0.259 596.30 595.22 A 1 .01 -1 .0873

2 0.000 288.706 .47004 10.047 584.00 583.44 .10 -1 . 1253

2 0.000 310.928 .39350 9. 597 557.80 557.45 •06 -1 .2197

2 0.000 "Z 0 T A "Z A 5/2.039 .35522 9.353 544.20 543.55 .12 -1 .2809

z 0. IJlJU A 1 AOy. 1U0 CO A >l A 529.40 528.93 AA 1 T C C A -1 .3550

1 0.000 .64213 1 0.946 at c OA O35.20 636. 1

2

A 1 •01 -.9995

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71 A AAA U.UUU 000 C EC A ZOO •o!)U y1 ~7 A'3 / 1 A AC /I 1U.U^4 c 0 yi Ar\ 5o4 .4U CCZ CA 5c J . 5U • 1 D1 1 0 C 1 -1 . Iz51

-7 A AAA 0.000 A A 1 A CA z9 1 .950 .45887 A AO "7 9.987 CO A CA 580.50 C "7 A 11 5 / 9.77 1 1 "Z "7 1 -1.1371

1 A AAA 0. 000 OA^ A CA 296 .450 .44337 9.905 c 7 '7'"^ 5 74.62 1 A

• 19 -1.1 546

1 0.000 AA A ^ C A 299.650 .43235 9.832 571 .50 570.90 • 1

1

-1 . 1678

1 0.000 302.450 .42270 9.774 568 . 1

0

557.61 • 09 -1 . 1798

7 0.000 305.650 .41 168 9.710 554.40 563.81 • 10 -1.1 943

8 0.000 293. 1 50 .45474 9.960 578.90 578.40 • 09 -1.1417

8 0.000 298. 150 .43751 9.862 573.20 572.65 ^ . 10 -1 . 1615

1 0 0.000 273. 1 50 .52363 10.309 599.20 500. 54 -•22 -1 .0756

10 0.000 281 . 150 .49607 10. 153 590.70 591 .84 -. 19 -1.0997

10 0.000 AO A 1 c r\ 289. 150 .46852 10.013 582.00 582 .94 -. 16 -1 . 1269

10 0.000 297. 1 50 .44096 9.850 572.50 573.81 -.23 -1 . 1574

10 0.000 305. 1 50 .41 340 9.695 553 . 50 564 .41 -. 16 -1 . 1920

10 0.000 313. 150 .38584 9.528 553.80 554.72 -. 17 -1 .231

1

10 0.000 32 1 . 1 50 .35828 9.352 543.50 544.70 -.20 -1 .2755

10 0.000 329. 1 50 .33073 9.161 532.50 534.30 -.34 -1 .3255

15 0.000 293. 150 .45474 9.953 579. 10 578.40 .12 -1.1417

1

7

0.000 21 3. 1 50 .73031 1 1 .383 551 .50 661 .24 •06 -.9554

1 / 0.000 AO 1 1 C

A

223. 150 .69587 11.216 651 .90 651 .53 .06 -.9768

1 / 0.000 233. 1 50 .66142 1 1 .047 642. 10 54 1 .69 .06 -.9905

17 0.000 243.150 .62697 10.875 532.10 631.71 .06 -1 .0071

17 0.000 253.150 .59252 10.701 522.00 521.54 •07 -1 .0265

17 0.000 263.150 .55808 10.519 511.40 51 1 .16 .04 -1.0492

17 0.000 273.150 .52363 10.337 600.80 600.54 •04 -1.0756

17 0.000 283.150 .48918 10.147 589.80 589.64 • 03 -1.1062

17 0.000 293.150 .45474 9.955 578.70 578.40 .05 -1.1417

18 0.000 288.750 .46989 10.054 584.40 583.39 • 17 -1.1254

18 0.000 327.550 .33624 9.238 535.95 535.41 • 10 -1.3158

19 0.000 325.040 .34488 9.309 541.10 539.59 • 26 -1.2995

55
Table 2. (Continued).

Data sources and ID numbers: (2)Carney, (7)Coffin, (8)Connolly, (lO)Dana, (15)Foehr,

( 17)Benol iel , ( 18)Kahre, (19)Kay, (25)0lds, (29)Sage, (32)SI iwinski , {33)NGAA, (90)Haynes,

(91)0rrit, (92)McClune, (93)Van der Vet.

ID Weight Temp. {Tc-T)/(Tc-Tt) Dens i ty ( expt) Density (calc) Diff. dP£,/dT K mol/L kg/m3 kg/m3 % kg/(m3.K)

19 0.000 336.480 .30548 9.045 525.73 524.38 .26 -1.3802

19 0.000 345.650 .27389 8.827 513.07 51 1 .37 .33 -1 .4589

19 0.000 353.870 .24557 8.618 500.90 499.04 .37 -1.5436

19 0.000 361 .310 .21994 8.414 489.05 487.23 .37 -1 .6354

19 0.000 367.980 .19697 8.215 477.51 476.00 .32 -1.7341

19 0.000 373.980 .17630 8.031 466.78 465.29 .32 -1 .8404

19 0.000 379.430 .15753 7.854 456.53 454.95 .35 -1.9564

19 0.000 384.710 .13934 7.670 445.00 444.27 .34 -2.0925

19 0.000 389.370 .12329 7.493 435.54 434.19 .31 -2.2392

19 0.000 393.760 .10816 7.314 425. 13 424.00 .27 -2.4093

19 0.000 402.040 .07964 6.931 402.87 402.32 .14 -2.8669

19 0.000 405.870 .06645 6.730 391 .17 390.76 .10 -3. 1830

19 0.000 409.320 ,05456 6.529 379.48 379.15 .09 -3.5714

19 0.000 412.870 .04234 6.292 365.70 365.51 .05 -4.1501

19 0.000 415.980 .03162 6.046 351.44 351.47 -.01 -4.9439

19 0.000 419.260 .02032 5.743 333.83 333.05 .23 -6.4725

19 0.000 422.320 .00978 5.330 309.80 308.68 .36 -10. 1943

29 0.000 294.260 .45091 10.007 581 .64 577. 13 .78 -1 .1460

29 0.000 310.930 .39349 9.650 560.87 557.44 .61 -1.2197

29 0.000 327.590 .33610 9.301 540.61 536.36 .79 -1 .3161

29 0.000 344.260 .27868 8.919 518.40 513.39 .98 -1 .4460

29 0.000 350.930 .22125 8.449 491 .06 487.85 .66 -1 .6303

29 0.000 377.590 .16386 7.928 460.83 458.51 .51 -1 .9148

29 0.000 394.260 .10644 7.258 421.87 422.79 -.22 -2.431

1

91 0.000 135.366 .99826 12.640 734.70 734.79 -.01 -.9439

91 0.000 139.441 .98422 12.574 730.88 730.95 -.01 -.9425

91 0.000 144.783 .96582 12.489 725.91 725.92 -.00 -.941

1

91 0.000 150.530 .94602 12.397 720.55 720.52 .00 -.9400

91 0.000 155.930 .92742 12.310 715.48 715.44 .01 -.9395

91 0.000 161 .370 .90868 12.221 710.35 710.33 .00 -.9394

91 0.000 166.654 .89048 12.138 705.49 705.37 .02 -.9398

91 0.000 172. 198 .87138 12.047 700.24 700. 15 .01 -.9407

91 0.000 177.707 .85240 1 1.959 695.10 694.97 .02 -.9422

91 0.000 183.502 .83244 11.864 689.57 689.50 .01 -.9443

91 0.000 189.090 .81319 1 1.772 684.23 684.22 .00 -.9470

91 0.000 194.492 .79458 11.683 679.09 679.09 -.00 -.9501

91 0.000 202.744 .76616 1 1.544 670.99 671 .23 -.04 -.9559

91 0.000 205.434 .75689 1 1 .503 668.61 668.66 -.01 -.9582

91 0.000 21 1.023 .73764 1 1.41

1

663.23 663.29 -.01 -.9633

91 0.000 216.623 .71835 1 1 .318 657.86 657.88 -.00 -.9691

91 0.000 222.085 .69953 1 1.226 652.52 652.57 -.01 -.9755

91 0.000 230.623 .67012 1 1.083 644.16 644.19 -.00 -.9869

91 0.000 236.1 1

1

.65122 10.988 638.64 638.75 -.02 -.9952

91 0.000 244.335 .62289 10.844 630.28 630.51 -.04 -1 .0092

91 0.000 249.972 .60347 10.744 624.47 624.79 -.05 -1.0200

91 0.000 255.364 .58490 10.649 618.94 619.26 -.05 -1.0312

91 0.000 261.019 .56542 10.547 613.04 613.40 -.06 -1.0441

91 0.000 266.732 .54574 10.443 607.00 607.39 -.06 -1 .0582

Qy 1

1 u.uuu Ann 1

Q

DUU •DO — HQ •UO —— 1 Cilf^X 1 •U / DS> 93 0.000 283. 150 .48918 10.130 588.80 589.64 -. 14 -1.1062

93 0.000 288.710 .47003 10.023 582.60 583.44 -.14 -1.1253

93 0.000 293.150 .45474 9.944 578.00 578.40 -.07 -1 . 1417 93 0.000 298.150 .43751 9.846 572.30 572.65 -.06 -1.1615

93 0.000 303.150 .42029 9.746 566.50 566.79 -.05 -1. 1829 93 0.000 308.150 .40307 9.641 560.40 560.81 -.07 -1.2061

93 0.000 313.150 .38584 9.538 554.40 554.72 -.06 -1.2311

93 0.000 318. 150 .36862 9.435 548.40 548.50 -.02 -1.2582

93 0.000 323.150 .35140 9.328 542.20 542.14 .01 -1 .2877

Number of data points used in f i t = 71; rms density deviation = 0.054^.

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r^c7Nr--o — K^"— yor^inincN^r^ — >*oohoo ONCTNOCMOOOCMO^oinocncooovO'^i^ON OOONin>i)OOOtnoOhOLOCO'— ON|-~vDr<~l'*CMC3N ^^ooOln^CM^DOlnc^^lnooK^oo«*^DCJ^ t^^vOt^Ch— >— CNCNIhO'S-inoO'— CMfO-tJ-VDl^

— f^Csl^OinK^r~-CMvOOvCMON\ClLn oO'3l^l^^^c^ — incjNvDi^in — CO ^OvO(~~coC3NO"— K^'S-inyOt^CJNCsiin

in<;t'3-Ot^l^^coin — CMinhor-i^CMinoCTN i£icDOK>v£)Oooinmcor^<T>int^incM\0'*vo OO"— — — CM(NrO'a-*or~-0'— CMrOinr-—

O

ooooooooooooooo oooc^ — r^vom^r^CMhor--oovDCM

o^ — inr~-fOr-'-oco^~iC7>coONCMro

ooooooooooooooooooo ^nlnlnlnlnlnoolnl^oo^~^^O^^CT^yD^oo^^oo — ^VDOOON-^CNCJNinCNICJNinCMCM

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>— o>(^inro — vOinrOroO»9-Op--^Ot^tr^

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oooooocjNCjNCjNCJNONCjNcyiCTNONCJNCJNONrNj

.— — •- — '— — >— — •-— --CMrslCMCMrNlCMCNhO

c CJN (Nl CM (N <N CM CM CM CNJ CM CM CM CM CM CM CM CM (Nl — CM CM CNI CM CM CM o (N to O ?? O o o o o o o o ?? o o O

?

o o o o ?

O o O O O O O ?? o O O • u + + + + + + + + + + + + + + + + + + + + + + + + + + o

LU UJ LU LU UJ LU UJ LU LU UJ LU LU LU LU LU LU LU LU LU LU LU LU LU LU LU UJ LU LU 'JJ LU LU LU LU LU 00 >— 0^ in vo ON CM in O o r~ K> in in O CNJ r-- C7N ON OO II • >- \ ON C7N C7> 00 ON o hn 00 ON CO On CM a\ CO ^- — a^ VD ON O r~ O ON CO — o ON (N rsi "O H CO O — to CO 'd- ^ K1 CM in ON 0\ O CM ON CJN \D CM vD O 1^ O CM 0\ r- r~ in o CNJ 00 c

in in o vO CMONU^^C^JUDO — (Nl in VD ctn m ^ in O in ^ OO K^ o o KN 1^ CO o

0) O CO in m >£) P~- OO C7N c^ in ON CM CM >* ^ in CO CNj <£> c +->

<D o

in

II

0) n

E3

58
Table 4. Comparisons of second virial coefficients with eq (5).

Data sources and ID numbers: (2)Beattie (1939), (3)Beattie (1942), (4)Bottomley (1964),

(5)Bottom!ey (1977), ( 19)Kay, (25)0ids, (26)Gunn, (?7)Jones, (28)Kapal!o, (29)Sage,

(30)Kretsclimer, (31 )McGlashan, (32)Tripp, (33)Strein, (35)Das, (37)Connolly.

ID We i g ht Temp. T /T T/Tc QD Bp( expT) bp ( Cd 1 C ) D 1 tt

,

Di tt.

w

IS cm^/mo

1

% OQ 1 r\f\(\ 9/1 A AA Z4'4 • UU ,9/4 1 9TA A

A

- 1 Z_)U, UU -4A Q99 ,oZZ -4A D TQ ,090 A1 7 T/I

, 34 4 1 •UUU 97X A<^ Z / j.Uu tkA 9 , D4Z QQ 7 AA -oy / ,uu T R 1 A -J, 9 lo -9,D4y ITT , 1 33 T R 3,09

Zo 1 .UUU 97 -I /I A Z / J • 4U ,04 J 09^ AA -yZ J , UU -_),o 1 O -9,09o A9A • UZU RR , 99 jD 1 AAA 1 . UUU 90 A AA ZoUoUU .opy A A9 AA -yuz ,uu -9 , 9 JO T /I T A -J ,49U -, 1 A^ lUO -3,T 1 A1 U Zo 1 AAA 1 . UUU 9Q9 7A ZBZ . jU , D04 -.QA9 —CSdZ AA , UU -J , J /y -J , 90

1

-, A 1 Q U 1 0 — RT , JJ

1 AAA 1 . UUU ZOJ . 1

D

, ODD —— QylA AA C540,UU —J, 9 1

O

-9, JJO A9 A , UZU RQ , jy

79 \ . UUU 9R^ ZD J . \«1

O

, ODD _DCO AA OOZ , UU -TJ , 9T7Q/y —9 , 990 — , Uh9 — 11 , 90zy

j£. 1 nnn , ODD -Rfi9 OD^ oUUnn J • J 1 y J , J9D , UH9 _ 1 OA ^9J£. 1

1 . nnn UUU , ODD -RR1 oo 1 , nnUU 9 , '+9^ 9 , 999 - ,11' 117 -^9 • 9ZR9 J^RJ

1

1 • nnn UUU 7QA z^u . nnuu , DOZ -R9S OZ , nnUU 9 , Z9^ 9, 1 ^D _ AQQ , UOO -9Z ,OURn

1 nnn 9Qfi 1 n , O jD -7d^ nn -9Z Q 1 , y 1 9 -9^, QQn 7 7U , n77 u / / 9Z , 99oR 9R 1

1 .UUU nnn 9Q71 % nnUU fiQQ -7Sfl / JO , nnUU -9 071 -9 , QftR y DO - , nn4 UU*t - 1 9

A 1

1 . nnn UUU 9Q7 zy \tL/ . 1 ^ , oyy — 77S / j9, nnUU — 9 RH

1

— Z , 00

1

—9Z , Qftd yOH ,Uo9 ART Z,qU 9 fln

1

1 .UUU nnn TAA AA _)UU .UU 7nfi , / UD _7R7 ~ 1 J 1 ©UUnn — 9z Qft7 , yo / —9— ROfi z ,oyo —— ,Un 79/

Z

-9— Z ,^AV/ jL 1

1 .UUU nnn TA^ r\A 71 T , / 1 -J _7/|c; — AA / 4 9 , UU —— z

9 , Q9n y ZU —— 9Z R9fi , OZO —— no R , uy9 _T— Tfi 9 • 90

^9 1

1 .UUU AAA Z A-J A>1 7 1 T —— 7/

1

1 RJ , nnUU —— 9Z ,OU9 RAT —9— R9ft Z , OZO ,UZ9 n9T fl 1 T9 1

1 AAA • UUU "^A"^ r\A jUj. U4 7 1 T , / 1 J) —f^QI AA —oy 1 . UU _9 7AQ —z , /uy ——

9Z ,OZO Q9A 117 • 11/ A4,141 /) T9JZ 1 AAA 1 .UUU TAT r\A 3U3.U4 7 1 X AQ R AA -oy J.UU 9 79/1 -Z , / Z4 -Z,oZD 9 Q9A 1 A 1 , 1 U 1 T RR J , 90 9QZo 1 AAA 1 . UUU TA AA 3U3 . OU 7 1 Q , / 1 y - 7 1 Q AA / 1 O , UU 9 Q 1 R -Z ,9 1 9 - 9 7^, Q Z , / D 9 -, A/I U4o -1,0/

DD 1 AAA 1 .UUU 7 no E^A 3Uy . DU 7 O'J

, / Zo -OD 1 , UU 9 RQ

1

-z, jy

1

9 AQ/1 -Z,Do4 AOT ,uy3 T y1 Q 3,4o

z5 1 AAA 1 .000 Z 1 A r\A 31U.y4 . 73 1 "I AT Cf\ -/U/,dU O "7~7 /I -Z , / /4 O £ R /I -Z,0 94 -,119 1 1 A A RA -4, 50 zo

1 AAA 1 .000 Z 1 T AA 31 z.OO , /34 O yl AA -0/4,00 o /I o -Z,d4Z o c z z -z,533 AAA -,009 Z ^ -,36

35 1 AAA 1 .000 Z OA AA 3z0 .00 T C Z ,753 C A A AA -d44 ,0U -2 , 524 O A1 -Z ,4 /O -,048 -1 ,94 ZD 1 AAA 1 .UUU Z O 1 AA 32 1 .UU 7

. /55 CZ^ AA -o3 5,UU O ^ O A -z,4oy O /I RO -Z,458 ATI -,031 1 O "7 -1,2/

32 1 .000 323.2

1

,760 -599.00 -2.348 -2,418 ,070 2,88

32 1 .000 323.21 .760 -602.00 -2.360 -2,418 ,058 2,39

32 1 .000 323.21 ,760 -619.00 -2,426 -2,418 -,009 -,37

32 1 .000 323.21 ,760 -64 1 .00 -2,513 -2,418 -,095 -3,93

4 1 .000 323. 16 ,760 -606.00 -2,376 -2,419 ,043 1 ,78 4 1 .000 325.68 ,766 -595.00 -2,332 -2,374 ,041 1 ,74

33 1 .000 334 . 60 ,787 -555.70 -2, 178 -2,225 ,046 2,08

35 1 .000 340.00 ,800 -554,00 -2, 172 -2,141 -,031 -1 ,43

25 1 .000 344.27 ,810 -544,20 -2. 1 33 -2,078 -,055 -2,55

26 1 .000 344,30 ,810 -505,70 - 1 .982 -2,078 ,095 4,60

4 1 .000 346.46 ,81

5

-522,00 -2.046 -2,047 ,001 ,04

33 1 .000 353, 10 ,831 -489.20 -1.918 -1 ,957 ,039 1 .99 35 1 .000 360,00 ,847 -48 1 .00 -1 .886 -1 ,869 -,017 -.90

27 1 .000 368.25 ,865 -443.49 -1 .738 -1 ,77

1

,033 1 .84 z7 1 .000 368.25 ,865 -444.20 - 1 .74

1

-1 ,771 ,030 1 .58

4

1 AAA 1 .000 370.86 ,872 -449 .00 -1 ,760 - 1 ,742 -,018 -1 .06 Z/ 1 AAA 1 .UUU Z "7 Z OO 373, zZ O "TO ,878 -427.53 1 C ~1 c - 1 ,576 - 1 .716 ,040 2.32

Z/ 1 AAA 1 .UUU Z T Z OO 0"70 ,878 -429. 50 - 1 ,684 - 1 .716 ,032 1 .87

•z*z 1 AAA 1 .UUU Z7 >1 OA 3/4, ZU O O A

• ooU >1 Z 1 OA -43 1 .oO 1 £ A Z - 1 ,693 1 ~7 A R -1 .705 A 1 Z ,013 .73 9RZP 1 AAA 1 .UUU Z77 tz.r\ 3/ /,oU o c o ,ooo >1 Z Z O 1 -433.21 1 AO -1 ,698 - 1 .569 AOA -, 029 - 1 .74

9<C Zo 1 AAA 1 .UUU Z7 7 C A 3/ /,DU o o o .888 yl o ^ AA -4z4.y0 - 1 ,06d - 1 .o5y ,004 O 1 .21 Z/ 1 AAA 1 .UUU 378 , 1

8

O A A .890 -4 1 8 . 30 - 1 ,640 - 1 .563 ,023 1 .40

Z/ 1 AAA 1 .UUU Z "70 1 O 3/0, lo O AA ,890 -4 1 8.00 -1 ,639 - 1 ,563 ,025 1 .48 33 1 AAA 1 • UUU zo A AA 3oU,UU o A yi ^ O 1 AA -4Z 1 .UU 1 C K A - 1 ,090 - 1 a A A

1 , 544 AA^C -,005 Z £i -.35

•» -z JJ 1 AAA 1 .UUU XQX QA 3y3, oU 09A ,yzD ZQ R OA -3o5.yu -1,913 1 R 1 Z -11 RIO ,9lZ AA 1 -,UU 1 -.00A^; 4

1 AAA 1 .UUU Z07 1.A 3y /, 34 QT R z Q o AA -3oy, UU 1 RO R -1

,

jZj - 1 ^ O A

1 ,4o

J

A /I R -, U49 Z A 1 -3.01

9"7 Z /

1 AAA 1 « UUU ZQQ 1 A 3yo, 14 ,y3D -3"Z7 A AO /U,UZ - 1 A RA

1 ,450 -11 /I 7Z ,4/3 AO Z ,UZ3 1 R R1 .55 97Z /

1 AAA 1 . UUU Z QQ 1 A 3yo, 14 ,y3o -3Z7^^ AA /D,UU - 1 A ~l A

1 ,4/4 - 1 A' iX

1 ,4/3 AA 1 -, UU 1 A/1 -. U4 35 1.090 400,00 ,941 -371,00 -1,454 -1,457 ,003 .20

26 1.000 410,90 ,966 -353,60 -1,386 -1 ,358 -,018 -1 .33 25 1.000 410,94 .967 -358,02 -1,403 -1,368 -.035 -2.62

33 1 .000 413,00 ,971 -345.90 -1 .356 -1,352 -.004 -.31

35 1.000 420.00 .988 -329.00 -1.290 -1,299 ,010 .75

27 1.000 423. 14 .995 -325.61 -1 ,276 -1 ,277 .000 .04 27 1.000 423.14 ,995 -326,10 -1,278 -1,277 -.001 -.12

2 1.000 423. 16 ,995 -328,75 -1,289 -1 ,277 -.012 -.94

3 1.000 423,16 ,995 -328,70 -1,289 -1,277 -.012 -.92

4 1.000 426,37 1,003 -331,00 -1 ,298 -1 ,254 -.043 -3.45

26 1.000 427,60 1,006 -322,10 -1,263 -1,246 -.017 -1.35

59
Table 4. (Continued),

Data sources and ID numbers: (2)3eattie (1939), (3)Beattie (1942), (4 ) Bottom I ey (1964),

(5)Bottomley (1977), ( 19)Kay, (25)Olds, (26)Gunn, (27)Jones, (28)Kapallo, (29)Sage,

(30)Kretschmer, (31 ) McG I ashan , (32)Tripp, (33)Strein, (35)Das, (37 )Connol I y.

ID Weight Temp. T/Tc B Br.(expt) Bp(calc) Diff. Diff.

K cm-" /mo 1 %

33 1.000 433.30 1 .019 -314.30 -1 .232 -1,208 -.024 -2.02

35 1.000 440.00 1.035 -294.00 -1.152 -1.165 .012 1.06

25 1 .000 444.27 1 .045 -289,98 -1 . 137 -1.139 .002 .18 26 1.000 444.30 1.045 -293.40 -1.150 - 1 . 1 39 -.012 -1.02

2 1 .000 448.16 1 .054 -286. 14 -1.122 -1.116 -.006 -.54

3 1.000 448,16 1,054 -287.30 -1. 126 -1.1 16 -.01

1

-.95

27 1 .000 448, 18 1,054 -286.24 -1.122 -1.116 -.007 -.59

27 1.000 448.18 1,054 -284.80 -1.1 16 -1.116 -.001 -.08

26 1 .000 460.90 1 .084 -272.20 -1.067 -1.044 -.023 -2. 16 35 1.000 470.00 1.105 -250.00 -.980 -.997 .017 1.74

33 1.000 472.80 1.112 -253.30 -.993 -.983 -.009 -.96

2 1 .000 473.16 1,1 13 -252.71 -.991 -.982 -.009 -.91

3 1.000 473. 16 1,113 -254,20 -.996 -.982 -.015 -1 .50 27 1.000 473,21 1,113 -255,50 -1.002 -.981 -.020 -2.05

27 1 .000 473,21 1,113 -256,30 -1.005 -.981 -.023 -2.37

25 1.000 477,60 1,123 -237,28 -.930 -.960 .030 3.14

26 1 .000 477,60 1,123 -245,90 -.964 -.960 -.004 -.38

33 1 .000 498,00 1,171 -220,30 -.864 -.870 .006 .69

2 1.000 498,16 1,172 -223,37 -.876 -,869 -.007 -.77

3 1.000 498.16 1,172 -224,50 -.880 -,869 -.01

1

-1.28

27 1 .000 498 70 1 . 1 77 -228. 48 - 077

27 1.000 498.20 1.172 -228.70 -.897 -,869 -.028 -3.19

35 1 .000 500.00 1,176 -215.00 -.843 -,861 .019 2.16

26 1.000 510.90 1,202 -199.90 -.784 -,818 .035 4.22

25 1 .000 510.94 1.202 -193.83 -.779 -.818 .039 4.72

2 1,000 523.16 1,231 -193.19 -.777 -.773 -.004 -.51

3 1.000 523,16 1,231 -198.10 -.777 -.773 -.004 -.47

35 1,000 530,00 1,247 -186.00 -.729 -.749 .020 2.67

35 1 .000 560,00 1,317 -161.00 -.631 -,655 .024 3.68

2 1.000 573,16 1.348 -154.09 -.604 -,619 .015 2.38

3 1 .000 573.16 1.348 -157.40 -.617 -,619 .002 .28

5 0.000 316,18 .744 -612.30 -2.400 -2.549 .149 5.85

5 0.000 341 ,49 .803 -518.90 -2.034 -2,119 .085 4,00

5 0.000 341,54 .803 -503.60 -1 .974 -2,1 18 .144 6,80

5 0.000 341,75 .804 -512.00 -2.007 -2,115 .108 5,11

5 0.000 341,83 .804 -513,30 -2.012 -2,114 .102 4,81

5 0.000 367,09 .863 -432,90 -1 .697 -1 .784 .087 4,90

5 0.000 367,13 .864 -432.30 -1 .695 -1.784 .089 5,00

5 0.000 367,83 .865 -435.30 -1.706 -1.776 .069 3,91

5 0.000 367,99 ,866 -429.70 -1.684 -1.774 .090 5.05

5 0.000 396,39 ,932 -368.60 -1 .445 -1.489 .044 2.94

5 0.000 396,46 .932 -367.60 -1.441 -1.488 .047 3.16

5 0.000 396,60 .933 -363.80 -1 .426 -1 .487 .061 4.08

5 0.000 427,88 1.006 -303.80 -1.191 -1.244 .053 4.26

5 0.000 427.88 1.006 -306.50 -1 .201 -1.244 .042 3.41

5 0.000 462.69 1.088 -248.60 -.975 -1.035 .060 5.84

5 0.000 462,86 1.089 -246.60 -.967 -1 .034 .067 6.51

5 0.000 463,32 1.090 -243.90 -.956 -1.032 .076 7.32

5 0.000 498,81 1.173 -213.90 -.838 -.866 .028 3.21

5 0.000 498,98 1.174 -201.40' -.789 -.866 .076 8.79

5 0.000 537,16 1.263 -167.10 -.655 -.725 .070 9.68

5 0.000 537,32 1.264 -160.50 -,629 -.725 .096 13.19

5 0.000 537,38 1 .264 -158.10 -,620 -.725 .105 14.46

5 0.000 579,46 1.363 -125,90 -,494 -.602 .109 18.05

5 0.000 580,48 1 .365 -124,60 -.488 -.600 .111 18.54

19 0.000 310,94 .731 -742,80 -2.912 -2.554 -.257 -9.69

19 0.000 338,72 .797 -585.19 -2,294 -2. 161 -. 133 -6. 18 19 0.000 366,49 .862 -502,69 -1,971 -1.791 -.179 -10.01

19 0.000 394.27 .927 -421.99 -1,654 -1.508 -. 147 -9.73

19 0.000 422.05 .993 -333.38 -1,307 -1.285 -.022 -1.73

19 0.000 449.83 1.058 -294.38 -1,154 -1 .106 -.043 -4.34

19 0.000 477.60 1.123 -257.05 -1,008 -.960 -.047 -4.93

60
Table 4. (Cont inued )

.

Data sources and ID numbers: (2)Beattie (1939), (3)Beattle (1942), (4 ) Bottom I ay (1964),

(5)Bottomley (1977), ( 19)Kay, (25)Olds, (26)Gunn, (27)Jones, (28)Kapallo, (29)3age,

(30)Kretschmer, (31 )McGlashan, (32)Tripp, (33)Strein, (35)Das, (37)Connol I y.

1 n1 U We i g ht Temp. T/T D

dpi ex p r

;

Dp \ Co 1 C J n ; P f u 1 r T . n I f f U 1 T T .

i\ cm^ /mo 1 d

f>

1 o u • uuu PUj . JO 1

1 .

1

1 RQoy —ZZj . 0

/

—~ Q/in • 0^ \j — • UJ 1 A AO

1 Q u«uuu J . ID 1 9'^4 —9n 1 ^^7 —ZU 1 . J

/

_ 7QQ —— .Un mJ 1 _fi — ftQ 0 .oy

1 o nu • nnn uuu JDU .1

1 • J 11 Q^ I O ^ . J 1 _ 71c: — nfi ^ . UOJ -0— <^4 y . 0'+

1

1 Q^ nu» nnn uuu "iRft 79 1 . JO J -IfiR 1 oo 9Q

.

• DOU _ K7Q - ns 1 . UO 1 - 1 Q7

n non 1 n Qd 7^ 1 . / J 1 -fifin fii -? son -9 fiSA nfis 9 44

nJ • nnn uuu ^77 fin 771 -filfi '^^ U t U . JJ -9 "^4.0 - .un7fi/ u J . J nu • nnn uuu ^44 97 . SIO 1 nu -'ifi7 JU / . S7J

/

-9 99 S -9z • n7ft u / 0 _ 147 -7/ . nRUJ nu • nnn uuu JUU

.

fi&Q -S9'^ fi7 -9 ns"^ - 1 RS7 _ 1 qc

. 1 -in 'i'^ 1 U . > J 9Q nu • nnn uuu ^77 fin . ooo -sni JU "14 1 . JH 1 • ^Uu _ 1 f:;f;q _ 907 - 1 7 7Q

9Q n nnn 997 -479 9ft - 1 RSI -11 • JKJO SOR . JH -t -99^ ^ .0R 1

t n nnn ^03 Ifi . 7/

11 J3 -7fii nn -9 Qft"^ -9 ^9"^ z • oz_y - . ifin 1 uu J fift . 00

XIJ \ n nnn 9Qfi 40 697 -790. on -9 ft99 -9Z • Qft9 70Z . 1 uu J. JU

1. 1 J \ n.onn .723 -667.00 -9.797 z • / z / 1 1

9

4.19

T

1

J 1 nu • nnn uuu 1 fi 90 74R -fiiQ O 1 -7 . nnuu -9 A9fi -9 Sin . nft4 UOH J • JH

D 1 nJ • nnn uuu J^O ^9ft . on7U 9 11& f / H -Sfift joo .uunn -9 997 —9 "^1

A

"z • J 1

0

nQ9 J Qfi . yo

T 1 J 1 nu«uuu nnn z^7 on J J ( . OU . 7QR / y J — pix'^ nn — JJ J.UU — z«uoy 1 7 R AQ R .Uo J X Q9 J .y^

J 1 nu • nnn uuu -KAQ /in J'to . 'fU .ofi 1

1 Qy _Rni — JU 1 . nnuu _—

1 QA>1 1 • yD4 —z wUzU .U JD 9 7Q

7 1 J 1 n nnn U • uuu x^i5 >in J JO .4U . OHJ —HDD .uu 1 007 _—

1 QQ Q 1 •ooy AA9 J. ZO

31 0.000 368.40 .866 -440.00 -1.725 -1 .769 .045 2.52

J

1

U« UUU J / / .yu .otsy -4yi 1 n on 1 U. UU - 1 .OU

/

- 1 .boo A CA 3.53

31 0.000 387.60 .912 -383.00 -1 .501 -1 .569 .068 4.33

—' 1 0.000 400.40 .949 -353 J J J . on(Jv - 1I . JO^ ^R4 -11 .H4S4JH .un7n/ u 4 •0ft9z 31 0.000 413.40 .972 -322.00 -1 .262 -1.349 .086 6.40

37 0.000 344.26 ,810 -517.00 -2.027 -2.078 .052 2.49

37 0.000 360.93 .849 -464.70 -1.822 -1.857 .036 1 .92 37 0.000 377.59 .888 -418.60 -1.641 -1.669 .028 1.70

37 0.000 394.26 .927 -381 .30 -1 .495 -1 .508 .013 .86 37 0.000 406.87 .957 -356.10 -1.396 -1.400 .004 .29

37 0.000 410.93 .967 -348.60 -1 .367 -1.368 .001 .09 37 0.000 444.26 1.045 -289.80 -1.136 -1.139 .003 .24

Number of data points = 94; rms deviation = 2.11?.

61
Table 5. Behavior of coefficients of equation of state for normal butane (eq (6)).

P/Pc To e

K K

.10 348,775 326.499

.20 379.794 362.591

.30 397.551 385.396

.40 408.763 400.847

.50 415.972 41 1.292

.60 420.518 418.089

.70 423.211 422.177

.80 424.589 424.282

.90 425.091 425.053

1.00 425.160 425. 160 1.10 425.081 425.043

1.20 424.595 424.287

1.30 423.384 422.351

1.40 421 ,193 418.760

1 .50 417,816 413.115

1 .60 413,099 405.099

1.70 406,927 394.485

1 .80 399,224 381.141

1.90 389,940 365.035

2.00 379,049 346,239

2.10 366,541 324.930

2.20 352,424 301.385

2.30 336,719 275.985

2.40 319,471 249.196

2.50 300,745 221.563

2.60 280,642 193.688

2.70 259,299 166.199

2.80 236,894 139,716

2.90 213,646 1 14.817

3.00 189.803 91,993

3.10 165.632 71,616

3.20 141.394 53,922

3,30 1 17.329 38,996

Pg B(P) C(p) MPa

.9207 .45827 -.52914

1.7320 .46342 -.44607

2.3859 .47199 -.36821

2.8891 .48399 -.29608

3.2581 .49942 -.23011

3.5131 .51828 -.17061

3.6739 .54056 -.1 1780

3.7597 .56628 -.07177

3.7916 .59542 -.03254

3.7960 .62800 0.00000

3.7909 .66400 .02603

3.7600 .70343 ,04583

3.6845 .74629 .05975

3.5526 .79258 .06819

3.3593 .84230 .07161

3.1062 .89544 .07053

2.8012 .95202 .06547

2.4561 1.01202 .05700

2.0860 1.07546 .04567

1.7079 1.14232 .03203

1.3394 1.21261 .01663

.9975 1.28633 .00000

.6976 1.36347 -.01738

.451 1 1.44405 -.03505

.2641 1.52806 -.05259

.1361 1.61549 -.06964

.0592 1 .70635 -.08588

.0205 1.80064 -.10103

.0052 1.89836 -.1 1488

.0008 1.99951 -.12724

.0001 2.10409 -.13800

.0000 2.21210 -. 14707

.0000 2.32353 -. 15442

62
63
Table 7. Comparisons of experimental P-p-T data of normal butane

with eq (6).

Summary of P-p-T data comparisons.

. — Range of Data IMo. of Dev i at ions

Authors T(K) P(MPa) p( kg/m3

)

Poi nts Ap/p, rms AP/P,mean

(%) {%)

Beattie [31 423-573 1.5 - 36.3 29-494 115 0.54 0.56

Kay [441 31 1-589 0.2 - 8.3 5-513 437 0.50 0.43

Olds [51] 311-511 0.07- 68.9 1-632 209 0.27 1.18

Sage [64] 294-394 0.1 - 20.7 2-610 154 0.75 11.27

Haynes [351 140-300 1.7 - 36.1 572-745 105 0.06 4.55

Virial equation

(this report) 300-700 0.2 - 0.6 5.8 41 0.26 0.24

Total number of points used in fit = 907

Overall rms density deviation = 0.42?

Overall mean pressure deviation = \.09%

64
Table 7. (Continued)

Data sources and ID numbers:

(XXXX)Haynes.

(l)Virial Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage

ID Data Weight Temp. Dens i ty Dens i ty Dens i ty f^expt ^ca 1 c Pressu Point ex pt calc Diff. Diff.

No. K mol/L kg/m^ kg/m-5 i MPa MPa %

1 1 .000 300.000 .100 5.81 5.78 .52 .2310 .2321 -.48

2 1.000 310.000 .100 5.81 5.79 .40 .2402 .241

1

-.38

3 1 .000 320.000 .100 5.81 5.80 .30 .2493 .2500 -.28

4 1.000 330.000 .100 5.81 5.80 .20 .2583 .2588 -. 19

5 1.000 340.000 .100 5.81 5.81 .12 .2673 .2676 -.11

6 1.000 350.000 .100 5.81 5.81 .05 .2762 .2763 -.04

7 1.000 360.000 .100 5.81 5.81 -.02 .2851 .2850 .01

8 1.000 370.000 .100 5.81 5.82 -.07 .2939 .2937 .07

9 1 .000 380.000 .100 5.81 5.82 -.11 .3027 .3024 .11

10 1.000 390.000 .100 5.81 5.82 -.15 .3115 .31 10 .15

1

1

1.000 400.000 .100 5.81 5.82 -.19 .3202 .3196 .18

12 1.000 410.000 .100 5.81 5.82 -.21 .3289 .3283 .21 13 1.000 420.000 .100 5.81 5.83 -.24 .3376 .3369 .23

14 1.000 430.000 .100 5.81 5.83 -.25 .3463 .3455 .25

15 1 .000 440.000 . 100 5.81 5.83 -.27 .3550 .3540 .26

16 1.000 450.000 .100 5.81 5.83 -.28 .3636 .3626 .27

17 1.000 460.000 . 100 5.81 5.83 -.29 .3722 .3712 .28

18 1.000 470.000 .100 5.81 5.83 -.30 .3808 .3797 .29

19 1.000 480.000 .100 5.81 5.83 -.30 .3894 .3883 .29 20 1.000 490.000 .100 5.81 5.83 -.30 .3980 .3968 .30

21 1.000 500.000 .100 5.81 5.83 -.31 .4066 .4054 .30

22 1.000 510.000 .100 5.81 5.83 -.31 .4152 .4139 .30 23 1 .000 520.000 . 100 5.81 5.83 -.31 .4237 .4224 .30

24 1.000 530.000 .100 5.81 5.83 -.30 .4322 .4310 .30 25 1.000 540.000 .100 5.81 5.83 -.30 .4408 .4395 .30

26 1.000 550.000 .100 5.81 5.83 -.30 .4493 .4480 .29 27 1.000 560.000 .100 5.81 5.83 -.29 .4578 .4565 .29

28 1.000 570.000 .100 5.81 5.83 -.29 .4663 .4650 .28 29 1.000 580.000 . 100 5.81 5.83 -.28 .4748 .4735 .28 30 1.000 590.000 .100 5.81 5.83 -.28 .4834 .4820 .27

31 1.000 600.000 .100 5.81 5.83 -.27 .4918 .4905 .27 32 1.000 610.000 .100 5.81 5.83 -.26 .5003 .4990 .26 33 1 .000 620.000 .100 5.81 5.83 -.26 .5088 .5075 .25 34 1 .000 630.000 .100 5.81 5.83 -.25 .5173 .5160 .25 35 1.000 640.000 .100 5.81 5.83 -.24 .5258 .5245 .24

36 1.000 650.000 .100 5.81 5.83 -.24 .5343 .5330 .24

37 1.000 660.000 .100 5.81 5.83 -.23 .5427 .5415 .23 38 1.000 670.000 . 100 5.81 5.83 -.22 .5512 .5500 .22 39 1.000 680.000 .100 5.81 5.82 -.22 .5597 .5585 .21 40 1 .000 690.000 . 100 5.81 5.82 -.21 .5681 .5669 .21

41 1.000 700.000 .100 5.81 5.82 -.20 .5766 .5754 .20

65
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)Olds, (29)Sage,

(XXXX)Haynes.

Data Weight Temp. Density

Point expt

No, K mol/L kg/mDensity Density ^expt ^calc Pressure

caic Diff. Diff.

I<g/m^ % MPa MPa %

3 42 1.000

3 43 1 .000

3 44 1.000

3 45 1.000

3 46 1.000

3 47 1.000

3 48 1 .000

3 49 1.000

3 50 1.000

3 51 1.000

3 52 1.000

3 53 1.000

3 54 1 .000

3 55 1.000

3 56 1.000

3 57 1.000

3 58 1.000

3 59 1.000

3 60 1 .000

3 61 1.000

3 62 1.000

3 63 1.000

3 64 1.000

3 65 1.000

3 66 1.000

3 67 1.000

3 68 1 .000

3 69 1.000

3 70 1.000

3 71 1.000

3 72 1 .000

3 73 1.000

3 74 1.000

3 75 1.000

3 76 1.000

3 77 1.000

3 78 1.000

3 79 1 .000

3 80 1.000

3 81 1.000

3 82 1.000

3 83 1 .000

3 84 1.000

3 85 1.000

3 86 1.000

3 87 1 .000

3 88 1.000

3 89 1.000

3 90 1.000

3 91 1.000

3 92 1.000

3 93 1.000

3 94 1.000

3 95 1 .000

3 96 1.000

423.150 .500

448.150 .500

473.150 .500

498.150 .500

523.150 .500

548.150 .500 573.150 .500

423.150 1.000

448.150 1.000

473.150 1.000

498.150 1.000

523.150 1.000

548.150 1.000

573.150 1.000

423.150 1.500

448.150 1.500

473.150 1.500

498.150 1.500

523.150 1.500

548.150 1.500

573.150 1.500

423.150 2.000

448.150 2.000

473.150 2.000

498.150 2.000

523.150 2.000

548.150 2.000

573.150 2.000

423.150 2.500

448.150 2.500

473.150 2.500

498.150 2.500

523.150 2,500

548.150 2.500

573.150 2.500

448.150 3.000

473.150 3.000

498.150 3.000

523.150 3.000

548.150 3.000

573.150 3.000

448.150 3.500

473.150 3.500

498.150 3.500

523.150 3.500

548.150 3.500

573.150 3.500

448.150 4.000

448.150 4.000

473.150 4.000

473.150 4.000

498.150 4.000

498.150 4.000

523.150 4.000

523.150 4,000

29.06 28.97

29.06 29.00

29.06 29.01

29.06 29.02

29.06 29.04

29.06 29.05

29.06 29.06

58.12 57.67

58.12 57.67

58.12 57.69

58.12 57.73

58.12 57.75

58.12 57.84

58.12 57.87

87.19 86.46

87.19 86.31

87.19 86.31

87.19 86.44

87.19 86.51

87.19 86.68

87.19 86.79

116,25 115.51 116.25 115.22

116.25 115.24

116.25 115.44

116.25 115.74

116.25 115.91

116.25 116.10

145.31 144.87

145.31 144.31

145.31 144.55

145.31 144.91

145.31 145.17

145.31 145.59

145.31 145.84

174.37 173.57

174.37 174.12

174.37 174.60

174.37 174.91 174.37 175.44

174.37 175.70

203.44 202.22

203.44 203.09

203.44 203.85

203.44 204.21

203.44 204.86

203.44 205.17

232.50 229.40

232.50 229.77

232.50 231.80

232.50 231.15

232.50 232.98

232.50 232.27

232.50 233.69

232.50 232.90

.33 1.4875

.22 1 .6121

. 19 1.7337

.14 1 .8542

.09 1 .9738

.05 2.0924

.02 2.2099

.77 2.5007

.79 2.7864

.74 3,0641

.68 3.3356

.64 3.6021

.49 3.8686

.43 4.1300

.83 3.1350

1.00 3.6153

1.01 4.0753

.85 4.5262

.77 4.9659

.58 5.4037

.45 5.8343

.63 3.4846

.89 4. 1857

.87 4.8514

.70 5.5009

.43 6. 1423

.29 6.7705

.13 7.3937

.30 3.6406

.69 4.5748

.52 5.4634

.28 6.3328

. 10 7. 1870 -.19 8.0391

-.36 8.8791

.46 4.8525

.15 5.9772

-.13 7.0857

-.31 8.1810

-.61 9.2793

-.76 10.3635

.60 5.0744

.17 6.4493

-.21 7.8233

-.38 9.1871

-.70 10.5631

-.85 1 1.9260

1.33 5.2861

1.17 5.2892

.30 6.9519

.58 6.9397

-.21 8.6329

.10 8.61 16 -.51 10.3189

-.17 10.2865

1.4915 -.27

1.6151 -.19

1 .7366 -.17

1.8566 -.13

1.9754 -.08

2.0933 -.04

2.2104 -.02

2.5133 -.50

2.8022 -.56

3.0814 -.56

3.3539 -.54

3.6213 -.53

3.8850 -.42

4.1456 -.38

3.1469 -.38

3.6360 -.57

4.1022 -.65

4.5538 -.61 4.9951 -.58

5.4287 -.46

5.8562 -.37

3.4905 -.17

4.2023 -.39

4.8750 -.48

5.5257 -.45

6. 1612 -.31

6.7856 -.22

7.4012 -.10

3.6419 -.04

4.5859 -.24

5.4776 -.26

6.3433 -.17

7. 1918 -.07

8.0275 .15 8.8531 .29 4.8591 -.14

5.9813 -.07

7.0801 .08 8.1632 .22 9.2344 .49 10.2961 .65 5.0835 -. 18 6.4551 -.09

7.8124 .14

9. 1594 .30 10.4980 .62 11.8292 .82 5.31 18 -.48

5.31 18 -.43

6.9650 -.19

6.9650 -.36

8.6183 .17 8.6183 -.08

10.2698 .48 10.2698 .16

66
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp. Density Density Density ^expt '^calc Pressure

Point expt calc Diff. Diff.

No. K mol/L kg/m^ Wg/m^ % MPa MPa %

3 97 1 .000 548. 150 4.000 232.50 234.31 -.78 12.0141 1 1 .9183 .80 3 98 1 .000 548.150 4.000 232.50 233.66 -.50 1 1.9797 1 1.9183 .51 3 99 1 .000 573. 150 4.000 1S32.50 234.71 -.95 13.7062 13.5629 1 .05

3 100 1 .000 573. 150 4.000 232.50 234.09 -.68 13.6657 13.5629 .76

3 101 1 .000 448. 150 4.500 261 .56 257.05 1.72 5.5354 5.5818 -.83

3 102 1.000 473.150 4.500 261 .56 259.28 .87 7.5143 7.5663 -.69

3 103 1 .000 498. 150 4.500 261 .56 260.68 .34 9.5367 9.5684 -.33

3 104 1.000 523.150 4.500 261 .56 261.49 .03 1 1.5754 1 1 .5789 -.03

3 105 1.000 548.150 4.500 261.56 262.27 -.27 13.6383 13.5930 .33

3 106 1.000 573.150 4.500 261 .56 262.67 -.42 15.6932 15.6074 .55

3 107 1.000 425.160 5.000 290.62 288.79 .63 3.8260 3.8302 -.11

3 108 1.000 448.150 5.000 290.62 287.60 1.04 5.9072 5.9536 -.78

3 109 1.000 448.150 5.000 290.62 286.51 1 .41 5.8910 5.9536 -1 .05 3 110 1.000 473.150 5.000 290.62 289.42 .41 8.3046 8.3417 -.44

3 111 1.000 473.150 5.000 290.62 288.16 .85 8.2661 8.3417 -.91 3 112 1.000 498.150 5.000 290.62 290.60 .01 10.7638 10.7647 -.01

3 113 1 .000 498.150 5.000 290.62 289.54 .37 10.7141 10.7647 -.47

3 114 1.000 523. 150 5.000 290.62 291.36 -.25 13.2533 13.2064 .35

3 1 15 1.000 523.150 5.000 290.62 290.35 .09 13. 1895 13.2064 -.13

3 116 1.000 548.150 5.000 290.62 291 .95 -.46 15.7652 15.6581 .68 3 117 1.000 548.150 5.000 290.62 290.93 -.11 15.6831 15.6581 .16

3 118 1.000 573.150 5.000 290.62 292.48 -.64 18.2952 18. 1 142 1.00

3 119 1.000 573.150 5.000 290.62 291 .32 -.24 18. 1818 18.1 142 .37

3 120 1.000 425.160 5.500 319.68 318.19 .47 3.9669 3.9798 -.33

3 121 1 .000 448.150 5.500 319.68 317.90 .56 6.5041 6.5506 -.71

3 122 1.000 473.150 5.500 319.68 318.97 .22 9.4101 9.4425 -.34

3 123 1.000 498.150 5.500 319.68 319.80 -.04 12.3900 12.3822 .06

3 124 1 .000 523.150 5.500 319.68 320.41 -.23 15.4105 15.3483 .41 3 125 1 .000 548 . 1 50 5.500 319.68 320.87 -.37 18.4553 18.3291 .69

3 126 1 .000 573.150 5.500 319.68 321 .27 -.50 21 .5174 21 .3169 .94 3 127 1 .000 425. 160 6.000 348.75 347.41 .38 4.3975 4.4284 -.70

3 128 1 .000 448. 150 6.000 348.75 347.61 .32 7.5305 7.5823 -.68

3 129 1 .000 473. 150 6.000 348.75 348. 17 . 16 1 1 .0677 1 1 .1081 -.36

3 130 1 .000 498. 150 6.000 348.75 348.83 -.02 14.6942 14.6861 .05

3 131 1 .000 523. 150 6.000 348.75 349.23 -.14 18.3510 18.2935 .31 3 132 1 .000 548. 150 6.000 348.75 349.59 -.24 22.0382 21 .9166 .55

3 133 1 .000 573. 150 6.000 348.75 349.85 -.32 25.7325 25.5466 .73

3 134 1 .000 425. 160 6.500 377.81 376.37 .38 5.4047 5.4769 -1 .32

3 135 1 .000 448. 150 6.500 377.81 376.76 .28 9.2885 9.3713 -.88

3 136 1 .000 473. 1 50 6.500 377.81 377. 15 .17 13.6171 13.6886 -.52

3 137 1 .000 498. 150 6.500 377.81 377.58 .06 18.0207 18.0530 -. 18 3 138 1 .000 523. 150 6.500 377.81 377.88 -.02 22.4556 22.4427 .06 3 139 1 .000 548. 150 6.500 377.81 378.1

1

-.08 26.9048 26.8444 .23 3 140 1.000 573.150 6.500 377.81 378.32 -.14 31 .3662 31 .2488 .38 3 141 1 .000 425. 160 7.000 406.87 405.33 .38 7.4241 7.5699 -1 .93 3 142 1.000 448.150 7.000 406.87 405.63 .31 12.2188 12.3801 -1 .30

3 143 1.000 473.150 7.000 406.87 405.95 .23 17.5161 17.6701 -.87

3 144 1.000 498.150 7.000 406.87 406.24 .16 22.8640 22.9929 -.56

3 145 1.000 523. 150 7.000 406.87 406.41 .11 28.2200 28.3301 -.39

3 146 1.000 548.150 7.000 406.87 406.47 .10 33.5588 33.6696 -.33

3 147 1.000 425.160 7.500 435.93 434.23 .39 1 1 .0404 1 1.3183 -2.46

3 148 1 .000 448.150 7.500 435.93 434.54 .32 16.9507 17.2358 -1 .65

3 149 1 .000 473. 150 7.500 435.93 434.63 .30 23.3767 23.7006 -1.37

3 150 1.000 498.150 7.500 435.93 434.94 .23 29.8848 30.1760 -.97

3 151 1.000 523.150 7.500 435.93 434.98 .22 36.3281 36.6481 -.87

3 152 1.000 425.160 8.000 464.99 463.13 .40 17.0337 17.5247 -2.80

3 153 1.000 448.150 8.000 464.99 463.42 .34 24.2663 24.7575 -1 .98

3 154 1.000 473.150 8.000 464.99 463.27 .37 31 .9893' 32.6184 -1 .93

3 155 1.000 425.160 8.500 494.06 492.07 .40 26.4134 27.2128 -2.94

3 156 1.000 448.150 8.500 494.06 492.26 .36 35.1618 35.9860 -2.29

67
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp. Dens i ty Dens i ty Dens i ty expT pca 1 c Pressure

Poi nt expt

kg/m-^ ca 1 c Diff

.

Diff.

No. K mol/L kg/m^ % MPa MPa $

19 157 1 .000 310.928 .079 4.58 4.56 .41 .1924 .1931 -.39

19 158 1.000 338.706 .079 4.58 4.57 .23 .21 17 .2121 -.22

19 159 1 .000 366.483 .079 4.58 4.58 .01 .2310 .2310 -.01

19 160 1 .000 394.261 .079 4.58 4.57 .07 .2496 .2498 -.07

19 161 1.000 422.039 .079 4.58 4.58 -. 17 .2689 .2684 .17

19 162 1.000 449.817 .079 4.58 4.58 -.15 .2875 .2871 .15

19 163 1 .000 477.594 .079 4.58 4.57 .08 .3054 .3057 -.08

19 164 1.000 505.372 .079 4.58 4.57 .06 .3241 .3242 -.06

19 165 1.000 533. 150 .079 4.58 4.57 .04 .3427 .3428 -.04

19 156 1.000 560.928 .079 4.58 4.57 .20 .3606 .3613 -.20

19 167 1 .000 588.706 .079 4.58 4.57 .17 .3792 .3798 -.17

19 168 1 .000 310.928 .085 4.93 4.90 .52 .2062 .2072 -.49

19 169 1.000 338.706 .085 4.93 4.92 .10 .2275 .2277 -.09

19 170 1.000 366.483 .085 4.93 4.92 .25 .2475 .2481 -.24

19 171 1.000 394.261 .085 4.93 4.94 -.21 .2689 .2684 .20

19 172 1.000 422.039 .085 4.93 4.95 -.37 .2896 .2885 .36

19 173 1 .000 449.817 .085 4.93 4.93 -.08 .3089 .3086 .08

19 174 1.000 477.594 .085 4.93 4.93 -.05 .3289 .3287 .05

19 175 1.000 505.372 .085 4.93 4.93 -.04 .3489 .3487 .04

19 176 1.000 533. 150 .085 4.93 4.92 .16 .3682 .3687 -.15

19 177 1 .000 560.928 .085 4.93 4.92 .15 .3882 .388 7 -.14

19 178 1.000 588.705 .085 4.93 4.91 .30 .4075 .4087 -.30

19 179 1 .000 310.928 .092 5.34 5.32 .33 .2227 .2234 -.31

19 180 1.000 338.706 .092 5.34 5.33 .15 .2455 .2458 -.14

19 181 1 .000 366.483 .092 5.34 5.33 .17 .2675 .2680 -.16

19 182 1.000 394.261 .092 5.34 5.33 .14 .2896 .2900 -.13

19 183 1.000 422.039 .092 5.34 5.35 -.15 .3123 .31 19 .15

19 184 1.000 449.817 .092 5.34 5.34 .00 .3337 .3337 -.00

19 185 1 .000 477.594 .092 5.34 5.33 .12 .3551 .3555 -. 12 19 186 1.000 505.372 .092 5.34 5.34 .03 .3771 .3772 -.03

19 187 1.000 533. 150 .092 5.34 5.33 .11 .3985 .3990 -.11

19 188 1.000 560.928 .092 5.34 5.33 .18 .4199 .4206 -. 18

19 189 1.000 588.706 .092 5.34 5.33 .24 .4413 .4423 -.24

19 190 1.000 310.928 .100 5.82 5.80 .47 .2413 .2424 -.44

19 191 1.000 338.706 .100 5.82 5.82 .05 .2568 .2570 -.05

19 192 1.000 365.483 .100 5.82 5.82 .10 .2910 .2912 -.10

19 193 1.000 394.261 .100 5.82 5.82 .08 .3151 .3153 -.08

19 194 1.000 422.039 .100 5.82 5.84 -.18 .3399 .3393 .17

19 195 1.000 449.817 .100 5.82 5.83 -.04 .3634 .3632 .04

19 196 1.000 477.594 .100 5.82 5.82 .07 .3868 .3870 -.06

19 197 1.000 505.372 .100 5.82 5.83 -.03 .4109 .4108 .03

19 198 1.000 533.150 .100 5.82 5.82 .04 .4344 .4346 -.04

19 199 1.000 560.928 .100 5.82 5.81 .25 .4571 .4583 -.25

19 200 1.000 588.706 .100 5.82 5.82 .15 .4813 .4820 -.14

19 201 1.000 310.928 .110 6.41 6.39 .32 .2641 .2649 -.30

19 202 1 .000 338.706 .1 10 6.41 6.40 .16 .2916 .2921 -.15

19 203 1.000 366.483 .110 6.41 6.38 .36 .3178 .3190 -.35

19 204 1.000 394.261 .1 10 6.41 6.40 .05 .3454 .3456 -.05

19 205 1.000 422.039 .1 10 6.41 6.41 -.07 .3723 .3721 .07

19 206 1 .000 449.817 .1 10 6.41 6.41 -.02 .3985 .3984 .02

19 207 1.000 477.594 .1 10 6.41 6.42 -.16 .4254 .4247 .16

19 208 1.000 505.372 .1 10 6.41 6.41 .01 .4509 .4510 -.01

19 209 1.000 533.150 .1 10 6.41 5.40 .15 .4764 .4771 -.15

19 210 1.000 560.928 .110 6.41 6.40 .13 .5026 .5033 -.13

19 21

1

1.000 588.706 .110 5.41 6.39 .24 .5281 .5294 -.24

68
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)Olds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp. Dens i ty Dens i ty Dens i ty f^expt ^ca 1 c Pressure

Poi nt expt ca 1 c Di f f

.

D i f f

.

No. K mol/L

z kg/m-^ kg/m-' % MPa MPa %

19 212 1.000 310.928 .122 7.12 7.09 .35 .2910 .2919 -.32

19 213 1.000 338.706 .122 7.12 7.1

1

.15 .3220 .3224 -.14

19 214 1 .000 366.483 .122 7.12 7.10 .25 .3516 .3525 -.24

19 215 1.000 394.261 .122 7.12 7. 1

1

.07 .3820 .3822 -.07

19 216 1.000 422.039 .122 7.12 7.13 -.13 .4123 .41 18 .12

19 217 1.000 449.817 .122 7.12 7,12 -.01 .4413 .4412 .01 19 218 1.000 477.594 .122 7.12 7.11 .07 .4702 .4705 -.07

19 219 1.000 505.372 .122 7.12 7.12 -.02 .4999 .4998 .02

19 220 1.000 533. 150 .122 7.12 7.12 .03 .5288 .5290 -.03

19 221 1.000 560.928 .122 7.12 7.11 .06 .5578 .5581 -.06

19 222 1 .000 588.706 .122 7.12 7.10 .20 .5861 .5872 -.20

19 223 1.000 310.928 .138 8.01 7.97 .54 .3234 .3250 -.49

19 224 1 .000 338.706 .138 8.01 7.98 .36 .3585 .3597 -.33

19 225 1.000 366.483 .138 8.01 7.99 .23 .3930 .3938 -.21

19 226 1.000 394.261 .138 8.01 8.01 .02 .4275 .4276 -.02

19 227 1 .000 422.039 .138 8.01 8.01 -.06 .4613 .4610 .05

19 228 1 .000 449.817 .138 8.01 8.01 -.01 .4944 .4943 .01 19 229 1.000 477.594 .138 8.01 8.00 .13 .5268 .5274 -.13

19 230 1 .000 505.372 .138 8.01 8.01 -.01 .5605 .5605 .01

19 231 1 .000 533. 150 .138 8.01 8.00 .09 .5929 .5935 -.09

19 232 1 .000 560.928 .138 8.01 8.01 .05 .6260 .6264 -.05

19 233 1 .000 588.706 .138 8.01 8.00 .12 .6584 .6592 -. 12 19 234 1 .000 338.706 .157 9.15 9.14 . 16 .4061 .4067 -.15

19 235 1 .000 366.483 .157 9.15 9. 14 . 18 .4454 .4461 -. 16 19 236 1 .000 394.261 .157 9.15 9.13 .22 .4840 .4850 -.21

19 237 1 .000 422.039 .157 9.15 9. 1 5 .05 .5233 .5236 -.05

19 238 1 .000 449.8 17 .157 9. 15 9. 14 . 12 .5612 .5619 -. 1

1

19 239 1 .000 477.594 .157 9.15 9. 16 -. 1

0

.6005 .6000 .09

19 240 1 .000 505.372 .157 9.15 9. 16 -.08 .6385 .6380 .08

19 241 1 .000 533. 150 .157 9.15 9. 1

5

.02 .6757 .6758 -.02

19 242 1 .000 560.928 .157 9.15 9.15 .00 .7136 .7136 -.00

19 243 1 .000 588.706 .157 9.15 9. 1 5 .07 .7508 .7514 -.07

19 244 1 .000 338.706 .184 10.68 10.66 .19 .4668 .4676 -.17

19 245 1 .000 366.483 .184 10.68 10.68 -.01 .5143 .5143 .01 19 246 1 .000 394.261 .184 10.68 10.66 .21 .5592 .5603 -.19

19 247 1.000 422.039 .184 10.68 10.67 .06 .6054 .6057 -.06

19 248 1 .000 449.817 .184 10.68 10.67 .10 .6502 .6508 -.10

19 249 1 .000 477.594 .184 10.68 10.69 -.11 .6964 .6956 .10

19 250 1.000 505.372 .184 10.68 10.68 -.03 .7405 .7403 .03

19 251 1 .000 533. 150 .184 10.68 10.70 -. 16 .7860 .7848 .15

19 252 1.000 560.928 .184 10.68 10.68 -.03 .8294 .8292 .03

19 253 1 .000 588.706 .184 10.68 10.67 .07 .8729 .8735 -.07

19 254 1 .000 338.706 .197 11.44 1 1 .40 .34 .4957 .4972 -.30

19 255 1 .000 366.483 .197 1 1.44 1 1 .42 .20 .5468 .5477 -.18

19 256 1 .000 394.261 .197 1 1 .44 1 1 .42 .16 .5964 .5973 -.15

19 257 1 .000 422.039 .197 1 1 .44 1 1 .44 .03 .6460 .6462 -.03

19 258 1.000 449.817 .197 11.44 1 1 .43 .07 .6943 .6948 -.07

19 259 1 .000 477.594 .197 1 1.44 11.45 -.03 .7433 .7430 .03

19 260 1.000 505.372 .197 11.44 11 .46 -.15 .7922 .7910 .15

19 261 1.000 533.150 .197 1 1.44 1 1 .43 .06 .8384 .8389 -.06

19 262 1.000 560.928 .197 1 1.44 11.45 -.09 .8874 .8866 .08

19 263 1.000 588.706 .197 1 1.44 1 1.44 -.00 .9342 .9342 .00

19 264 1.000 338.706 .212 12.32 12.30 .14 .5302 .5308 -. 12 19 265 1.000 366.483 .212 12.32 12.30 .20 .5847 .5857 -.18

19 266 1.000 394.261 .212 12.32 12.30 .18 .6385 .6395 -.16

19 267 1.000 422.039 .212 12.32 12.32 .05 .6922 .6925 -.05

69
Table 7. { Cont i nued

)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp. Dens i ty Dens ity Dens i ty '^expt '^ca 1 c Pressui

Point expt ca 1 c Diff

.

Diff.

No. K mol/L kg/m^ kg/m-' % MPa MPa %

19 268 1.000 449.817 .212 12.32 12.31 .07 .7446 ,7451 -.06

19 269 1 .000 477.594 .212 12.32 12.35 -.23 .7991 ,7973 .22

19 270 1.000 505.372 .212 12.32 12.36 -.27 ,8515 ,8493 .26

19 271 1 .000 533.150 .212 12.32 12.35 -.25 ,9032 ,9010 .24

19 272 1 .000 560.928 .212 12.32 12.35 -.25 .9549 ,9526 .25

19 273 1 .000 588.706 .212 12.32 12.33 -.05 1 .0046 1,0040 .05

19 274 1 .000 338.706 .230 13.35 13.30 .36 ,5674 ,5692 -.31

19 275 1.000 366.483 .230 13.35 13.32 .22 ,6281 .6294 -.20

19 276 1 .000 394.261 .230 13.35 13.33 .1

1

,6874 ,6881 -.10

19 277 1,000 422.039 .230 13.35 13,32 .20 .7446 .7460 -. 18

19 278 1 .000 449.817 .230 13.35 13,35 .01 ,8032 .8033 -.01

19 279 1 .000 477.594 .230 13.35 13.38 -.21 .8618 .8602 .19

19 280 1 .000 505.372 .230 13.35 13.41 -.42 .9205 .9167 .40

19 281 1 .000 533.150 .230 13.35 13.40 -.42 .9770 .9731 .40

19 282 1 .000 560.928 .230 13.35 13.38 -.23 1 .0315 1 .0292 .22

19 283 1 .000 588.706 .230 13.35 13.37 -.14 1.0866 1.0852 .13

19 284 1 .000 338.706 ,251 14.56 14.57 -.05 .6136 .6134 .05

19 285 1 .000 366.483 .251 14.56 14.54 .12 .6791 .6799 -. 1

1

19 286 1 .000 394.261 .251 14.56 14.55 . 10 .7439 .7446 -.09

19 287 1.000 422.039 .251 14.56 14.56 .03 .8081 .8083 -.03

19 288 1.000 449.817 .251 14.56 14.57 -.02 .8715 .8713 .02

19 289 1.000 477.594 .251 14.56 14.60 -.29 .9363 .9338 ,27

19 290 1 .000 505.372 .251 14.56 14.63 -.48 1 .0004 ,9958 ,46

19 291 1.000 533.150 .251 14.56 14.63 -.48 1.0625 1 ,0576 .46

19 292 1 .000 560.928 .251 14.56 14.61 -.31 1.1225 1 . 1 1 92 .29

19 293 1.000 588.706 .251 14.56 14.59 -.17 1,1825 1.1805 .16

19 294 1 .000 338.706 .276 16.02 16.00 .12 ,6640 .6646 -.10

19 295 1.000 366.483 .276 16.02 16.00 .09 .7384 .7390 -.08

19 296 1.000 394.261 .276 16.02 15.98 .23 .8094 .8111 -.21

19 297 1.000 422.039 .276 16.02 16.03 -.07 .8825 .8819 .07

19 298 1.000 449.817 .276 16.02 16.05 -.19 .9535 .9518 .18

19 299 1.000 477.594 .276 16.02 16.1 1 -.58 1.0266 1.0211 .54

19 300 1.000 505.372 .276 16.02 16.12 -.62 1.0963 1 .0899 .58

19 301 1.000 533.150 .276 16.02 16,10 -.50 1.1638 1 . 1 583 .48

19 302 1.000 560.928 .276 16,02 16.08 -.36 1.2307 1.2264 .35

19 303 1 .000 588.706 .276 16.02 16.04 -.15 1.2962 1 .2943 .14

19 304 1.000 338.706 .306 17,80 17.86 -.34 .7267 .7247 .27

19 305 1.000 366.483 .306 17.80 17.79 .05 .8088 .8091 -.05

19 306 1.000 394.261 .306 17,80 17.76 .23 .8887 ,8905 -.20

19 307 1.000 422.039 .306 17,80 17.81 -.07 .9708 ,9702 ,06

19 308 1.000 449.817 .306 17,80 17.84 -.21 1.0508 1,0487 ,19

19 309 1 .000 477.594 .306 17,80 17.88 -.48 1.1314 1 , 1 264 .44

19 310 1.000 505.372 .306 17,80 17.89 -.51 1.2093 1,2035 .48

19 31

1

1.000 533.150 .306 17,80 17.88 -.47 1 ,2859 1 ,2802 .44

19 312 1 .000 560.928 .306 17.80 17.86 -.35 1 ,3610 1,3565 .34

19 313 1.000 588.706 .306 17.80 17.82 -.12 1 ,4341 1 ,4325 .12

19 314 1 .000 366.483 .344 20.02 20.05 -. 1

1

,8942 .8934 .09

19 315 1.000 394.261 .344 20.02 20.00 .10 ,9860 ,9868 -.09

19 316 1.000 422.039 .344 20.02 20.05 -.12 1,0790 1 .0779 .11 19 317 1.000 449.817 .344 20.02 20.11 -.44 1,1721 1 .1674 .40

19 318 1.000 477.594 .344 20.02 • 20.12 -.50 1,2617 1.2559 .46

19 319 1.000 505.372 .344 20.02 20.14 -.56 1.3507 1.3436 .52

19 320 1.000 533.150 .344 20.02 20.13 -.56 1.4382 1.4307 .52

19 321 1.000 560.928 .344 20,02 20.11 -.44 1.5237 1.5174 .42

19 322 1.000 588.706 .344 20,02 20.06 -.19 1.6065 1.6036 .18

19 323 1.000 366.483 .394 22,88 22,92 -.16 .9977 .9964 .13

70
Table 7. (Continued)

Data sources and ID numbers: (DVirial Equation, (3)Beattie, {19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp. Density Density Density ^expt ^calc Pressure

Point expt calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa %

19 324 1.000 394.261 .394 22.88 22.87 .07 1.1052 1.1059 -.06

19 325 1.000 422.039 .394 22.88 22.90 -.07 1.2128 1.2121 .06

19 326 1.000 449.817 .394 22.88 22.91 -.12 1.3176 1.3162 .10

19 327 1.000 477.594 .394 22.88 22.99 -.48 1.4251 1 .4189 .44

19 328 1 .000 505.372 .394 22.88 23.04 -.67 1 .5299 1 .5206 .62

19 329 1.000 533.150 .394 22.88 23.06 -.79 1 .6334 1.6214 .74

19 330 1.000 560.928 .394 22.88 23.04 -.68 1.7327 1.7217 .64

19 331 1.000 588.706 .394 22.88 23.05 -.73 1.8340 1.8214 .69

19 332 1.000 366.483 .459 26.70 26.77 -.28 1 . 1 266 1.1242 .21

19 333 1.000 394.261 .459 26.70 26.66 .15 1.2548 1.2564 -.12

19 334 1.000 422.039 .459 26.70 26.67 .11 1.3824 1.3837 -.09

19 335 1.000 449.817 .459 26.70 26.72 -.09 1.5093 1 .5080 .08

19 336 1.000 477.594 .459 26.70 26.78 -.30 1 .6347 1 .6303 .27

19 337 1.000 505.372 .459 26.70 26.84 -.53 1.7595 1 .751 1 .48

19 338 1.000 533.150 .459 26.70 26.86 -.63 1.8816 1 .8708 .58

19 339 1.000 560.928 .459 26.70 26.89 -.72 2.0029 1.9896 .67

19 340 1.000 588.706 .459 26.70 26.86 -.59 2.1 194 2.1077 .56

19 341 1.000 366.483 .501 29. 12 29.30 -.59 1.2052 1.2000 .43

19 342 1.000 394.261 .501 29.12 29.10 .08 1.3465 1 .3473 -.06

19 343 1.000 422.039 .501 29.12 29.12 .00 1.4886 1.4886 -.00

19 344 1.000 449.817 .501 29.12 29.14 -.07 1.6272 1.6262 .06

19 345 1.000 477.594 .501 29.12 29.21 -.28 1.7657 1 .7613 .25

19 346 1.000 505.372 .501 29.12 29.27 -.49 1 .9030 1.8947 .44

19 347 1.000 533.150 .501 29.12 29.26 -.47 2.0353 2.0266 .43

19 348 1.000 560.928 .501 29.12 29.25 -.44 2. 1663 2.1575 .41

19 349 1.000 588.706 .501 29.12 29.24 -.39 2.2960 2.2875 .37

19 350 1.000 366.483 .551 32.04 32.21 -.54 1.2900 1.2852 .38

19 351 1.000 394.261 .551 32.04 31.97 .21 1.4493 1.4516 -. 16 19 352 1.000 422.039 .551 32.04 31.98 .18 1.6079 1.6102 -.15

19 353 1.000 449.817 .551 32.04 32.06 -.06 1.7651 1 .7642 .05

19 354 1.000 477.594 .551 32.04 32.12 -.27 1.9195 1.9151 .23

19 355 1.000 533.150 .551 32.04 32.20 -.50 2.2208 2.2107 .46

19 356 1.000 560.928 .551 32.04 32.21 -.55 2.3683 2.3564 .51 19 357 1.000 588.706 .551 32.04 32.16 -.37 2.5097 2.501

1

.35

19 358 1.000 394.261 .612 35.60 35.56 .11 1.5706 1.5719 -.08

19 359 1.000 422.039 .612 35.60 35.57 .09 1.7513 1.7525 -.07

19 360 1 .000 449.817 .612 35.60 35.61 -.04 1.9278 1.9271 .03

19 361 1.000 477.594 .612 35.60 35.66 -.17 2.1008 2.0978 .14

19 362 1.000 505.372 .612 35.60 35.71 -.31 2.2718 2.2657 .27

19 363 1.000 533.150 .612 35.60 35.72 -.36 2.4394 2.4315 .32

19 364 1 .000 560.928 .612 35.60 35.71 -.33 2.6035 2.5957 .30

19 365 1.000 588.706 .612 35.60 35.68 -.24 2.7648 2.7586 .22

19 366 1.000 394.261 .689 40.05 39.86 .47 1.7058 1.71 14 -.33

19 367 1.000 422.039 .689 40.05 39.92 .32 1.9161 1 .9207 -.24

19 368 1.000 449.817 .689 40.05 39.98 .16 2.1 194 2.1222 -.13

19 369 1.000 477.594 .689 40.05 40.05 -.01 2.3187 2.3184 .01 19 370 1.000 505.372 .689 40.05 40.08 -.09 2.5131 2.51 1 1 .08

19 371 1.000 533.150 .689 40.05 40.15 -.27 2.7076 2.701 1 .24

19 372 1.000 560.928 .689 40.05 40.15 -.26 2.8958 2.8891 .23

19 373 1.000 588.706 .689 40.05 40.14 -.23 3.0820 3.0754 .21 19 374 1.000 394.261 .787 45.77 45.69 .17 1.8712 1.8733 -.11

19 375 1.000 422.039 .787 45.77 45.58 .42 2.1 153 2.1218 -.31

19 376 1.000 449.817 .787 45.77 45.58 .40 2.3518 2.3592 -.31

19 377 1.000 477.594 .787 45.77 45.68 .20 2.5855 2.5897 -.16

19 378 1.000 505.372 .787 45.77 45.79 -.04 2.8165 2.8155 .04

19 379 1.000 533.150 .787 45.77 45.88 -.24 3.0440 3.0376 .21

71
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)8eattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp. Density Density Density ^expt '^calc Pressure

Point expt calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa %

19 380 1.000 560.928 .787 45.77 45.94 -.38 3.2681 3.2571 .34

19 381 1.000 588.706 .787 45.77 45.97 -.45 3.4887 3.4745 .41 19 382 1 .000 394.261 .919 53.39 53. 17 .43 2.0546 2.0597 -.25

19 383 1.000 422.039 .919 53.39 53.08 .60 2.3546 2.3641 -.40

19 384 1.000 449.817 .919 53.39 53.29 .20 2.6483 2.6522 -.15

19 385 1 .000 477.594 .919 53.39 53.39 .01 2.9303 2.9305 -.01

19 386 1.000 505.372 .919 53.39 53.40 -.01 3.2026 3.2023 .01

19 387 1.000 533.150 .919 53.39 53.39 .01 3.4688 3.4692 -.01

19 388 1.000 560.928 .919 53.39 53.24 .28 3.7232 3.7324 -.25

19 389 1.000 588.706 .919 53.39 53.13 .50 3.9748 3.9928 -.45

19 390 1.000 394.261 1.002 58.25 58.36 -.19 2.1636 2. 1614 .10

19 391 1.000 422.039 1.002 58.25 57.80 .78 2.491 1 2.5036 -.50

19 392 1.000 449.817 1.002 58.25 57.81 .75 2.8103 2.8254 -.54

19 393 1.000 477.594 1.002 58.25 57.97 .47 3.1240 3.1354 -.36

19 394 1.000 505.372 1.002 58.25 58.02 .39 3.4267 3.4375 -.32

19 395 1.000 533.150 1.002 58.25 58.05 .34 3.7232 3.7339 -.29

19 396 1.000 560.928 1.002 58.25 58.1 1 .24 4.0176 4.0260 -.21

i9 397 1.000 588.706 1.002 58.25 58.1 1 .23 4.3058 4.3147 -.21

19 398 1.000 422.039 1.102 64.07 63.52 .86 2.6428 2.6567 -.52

19 399 1.000 449.817 1.102 64.07 63.55 .8 5 3.0027 3.0204 -.59

19 400 1.000 477.594 1.102 64.07 63.67 .63 3.3536 3.3695 -.47

19 401 1.000 505.372 1.102 64.07 63.85 .35 3.6990 3.7092 -.27

19 402 1.000 533.150 1.102 64.07 63.91 .26 4.0334 4.0420 -.21

19 403 1.000 560.928 1.102 64.07 63.87 .32 4.3575 4.3696 -.28

19 404 1.000 588.706 1.102 64.07 63.79 .45 4.6746 4.6932 -.39

19 405 1 .000 422.039 1.225 71 .19 70.41 1.10 2.8062 2.8235 -.61

19 406 1.000 449.817 1.225 71 .19 70.55 .91 3.2212 3.2403 -.59

19 407 1.000 477.594 1.225 7.1 . 1

9

70.78 .58 3.6239 3.6391 -.42

19 408 1.000 505.372 1.225 71.19 70.89 .43 4.0127 4.0261 -.33

19 409 1.000 533. 150 1.225 71 .19 71 .08 .17 4.3989 4.4047 -.13

19 410 1.000 560.928 1 .225 71 .19 71 .09 .15 4.7712 4.7772 -.13

19 41

1

1.000 588.706 1.225 71 .19 70.95 .34 5. 1297 5. 1448 -.29

19 412 1 .000 422.039 1 .378 80.09 79.01 1 .35 2.9827 3.0028 -.67

19 413 1.000 449.817 1 .378 80.09 79.31 .98 3.4681 3.4889 -.60

19 414 1 .000 477.594 1 .378 80.09 79.61 .60 3.9355 3.9518 -.41

19 415 1 .000 505.372 1.378 80.09 79.64 .57 4.3816 4.4002 -.42

19 416 1 .000 533. 150 1 .378 80.09 79.77 .41 4.8229 4.8384 -.32

19 417 1 .000 560.928 1 .378 80.09 79.81 .35 5.2538 5.2690 -.29

19 418 1 .000 588.706 1 .378 80.09 79.89 .25 5.6813 5.6937 -.22

19 419 1 .000 422.039 1 .450 84.31 83.57 .87 3.0647 3.0772 -.41

19 420 1 .000 449.817 1 .450 84.31 83.70 .72 3.5818 3.5971 -.42

19 421 1 .000 477.594 1 .450 84.31 83.87 .52 4.0769 4.0912 -.35

19 422 1.000 505.372 1.450 84.31 83.83 .57 4.5505 4.5694 -.41

19 423 1 .000 533.150 1 .450 84.31 83.86 .53 5.0159 5.0366 -.41

19 424 1.000 560.928 1.450 84.31 83.98 .39 5.4779 5.4955 -.32

19 425 1.000 588.706 1.450 84.31 84.06 .30 5.9329 5.9480 -.25

19 426 1 .000 422.039 1.531 88.99 88.00 1.12 3.1371 3.1524 -.49

19 427 1.000 449.817 1.531 88.99 88.21 .87 3.6921 3.7105 -.50

19 428 1.000 477.594 1.531 88.99 88.45 .61 4.2230 4.2399 -.40

19 429 1.000 505.372 1.531 88.99 88.51 .54 4.7333 4.7518 -.39

19 430 1.000 533.150 1.531 88.99 88.66 .37 5.2366 5.2517 -.29

19 431 1.000 560.928 1.531 88.99 88.68 .35 5.7261 5.7426 -.29

19 432 1.000 588.706 1.531 88.99 88.75 .28 6.2122 6.2266 -.23

19 433 1.000 422.039 1.621 94.23 93.14 1.15 3.2130 3.2278 -.46

19 434 1.000 449.817 1.621 94.23 93.48 .80 3.8128 3.8293 -.43

19 435 1 .000 477.594 1.621 94.23 93.77 .49 4.3851 4.3987 -.31

72
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)Olds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp, Density Density Density ^expt '^calc Pressure

Point expt calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa %

19 436 1.000

19 437 1.000

19 438 1 .000

19 439 1.000

19 440 1 .000

19 441 1.000

19 442 1 .000

19 443 1 .000

19 444 1 .000

19 445 1 .000

19 446 1 .000

19 447 1 .000

19 448 1 .000

19 449 1 .000

19 450 1 .000

19 451 1 .000

19 452 1 .000

19 453 1 .000

19 454 1 .000

19 455 1 .000

19 456 1 .000

19 457 1 .000

19 458 1 .000

19 459 1 .000

1

9

460 1 .000

19 461 1 .000

19 462 1 .000

19 463 1 .000

19 464 1 .000

19 465 1 .000

19 466 1 .000

19 467 1 .000

19 468 1 .000

19 469 1.000

19 470 1.000

19 471 1.000

19 472 1.000

19 473 1 .000

19 474 1.000

19 475 1.000

19 476 1.000

19 477 1.000

19 478 1.000

19 479 1.000

19 480 1.000

19 481 1.000

19 482 1.000

19 483 1 .000

19 484 1.000

19 485 1.000

19 486 1.000

19 487 1.000

19 488 1.000

19 489 1.000

19 490 1.000

19 491 1.000

505.372 1.621 533.150 1.621 560.928 1 .621 588.706 1.621 422.039 1.722

449.817 1.722

477.594 1.722

505.372 1.722

533.150 1.722

560.928 1.722

588.706 1.722

422.039 1.837

449.817 1.837

477.594 1.837

505.372 1.837

533.150 1.837

560.928 1.837

588.706 1.837

422.039 1.968

449.817 1.968

477.594 1.968

505.372 1.968

533.150 1.968

560.928 1.968

588.706 1.968

422.039 2.120

449.817 2.120

477.594 2.120

505.372 2.120

533.150 2.120

560.928 2.120

588.706 2.120

422.039 2.297

449.817 2.297

477.594 2.297

505.372 2.297

533.150 2.297

560.928 2.297

436.428 2.505

455.150 2.505

474.428 2.505

494.094 2.505

513.983 2.505

533.983 2.505

554.150 2.505

434.317 2.756

450.817 2.756

467,706 2.756

484.983 2.756

502.594 2.756

519.817 2.756

537.039 2.756

432.650 3,062

447.039 3.062

461.983 3.062

476.983 3.062

94.23 93.80

94.23 93.96

94.23 93.93

94.23 93.86

100.12 98.87

100.12 99.64

100.12 99.60

100.12 99.77

100.12 99.81

100.12 99.98

100.12 100.01

106.79 105.13

106.79 105.98

106.79 106.26

106.79 106.37

106.79 106.48

106,79 106.58

106.79 106.68

114.42 112.45

114.42 113.71 114.42 113.73

114.42 114.08

114.42 114.20

114.42 114,31

114.42 114.45

123.22 121.72

123.22 122.55

123.22 122.73

123.22 122.80

123.22 123.21

123.22 123.46

123.22 123.77

133.49 131.89

133.49 132.25

133.49 133.03

133.49 133.41

133.49 133.76

133.49 133.92

145.62 143.07

145.62 144.35

145.62 144.97

145.62 145.35

145.62 145.71

145.62 146.09

145.62 146.40

160.18 155.84

160.18 158,39

160.18 159.49

160.18 159.91

160.18 160.04

160,18 160,83

160.18 161.55

177,98 172,67

177,98 176,67

177.98 176,91

177.98 177.44

.4 5 4.9332

.28 5.4744

.31 5.9984

.39 6,5121

1 ,25 3,2874

,48 3.9438

.52 4.5540

.35 5, 1504

.31 5,7295

.14 6,3053

.11 6,8672

1.56 3.3577

.76 4.0679

.50 4.7367

.40 5.3814

.29 6.0122

.20 6.6328

,10 7.2464

1 .72 3.4267

.62 4.2058

.60 4.9298

.30 5.6399

. 19 6.3294

.09 7.0085

-.03 7.6808

1.21 3.4956

.55 4.3471

.40 5. 1469

,34 5.9191

,01 6.6879

-.20 7.4429

-.45 8.1944

1.20 3.5508

,92 4.4850

,34 5.3779

.06 6.2432

-.21 7.0947

-.32 7.9290

1.75 4.1369

.88 4.8263

.45 5.5158

.19 6.2053

-.06 6.8948

-.32 7,5842

-.53 8.2737

2.71 4.1369

1,12 4.8263

.43 5.5158

.17 6.2053

.09 6.8948

-.40 7.5842

-.85 8.2737

2.99 4.1369

.74 4.8263

.61 5.5158

.30 6.2053

4.9490 -.32

5.4861 -.21

6.0135 -.25

6.5335 -.33

3.3023 -.45

3.9535 -.24

4.5686 -.32

5.1628 -.24

5,7427 -,23

6.3121 -.11

6.8734 -.09

3.3746 -.50

4.0830 -.37

4,7509 -,30

5.3958 -,27

6,0252 -.22

6.6433 -.16

7.2526 -.09

3.4430 -.47

4.2177 -.28

4.9468 -.34

5.6510 -.20

6.3384 -.14

7.0135 -.07

7.6792 .02 3.5050 -.27

4.3572 -.23

5.1583 -.22

5,9323 -.22

6.6884 -.01

7.4314 .15 8.1642 .37 3.5578 -.20

4.5014 -,36

5,3878 -.18

6.2455 -.04

7.0842 .15 7.9091 .25 4.1557 -.45

4.8431 -.35

5.5283 -.23

6.2120 -.11 6.8921 .04 7.5669 .23 8.2400 .41 4.1592 -.54

4.8446 -.38

5.5265 -.19

6,2110 -,09

6.8986 -.06

7.5634 .28 8.2220 .63 4.1542 -.42

4.8365 -.21 5.5294 -.25

6.2148 -.15

73
Table 7. (Continued)

Data sources and

(XXXX)Haynes.

ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage,

ID

19

1919

1919

19

19

19

19

1919

1919

1919

1919

19

19

1919

1919

19

19

1919

19

19

19

19

19

19

1919

19

1919

1919

19

19

1919

1919

19

1919

19

1919

19

19

1919

Data

Poi nt

No.

492

493

494

495

496

497

498

499

500

501 502

503

504 505

506

507

508

509

510

51 1 512 513

514

515

516

517

518

519

520

521 522

523

524 525

526

527

528 529 530

531 532

533

534 535

536

537

538 539

540

541 542

543

544 545

546

547

Weight Temp.

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1 .000

1.000

1.000

1 .000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1 .000

1.000

1.000

1.000

1.000

1 .000

1.000

1.000

1.000

1.000

1.000

1 .000

1 .000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1.000

1 .000

1.000

K

491 .983

507.039

522.317

431.150

444.094

456.928

469.594

482.261

494.983

507,706

430.761

443.039

454.650

466.261

477.706

489.261

500.928

441 .650

452.150

462.983

473.539

483.928

494.428

438.372

446.928

455.428

463.872

472.428

480.817

433.039

439.150

445.206

451 .261 457.428

463.261

417.039

426.983

431.594

436.428

440.928

445.872

450.428

413.706

422,039

425.928

429.872

433.928

438.039

442,039

403.261

407.039

414.317

418.150

421,539

424,928

428.206

Dens i ty

expt

mol/L l<g/m^

3.062

3.062

3.062

3.445

3.445

3.445

3.445

3.445

3.445

3.445

3,675

3,675

3,675

3,675

3,675

3,675

3,675

3,937

3.937

3,937

3,937

3,937

3,937

4,593

4.593

4,593

4.593

4.593

4,593

5.512

5,512

5,512

5,512

5,512

5,512

6,124

6.124

6,124

6.124

6,124

6, 124 6,124

6,484

6,484

6.484

6.484

5.484

6.484

6,484

6,890

6,890

6,890

6,890

6,890

6.890

6.890

177.98

177.98

177.98

200,23

200.23

200.23

200.23

200,23

200,23

200,23

213,58

213,58

213.58

213.58

213.58

213,58

213,58

228,84

228,84

228,84

228,84

228,84

228,84

266,97

266,97

266,97

266,97

266,97

266.97

320.37

320.37

320.37

320,37

320,37

320,37

355,97

355,97

355,97

355,97

355,97

355,97

355,97

376,91

376,91

376,91

376,91

376,91

376,91

376,91

400.46

400.46

400.46

400.46

400.46

400.46

400.46

Dens i ty

calc

kg/m^

178.07

178.59

178.79

203.58

198.09

198.59

199.76

200.60

201 ,14

201 .59

216,60

207,90

210,90

212.33

213.73

214.40

214.67

222.59

226.35

226.37

227.37

228.47

228.96

263.49

264.55

264.94

265.20

264.85

265.02

318.41

318.99

319.28

319.27

318.73

319.23

354.19

354.30

355.41

355.31

356.18

355.52

355.94

373.78

374.93

376.05

376.72

376.91

376.87

377.06

401.24

400,53

400.01

399.20

399,57

399,87

400,35

Dens i ty

Diff,

-,05

-,34

-,45

-1 ,67

1,07

,82

,23

-,19

-,45

-,68

-1,41

2,66

1 ,26

,58

-,07

-,38

-,51

2,73

1,09

1,08

,64

,16

-,05

1,30

.91 ,76

,67

,80

,73

,61

,43

,34

,34

,51 ,36

,50

,47

,16

,18

-.06

,13

,01

,83

,52

,23

,05

0,00

,01

-.04

-,20

-,02

,11

,32

,22

,15

,03

''^expt MPa

6,8948

7,5842

8,2737

4.1369

4,8263

5,5158

6,2053

6,8948

7,5842

8,2737

4.1369

4,8263

5.5158

6.2053

6.8948

7.5842

8.2737

4.8263

5.5158

6,2053

6,8948

7.5842

8.2737

4,8263

5,5158

6.2053

6,8948

7.5842

8.2737

4.8263

5.5158

6.2053

6.8948

7.5842

8,2737

3,4474

4.8263

5,5158

6,2053

6,8948

7,5842

8,2737

3,4474

4,8263

5,5158

6.2053

5.8948

7.5842

8.2737

2.7579

3.4474

4.8263

5,5158

6,2053

6,8948

7,5842

' ca i c MPa

6,8928

7,5674

8,2469

4.1306

4.8395

5.5332

6,2123

6,8874

7,5620

8,2336

4,1318

4,8593

5.5427

6,2233

6.8918

7.5650

8.2428

4,8614

5,5400

6,2401

6,9220

7, 5927

8,2703

4,8481

5,5411

6,2352

6.9287

7,6343

8,3286

4,8554

5,5428

6,2317

6.9267

7,6394

8,3175

3,4821

4.8769

5.5356

6.2320

6.8850

7.5068

8,2753

3,5525

4,9150

5,5587

6,2156

6,8948

7,5866

8,2626

2,7173

3,4436

4.8573

5,6082

6.2750

6.9443

7.5939

Pressure

Diff,

,03

.22

,33 .15 -.27

-.31

-.11

.11 .29

,49

,12

-,68

-,49

-,29

,04

.25 ,37

-,72

-,44

-,56

-.39

-, 1

1

,04

-,45

-,46

-,48

-,49

-,66

-,66

-,60

-,49

-,42

-,46

-,72

-.53

-1.00

-1 .04 -.36

-.43

.14 -.30

-.02

-2.96

-1 .80 -.77

-.17

-.00

-.03

.13 1.49

.11 -.64

-1.65

-1.11

-.71 -.13

74
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)Olds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp. Density Density Density ^^expt '^calc Pressure

Point expt calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa %

19 548 1 .000 43 1 .483 6.890 400.46 400.76 -.08 8.2737 8.24 54 .34

19 549 1 .000 394 .81

7

7.349 427. 1

6

427.37 -.05 2.7579 2.7394 .67

19 550 1 .000 397.761 7.349 427. 16 427.32 -.04 3.4474 3.4321 .45

19 551 1 .000 403.706 7.349 427. 16 427.05 .03 4.8263 4.8376 -.23

19 552 1 .000 406.817 7.349 427. 16 426.60 .13 5.5158 5.5765 -1 .09

19 553 1 .000 409.872 7.349 427. 16 426.29 .20 6.2053 6.3042 -1 .57

19 554 1 .000 413.039 7.349 427. 16 425.77 .33 6.8948 7.0601 -2.34

19 555 1 .000 415.928 7.349 427. 16 425.81 .31 7.5842 7.751

3

-2.16

19 556 1 .000 419.094 7.349 427. 16 425.33 .43 8.2737 8.5104 -2.78

19 557 1 .000 388.817 7.602 441 .89 442.26 -.08 2.7579 2.7161 1 .54 19 558 1 .000 391 .483 7.602 44 1 .89 442. 15 -.06 3.4474 3.4 160 .92

19 559 1 .000 396.539 7.602 441 .89 442.50 -. 14 4.8263 4.7474 1 .66

19 560 1 .000 399.261 7.602 44 1 .89 442.26 -.08 5.5158 5.4664 .90

19 561 1 .000 401 .817 7.602 44 1 .89 442.34 -. 10 6.2053 6. 1425 1 .02

19 562 1 .000 404.261 7.602 44 1 .89 442.61 -.16 6.8948 6.7903 1 .54

19 563 1 .000 407. 1 50 7.602 44 1 .89 442.07 -.04 7.5842 7.5570 .36

19 564 1 .000 41 0.872 7.602 44 1 .89 440. 12 .40 8.2737 8.5466 -3. 19 19 565 1 .000 38 1 .872 7.874 457.67 457.33 .07 2.7579 2.8068 -1 .74

1 nnn 384 .094 7 R74. 457 fi7 4'57 57 . 09u^ 3,4474 3.462

1

-.43

Jyj 1

1 nnn ^RR 7nfi 7.R74 4. '57 fi7 457 ^ J 1 . fiR uu - . onuu 4.8263 4.8245 .04

19 1 nnn 3qn 92R 7 R74 457 .67 457.87 -.04 . u^ 5. 5 1 58 5.4822 .61 1Q 1 nnn ^Q"? R79 7 R74. 4'i7 ft7 4 5R w\ - . 1Q1 y 0. £-\jJJ \Jm\JJOJ n5R'^ 9 4"^

1 Q JS7nl\J 1 nnn 7 R74 H J 1 •O

/

4^ JO5R . 4Q^y _ 10 e. QQ4Q fi 75n9 9 1 4

1Q J 1 \ 1 nnn Dy 1 • / o \ 7 R74 H J 1 . D / 4"t JO5R . nou^ _ AO . uy 7 5R4 9 7/ . J\JO 5nR711

I . niU 1 1Q R79 1 nnn AC\ H\J 1

I .

1

1 JUsn 7 R74 A ^7 fi7 /I -ZfT ^ JO

.

m /.y 9Q 0 • £. I J 1 R0 • J5 1

\ J571 -9 R4

1

Q

1 y J I

D

1

1 . nnn UUU "^7'^ 11 -^U sn R0 .

1

1 «f\ 00 474 fi9 474 n7 1 9 9z . 71 J57Q1 y 9£. . R5Q9 0 jy£- J . 54JH

1

1 Qy R7A 11 . nnn UUU _3 / . Z.D I R0 . \«« 1 00 474 fi9 474 ni 1 . 1 J

T. A AlA J? . J>D J 9fi . ZD

1Q1 y J 1

J

1

1 . nnn UUU "^7R Q9R R0 1 fifi . 100 474 fi9 474 R

1

- n4 4t 7R8 1 . / 00

1

.ouRn

1

1 Qy JR7fi l\j 11 . nnn UUU ''iRn Q9fl AlA fi9 474 Q

1

H / H ^y

\

- nfi . UD J5 u J5 1

I 5RJO 5 45fi5 11 . nou^

1Qly Oil 1

I . nnn UUU R0 .

1

1 ««DO 474 fi9 475 ^ 1 Jm 5^J

J

_ 1 Q f. 905"^ D. ^Vjj D.Un 1 '^R 1 JO J. 10 101 y J«S7fl lO 1

1 . nnn UUU j)OH ^R4 .01/ R17 0 . I DO 474 fi9 47H 5 9fi f J • (CD _ 1 T

• \ J

C OQ/IQ D . OyHO «D . 7579 /J / Z L.9 m n4UH

19 579 1.000 387.150 8.166 474.62 474.83 -.04 7.5842 7.5381 .61 19 580 1 .000 390.317 8.166 474.62 473.17 .30 8.2737 8.5985 -3.78

19 581 1.000 367.594 8.480 492.88 492.81 .01 4.8263 4.8427 -.34

19 582 1.000 369.261 8.480 492.88 493.03 -.03 5.5158 5.4770 .71 19 583 1.000 370.928 8.480 492.88 493.24 -.07 6.2053 6. 1 1 14 1.54

19 584 1.000 372.594 8.480 492.88 493.44 -.11 6.8948 6.7458 2.21

19 585 1.000 374.594 8.480 492.88 493.16 -.06 7.5842 7.5072 1.03

19 586 1.000 377.039 8.480 492.88 492.28 .12 8.2737 8.4377 -1 .94

19 587 1.000 349.483 8.819 512.59 512.16 .08 2.7579 2.8876 -4.49

19 588 1.000 351.039 8.819 512.59 512.20 .08 3.4474 3.5684 -3.39

19 589 1.000 353.706 8.819 512.59 512.88 -.06 4.8263 4.7353 1.92

19 590 1.000 355.094 8.819 512.59 513.13 -. 10 5.5158 5.3428 3.24

19 591 1.000 356.483 8.819 512.59 513.37 -.15 6.2053 5.9502 4.29

19 592 1.000 359.594 8.819 512.59 513.41 -.16 7.5842 7.3103 3.75

19 593 1.000 361 .650 8.819 512.59 512.78 -.04 8.2737 8.2086 .79

75
Table 7. (Continued)

Data sources and ID numbers; (l)Virial Equation, {3)Beattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

ID Data We ight Temp. Density Dens i ty Dens i ty pexpt p , ca I c Pressur

Poi nt expt ca 1 c Di ff

.

Diff

.

No. K mol/L kg/m-^ kg/m^ % MPa MPa % 4302 594 1.000 140.000 12.809 744.53 743.88 .09 31.2779 32.8854 -4.89

4303 595 1 .000 140.000 12.784 743.04 742.49 .07 27.8345 29. 1743 -4,59

4304 596 1 .000 140.000 12,758 741.56 74 1 .08 .06 24.3914 25.5359 -4.48

4305 597 1.000 140.000 12.733 740.07 739.65 .06 20.9481 21.9549 -4.59

4306 598 1.000 140.000 12.707 738.59 738.20 .05 17.5051 18.4307 -5.02

4307 599 1.000 140.000 12.681 737.08 736.72 .05 14.0619 14.8951 -5.59

4308 600 1.000 140.000 12.655 735.54 735.22 .04 10.6191 1 1 .3508 -6.45

4309 601 1 .000 140.000 12.628 733.98 733.69 .04 7.1760 7.8265 -8.31

4310 602 1.000 140.000 12.601 732.44 732. 14 .04 3.7333 4.4005 -15.16

3601 603 1 .000 160.000 12.548 729.37 729.01 .05 36.0986 36.9184 -2.22

3602 604 1 .000 160.000 12.516 727.45 727. 18 .04 31 .9664 32.5829 -1 .89 3603 605 1 .000 160.000 12.483 725.55 725.31 .03 27.8343 28.3496 -1 .82 3604 606 1 .000 160.000 1 2.454 723.90 723.73 .02 24.391

1

24.7550 -1 .47 3605 607 1.000 160.000 12.426 722.25 722,12 .02 20.9479 21 .2376 -1 .36

3606 608 1 .000 160.000 12.397 720.58 720.47 .01 1 7.5048 1 7.7234 -1 .23 3607 609 1 .000 160.000 12.368 718.90 718.80 .01 14.0617 14,2744 -1 .49 3608 610 1 .000 160.000 12.345 71 7.55 717.44 .02 1 1 .3074 1 1 .5312 -1 .94 3609 61

1

1 .000 160.000 12.322 716.19 716.06 .02 8.5529 8.8182 -3.01

3610 612 1 .000 160.000 12.298 714.83 714.65 .02 5.7987 6. 1467 -5.66

361

1

613 1 .000 160.000 12.281 713.81 713.58 .03 3.7330 4. 1760 -1 0.61 3612 614 1 .000 160.000 12.263 71 2.77 712.50 .04 1 .6672 2. 1727 -23.27

3701 61 5 1 .000 180.000 12.263 712.75 712.48 .04 36.0984 36.6620 -1 .54 3702 616 1 .000 180.000 1 2.226 710.65 710.44 .03 31 .9664 32.3878 -1 .30 3703 617 1 .000 180.000 12. 189 708.47 708.35 .02 27.8343 28.0762 -.86

3704 618 1 .000 180.000 12. 157 706.62 706.57 .01 24.391

1

24.4925 -.41 3705 619 1 .000 180.000 12. 125 704.77 704.76 .00 20.9478 20.9834 -. 17 3706 620 1.000 180.000 12.093 702.90 702.90 0.00 17.5047 1 7.5051 -.00

3707 621 1 .000 180.000 12.061 701 .03 701 .01 .00 14.0616 14.1012 -.28

3708 622 1.000 180.000 1 2.034 699.49 699.46 .00 1 1 .3073 1 1 .3552 -.42

3709 623 1 .000 180.000 12.008 697.93 697.89 .01 8.5528 8.6180 -.76

3710 624 1.000 180.000 1 1 .980 696.33 696.29 .01 5.7986 5.8816 -1 .41 371

1

625 1.000 180.000 1 1 .961 695.20 695.06 .02 3.7329 3.9557 -5.63

3712 626 1 .000 180.000 1 1 .940 694.01 693.82 .03 1.6671 1 .9791 -15.76

3801 627 1 .000 200.000 1 1 .981 696.38 696.14 .03 36.0981 36.5395 -1 .21 3802 628 1 .000 200.000 1 1 .940 694.00 693.86 .02 31 .9662 32.2189 -.78

3803 629 1 .000 200.000 1 1 .899 691 .63 691 .53 .01 27.8341 28 . 0 1 44 -.64

3804 630 1 .000 200.000 1 1 .864 689.58 689.54 .01 24.3910 24.4689 -.32

3805 631 1 .000 200.000 1 1 .828 687.48 687.49 -.00 20.9477 20.9206 .13 3806 632 1 .000 200.000 1 1 .792 685.38 685.40 -.00 17.5047 17.4691 .20 3807 633 1 .000 200.000 1 1 .755 683.25 683.25 -.00 14.0616 14.0573 .03 3808 634 1 .000 200.000 1 1 . 725 68 1 . 50 681 .50 0.00 1 1 .3073 1 1 .3074 -.00

3809 635 1 .000 200.000 1 1 M/l 679.70 .00 8.5528 8.5718 -.22

3810 636 1 .000 200.000 1 1 663 677.89 677.86 .00 5.7986 5.8354 -.63

381 1 637 1 .000 200.000 1 1 .639 676.50 676.46 .0

1

3.7329 3.7939 -1 .61 3812 638 1 .000 200.000 11.615 675.10 675.02 .01 1 .6671 1 .7793 -6.31

3901 639 1.000 220.000 1 1.701 680.1

1

679.94 .02 36.0987 36.3776 -.77

3902 640 1.000 220.000 1 1.655 677.44 677.40 .01 31.9668 32.0217 -.17

3903 641 1.000 220.000 1 1.608 674.72 674.79 -.01 27.8346 27.7285 .38 3904 642 1.000 220.000 1 1 . 569 672.44 672.55 -.02 24.3914 24.2220 .70 3905 643 1.000 220.000 1 1 . 530 670.15 670.25 -.01 20.9481 20.8026 .70 3906 644 1.000 220.000 1 1.489 667.77 667.88 -.02 17.5050 17.3531 .88 3907 645 1.000 220.000 1 1.446 665.30 665.44 -.02 14.0618 13.8668 1.41 3908 646 1.000 220.000 11.410 663.20 663.43 -.03 1 1.3076 10.9962 2.83

3909 647 1.000 220.000 11.374 661 .1

1

661 .37 -.04 8.5530 8.2088 4.19

3910 648 1.000 220.000 1 1.338 658.98 659.25 -.04 5.7987 5.4583 6.24

76
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

1

D

Data We i ght Temp. Dens i ty Dens i ty Dens i ty pexpt p

ca 1 c Pressur

Poi nt expt ca 1 c Diff. Diff.

No. K mol/L kg/m-^ kg/m-^ % MPa MPa %

391

1

549 1 .000 220.000 1 1 .310 657.39 657.62 -.04 3.7331 3.4357 8.66

391

2

650 1 .000 220.000 1 1 .283 655.79 655.96 -.03 1 .6672 1 .4551 14.57

4001 651 1 .000 240.000 1 1 .424 663.98 663.83 .02 36.0977 36.3296 -.64

4002 652 1 .000 240.000 1 1 .372 661 .00 661 .00 .00 31 .9657 31 .9687 -.01 4003 653 1 .000 240.000 1 1 .320 657.98 658.07 -.01 27.8336 27.7063 .46 4004 654 1 .000 240.000 1 1 .275 655.36 655.55 -.03 24.3909 24. 1434 1 .03 4005 655 1 .000 240.000 1 1 .229 652.66 652.94 -.04 20.9473 20.5820 1 .77 4006 656 1 .000 240.000 11.181 649.91 650.25 -.05 17.5042 17.0823 2.47

4007 657 1 .000 740.000 1 1 . 1 33 647.07 647.46 -.06 14.061

1

1 3.5989 3.40

4008 658 1 .000 240-000 1 1 .092 644.74 645. 1

5

-.06 1 1 .3069 10-8748 4.45

4009 659 1 .000 240.000 1 1 .051 642.31 642.77 -.07 8.5522 8.0299 6.50

660 1 .000 240.000 1 1 .008 639.86 640.3

1

-.07 5.7980 5.2994 9.41

40 1

1

661 1 .000 740.000 1 0.976 638.00 638.41 -.06 3.7324 3.2889 1 3.49

4012 662 1 .000 240.000 10.945 636 . 18 636.46 -.04 1 .6665 1 .3777 20.96

4101 663 1 .000 760.000 1 1 . 149 648.02 647.76 .04 36.0979 36.4519 -.97

4 102 664 1 .000 760-000 1 1 .092 644.71 644.60 .02 31 .9659 32 . 1 1 1

7

-.45

4 1 03 665 1 .000 760-000 1 1 .033 64 1 .31 64 1 .30 .00 27 .8339 27 .8391 4104 666 1 .000 260-000 10.983 638 . 39 638.45 -.01 24. 3908 24 . 3 1 6

1

.31 4 105 667 1 .000 260-000 1 0.931 635.35 635.49 -.02 20.9475 20.7759 .82 4106 668 1 .000 260-000 1 0.876 632. 17 632.42 -.04 17. 5045 17 .2294 1 .60 4107 669 1 .000 260-000 10.819 628.84 629.21 -.06 1 4.0613 1 3.5707 2.86

4 108 670 1 .000 260.000 10.771 626.07 626. 54 -.07 1 1 .3071 10.8399 4.31

4109 671 1 .000 260.000 10.723 623.27 623.76 -.08 8,5526 8.0753 5.91 4110 672 1 .000 260.000 10.673 620.36 620.88 -.08 5.7984 5.3 147 9. 10 4111 673 1 .000 260.000 10.635 618.17 618.64 -.08 3.7328 3.3 1 16 1 2 .72

41 12 674 1 .000 260.000 10.597 61 5.91 616.32 -.07 1 .6669 1 .3154 26.72

4201 675 1 .000 280.000 10.846 630.43 630 . 52 -.01 34.7206 34.6103 .32 4202 676 1 .000 280.000 10.794 627.38 627.54 -.02 31 .2773 31.1014 .57 4203 677 1 .000 280.000 10.739 624. 17 624.44 -.04 27.8338 27.5496 1 .03 4204 678 1 .000 280.000 10.681 620.80 621 .20 -.07 24.3907 23.9675 1 .77 4205 679 1 .000 280.000 10.620 617.26 617.83 -.09 20.9475 20.3804 2.78

4206 680 1.000 280.000 10.557 613.59 614.29 -. 1

1

17.5045 16.8400 3.95

4207 681 1.000 280.000 10.491 609.80 610.58 -.13 14.0614 13.3646 5.21 4208 682 1.000 280.000 10.437 606.64 607.46 -.14 1 1.3071 10.6033 6.54

4209 683 1 .000 280.000 10.381 603.39 604. 19 -.13 8.5526 7.8982 8.29

4210 684 1 .000 280.000 10.323 600.02 600.77 -.12 5.7984 5.2 194 1 1 .09

421

1

685 1.000 280.000 10.279 597.45 598.08 -.11 3.7328 3.2524 14.42

4212 686 1.000 280.000 10.234 594.83 595.27 -.07 1 .6669 1 .3515 23.33

3501 687 1 .000 300.000 10.573 614.53 614.27 .04 34.7208 34.9909 -.77

3502 688 1.000 300.000 10.514 61 1.1 1 610.92 .03 31.2774 31.4665 -.60

3503 689 1.000 300.000 10.452 607.49 607.41 .01 27.8340 27.9054 -.26

3504 690 1.000 300.000 10.386 603.65 603.73 -.01 24.3909 24.3144 .31 3505 691 1.000 300.000 10.316 599.58 599.86 -.05 20.9476 20.7038 1.18

3506 692 1.000 300.000 10.242 595.31 595.77 -.08 17.5045 17.1296 2.19

3507 693 1.000 300.000 10.166 590.90 591.44 -.09 14.0613 13.6494 3.02

3508 694 1.000 300.000 10.100 587.07 587.76 -.12 11.3071 10.8072 4.63

3509 695 1.000 300.000 10.031 583.02 583.87 -.14 8.5525 7,9763 7.22

3510 696 1.000 300.000 9.958 578.82 579.73 -.16 5.7983 5.2152 1 1.18 3511 697 1.000 300.000 9.904 575.64 576.44 -.14 3.7326 3.2438 15.07

3512 698 1.000 300.000 9.848 572.40 572.97 -.10 1.6667 1.3373 24.63

77
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

1 n1 u Ucl 1 O Wc 1 y n

1

Temp. Dens ity \JKS \ lot 1 y net +\/ 1 1 ^ 1 1 y '^expt p^ca 1 cr 1 t?o o ui Pr» rvJ f

1 n +1 expt ca I C n i f f n i f f NU • v mo 1/L p MPa MPa fi

oyy 1 nnn I .uuu j>z 1

1 nu . Q7P yzo .027 1 CO

1 •DO 1

1 . 5HPo — .un7/ .UDoy nftRQ nftRQ • UDoy •un7/ Z.J /UU 1 • uuu J44 . ZD 1 .024 1 .42 1

1 .4Z47 _ 1

R

.UDoy nftRQ • nftRR UDOO 1 7 • 1 / CO /U 1 1 nnn 1 .UUU J 1 1 »J y'i .022 1 .29 1

1 . 7Qzy _ OT .UDoy nftfio nftftft

• UDOO 77 • ZP

1 ^ Z 0 /UZ 1 • UUU A 1 n Q7R .020 1 • 18 1 1 ft

1 . 1 0

—~. 7ZP5 .uooy nftRO nftftft

• UDOO 7 R • Z P

/U-> 1 • UUU . ZD 1 .019 1 .09 1

1 .uyno — 7ft . ZD .UDoy nftfto nftftft

• UDOO 7ft • ZD ZD 1 •UUU 477 KQ/l .0 1

7

1 .01 11 . n7UZ —— .Z77/ .UDoy nftfto nftftft

• UDOO • 77Z / /UP 1 nnn 1 • UUU 5 1 n Q7fi 3 1 u. yzo .016 .95 .yp05 —~.ZP75 nftfto • UDoy nftftft • UDOO • 7RZP

/Uo 1 nnn 1 • UUU 1 n 07Q J 1 u. yzcs .040 2.34 7 74 Z. j4 n7 • U J

1 ni 7 . 1 U 1 P1 n 1

4

• 1 U 1 4 n7 -•Up

/u /

1

1 • nnn UUU T/14 9(;i

J'f H . ZD 1 .036 z. 10 7Z .

1

i nu

— 17 1 n 1

7

. 1 U 1 P

1 n 1

7

. 1 U 1 z

1 -z • 1 J

1.0 7Ai5 /Uo 1

1 • nnn UUU T77 RQ/I r\ "Z "z .033 1 nn 1 .90 1 Q

1

1 . y 1 - . 77ZZ .

1

1 niU 1 P7 .lull mil 7 1 • Z 1 £.0 700 1

1 • nnn UUU /in Q7ft nz n .030 1 • 74 11 . 75/ P - . 77Z /

1 n 1

7

. 1 U 1 P .lull mil • Z77/ Z 3 7/

1

1 nu

1

1 • nnn UUU . ZD 1 • Ozo 1 £ 11 .51 1 ft 1

1 . O 1 _~. 3U7n .

1

I niU 1 P7 . mi1 U 1 nu • PU7n

I. J 7 1 1 / 1 i 11 • nnn UUU 477 504 .UZO 1 ACS

1 .4y 11 . PU5n _~ . JU7n .

1

1 niU I P7 . mm1 U 1 u • JU7n

7R 71 9 1 nnn 511 nu . Q7R y zo .UZ4 1 7n 1 .39 1

1 . 4n4U - . 7Qzy .

1

1 niU 1 P7 . mm1 U 1 u • 7Qzy

"^R 7 1 1

1 • nnn UUU ->'I in1 u . Q7R ^zo 7 OO j.zz D7 . 77ZZ a

1

1 A4 1 770 1 7ft 1 . 1 PO i - •

1IP7

71 A 1

1 • nnn UUU jH't 7/14 7fi1 . ZO 1 n (^n 7 Q Q Z.OO 7Z.OOftft _ nfi . UD .

1

t 770 p / y .

1

1 P77R/ O nfi • uo

9S 7 1 S 1 nnn 777 5Q4 n4 ^ .U4P 7Z.DUftn 7 fil - 1R 1 770 .1

1 J77fi / u 1R 7^£- J 71

6

1 .000 410.928 n4 1 .U4 1 7Z.JO7Q 7 39 -.26 . 1 379 . 1 375 .76

71

7

1 .nnn 444.261 n7Q .Ujo 7 1

Q

z. ly 2.20 -.31 . 1 379 . 1 375 .31

z -J 71ft 1 nnn 477 5Q4 n7 R .U J J 7Z . n4U4 7 04 - . jH34 1 379

25 719 1 .000 51 0.928 n77 1

1 .yuon 1 .91 -.32 . 1 379 . 1 375 .32 720 1 ,000 310.928 no 5 44 .y4Q4 4.92 .32 .2068 .2075 -•30

75 721 1 .nnn 344 .261 n7 R A 7Q 4 ._)0 4.38 .08 .2068 .2070 -•08

75 777 1 nnn 777 5Q4 nftQ .UDo 7 Q ^ j.y p 7 Q5 - 1

1

7nfiR 1

0

75 77"^ 1 nnn 4 1 0.928 nft7 .UDZ 7 ftn J .ou 3.61 -.77 7064 .77 75 1 nnn 444.261 n c:7 .up / 7 7 1 J. J 1 3 37 -. 37 .2068 .7067 .37 • j^

75z. J 775 1

1 • nnn UUU 477 5Q4 n^7 7 n 1^ J. UP 3 OR - 75 .7053 .74 75 1 £.0 1

1 .UUU nnn -/511 nu . Q7ft y ZO A4 Q 7 G ft Z.OO 7z . R7o / - 7ft . 7nfiR ZUDO . 7nfti ZUO 1 7fi 75 777 1 nnn _>7in1 u . Q7ft ^zo 11ft

• 1 1 O D. /Z ftO fiO . D^ 47 . 77Z / JO5R 77ft0 - • j^7Q

75 / zo 1

1 . nnn UUU 744 7fi1 _J44 . ZO 1 .102 5.93 p.y 5 0 11 . 7nzu . 77Z / PO5R .Z77ft7 / OP - 1

Q

• 1 y 75 77Q / zy 1

1 .UUU nnn 77 7 5Q4 .092 5.32 P.5 JZ77 .UUnn • Z775R / PO . Z77/ PO5R —— •UUnn

£0 /jU 11 . nnn UUU 4

4 1

1 n Q7Q u . yzo .083 4.84 4 04 4 . 04 _—

1 Q . 1 y .Z77RR / PO . Z77/ 57PP 1 R • 1 0 75 77 1 /J) 1 1

I .UUU nnn 444 7fi1 *+4*f . ZD 1 r\7£ .076 4.44 4 .4P4 5 — .PU7n . 775R Z / PO . Z775n / PU • zy7Q 75 7*^7 1

1 .UUU nnn 477 *\ 1 1 % jy'\ 5Q4 mi .0 /I A 11 4. 1 1 4 .

1

1 7Z — .p77/ .Z775R / PO . Z774R / 40 7ft • PO

75 1

1 . nnn UUU 13511 nu. Q7R yzo .056 3.8z D7 ft4 . 04 - . PO7R . 77Z / PO5R . 774R Z / 40 • PO7R

75 T'.A 1

1 . nnn UUU 744 7ft 1 J>44 . ZD 1 .1 58 9.16 0 1

7

y . 1 -J z c .P P .44 11 77P / .44 1

1 PU5n —— • PZ77

75 /_> 131

1 .UUU nnn J7771 1 % 5Q4 jy'\ .140 8. 16 Q 14 O . 1 4

1 R . 1 0

4 1 77 .4 1 J / 4 14 4 .4 1 44 _— •ID1ft 75 / jD 1

1 . nnn UUU 44 1 n Q7fl I u . yzo . 127 1 ,YI 7 77 —— n7 .u / A 1 77 .4 1 P/ 4 1 74 .4 1 J4 n7 • U / 7 R /J /

1

1 . nnn UUU 444 /I 4 / 7ft 1 • ZD 1 .116 6. 74 ft 7 R 0. / P -. 7ft ZD A 1 77 .4 1 J / A 1 7ft .4 1 ZO 7 R • ZP

7^ 1 nnn 1 . UUU 477 RQ4 . 107 6.21 ft OA D .Z4 Z-7 -._>/ A 1 77 .413/ 4 1 77 .4 1 ZZ 7ft

• JO

75 1

I . nnn UUU 519 1 nu. Q7R yzo

Ann .099 5.n 5 ftn P. OU —— .4411 .44 1

1 77J / .4A 11 7nzu •4U 4n

75 IAD 1

1 . nnn UUU 744 7ft

1

. ZO

1

OO 1 .281 16.31 1

1 ft0 .zy70 .

1

t 7Z .Doyp ftRQ5 .oyu ft on 11 —— in • 1 u 75 74 1 1

1 .UUU nnn 77 7 504 J 1 I • _3y4 .245 14.24 14 1ft 1 4 . 1 O

4 7 .4 JftRQR .Doyp .oyz ftQ7 1

1 —— • JO7R 75 7A7 / HZ 1

1 .UUU nnn 44 1 n Q7f? 1 u. yzo .2 18 1 Z.70 1 7 ftQ

1 Z .Do 1 4

. 1 4 .Doyp fton7 .Dyup _-•IP17 75 74 \ 1

1 . nnn UUU 444 7ft1 . ZO

1

.198 1 1.50 1

1 11 57 . PZ —— . 171 / .Doy ftRO 5p .D004 ftRR4 1 ft • 1 D 25 744 1.000 477.594 .181 10.55 10.58 -.33 .6895 .6873 •31 25 745 1.000 510.928 .168 9.76 9.80 -.38 .6895 .6870 •37 25 746 1.000 377.594 .393 22.82 22.71 .50 1 .0342 1.0385 -•41 25 1^1 1.000 410.928 .343 19.93 19.86 .36 1.0342 1.0375 -•31

25 748 1.000 444.261 .306 17.81 17.82 -.03 1.0342 1 .0339 • 03

25 749 1.0C0 477.594 .279 16.19 16.24 -.27 1.0342 1.0316 •25 25 750 1.000 510.928 .256 14.91 14.96 -.35 1.0342 1.0308 .33 25 751 1.000 377.594 .566 32.93 32.88 .14 1.3790 1.3803 -.10

25 752 1 .000 410.928 .481 27.96 27.80 .56 1.3790 1.3854 -.46

25 753 1 .000 444.261 .423 24.58 24.56 .07 1 .3790 1.3798 -.06

78
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)Olds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp. Density Density Density ^expt ^calc Pressure

Point expt calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa %

25 754 1 .000

25 755 1 .000

?'5 1 .000

75 757 1 .000

C J 75R 1 .000

75 1 .000

75 760 1 .000

7'i 7fi1 1 .nnn

7'S 7fS7 1 000

7'i / U-^ 1 .000

7S / OH 1 nnn

0^i.J / DD 1 nnn

/ DD 1 nnn

ZD /O /

1 nnn

Z.J /DO 1

1 .uuu nnn

ZD /oy 1 nnn 1 . UUU

ZD / /U 1

1 nnn .UUU

ZD / / 1 1 AAA 1 .UUU

ZD / /Z 1 AAA 1 .UUU ZD / /J 1 AAA 1 .UUU

ZD 1 /4 1 AAA 1 .UUU ZD *7 7 R / /D 1 AAA 1 . UUU

zD / /D 1 AAA 1 .UUU

ZD "7 "7 "7 III 1 AAA 1 .UUU

ZD 1 lo 1 AAA 1 .UUU

ZD / /y 1 AAA 1 .UUU

ZD 1 AAA 1 .UUU ZD "7Q 1 lo I 1 AAA 1 .UUU

ZD / tsz 1 AAA 1 .UUU zD "70 T 1 AAA 1 .UUU

ZD /C)4 1 AAA 1 . UUU

ZD 7R R /O D

1

1 . nnn uuu

ZD / OD 1

1 . nnn uuu

ZD 7ft7 /Of 11 .uuu nnn

7R 7RR 1 nnn 7SZD 7fiQ 1

1 .uuu nnn

7RZD 1 nnn

7S 1 J7 I 1

1 . nnn uuu

ZD 7Q9 / ^Z 11 . nnn uuu

9S 1

1 . nnn uuu

7'i 1

1 . nnn uuu

25 795 1.000

25 796 1.000

25 191 1.000

25 798 1.000

25 799 1.000

25 800 1.000

25 801 1.000

25 802 1.000

25 803 1.000

25 804 1.000

25 805 1.000

25 806 1.000

25 807 1.000

25 808 1.000

25 809 1.000

477.594 .381 510.928 .348

310.928 9.639

344.261 8.887

377.594 7.908

410.928 .637

444.261 .549

477.594 .489

510.928 .444

310.928 9.653

344.261 8.907

377.594 7.947

410.928 .819

444.261 .686

477.594 .603

510.928 .543

310.928 9.677

344.261 8.948

377.594 8.023

410.928 1.336

444.261 1.006

477.594 ,854

510.928 .755 310.928 9.700

344.261 8.983

377.594 8.091

410.928 6.641

444.261 1,426

477.594 1.144

510.928 .987

310.928 9.724

344.261 9.018

377.594 8.156

410.928 6.876

444.261 2.057

477.594 1.486

510.928 1.244

310.928 9.769

344.261 9.083

377.594 8.276

410.928 7.192

444.261 4.960

477.594 2.407

510.928 1.844

344.261 9.147

377.594 8.379

410.928 7.410

444.261 5.938

477.594 3.672

510.928 2.558

310.928 9.864

344.261 9.211

377.594 8.495

410.928 7.621

444.261 6.492

477.594 4.929

22.14 22.18

20.24 20.30

560.28 560.20

516.56 516.36

459.64 458.95

37,04 36.77

31.88 31.82

28.40 28.42

25.79 25.85

561.07 560.88

517.73 517.47

461,89 461,35

47.60 47.22

39.85 39.71

35.04 35.02

31.56 31.61

562.45 562.21

520.08 519.61

466.33 465.79

77.67 77.52

58.46 58,12

49,64 49,47

43.90 43.86

563.83 563.51

522.11 521.67

470.30 469.84

385.99 386.18

82.86 82.28

66.47 66.08

57.39 57.23

565.22 564,78

524.16 523.65

474.06 473.56

399.66 399.50

119.54 119,17

86.35 85.72

72.28 71.97

567.83 567.25

527.97 527.42

481.03 480.26

418.02 417.31

288.31 285.03

139.91 139.55

107.16 106.59

531.64 530.96

487.03 486.18

430.72 429.97

345.15 345.18

213.44 214.08

148.69 149.16

573.32 572.47

535.38 535.09

493.79 492.76

442.99 442.25

377.35 376.62

286.50 286.03

-. 17 1 .3790

-.30 1 .3790

.01 1 .7237

.04 1 .7237

. 1

5

1 .7237

.72 1 .7237

.2

1

1 .7237

-.07 1 .7237

-.24 1 .7237

.03 2.0684

05 2.0684

1

7

7 nfifi4

. O 1 7 nfiftd 7 nfiR4

nfi . uo

_ ID 7 nf,RA

. u^ 7 7'=i7Q .uyno 7Z . 7/ ^70 J 1 y

.

1

1 9z Z.7 7^70 Ijiy

1 Q Z.9 7 '=i7Q 1 J ly

. DO 9 7R7Q

. jD 9 7 R7Q Z. 1 0 ly

. nouy 9 7^70

.UD

. nouy

1 n . 1 u

-z AA1A

nR -.UD "Z A A 1A J. 44 /4 7 1 A A ~1 A D.44 /

4

RD . DO A A ~IA D.44 /4 .ZO9fl D.44 z AAIA74 .uonn 4 . 1 Doy

1 n . 1 u 4. 1 DDy

.

1

1 nu A4 1 ^ftO .

1

DOy

OA. A4 1 "^fiQ . 1 ^yjy ^1

. J 1 79 A 1 "^fiq AA A 1 "^fiQ

• in1 u J m J \ JO

,

1

1 nu S J 11 SRJO

, 1 u J u J t JO

5 51 58 1.14 5.5158

.26 5.5158

.53 5.5158

.13 6.8948

.18 6.8948

.17 6.8948

-.01 6.8948

-.30 6.8948

-.32 6.8948

.15 8.6184

.05 8.6184

.21 8.6184

.17 8.6184

.19 8.6184

.17 8.6184

1 .3768 . 1

6

1 .3751 .28

1 .7638 -2.27

1 .784 5 -3.41

1 .8207 -5.33

1 .7332 -.55

1 .7267 -. 1

7

1 .7226 .06

1 .7200 .22

2. 1654 -4.48

2. 1509 -3.83

2. 1487 -3.73

7 nfinn 7 n74 1 - 77

9^ • nfiQR UU jO - C\l • \J 1

z.7 . nfisi UU J 1 . 1 u

9 RR'^Q -4 '^7 4 . D / 9 Q 1 ^^7 Z . 7 ID/ J , _> D Z9 , RA04 RQDy —^— D,uyno

9Z, 7fin9 /DUZ — , uo

Z

9 . 7^Q9 / D y/ _ /1

1

— ,4 1 Z . / DD

/

—— , 7RZD

9z • 7/ Dyy RQQ —— . n7u / ^ C997 D.DZZ

/

—4 a 04

z fiAA4 D •DUU4 —A—4. ZD9R

z R'Z A 1 D. DDU

1

—9—Z '^/l . D4 D.4DyU "Z >1 "ZQA OA ,Z4

Z / A 1 ,1 D. 4D 1

4

— .4 1 D.4DZ "Z yl f^O 1

1

A "Z D.4DDJ z /I R R'Z _ 9"^ — . ZD

4 . juZ.^ —— D.DU R Kn

A4.D IRQ loy —4 . 97Z Z A4 . 9'^9R ZDZO -9z . 97z / AH .

1

1 4fiR HwO - . 94ZH

A4 .1

1 491 4Z I - .ID1 AH .

11 J\J\J 'ifiR _ A9, A 1 snq - ^^4 5.R507 -5 .77

5 777R -3 67

5.6882 -3 03

5J • J5R37 U_J / -1 . 22 5.5569 -.74

5.5233 -.14

5.5360 -.37

7.1738 -3,89

7.1066 -2,98

6.9882 -1 ,34

6.8936 ,02

6.8827 .18 6.8806 .21 9.1491 -5,80

8.7410 -1,40

8.9048 -3,22

8.7354 -1.34

8.6720 -.62

8.6338 -.18

79
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

ID Data Weight Temp. Density Density Density ^expt ^calc Pressure

Point expt calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa %

91^ CJ 0 1 U

1

1 . onA uuu

9Si.j R 1 1 1 nnn

9S S0 1

1 z9 1 nnn

6.0 0 1 J 1 • UUU

ZD Q 1 >1 1 nnn 1 .UUU

Q 1 R o 1 D1 nnn 1 »UUU

9R sift O t D 1

1 . nnn UUU

O c: /LO 0 1 *7 0 1 /1 nnn 1 .uUu

ZD Q 1 Q 1 nnn 1 .UUU

9 R i-J Q 1 Q 1

1 . nnn UUU

9 R ozu 1 .UUU

9 R Q9 1 OZ 1 1

1 nnn . UUU

9C; ZD Q99 tszz 1 nnn 1 .UUU

9 R ZD Q9 T oZd 1 nnn 1 . UUU

9c; ZD Q 9>1 0Z4 1 nnn 1 . UUU

9 R ZD Q9 R yzD 1 nnn 1 .UUU

9 R ZD Q 9ft oZo 1 nnn 1 . UUU

9ZDR Q9 7 oZ /1

1 nnn .UUU

ZD9S 1! . nno UUU

ZD 39ozyQ 11 . nnn UUU

9RZD 0 J)U 1

1 . nnn UUU

9RZD 1 1

1 .UUU nnn

9R ODS. 1

1 . nnn UUU

9RZD OJ D

1

1 .UUU nnn

ZD 0J4 11 .UUU nnn

9^ZD ODD 1

1 .UUU nnn

9SZD 1

1 . nnn UUU

9RZD OD /1

1 .UUU nnn

9RZD 0JO 1

1 .UUU nnn

ZD9R 11 .UUU nnn

ZD9R R/10 O'tU 1

1 .UUU nnn

9 R ZD Q /I 1 1 nnn 1 .UUU

ZD 842 1 .000

ZD 843 1 nr\A

1 .000

ZD 844 1 Ann 1 .000

25 845 1 .000

25 846 1 .000

25 847 1 .000

25 848 1 .000

25 849 1 .000

25 850 1 .000

25 851 1 .000

25 852 1.000

25 853 1.000

25 854 1.000

25 855 1.000

25 856 1.000

25 857 1.000

25 858 1.000

25 859 1.000

25 860 1 .000

25 861 1.000

25 862 1.000

25 863 1.000

25 864 1.000

25 865 1.000

510.928 3.533

344.261 9.285

377.594 8.599

410.928 7.796

444.261 6.832

477.594 5.627

510.928 4.372

310.928 9.956

344.261 9.348

377.594 8.694

410.928 7.947

444.261 7.083

477.594 6.066

510.928 5.000

310.928 10.003

344.261 9.406

377.594 8.777

410.928 8.072

444.261 7.281

477.594 6.381

510.928 5.452

310.928 10.084

344.261 9.520

377.594 8.925

410.928 8.291

444.261 7.598

477.594 6.842

510.928 6.085

310.928 10.154

344.261 9.619

377.594 9.054

410.928 8.474

444.261 7.845

477.594 7.179

510.928 6.517

310.928 10.226

344.261 9.707

377.594 9.171

410.928 8.626

444.261 8.049

477.594 7.442

510.928 6.844

310.928 10.287

344.261 9.787

377.594 9.273

410.928 8.760

444.261 8.227

477.594 7.664

510.928 7.108

310.928 10.345

344.261 9.864

377.594 9.374

410.928 8.879

444.261 8.377

477.594 7.856

510.928 7.353

205.34 207.17

539.71 538.96

499.80 498.66

453.14 452.21

397.09 396.23

327.04 326.98

254.10 255.54

578.70 577.81

543.37 542.61

505.31 504.01

461.89 460.66

411.68 410.76

352.60 352.94

290.61 291.60

581.43 580.33

546.71 546.05

510.14 508.93

469.20 468.04

423.21 422.43

370.88 371.70

316.88 318.27

586.11 585.10

553.31 552.43

518.73 517.73

481.90 480.58

441.64 440.75

397.68 398.50

353.69 355.09

590.22 589.57

559.11 558.26

526.23 525.49

492.57 491.08

455.98 455.07

417.26 417.85

378.78 380.29

594.38 593.77

564.23 563.63

533.06 532.44

501.36 500.15

467.83 466.91

432.58 433.11

397.78 399.40

597.93 597.74

568.84 568.62

538.98 538.77

509.17 508.19

478.16 477.07

445.45 445.78

413.17 414.82

601.29 601.52

573.32 573.29

544.85 544.58

516.06 515.42

486.88 486.00

456.63 456.65

426.25 427.79

_ DO .07 Q C 1 0 .O 1 04

.

1

( L4 1 U. _?4^ 1 9'^

. ZJ in ^491 1 U . J)4^ t 9 1 .Z 1 1 n ^^49

1

1 U. J4Z

1

. ZZ99 1 n 'KA 9 11 U. J4Z

1

.UZn9 1 n "XA 9 1

1 U. J4Z

1

_~ . R7D /

1 n ^^49

1

1 U.D4Z

1

• 1 D

19 nft Rfl

1 Z.UDDo

1 A

. 1 4

1 9 nft RQ 1 Z.UODo

9ft

. ZD 1 9 nft RQ 1 Z.UDDO

9"7 .z/ 1 9 nft RQ 1 Z .UDDO

99 . ZZ 1 9 nft RQ 1 Z .UDDO -.101 n 1 9 Aft RQ 1 Z.UoDo

-. J4 1 9 nftRO 1 Z.UDDo

1 Q . ly 1 J . /oyD

1 9

• 1 Z

1 7 on R Id. /oyD

9y1 .Z4 1 T 7Q n R

1 J . /oyD

9R .ZD 1

1 T 7QQR J. /oyD

1

R

1 X 7RQR 1 J . /oyD

— . 99ZZ ID./ oyD

- /I A .44 1 J . /oyD

1 7 17 D'^ftQ 1 / . ZDoy

1ft 1

1 7 9^ftQ / . ZDoy

1 Q . ly 17 9'^ftQ 1 / .ZDoy

97 1 7 9XftQ 1 / .ZDDy

• 9nzu 17 9'^ftQ 1 / . ZDoy

- .Z9 1

1 171 9'^ftQ / . ^ joy

—— .4UAO 17 9'^ftQ 1 / . zDoy

1 1 . 1 1 ZU.D04D 9n ftRA'^

. 1 D 9nzu. ftR/1'^ 004 J

1 4 . 1 9nzu ftRid'^

. 004

J

^n . jU 9n ftQ>i T ZU.004

J

9n .ZU 9n ft QA T. ZU.0043

1 A -. 14 9n ftQyl ZU.D04

3

A n -.4U 9n ft Qyl ZU.D04J

1 A

. 1

0

24. 1315

1 1 .1 1 24. 1316

. 12 24. 1316

.24 24. 1316

,20 24. 1316

-. 1

2

24. 1316

-.41 24. 13 16 .03 27.5790

.04 27.5790

.04 27.5790

.19 27.5790

.23 27.5790

-.07 27.5790

-.40 27.5790

-.04 31 .0264

.00 31 .0264

.05 31 .0264

.12 31 .0264

.18 31 .0264

-.01 31.0264

-.36 31.0264

8.5611 .67 10.6851 -3.21

10.6951 -3.30

10.5198 -1.69

10.4325 -.87

10.3453 -.03

10.2832 ,57

12.6701 -4.77

12.4388 -3.00

12.5087 -3.54

12.3394 -2.22

12.1901 -1.02

12.0384 .23 12.0104 .46 14.5673 -5.34

14.1284 -2.40

14.2364 -3.14

14.0792 -2.06

13.9167 -.91

13.7045 .62 13.6869 .75 18.0005 -4.24

17.7406 -2.84

17.6585 -2.39

17.6406 -2.29

17.4305 -1.11

17.1102 .74 17.0750 ,95

21,2051 -2.46

21.2133 -2.49

21.0366 -1.67

21.2216 -2.53

20.9289 -1.17

20.5648 ,58

20.4452 1.17

24.6478 -2.09

24.5336 -1.64

24.4558 -1.33

24.6249 -2.00

24.4237 -1.20

24.0008 .55 23.8062 1.37

27.7434 -.59

27.7331 -.56

27.7010 -.44

28.0273 -1.60

27.9790 -1.43

27.4837 .35 27.1768 1.48

30.8183 .68 31.0428 -.05

31.1915 -.53

31.3489 -1.03

31.3901 -1.16

31.0184 .03 30.5886 1.43

80
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

D Data Weight Temp. Dens ity Dens i ty Dens i ty ^C3 I C Pressur Point expt calc Diff. Diff.

No. K mol/L kg/m^ i<g/m^ % MPa MPa %

25 866 1.000 310.928 10.404 604.70 605.11 -.07 34.4738 34.0697 1.19

25 867 1.000 344.261 9.935 577.45 577.69 -.04 34.4738 34.2789 .57 25 868 1.000 377.594 9.464 550.08 549.97 .02 34.4738 34.5517 -.23

25 869 1.000 410.928 8.989 522.45 522.01 .09 34.4738 34.7202 -.71 25 870 1 .000 444.261 8.516 495.01 493.99 .21 34.4738 34.9397 -1.33

25 871 1.000 477.594 8.023 466.33 466.20 .03 34.4738 34.5225 -.14

25 872 1.000 510.928 7.526 437.42 439.00 -.36 34.4738 33.9619 1.51 25 873 1.000 310.928 10.515 61 1.16 61 1.84 -.11 41.3685 40.6438 1.78

25 874 1.000 344.261 10.076 585.68 585.79 -.02 41.3685 41.2710 .24 25 875 1.000 377.594 9.629 559.69 559.72 -.00 41.3685 41 .3507 .04 25 876 1.000 410.928 9.186 533.95 533.69 .05 41.3685 41.5322 -.39

25 877 1.000 444.261 8.754 508.85 507.87 .19 41.3685 41.8994 -1 .27 25 878 1.000 477.594 8.306 482.77 482.47 .06 41.3685 41 .5091 -.34

25 879 1.000 510.928 7.847 456.11 457.75 -.36 41.3685 40.7022 1 .64 25 880 1.000 310.928 10.612 616.81 618.05 -.20 48.2633 46.8447 3.03

25 881 1.000 344.261 10.199 592.84 593.14 -.05 48.2633 47.9678 .62 25 882 1.000 377.594 9.773 568.03 568.39 -.06 48.2633 47.9615 .63 25 883 1.000 410.928 9.364 544.29 543.87 .08 48.2633 48.5648 -.62

25 884 1.000 444.261 8.959 520.76 519.71 .20 48.2633 48.9193 -1.34

25 885 1.000 477.594 8.545 496.70 496.08 .12 48.2633 48.6023 -.70

25 886 1.000 510.928 8.118 471.83 473.16 -.28 48.2633 47.6182 1.35

25 887 1.000 310.928 10.703 622.08 623.82 -.28 55. 1581 53.0290 4.01

25 888 1.000 344.261 10.318 599.72 599.88 -.03 55.1581 54.9898 .31 25 889 1.000 377.594 9.910 576.00 576.23 -.04 55.1581 54.9459 .39 25 890 1.000 410.928 9.520 553.31 552.93 .07 55.1581 55.4693 -.56

25 891 1.000 444.261 9.129 530.59 530.08 .10 55.1581 55.5157 -.64

25 892 1.000 477.594 8.741 508.04 507.82 .04 55.1581 55.2935 -.24

25 893 1.000 510.928 8.351 485.41 486.29 -.18 55. 1581 54.6653 .90 25 894 1.000 310.928 10.795 627.44 629.22 -.28 62.0528 59.7311 3.89

25 895 1.000 344.261 10.419 605.61 606.11 -.08 62.0528 61 .4836 .93 25 896 1.000 377.594 10.032 583.13 583.39 -.05 62.0528 61 .7870 .43 25 897 1.000 410.928 9.656 561 .26 561.11 .03 62.0528 62.1925 -.22

25 898 1.000 444.261 9.288 539.89 539.34 .10 62.0528 62.4870 -.69

25 899 1.000 477.594 8.916 518.23 518.18 .01 62.0528 62.0842 -.05

25 900 1.000 510.928 8.553 497.16 497.76 -.12 62.0528 61.6728 .62 25 901 1.000 310.928 10.876 632.14 634.30 -.34 68.9476 65.9679 4.52

25 902 1.000 344.261 10.515 61 1.16 61 1.92 -.13 68.9476 68.0138 1.37

25 903 1.000 377.594 10.147 589.78 590.00 -.04 68.9476 68.7078 .35 25 904 1.000 410.928 9.790 569.04 568.58 .08 68.9476 69.3934 -.64

25 905 1.000 444.261 9.444 548.95 547.71 .23 68.9476 70.0280 -1.54

25 906 1.000 477.594 9.086 528. 14 527.48 .13 68.9476 69.4654 -.75

25 907 1.000 510.928 8.729 507.40 507.96 -.11 68.9476 68.5440 .59

81
Table 7. (Continued)

Data sources and ID numbers: (DVirial Equation, (3)Beattie, (19)Kay, (25)01ds, (29)Sage,

(XXXX)Haynes,

D Data We ight Temp, Dens i ty Dens i ty Dens ity ^©x pi" P C9 1 C Pressur

Poi nt expt ca 1 c Diff, Diff.

No, K moi/L kg/frP kg/m-^ % M.Pa MPa %

29 908 .000 294.261 .043 2.48 2.49 -,21 .1013 .101

1

.21 29 909 .000 294.261 .059 3.42 3.43 -,09 .1379 .1378 .09 29 910 .000 294.261 .091 5.26 5.26 ,09 .2068 ,2070 -.08

29 91 1 .000 294.261 10.062 584.83 579.62 ,89 1.7237 5,0879 -66. 12 29 912 .000 294.261 10.121 588.27 582.34 1,01 3.4474 7.4607 -53.79

29 913 .000 294.261 10, 173 591.31 584.95 1,07 5. 171

1

9.6655 -46.50

29 914 .000 294.261 10.218 593,94 587.46 1.09 6.8948 1 1.5557 -40.85

29 915 .000 294.261 10,256 596, 15 589.88 1.05 8,6184 13.3881 -35.63

29 916 .000 294.261 10.299 598,60 592.21 1.07 10,3421 15.3744 -32.73

29 917 .000 294.261 10.341 601 ,07 594.47 1.10 12,0658 17.4482 -30.85

29 918 .000 294.261 10,380 603,33 596.65 1,11 13,7895 19.4126 -28.97

29 919 .000 294.261 10.41

5

605.38 598.77 1,09 15,5132 21.2471 -26.99

29 920 .000 294.261 10.447 607.22 600.82 1,05 17,2369 22.9325 -24.84

29 921 .000 294.261 10.475 608.84 602.82 ,99 18,9606 24.4507 -22.45

29 922 .000 294.261 10.487 609.53 604.76 .78 20,6843 25.1 140 -17.64

29 923 .000 310.928 .040 2.34 2.34 -. 18 ,1013 .1012 .17 29 924 .000 310.928 .055 3.22 3.22 -.12 ,1379 .1377 .12

29 925 .000 310.928 .085 4.92 4.92 -,02 ,2068 ,2068 .02

29 926 .000 310.928 .115 6.70 6.69 ,13 ,2758 ,2761 -.12

29 927 .000 310.928 .148 8.58 8.55 ,33 ,3447 ,3458 -.30

29 928 .000 310.928 9.71

1

564,43 560.20 ,75 1.7237 3,9457 -55.31

29 929 .000 310.928 9,773 568,03 563,51 ,80 3.4474 5,9663 -42.22

29 930 .000 310.928 9,825 571.07 566,64 ,78 5.1711 7,7630 -33.39

29 931 .000 310.928 9.881 574.34 569,62 ,82 6.8948 9,7990 -29,64

29 932 .000 310.928 9.935 577.45 572.47 ,86 8.6184 1 1,8259 -27,12

29 933 .000 310.928 9.982 580. 17 575.19 .86 10.3421 13,6799 -24,40

29 934 .000 310.928 10.025 582.70 577.81 .84 12.0658 15,4753 -22,03

29 935 .000 310.928 10.073 585.47 580.33 .88 13.7895 17,5152 -21,27

29 935 .000 310.928 10.117 588.05 582.75 .90 15.5132 19,4898 -20,40

29 937 .000 310.928 10.166 590.87 585.10 .98 17.2369 21,7325 -20,69

29 938 .000 310.928 10.207 593.28 587.37 1.00 18.9606 23,7179 -20,06

29 939 .000 310.928 10.241 595.26 589.57 .96 20.6843 25,4044 -18,58

29 940 .000 327.594 .038 2.21 2.22 -.11 .1013 ,1012 ,11

29 941 .000 327.594 .052 3.04 3.04 -.06 .1379 .1378 ,06

29 942 .000 327.594 .080 4.63 4.63 ,04 .2068 .2069 -,04

29 943 .000 327.594 .108 6.28 6.27 ,16 .2758 .2762 -,15

29 944 .000 327.594 .138 8.00 7.98 ,22 .3447 .3454 -,21

29 945 .000 327.594 .168 9.79 9.75 ,40 .4137 .4152 -,36

29 946 .000 327.594 .201 11.66 11.61 ,48 .4826 .4847 -,42

29 947 .000 327.594 ,235 13.63 13.55 ,58 .5516 .5543 -,49

29 948 .000 327.594 9,355 543.74 539.31 ,81 1.7237 3.5829 -51,89

29 949 .000 327.594 9,432 548.20 543.43 ,87 3,4474 5,6109 -38,56

29 950 .000 327.594 9,500 552. 17 547.26 ,89 5.1711 7,5451 -31.46

29 951 .000 327.594 9,566 556.00 550,87 ,92 6.8948 9,5360 -27,70

29 952 .000 327.594 9,633 559.89 554,27 1,00 8.6184 1 1,6824 -26,23

29 953 .000 327.594 9,690 563.24 557,49 1,02 10.3421 13,6372 -24,16

29 954 .000 327.594 9,742 566.22 560, 56 1,00 12.0658 15,4674 -21,99

29 955 .000 327.594 9.790 569.04 563,49 ,98 13.7895 17,2595 -20,15

29 956 .000 327.594 9.846 572.29 566.30 1,05 15.5132 19,4459 -20,22

29 957 .000 327.594 9.896 575.17 568.99 1,07 17.2369 21,4577 -19,57

29 958 .000 327.594 9.94 5 578.08 571.58 1,12 18.9606 23,5748 -19,57

29 959 .000 327.594 9.985 580.38 574.08 1,09 20.6843 25.3154 -18,29

29 960 .000 344.261 .036 2. 10 2.10 -,09 .1013 .1012 ,09 29 961 .000 344.261 .050 2.88 2,88 -.05 .1379 .1378 ,04 29 962 .000 344.261 .075 4.38 4,38 .03 .2068 .2069 -,03

82
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (3)Beattle, {19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes,

ID Data Weight Temp, Dens 1 ty Dens i ty Dens i ty ^expt '^ca 1 c Pressure

Pol nt expt calc DIff, Diff.

No. K mol/L kg/m-' kg/rn^ % MPa MPa %

29 963 .000 344.261 .102 5,92 5,91 ,16 ,2758 ,2762 -.16

29 964 .000 344.261 .129 7,52 7.50 .26 ,3447 .3456 -.24

29 965 .000 344.261 .158 9,17 9.13 .38 ,4137 .4151 -.35

29 966 .000 344.261 ,187 10.87 10.82 .43 ,4826 .4845 -.38

29 967 .000 344.261 ,217 12.63 12.57 .49 ,5516 .5540 -,43

29 968 .000 344.261 ,249 14.47 14.39 .53 ,6205 .6234 -,45

29 969 .000 344.261 .282 16.37 16.29 .50 ,6895 .6924 -.42

29 970 .000 344.261 8.977 521.77 516.36 1.04 1,7237 3.4838 -50.52

29 971 .000 344.261 9.074 527.44 521.67 1.10 3,4474 5.5245 -37.60

29 972 .000 344.261 9. 159 532.35 526.50 1.10 5. 171

1

7.4631 -30,71

29 973 .000 344.261 9.236 536.81 530.96 1.09 6,8948 9.3704 -26,42

29 974 .000 344.251 9.314 541.35 535.09 1.16 8.6184 1 1.4587 -24,79

29 975 .000 344.261 9.380 545.22 538.96 1.15 10.3421 13.3641 -22,61

29 976 .000 344.261 9.448 549. 14 542.61 1.19 12.0658 15.4180 -21 ,74 29 977 .000 344.261 9.510 552.74 546.05 1.21 13.7895 17.4131 -20,81

29 978 .000 344.261 9.569 556.20 549.32 1.24 15.5132 19.431

1

-20. 16 29 979 .000 344.261 9.623 559.30 552.43 1.23 17.2369 21,3355 -19.21

29 980 .000 344.261 9.670 562.05 555.41 1. 18 18.9606 23,0919 -17.89

29 981 .000 344.261 9.707 564.23 558.26 1.06 20.6843 24,5336 -15.69

29 982 .000 360.928 .034 2,00 2.00 -.05 .1013 ,1013 ,04 29 983 .000 360.928 .047 2,74 2,74 -.00 ,1379 ,1379 ,00

29 984 .000 360.928 .071 4,16 4,15 .07 ,2068 ,2070 -,07

29 985 .000 360.928 .097 5,61 5.60 .21 ,2758 .2763 -,20

29 986 .000 360.928 ,122 7,10 7.08 .32 ,3447 .3458 -,30

29 987 .000 360.928 .149 8,64 8.60 .41 ,4137 .4153 -,38

29 988 .000 360.928 .176 10,21 10. 16 .47 ,4826 .4847 -,43

29 989 .000 360.928 .203 1 1,83 1 1.77 .48 ,5516 .5540 -,43

29 990 .000 360.928 .232 13.50 13.42 .55 ,6205 .6236 -,49

29 991 .000 360.928 .262 15.21 15.13 .53 ,6895 .6927 -,46

29 992 .000 360.928 .340 19.79 19.68 .57 ,8618 .8659 -,47

29 993 .000 360.928 .427 24.79 24.71 .33 1,0342 1.0369 -,26

29 994 .000 360.928 8.495 493.79 490.31 .70 1,7237 2.5204 -31,61

29 995 .000 360.928 8.620 501.05 497.55 .70 3,4474 4.3730 -21,17

29 996 .000 360.928 8.729 507.40 503.89 .69 5,1711 6.2172 -16,83

29 997 .000 360.928 8.830 513.25 509.55 .72 6,8948 8.1 161 -15,05

29 998 .000 360.928 8.925 518.73 514.70 ,78 8,6184 10.0799 -14.50

29 999 .000 360.928 9.015 523.99 519.43 .87 10,3421 12.1408 -14.82

29 1000 .000 360.928 9.095 528,66 523.81 .92 12,0658 14,1236 -14,57

29 1001 .000 360.928 9. 171 533,06 527.90 .97 13,7895 16, 1297 -14.51

29 1002 .000 360.928 9.242 537,17 531.74 1.01 15,5132 18,1320 -14.44

29 1003 .000 360.928 9.307 540,98 535.37 1.04 17,2369 20, 1012 -14.25

29 1004 .000 360.928 9.205 535,02 538.80 -.71 18.9606 17,0679 1 1.09

29 1005 .000 360.928 9.415 547.27 542.07 .95 20.6843 23,5998 -12.35

29 1006 .000 377.594 .033 1.91 1.91 -.01 .1013 ,1013 .01 29 1007 .000 377.594 .045 2.61 2.61 .04 .1379 ,1380 -.04

29 1008 .000 377.594 .068 3.96 3.95 .14 .2068 .2071 -.14

29 1009 .000 377.594 .092 5,33 5.32 .27 .2758 .2765 -.26

29 1010 .000 377.594 .1 16 6.74 6.72 .34 .3447 .3459 -.33

29 1011 .000 377.594 .141 8. 18 8, 14 .47 .4137 ,4155 -.44

29 1012 .000 377.594 ,166 9,65 9,60 .52 ,4826 ,4850 -.49

29 1013 .000 377.594 .192 11.15 1 1,09 ,55 ,5516 ,5544 -.51

29 1014 .000 377.594 .218 12.69 12,62 ,56 ,6205 ,6237 -.51

29 1015 .000 377.594 .245 14.26 14, 18 ,55 ,6895 ,6929 -.49

29 1016 .000 377.594 .316 18,38 18,29 ,51 ,8618 ,8656 -,44

29 1017 .000 377.594 .392 22,81 22,71 ,45 1,0342 1.0380 -,37

29 1018 .000 377.594 ,476 27,66 27,53 ,46 1,2066 1.2109 -,36

83
Table 7, (Continued)

Data sources and ID numbers: (l)Virlal Equation, (3)Beattie, (19)Kay, (25)0lds, (29)Sage,

(XXXX)Haynes.

D Data We i ght Temp. Dens ity Dens i ty Dens I ty expt P„^ '1 „ ca 1 c Pressure

Point expt ca 1 c Dlff. Di f f

.

No. K mol/L kg/m-^ kg/m-^ % MPa MPa

29 1019 .000 377.594 .569 33.07 32.88 .57 1 .3790 1 .3847 -.4 1 29 1020 .000 377.594 .675 39.24 38.96 .72 1 .5513 1 .5587 -.47

29 1021 .000 377.594 7.937 461 .36 458.95 .52 1 .7237 2.0697 -16.72

29 1022 .000 377. 594 8.113 471 .55 469.84 .36 3.4474 3.7570 -8. 24 29 1023 .000 377.594 8.254 479.74 478.67 .22 5.171

1

5.4023 -4.28

29 1024 .000 377. 594 8. 392 487. 77 486. 18 .33 6.8948 7. 2934 -5.47

29 1 025 .000 377.594 R S97 40S fi9 492.75 .58 8.6184 9.4314 -8.62

29 1026 .000 377. 594 o. u^u S01 '^fi 498.66 .54 10.3421 1 1 . 1923 -7.60

29 1 027 .000 377. 594 ft 79

1

SOfi 0 1 504.01 .57 1 7.0658 1 3.0660 -7.65

1 09R .000 377. 594 ft ftOft ill J \ \ • 047*T 508.93 .59 13.7895 14.9132 -7 5"^

1 090 oon 377. 504 ft ftft4 JR 1

\ fi\J% _?7 ^0 51 3.4R .56 . JU 1 5. 51 39 1 6.6R00 -7 no

?9 1 030 000 J3771 1 .m 504 J 7^ ft Qfi? S90 O'^ 51 7.73 .61 17,2369 1ft. 6074 -7 ^7

1 f)"^ 1 000 377 "504 0 09 1 i94 "^4 .50 1ft OfiOfi -5 ftQ 9Q 000 377. 504 07. 077 U / / K97 CO / . DZ .40 90.6R43 91 7n^*S -4 70

000 J^047*+ . 9fi1 ^(J I O'^ 1 1 R9 1 ft? 101 1 ni4

90 000 -J'104 7H . 9fi11 04 9 "lO Z. IjU 9^ • AQ 1 "^70 . 1 -J / 7 1 '^RC\ • 1 DO\J

9Q 1 (W^ 000 ^047H . 9fi1 Z.U I 7ft ^ 77 1Q • £.\J f £- - 1 ft

1 (T^fi 000 "^04 9fi1 ORft J.S 00U7 ^ 07 97 Sft • ^,1 JO m £. 1 \J 1 - "^9 90 1t \JJ 1 000 J^047*T . 9fi1 ^ U 1 I 10 fi 49 u • 44 "^447 ^4^9 • DZ, - 49

90 1 U JO 000 394 961 1 . 1 7 7ft 7/ • 74. / *T • -^u 4 1 ^^7 4 1 SQ - 54 90 1i O'^O U J7 000 394.261 1 Sft . 1 JO 07 Ifi . I U • \j \ 4ft 54 - 57 90 000 ^04 9fi1 1 fl9 1 0 R7 in sn • u ^ 90 lOil 1 000 ^04 9fil 907 191 Z. 01U 1 1 1 Q"^ 6905 - fi4 90 1 049 000 ^04 9fi1 1 47 1 J • DO .uo 7 J - 5Q

90 1 043 000 394.961 . 907 ^ 7 /

1 7 9'=; 1 7. 1 S D\j .R6 %0\J IR\\J _ R 1 90 1 044 000 "^04 9fi1 . JUQ 91 96 1 .0349 - 45

99 1 045 .000 394.261 440 25.41 -54 1 .2066 K? 1 ?n -.45

90 000 304 96

1

570 30 9

1

^7.77 90.00 .71 1 .3790 5fi 90^ 7 1 047 000 304.961 .60R 35. 36 ^4.97 1.10 11 .5513 m J J \ J 29 1 048 .000 394.261 .706 4 1 . 06 40.46 1 .47 1 .7237 1 .74 16 -1 .03 90 1 049 .000 394.261 810 47. 59 46.63 2.02 1 .8961 1 .9209 -1 .29

29 1050 .000 394. 261 .949 . 7t 7 55.16 53.79 2.49 2.0684 2.0982 -1 .42 29 1 051 .000 394.261 7.471 434.22 435.83 -.37 3.4474 3.2783 5. 16 29 1052 .000 394.261 7.709 448.07 449. 50 -.32 5. 17 1

1

4.9656 4. 14 29 1053 .000 394.261 7.897 458.98 460.08 -.24 6.8948 6.6991 2.92

29 1054 .000 394.261 8.049 467.83 468.83 -.21 8.6184 8.4059 2.53

29 1055 .000 394.261 8. 178 475.33 476.38 -.22 10.3421 10.0880 2.52

29 1056 .000 394.261 8.293 482.05 483.03 -.20 12.0658 1 1.7982 2.27

29 1057 .000 394.261 8.397 488.07 489.02 -. 19 13.7895 13.5049 2.1

1

29 1058 .000 394.261 8.488 493.33 494.47 -.23 15.5132 15.1406 2.46

29 1059 .000 394.261 8.569 498.09 499.49 -.28 17.2369 16.7421 2.96

29 1060 .000 394.261 8.647 502.62 504.14 -.30 18.9606 18.3830 3.14

29 1061 .000 394.261 8.718 506.75 508.49 -.34 20.6843 19.9820 3.51

84
Table 8. Comparisons of data for ideal gas functions with eq (7).

Normal butane ideal gas functions from Chen, et al. (12]

Temp. J/mo 1 Di tf

.

S*^, J/(mol K) Di f f

.

C°, J/(mo 1 K) Di f f

.

K expt. cal c. % expt. ca 1 c. % expt. cal c. d

50.00 1718.0 1750.3 -1.88 198.363 198.892 -.27 38.07 38.08 -.01

100.00 4048.9 4041.8 .17 229.994 229.925 .03 55.35 55.34 .03 150.00 7142.7 7143.6 -.01 254.889 254.915 -.01 67.32 67.37 -.07

200.00 10736.1 10733.0 .03 275.516 275.505 .00 76.44 76.33 .14 273.15 16883.5 16881 .3 .01 301 .583 301 .574 .00 92.30 92.40 -. 1

1

298.15 19267.0 19268.1 -.01 309.909 309.931 -.01 98.49 98.59 -.10

300.00 19450.6 19450.9 -.00 310.536 310.542 -.00 98.95 99.05 -. 10 400.00 30636.9 30632.2 .02 342.544 342.533 .00 124.77 124.54 . 18 500.00 44333.7 44299.9 .08 373.004 372.932 .02 148.66 148.37 . 19 600.00 60259.6 60207.1 .09 401.999 401.877 .03 169.28 169.26 .01 700.00 78096.5 78054.9 .05 429.446 429.354 .02 187.02 187.23 -. 1

1

800.00 97584.3 97567.5 .02 455.428 455.386 .01 202.38 202.63 -.12

900.00 1 18507.2 118509.3 -.00 480.072 480.037 .01 215.73 215.88 -.07

1000.00 140674.4 140684.2 -.01 503.419 503.390 .01 227.36 227.35 .00 1100.00 163928.3 163930.2 -.00 525.552 525.538 .00 237.48 237.35 .06 1200.00 188124.4 188113.2 .01 546.640 546.574 .01 246.27 246.13 .06

85
I aD 1 e y

•

1 n r er po i d i cu lUtJdl IUIH-.I lUHo ^ r* r\rf\ ( 1 \ II \J\\\ cii^ V ' / •

Tornp • H°-H° II 1 IQ V P K J/mo 1 J/mo 1 J/ Cmol »K) J/ (mo 1 •t\.) J / (mo 1

130.0 4753.0 5833.9 245.551 55. 17 63.48

140.0 5315.

1

6479.

1

250.331 57. 20 £ C CI 55.51

150.0 5896.4 7143.6 254.915 59.05 "7 "7 "7 67.37

160.0 6495.8 7826.

1

259.3 1

9

60.82 69. 1

3

170.0 71 12.7 8526.2 263.563 62. 56 70.88

180.0 7747.

1

9243.7 267.663 64.32 72.54

190.0 8399.4 9979.

1

271.639 66. 14 1 A A C 74.45

200.0 9070.

1

10733.0 275. 505 68. 02 76.33

210.0 9760.0 1 1506.0 279.276 69.98 78.29

220.0 10469.9 12299.

1

282.965 72.02 80.33

230.0 1 1200.6 131 12.9 286.583 74. 14 82.45

240.0 1 1952.9 13948.4 290. 138 76. 34 84 .65

250.0 12727.6 14806.2 293.639 78.61 86.92

260.0 13525.2 15687.0 297.094 80.94 89. z5 270.0 14346.5 16591 .4 300.507 83.32 9 1 .54 280.0 15191 .9 17519.9 303.883 85.76 94.07

290.0 16061.8 18473.0 307.227 88.23 96.55

300.0 16956.6 19450.9 310.542 90.74 99.05

310.0 17876.6 20454.

1

313.831 93.27 10 1 .58 320.0 18822.0 21482.6 31 7.097 95.82 104. 13 330.0 19792.9 22536.7 320.340 98.38 106.69

340.0 20789.5 2361 6.4 323.563 1 00.94 1 U9. z6

350.0 2181 1 .8 24721 .8 326.767 103.51 1 1 1 .82 360.0 22859.7 25852.9 329.953 106.07 1 14.39

370.0 23933.2 27009.6 333. 122 108.63 1 16.95

380.0 25032.3 28 1 9 1 .

8

336.275 111.18 1 19.49

390.0 26156.7 29399.4 339.4 12 113.71 1 22.02

400.0 27306.4 30632.2 342. 533 1 16.22 1 O /I C^/l

1 Z4 . 1)4 410.0 28481 .

1

31890.

1

34 5.639 1 1 8.72 1 O ~7 CtA

1 z / . U4 420.0 29680.7 331 72.8 348.730 1 O 1 O ^ 1 Izl .ZU 430.0 30905.0 34480.2 35 1 .806 1 J 1 . yo 440.0 321 53.6 3581 2.0 354.867 1 0£ A~7

1 Z6. U / 1 j4. jy

450.0 33426.4 37167.9 357.9 14 1 28.48 1 JO. /y

460.0 34723.0 38547.7 360.947 1 30.85 139. Id 470.0 36043.3 39951 .

1

363.965 133. 19 141.51

480.0 37386.8 41377.8 366.969 135.51 1 j1 "7 O "Z

1 43.83

490.0 38753.4 42827.5 369.958 1 37.80 1 yl 11 146. 1 1 500.0 40142.7 44299.9 372.932 140.06 1 yi o x~i 510.0 41554.4 45794.8 375.893 142.28 1 C A C A

1 50.50

520.0 42988.2 4731 1 .8 378.838 144.48 1 52.79

530.0 44443.9 48850.6 381.769 146.64 1 54.96

540.0 45921.0 50410.9 384.686 148.78 1 57.09

550.0 47419.4 51992.4 387. 588 1 50.88 159.20

560.0 48938.6 53594.7 390.475 1 52.96 161 .27 570.0 50478.4 55217.7 393.347 1 55.00 163.32

580.0 52038.5 56861 .0 396.205 1 57.01 165.33

590.0 53618.6 58524.2 399.048 1 59.00 167.31 600.0 55218.4 60207.

1

401 .877 160.95 169.26

610.0 56837.5 61909.4 404.690 162.87 171.19

620.0 58475.8 63630.8 407.489 164.77 173.08

630.0 60132.8 65371 .0 410.274 166.63 174.95

640.0 61808.4 67129.6 413.043 168.47 1 76.78

650.0 63502.

1

68906.6 415.798 170.28 178. 59 660.0 65213.9 70701.4 , 418.539 1 72.06 180.37

670.0 66943.3 72514.0 421.264 173.81 182.13

680.0 68690.0 74343.9 423.975 175.54 183.86

690.0 70454.0 76191 .0 426.672 177.24 185.56

700.0 72234.8 78054.9 429.354 178.91 187.23

85
Table 10. Comparisons of heat of vaporization data with eq (9). Data sources and ID numbers: (lO)Dana, (ll)Das (1967), (29)Sage,

(35)Das ( 1973) , (40) 1 nerma

1

Loops, (4 1) C 1 apeyron

.

ID Weight Temp. Heat of Vaporization Diff,

K kj/mo

1

% expt. ca 1 c

.

40 1 .000 A OCA 28.746 28.789

40 .998 1 40.000 28.499 28.521 -•03

40 .995 1 C A AAA 150.000 28.022 28.016 AO .02 40 .992 1 /I A AAA 1 60.000 27.553 27.533 A~7 .0 / 40 A O O

• 988 170.000 27.090 27.067 AO .08 40 .984 1 O A AAA 1 80.000 26.635 26.615 A "7 .07 40 A~7 A 1 AA AAA 26. 186 26. 174 A C .05 40 AT>I .y /4 OAA AAA 25.742 25.739 A 1 .U 1 A A 40 .yoy O 1 A AAA 25.301 25.307 -. AOUz

A A40 .yoj OOA AAA 24.861 24.875 AC^ -.UP

A A OR"? .yp / 24.417 24.438 AQUo

A A •ysu Z4U»UUU 23.965 23.992 —— 11 • 1 1 Ar\ 4U »y4j Z.^\J • UUU 23.503 23.535 — 1 A

A A .yj4 23.024 23.061 .10 4U . yzz> z / U ©UUU 22.524 22.567 _ 1 A

A 1 .yyo 28.521 28.521 .UUnn

A 1 . yy3 23.032 28.016 . UP

j1 1 •yy 1 1 DU •UUU 27.551 27.533 .un7/

yi 1 •yoD nn1 nnn /U aUUU 27.082 27.067 .uoAA

/ 1 4 1 •yoz ion nnn 1 oU«UUU 26.624 26.615 A"^ .UP

A 1 4 1 .y / /„ 1 on nnn 1 yu .UUU 26.176 26.174 A 1 .U 1 A 1 4 1 ATI .971 OAA AAA 25.735 25.739 A 1 -.U 1

>i 1 4 1 •yoD O 1 A AAA Z 1 U.UUU 25.299 25.307 A'^ -.Up

4

1

.ypy OOA AAA ZZU.UUU 24.865 24.875 - .U4

4 1 •yDii OXA AAA Z^U.UUU 24.429 24.438 -. A/t U4

A 1 4 1 .945 O ^ A AAA Z4 U.UUU 23.987 23.992 -.02AO

A 1 .yjo OCA AAA zdU .UUU 23.536 23.535 AA .UU

4 1 AOT .92/ OjCA AAA zoU.UUU 23.070 23.061 r\A .U4

yi 1 4 1 AIT .y 1 / 0~lf\ AAA Z/U .UUU 22.586 22.567 AA .uy

4 1 AAC OOA AAA ZoUpUUU 22.077 22.048 . I 5

A 1 4 1 QQO .cjy^ OOA Ann zVU • UUU 21 .535 21 .500 . 1 / A 1 4 1 .875 "ZAA AAA 500.000 20.955 20.917 . 18 4

1

D KA •859 "Z 1 A AAA 510.000 20.328 20 . 294 . 1

7

it 1 4 1 • 859 T O A AAA 520.000 19.650 19.626 . 12

4 \ O 1 c •815 T "2 A AAA 530.000 18.915 18.906 A C .05

41 • 786 340.000 18.118 18.125 -.04

41 • 751 350.000 17.253 17.274 -.12

yi 1 41 • 708 1 £r A AAA 350.000 16.312 16.340 -. 1 7

A 1 4 1 • o53 ZTA AAA 37U .UQU 15.282 15.306 -.15

A 1 41 • 581 T O A AAA 580.000 14.139 14.147 -.06

4 1 •484 7AA AAA 590.000 12.841 12.824 1 "Z . 15 4

1

0.000 >I A A AAA 400.000 1 1.306 1 1.262 .39

A 1 4

1

0.000 ^ 1 A AAA 4 1 0 .000 9.344 9.292 .56

A 1 4 1 A AAA 0.000 y» O A AAA 420.000 6.264 6.273 1 c -.15

1 1 A AAA 0.000 2/2.550 22.389 22.431 1 A -. 19

1 A A AAA 0~7 >1 ATA 22.252 22.312 O "7

1 A1 u A AAA OIC. COA /LIO» PZU 22.162 22.284 -.40A

1 A1 uA AAA U.UUU QTQ T^A z /y . /5U 22.009 22.062 O A

1 1

1 1 A AAA U.UUU OQA AAA ZBU .UUU 22.016 22.048 -. 1 A14 J J A AAA U.UUU OQA AAA ZO U.UUU 22.037 22.048 -.up

1 A1 uA AAA U.UUU Zo4 .y4U 21.768 21 .781 A^^ -.U5

1 A1 uA AAA U.UUU OQC; TOA zop. /yu 21.749 21 .734 A*7 .U /

1 1

1 1 A AAA U.UUU OAA AAA zyu • UUU 21 .481 21.500 AQ -.uy

A AAA U.UUU OAA AAA zyu.uuu 21.548 21 .500 OZ .ZP

1 A1 (J A AAA U.UUU OAA >10A zyu.4oU 21.515 21.472 OA .ZU

10 0.000 295.310 21.240 21.195 .21

10 0.000 297.480 21.092 21.067 .12

1

1

0.000 300.000 20.887 20.917 -.14

35 0.000 300.000 21 .037 20.917 .57

11 0.000 310.000 20.251 20.294 -.21

35 0.000 310.000 20.510 20.294 1.06

1

1

0.000 320.000 19.581 19.626 -.23

35 0.000 320.000 19.933 19.626 1 .56

87
Table 10. (Continued).

^ T 3 CT/^ 1 1 r~ £i C ^ I'l

1 u 1 1 uiiiUo r b , (lOOana, ( 1 1 )Das ( 1967), (29)Sage,

IJ)-) ; UaS i \ y / j) , K 4u J 1 nerrna i Loops, (41 )Clapeyron.

ID Weight Temp. Heat of Vaporization Diff,

K K J/ mo 1 % ex pt. ca 1 c

,

-1 1 1 1 r\ Ann u.uuu

z"ZA Ann 18.903 18.906 A 1 -.01 DO A AAA U.UUU 19.255 18.906 1 O C

1 .OD

II U.UUU J^U •UUu 18. 184 18.125 . JJ jD A AHA U.UUU z / n nnn 18.477 18.125

1 1 u. uuu xc^n nnn 17.405 17.274

Jp A AAA U.UUU XRn nnn 17.569 17.274 1 ~l 1

1 1 u. uuu 'z.f.r) nnn _30U • uuu 16.552 16.340 1 7n JJ u.uuu Tcn nnn J>OU« UUU 16.564 16.340 1I.J/^7

1 1

1 1 nU. nno ^J\JU J / u • uuu 15.573 15.306 1 JJ

n nnn D 1 \J • nnn UUU 15.443 15.306 •yonu

It1 1 n nnn JO"^^^nw • nnn uuu 14.447 14.147 9 1

9

JJ- nU.UUU nnn J>OU ^on eUUU nnn 14.209 14.147

1 1

1 I nU.UUU nnn ->yu "^on .uuu nnn 13.138 12.824 Z. Hj JJ

nU.UUU nnn j^yj "^on ©uuu nnn 12.837 12.824 .1

1 nu

1 1

1 1 nu. nnn uuu Ann '+UU • nnn uuu 1 1.506 1 1.262 9 1

7

tR nU.UUU nnn Ann 'lUU.UUU nnn 1 1.209 1 1.262 -47

jO n nnn U.UUU Ar\^ nnn 4Uy • uuu 10.251 10.347 _ Q9

1

1

1 1 n nnn U.UUU 4

y! 1 n nnn 1 U« UUU 9.263 9.292 —.J 1 XR nU.UUU nnn A4

1

I nu .uuu nnn 9. 184 9.292 — I . I o jO A AAA U.UUU ^ 1 c nnn 4 I !3«UUU 7.895 8.012 — 1 Afi

1 .40

1

1

r 1 A AAA U. UUU yi'7n nnn 4ZU« UUU 6.138 6.273 9 1 *^ -Z . 10 XKj5 A AAA U.UUU ^ on nnn 4zU«UUU 5.916 6.273 -5.oy

n nnn U.UUU lri"t • ZDU 21.479 21.256 1

1 nR . uu 29 0.000 310.930 20.382 20.234 .73 29 0.000 327.590 19.120 19.085 .19 29 0.000 344.260 17.712 17.771 -.33

29 0.000 360.930 16.094 16.248 -.95

29 0.000 377,590 14.096 14.440 -2.38

29 0.000 394.260 11.622 12.194 -4.69

Number of data points used in fit = 41; rms deviation = 0.095|.

88
Table 11, Enthalpies of saturated liquid normal butane frorn eq (10).

Tsnp

.

M"a Mq I eq \ \ ) n i f f J/ mO 1 J/mO 1 h

1 j4 .OO • U

A AAA U. UUU

1 41). UU ou^«y AOT

1 3U.UU 1 ~7 7 1 C1 / / 1 .0 1 T7 1 a A A 1 .UU1 loU.UU OQ X 7 O AA R

1 /U.UU >1 1 AO /I 4 IU^«4 AAO loU.UU COT A C AA 1 -.UUl

1 on HA (LA /I A C 0444

•

D d444 •

/

- AAT .UUj OAA AA /D^ / • y -. AAT UU3

o 1 A AA ^ lU.UU OOZ J«4 Q QO X c; AAA -.UUU

OO A AA 1 UUj4. o 1 UUj4« 4 AAO

O"^ A AA /jU. uu I 1 ^d4 I 1 O^L"^ "7

I I Add m I AA'^ .UU3

O/l A AA Z4U.UU 1^:5 1 4,/ 1 O c; 1 /I A \^z> \ 4.U AA1 • UUl OCA AA ZDU.UU 1 "70 "7 O 1 "70 ~7 A

1 3 /o / .y AAA .UUU

A AA ^ou • UU 1 C^nO "7

1 -)Uo / • J

1 c; AO "7 c AA 1 -. UU 1 OTA AA Z /U.UU 1 gLA \ A Q

1 d4 1

4

.o 1 04 1 AAO

OQ A AA zyu . UU 1 ~t~I~JO X \ 1 1 1 1 / / /Z .D AAO

OQA AA 1 Q 1 1 A

1 y 1 D 1 .4 1 y 1 o 1 ©o AA -.UU

TAA AA JUU. UU ZUD04 • 1 iU-)04 • U .UU 1

•Z 1 A AA J 1 U.UU 9904 1 Q 9904 1 R nn 1 • UU 1 •ZO A AA JZU.UU OX^Xf. x. nn9

9sn7n ^ / u» Ro 9sn7n £.J\J 1 \) %\J • nmuu 1 X/IA AA -JHU . UU ^uut / • 1 _ AA1 • UU 1 j-^u . uu 9R9fift ft - .UUl nm

360.00 29940.6 29941.2 -.002

370.00 31668.3 31668.7 -.001

380.00 33460.0 33459.6 .001 390.00 35327.5 35326.6 .003

400.00 37293.8 37293.1 .002

410.00 39414.3 39416.2 -.005

420.00 41932.5 41931.6 .002

425.16 45399.8 45399.8 0.000

Number of points = 29; rms deviation = 0.005^.

1 Derived from ideal gas functions, the equation of state, and the formulated

heats of vaporization.

89
Table 12. Entropies and specific heats of saturated liquid norma! butane from eq (11).

1 emp.

1 So S o

( eq (11)) D 1 f f

.

Ca

K J/(mol 'K; J/(moi 'K) % J/(mol 'K)

134.86 1 33.544 1 33.544 0.000 1 1 7.39

140.00 137.932 137.929 .002 1 17.07

1 50.00 145.992 145.989 .002 1 16.61

1 60 . 00 153.507 153.507 .000 1 16.42

170.00 160.565 160.567 -.001 1 16.54

180.00 167.237 167.239 -.001 1 16.99

190.00 173.582 173.584 -.001 1 17.77

200.00 179.652 179.651 .000 1 18.88

21 0.00 185.486 185.484 .001 120.29

220.00 191 . 120 191.118 .001 121 .98 230.00 196.584 196.582 .001 123.92

240,00 201 .902 201 .901 .000 126, 10 250.00 207.096 207,097 -.000 128.48

260.00 212. 183 212. 185 -.001 131 .05 270.00 21 7. 180 21 7. 182 -.001 133.79

280.00 222.098 222. 100 -.001 136.70

290.00 226.950 226.950 -.000 139.78

300.00 231 .744 231 .743 .000 143.02

310.00 236.490 236.488 .001 146.44

320.00 241 .196 24 1 . 1 94 .001 150.05

330.00 245.870 245.869 .000 153.88

340.00 250.521 250.522 -.000 157.94

350.00 255. 160 255. 163 -.001 162.29

360.00 259.797 259.800 - . 00

1

167.03

370.00 264.446 264.447 -.000 172,29

380.00 269. 122 269. 120 .001 178.40

390.00 273.354 273.848 .002 186.05

400.00 278.689 278.686 .001 196.99

410.00 283.753 283.765 -.004 217.06

420.00 289.605 289.598 .002 287.81

425.16 297.647 297.647 0.000

Number of points = 29; rms deviation = 0.001$.

Derived from ideal gas functions, equation of state, and formulated heats of vaporization.

90
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Table 14. Comparisons with saturated liquid specific heats.

Data sources and ID numbers: (l)Aston, (2)Huffman, (3)Dana.

ID Temp. ^0' J/(mol ^K) Di f f

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K expt ca 1 c %

1 139.880 1 13.24 1 17.08 -3.28

1 142.220 1 13.45 1 16.95 -2.99

149.500 1 14.71 1 16.53 -1 .55

1 56.030 1 1 6.00 1 16.46 -.39

162.290 1 15.92 1 16.42 -.43

168.490 1 16.84 1 16.50 .29

174 .590 1 16.80 1 15.70 .08 180.830 1 17.09 1 1 7.04 .05 186.630 1 18.05 1 17.47 .50

191 .760 1 1 8.47 1 1 T A >1 1 1 7.94 • 45

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247.010 127.00 127.75 -.58

251 .430 129.22 128.84 .30 262.040 130.94 131 .59 -.50

268. 140 131.61 133.27 -1 .25

2 139.700 1 13.55 1 1 7 . 09 -3.02

2 150.200 1 14.04 1 16.61 -2.20

2 1 52.500 1 14.77 1 1 6.54 -1 .52

2 170.200 1 15.25 1 16.54 -1.11

2 187.000 1 17.69 1 17.50 .16 2 190. 1 00 1 17.44 1 17.78 -.29

2 230.000 123.03 123.92 -.72

2* 261 .800 129.60 131 .53 -1 .47 3 256.950 125.973 130.246 -3.39

3 270.550 131.324 133.948 -2.00

3 277.280 135.458 135.895 -.32

3 285.020 137.647 138.227 -.42

3 289.930 139. 106 139.757 -.47

3 267.020 130.594 132.957 -1.81

3 276.380 141.295 135.631 4.01

3 284.770 139.106 138.150 .69 3 289.760 140.808 139.704 .78 3 294.380 143.727 141 .179 1.77

Number of data points = 39; rms deviation = 1.49|.

95
Table 15. Comparisons with Cv and Cp data,

Cp data of Sage [551

P = 0. 101325 MPa ( 1 atm)

Temp. Cp, J/(nnol»K) Diff.

K expt calc %

294.261 95.964 99.246 -3.42

310.928 98.541 103.081 -4.61

327.594 101.314 107.088 -5.70

344.261 104.208 111.189 -6.70

360.928 107.223 115.333 -7.56

377.594 110.312 119.487 -8.32

394.261 113.400 123.625 -9.02

410.928 116.416 127.730 -9.72

Number of data points of Sage [651 = 8; rms deviation = 7.18^.

Cp data of Dai ley [ 18]

Temp. Cp, J/(mol»K) Diff.

K expt calc % 344.900 110.583 110.514 .06

359.600 114.934 114.285 .56 387.500 121.754 121.392 .30

451.600 137.988 137.171 .59 521.000 154.013 153.011 .65 561.300 162.256 161.540 .44 600.800 170.331 169.420 .53 692.600 185.853 185.9^3 -.08

Number of data points of Dai ley [181 = 8; rms deviation = 0.46^.

96
Table 16. Comparisons with velocity of sound data.

Saturated liquid velocities of sound from Rao (581

Temp. Dens i ty Vel . of Sound, m/s Dif f. K kg/m3 expt ca 1 c %

268. 150 605.89 1085 1049 3.31

263. 150 61 1.16 1 115 1074 3.62

253. 150 621.54 1173 1125 4.03

243.150 631.71 1230 1176 4.33

233. 150 641 .69 1286 1227 4.54

223. 150 651.53 1343 1278 4.81

213.150 661 .24 1400 1328 5.08

203. 150 670.84 1459 1379 5.46

193.150 680.37 1515 1429 5.65

183. 150 689.83 1573 1479 5.95

173.150 699.26 1630 1529 6. 18 158.150 713.36 1715 1603 6.48

153. 150 718.05 1743 1628 6.55

148. 150 722.75 1772 1653 6.66

143. 150 727.46 1800 1679 6.71

of data points of Rao (581 =: 15; mean deviation = 5.29^.

97
Table 17. Calculated P{T) isochores of normal butane.

Normal Butane 1 sochore at 25 kg/m"^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Der i vat i ve Der i vat i ve Curvature

K MPa MPaMn3/kg MPa/K

352.827 1.0063 .79753 .03014 .00465 -,0000149

360.000 1.0393 .80729 .03187 .00456 -.00001 15 368.000 1.0755 .81721 .03371 .00448 -.0000091

376.000 1.1110 .82627 .03547 .00441 -.0000074

384.000 1 .1461 .83461 .03719 .00436 -.0000062

392.000 1.1808 .84232 .03886 ,00431 -.0000053

400.000 1 .2152 .84948 .04050 ,00427 -.0000046

408.000 1.2492 .85616 .04211 .00424 -.0000040

416.000 1 .2830 .86241 .04370 .00421 -.0000036

424.000 1.3166 .86827 .04526 ,00418 -.0000032

432.000 1 .3499 .87379 .04680 .00416 -.0000028

440.000 1.3831 .87899 .04833 .00414 -.0000025

448.000 1.4161 .88390 .04984 .00412 -.0000023

456.000 1.4490 .88855 .05134 ,00410 -,0000021

464.000 1 .4817 .89296 .05282 ,00408 -,0000019

472.000 1.5143 .89715 .05430 ,00407 -.0000018

480.000 1 .5468 .901 13 .05576 ,00406 -.0000016

488.000 1.5792 .90492 .05722 .00404 -.0000015

496.000 1.6115 .90853 .05867 .00403 -.0000014

504.000 1.6438 .91 199 .0601

1

.00402 -.0000013

512.000 1 .6759 .91529 .06154 ,00401 -.0000012

520.000 1.7079 .91844 .06297 ,00400 -.000001

1

528.000 1 .7399 .92147 .06439 ,00399 -.0000010

536.000 1.7719 .92437 .06580 .00399 -.0000010

544.000 1 .8037 .92715 .06721 .00398 -.0000009

552.000 1.8355 .92983 .06861 .00397 -.0000008

560.000 1.8673 .93240 .07001 .00397 -,0000008

568.000 1.8990 .93487 .07141 .00396 -,0000007

576.000 1.9306 .93725 .07280 .00395 -,0000007

584.000 1.9622 .93955 .07419 ,00395 -,0000007

592.000 1 ,9938 .94176 .07557 .00394 -.0000006

600.000 2.0253 .94389 .07695 .00394 -.0000006

608.000 2.0568 .94596 .07833 ,00393 -.0000006

616.000 2.0883 .94795 .07970 ,00393 -.0000005

624.000 2.1197 .94987 .08108 ,00392 -.0000005

632.000 2.1510 .95173 .08244 .00392 -.0000005

640.000 2. 1824 .95353 .08381 .00392 -.0000005

648.000 2.2137 .95528 .08517 .00391 -.0000004

656.000 2.2450 95696 .08654 .0039

1

-.0000004

664.000 2.2763 .95860 .08789 .00391 -.0000004

672.000 2.3075 .96019 .08925 ,00390 -.0000004

680.000 2.3387 .96173 .09061 ,00390 -.0000004

688.000 2.3699 .96322 .09196 ,00390 -.0000004

696.000 2.401

1

.96467 .09331 .0 0 389 -.0000003

98
Table 17. (Continued),

Normal Butane I sochore at 50 kg/m1 sotherm 1 sochore 1 sochore

Temp, Pressure Z Der i vat ive Der i vat 1 ve Curvature

K MPa MPa.m3/kg MPa/K MPa/K^

383.962 1.8715 .68148 .02109 .01085 -.0000535

384.000 1.8719 .68156 .02111 .01085 -.0000534

392.000 1 .9572 .69808 .02354 .01050 -.0000375

400.000 2.0401 .71308 .02580 .01023 -.0000288

408.000 2.1211 .72686 .02796 .01003 -.0000232

416.000 2.2006 .73961 .03003 .00986 -.0000193

424.000 2.2789 ,75147 .03204 .00972 -.0000164

432.000 2.3561 .76254 .03400 .00959 -.0000142

440.000 2.4324 ,77293 .03591 .00949 -.0000124

448.000 2.5079 .78269 .03779 .00939 -.00001 10 456.000 2.5828 .79190 .03964 .00931 -.0000098

464.000 2.6569 .80060 .04146 .00924 -.0000088

472.000 2.7306 .80884 .04326 .00917 -.0000079

480.000 2.8037 .81666 .04503 .0091

1

-.0000072

488.000 2.8763 .82409 .04679 .00906 -.0000065

496.000 2.9486 .831 16 .04853 .00901 -.0000060

504.000 3.0204 ,83790 .05026 .00896 -.0000055

512.000 3.0919 .84433 .05197 .00892 -.0000051

520.000 3.1631 .85048 .05366 .00888 -.0000047

528.000 3.2340 .85636 .05535 .00884 -.0000043

536.000 3.3046 .86200 .05702 .00881 -.0000040

544.000 3.3749 .86740 .05869 .00878 -.0000038

552.000 3.4450 ,87258 .06034 .00875 -.0000035

560.000 3.5149 .87757 .06199 .00872 -.0000033

568.000 3.5846 .88235 .06363 .00870 -.0000031

576.000 3.6541 .88696 .06526 .00867 -.0000029

584.000 3.7233 .89140 .06688 .00865 -.0000027

592.000 3.7925 ,89567 .06850 .00863 -.0000026

600.000 3.8614 .89980 .07011 .00861 -.0000024

608.000 3.9302 .90378 .07171 .00859 -.0000023

616.000 3.9988 .90762 .07331 .00857 -.0000022

624.000 4.0673 .91 133 .07490 .00855 -.0000021

632.000 4.1357 .91492 .07649 .00854 -.0000020

640.000 4.2039 .91839 .07807 .00852 -.0000019

648.000 4.2721 ,92175 .07965 .00851 -.0000018

656.000 4.3401 ,92501 .08123 .00849 -.0000017

664.000 4.4080 .92816 .08280 .00848 -.0000016

672.000 4.4758 .93122 .08436 .00847 -.0000016

680.000 4.5435 .93418 .08592 .00846 -.0000015

688.000 4.6111 .93705 .08748 .00844 -.0000014

696.000 4.6786 .93984 .08904 .00843 -.0000014

99
Table 17.

Normal Butane I

Temp • Pressure Z

K MPa

411 .953 3.0475 .51715

416 .000 3. 151

1

,52952

424.000 3.3487 .55212

432.000 3.5400 .57286

440.000 3.7268 .59211 448.000 3.9100 .61012

456.000 4.0902 .62705

464.000 4.2680 .64302

472.000 4.4437 .65814

480.000 4.6175 .67249

488.000 4.7896 .68613

496.000 4.9604 .69912

504.000 5.1298 .71 152 512.000 5.2980 .72337

520.000 5.4651 .73472

528.000 5.6313 .74558

536.000 5.7965 .75601

544.000 5.9609 .76601 552.000 6.1246 .77564

560.000 6.2875 .78489

568.000 6.4497 .79380

576.000 6.61 13 .80239

584.000 6.7723 .81067

592 .000 6.9328 .81867

600.000 7.0927 .82639

608 .000 7.2522 .83385

616.000 7.41 1

1

.84106

624.000 7.5697 .84804

632.000 7.7278 .85479

640.000 7.8855 .86133

648.000 8.0428 .86767

656.000 8.1998 .87382

664.000 8.3564 .87978

672.000 8.5127 .88556

680.000 8.6687 .891 18 688.000 8.8244 .89664

696.000 8.9797 .90194

( Cont i nued )

.

sochore at 100 kg/m1 sotherm 1 sochore 1 sochore

Der i vat i ve Der ivat i ve Curvature

MPa.m3/kg MPa/K MPa/K^

.00819 .02600 -.0002358

.00973 .02523 -.0001567

.01245 .02426 -.0000967

.01499 .02360 -.0000705

.01742 .02310 -.0000554

.01978 .02270 -.0000455

.02209 .02237 -.0000384

.02435 .02208 -.0000330

.02659 .02184 -.0000288

.02880 .02162 -.0000255

.03098 .02143 -.0000227

.03315 .02126 -.0000205

.03530 .02110 -.0000185

.03743 .02096 -.0000169

.03954 .02083 -.0000154

.04165 .02071 -.0000142

.04374 .02060 -.0000131

.04582 .02050 -.0000121

.04789 .02041 -.00001 13 .04996 .02032 -.0000105

.05201 .02024 -.0000098

.05406 .02016 -.0000092

.05609 .02009 -.0000087

.05813 .02002 -.0000082

.06015 .01996 -.0000077

.06217 .01990 -.0000073

.06418 .01984 -.0000069

.06619 .01979 -.0000066

.06819 .01974 -.0000062

.07018 .01969 -.0000059

.07217 .01964 -.0000057

.07416 .01960 -.0000054

.07614 .01956 -.0000052

.07812 .01952 -.0000050

.08009 .01948 -.0000048

.08206 .01944 -.0000046

.08402 .01940 -.0000044

100
Table 17. (Continued).

Normal Butane I sochore at 150 kg/ttr

1 1 t III

1

1 Q(^r^hAf~f^ ^\J\^ WKJi "3 Tsmp • r 1 o Ul t; 7 \jss\ 1 V a 1 1 V c Hpr L/d i

1 Wrii" V CJ 1 i1 VPVU P iir\/;^ i" iirp

IS MP3 MPp^o • m3Ml—'// knr\y I t a / IN

^ZZ» Z /o T A 1 "7 1 AA 1 Q*^

• uu 1 yo .U4Z3y •UUUODoO

A A AAA /I r\^^A • UUZOJ) .U4 1 34 ~ • UUUh D I J) A "^O AAA A A 1 OR 4 •U I ZD •4 jZO

/

•UUPZO AZQCA • UJjy J4 ~ •UUU IP/!

vl y! A AAA 4 • j>Z4!? y1 CO A c •UU / OU .U JO 00 _~ •uuuuy nnnnQQ/iy4

>l >I O AAA 44o«UUU y1 TAA 4

•

DjUU .40 103 A 1 A"^A •U

1

UjU • U_) /o / — •UUUU /J)4 ytcc AAA yl AQ 4 •yj>Uo .!3Ujy4 A 1 01 Q •u 1 z / y nz7z CI - nnnn rq"^ • UUUUPoJ)

>1 £ y1 AAA 4o4 •UUU A 1 c:OP •U 1 PZO •u joyz _~ •UUUU40Z nnnn/iQO

A "70 AAA 4 /z •UUU C CO 1 -J C/1 CO 1 •U 1 / / D •Ujop / — • UUUU4 1

1

/I O A AAA C O 1 "ZA AOAOt^ •UzUzP .UjD2tD - AAAA "Z ^1 •UUUUpP /

>1 O O AAA 488.000 C 1 AO A

D. 1 OzO C OO T C .582 /5 AO 0"7 A A "2 CA A .u35yy A AA A "Z 1 A -•UUUU3 1

4

A f\£ AAA 495.000 C 1 O AA AA "Z 1 .50031 A O COT •Oz5z3 .Oji> /5 - AA A A OO A •UUUUzoU

Cir\ A AA A 504.000 D^D /4

1

1 "7 1 C .51 /Id AO"7"7

• Uz / Id A Z C C^ AAAAO CI'Z -• UUUUzPP

CIO AAA 512.000 •yp / / •Oj3j2 A "Z AOO •U3UzZ AT CTC .Uj535 - A A A AO OA •uuuuzzy

COA AAA 5zO. 000 ~7 TZ AO / •z3yo /Tyl Q Q C .54ooD A "Z 0"7 1 AT C 1 7 .0351 / AAAAO 1 A - • UUUUz 1

u

coo AAA .5ojol A"Z C^O 1 •U3Pz 1 AT CA 1 .0350

1

- A AAA ^ dT. .UUUU 1 y3 CZX AAA "7 Q A AA / •oUUU •D /o2 1 A'Z"7 "7 A • \}D I f\J AT /I D .U340D A AAA 1 ~I O -•UUUU 1 /y

C A A AAA 544.000 8 .0784 .69208 •040 19 .03473 A A A \ C £1 - .0000 156 ceo AAA 552.000 8^3557 .70545 •04268 .03460 A AA A 1 C C -.00001 55

CrCA AAA 5dU«UUU O •DJZU A >1 C 1 O

• U4 Plo AT ^ ^ Q .03448 - AA A A 1 A C .0000145

C£iQ AAA POO .UUU Q A A"7 T y .yu 1

J

"7Z AQ C •U4 10

1

A T /I T7 .0343/ A AAA 1 T 7 -.UUUU 1 3 / C^"7£ AAA /D.UUU A 1 Q 1 O y • ] o lo

"7/1 OA 1 A CA 1 • UpU id AT ^ OiC .03425 AAAA 1 OA -.UUUUl 29

CO /I AAA !>o4 .UUU A ^ p R y • 4DDD "7 C/1 C"7

. / 34D

/

•UPZD4 A T/1 1 .U34 15 AAAA 1 OO -.UUUU 1 22

CAO AAA -)yz. UUU A 70Q>1 y • /zo4 . /DDot) A K c; 1 "z •UPP 1

3

A T^ .U34U5 AAAA \ ^ C -.UUUU 1 1

b

CAA AAA duu»uuu 1A AAAPi 1 U^ UUUD -7-7^:-7A

• U D / OZ .uj jy

/

- AAAA 1 1 A . UUUU 1 1

U

zTAQ AAA oUo .UUU 1 A O "70A

1 U • z /zU "7Q "TZT A£: A 1 A •UdU 1

u

AT TOO .03389 AAAA 1 AC -.UUUU lU5

1 r AAA D 1 D •UUU 1 U •P4zo . / y / 5J •Udzpo AT TQ 1 .U33o

1

AAAA 1 AA -.UUUU 1 UU O^H • UUU 1 u • o 1 zy r\f. ^Pif. •UDPUD .uuuuuyo

632.000 11.0824 .81723 .06754 .03365 -.0000092

640.000 1 1.3513 .82660 .07002 .03358 -.0000089

648 .000 1 1.6197 .83570 .07249 .03351 -.0000085

656.000 11.8875 .84453 .07497 .03344 -.0000082

664.000 12.1548 .85312 .07744 .03338 -.0000079

672.000 12.4215 .86146 .07990 .03332 -.0000077

680.000 12.6878 .86958 .08237 .03326 -.0000074

688.000 12.9536 .87747 .08483 .03320 -.0000072

696.000 13.2190 .88515 .08729 .03314 -.0000070

101
Table 17. (Continued).

Normal Butane Isochore at 200 kg/m^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Der i vat i ve Der 1 vat i ve Curvature

K MPa MPa.m3/kg MPa/K MPa/K^

425.033 3.7879 .31 150 .00008 .05803 -.0067339

432.000 4. 1771 .33797 .00216 .05515 -.0001 184 440.000 4.6154 .36665 .00475 .05449 -.0000628

448.000 5.0496 .39398 .00747 .05407 -.0000441

456.000 5.4809 .42012 .01026 .05376 -.0000345

464.000 5.9099 .44520 .0131

1

.05351 -.0000286

472.000 6.3371 .46929 .01601 .05330 -.0000246

480.000 6.7628 .49246 .01896 .0531

1

-.0000218

488.000 7.1870 .51478 .02193 .05295 -.0000196

496.000 7.6100 .53628 .02494 .05280 -.0000179

504.000 8.0318 .55702 .02796 .05266 -.0000165

512.000 8.4526 .57705 .03101 .05253 -.0000154

520.000 8.8724 .59639 .03408 .05241 -.0000145

528.000 9.2912 .61508 .03716 .05230 -.0000138

536.000 9.7092 .63315 .04026 .05219 -.0000131

544.000 10. 1263 .65065 .04337 .05209 -.0000126

552.000 10.5426 .66758 .04649 .05199 -.0000121

560.000 10.9582 .68398 .04962 .05190 -.00001 17 568.000 1 1 .3730 .69987 .05275 .05181 -.0000113

576.000 11.7871 .71528 .05589 .05172 -.00001 10 584.000 12.2005 .73022 .05904 .05163 -.0000107

592.000 12.6132 .74472 . .06220 .05155 -.0000104

600.000 13.0252 .75880 .06535 .05146 -.0000102

608.000 13.4366 .77246 .06852 .05138 -.0000100

616.000 13.8474 .78574 .07168 .05130 -.0000098

624.000 14.2575 .79864 .07485 .05123 -.0000096

632.000 14.6670 .81118 .07801 .05M5 -.0000094

640.000 15.0759 .82337 .081 18 .05108 -.0000092

648.000 15.4842 .83523 .08435 .05100 -.0000091

656.000 15.8920 .84677 .08752 .05093 -.0000090

664.000 16.2991 .85800 .09070 .05086 -.0000088

672.000 16.7057 .86894 .09387 .05079 -.0000087

680.000 17.1 1 18 .87958 .09704 .05072 -.0000086

688.000 17.5172 .88996 .10021 .05065 -.0000085

696.000 17.9222 .90006 .10337 .05058 -.0000084

102
Table 17 . ( Cont i nued )

.

Normal Butane Isochore at 227.847 kg/m^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Der i vat i ve Der i vat i ve Curvature

K MPa MPa.m3/kg Wa/K MPa/K2

425. 160 3.7960 .27394 .00000 .06427 -.0000000

432.000 4.2356 .30082 .00216 .06427 -.0000007

440.000 4.7497 .33120 .00505 .06426 -.0000014

448.000 5.2638 .36049 .0081

1

.06425 -.0000021

456.000 5.7777 .38875 .01 128 .06423 -.0000028

464.000 6.2914 .41601 .01453 .06420 -.0000034

472.000 6.8049 - .44234 .01786 .06417 -.0000039

480.000 7.3182 .46778 .02123 .06414 -.0000044

488.000 7.8311 .49236 .02466 .06410 -.0000048

496.000 8.3438 .51613 .02812 .06406 -.0000052

504.000 8.8561 .53913 .03161 .06402 -.0000056

512.000 9.3681 .56138 .03514 .06397 -.0000060

520.000 9.8797 .58293 .03869 .06392 -.0000063

528.000 10.3909 .60380 .04226 .06387 -.0000066

536.000 10.9017 .62403 .04585 .06382 -.0000068

544.000 11.4120 .64364 .04945 .06376 -.0000071

552.000 11.9219 .66265 .05307 .06371 -.0000073

560.000 12.4313 .68109 .05670 .06365 -.0000075

568.000 12.9402 .69899 .06035 .06359 -.0000077

576.000 13.4486 .71636 .06400 .06352 -.0000079

584.000 13.9566 .73324 .06766 .06346 -.0000080

592.000 14.4640 .74963 .07133 .06340 -.0000081

600.000 14.9709 .76555 .07501 .06333 -.0000083

608.000 15.4773 .78103 .07869 .06326 -.0000084

616.000 15.9831 .79608 .08237 .06320 -.0000085

624.000 16.4884 .81072 .08606 .06313 -.0000085

632.000 16.9931 .82496 .08975 .06306 -.0000086

640.000 17.4973 .83882 .09344 .06299 -.0000087

648.000 18.0010 .85231 .09714 .06292 -.0000087

656.000 18.5041 .86545 .10083 .06285 -.0000088

664.000 19.0066 .87824 .10453 .06278 -.0000088

672.000 19.5085 .89070 .10822 .06271 -.0000089

680.000 20.0099 .90285 .1 1 192 .06264 -.0000089

688.000 20.5108 .91468 .1 1562 .06257 -.0000089

696.000 21.01 10 .92622 .1 1931 .06250 -.0000089

103
Table 17. (Continued).

Normal Butane I sochore at 250 kg/m1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Der i vat i ve Der i vat i ve Curvature

K MPa MPa.m3/kg NPa/K MPa/K^

425.087 3.7913 .24940 .00005 .06934 .0121526

432.000 4.2872 .27751 .00258 .07243 .0001 153 440.000 4.8695 .30947 .00588 .07307 .0000587

448.000 5.4557 .34053 .00936 .07345 .0000389

456.000 6.0445 .37066 .01297 .07372 .0000283

464.000 6.6351 .39986 .01668 .07392 .0000213

472.000 7.2270 .42815 .02046 .07407 .0000164

480.000 7.8200 .45556 .02431 .07418 .0000126

488.000 8.4139 .48212 .02820 .07427 .0000096

496.000 9.0083 .50786 .03214 .07434 .0000071

504.000 9.6032 .53280 .03612 .07438 .0000050

512.000 10.1984 .55698 .04012 .07442 .0000032

520.000 10.7938 .58043 .04416 .07444 .0000017

528.000 1 1.3893 .60318 .04822 .07444 .0000004

536.000 1 1 .9849 .62525 .05230 .07444 -.0000007

544.000 12.5804 .64666 .05641 .07443 -.0000018

552.000 13.1758 .66745 .06052 .07442 -.0000027

560.000 13.7710 .68764 .06465 .07439 -.0000035

568.000 14.3660 .70725 .06880 .07436 -.0000042

576.000 14.9608 .72630 .07295 .07432 -.0000048

584.000 15.5552 .74481 .0771

1

.07428 -.0000054

592.000 16.1493 .76280 .08128 .07424 -.0000059

600.000 16.7430 .78030 .08546 .07419 -.0000064

608.000 17.3363 .79732 .08964 .07414 -.0000068

616.000 17.9292 .81388 .09383 .07408 -.0000072

624.000 18.5216 .82999 .09802 .07402 -.0000075

632.000 19.1 135 .84568 .10221 .07396 -.0000078

640.000 19.7049 .86095 .10641 .07389 -.0000081

648.000 20.2958 .87582 .1 1060 .07383 -.0000084

656.000 20.8862 .89030 .1 1480 .073 7 6 -.0000086

664.000 21 .4760 .90441 . 1 1 900 .07369 -.0000088

672.000 22.0652 .91816 .12320 .07362 -.0000090

680.000 22.6539 .93157 .12740 .07355 -.0000092

688.000 23.2420 .94464 .13159 .07347 -.0000093

696.000 23.8295 .95738 .13579 .07340 -.0000094

104
Table 17 ( Cont i nued )

.

Mnrma 1 Ru'f^nG 1 sochorG ai" 300

1 1 1 1^ 1 III 1 sochore 1 sochore

1 c^Mip • Pr pc CM rfi Der i val" i ve Dsr i vat i ve Curvature

I\ MPa MPa . m3 /kn MPa/K

. 20 1 95 • \J\J c.^ J .09168 .00 18610

H H • VJ'J'-/ .2061

2

.00309 .09299 .001 m\J\J 1 1452 1 ^ t. 4 5 1 50 24^54 008 1 5 09 724 -0002997

5 '^nOQ 09907 nOOl 7Q7

44ft nnn o . \jyoj 7 1 721 1 0028 nnn i ?77

A'lfi nnn 6 Q04 5 .^ 5283 .02361 .101 17 .0000975

Af,A HUH • nnn UUU 7 7 1 67 ^87 54 02893 .10186 .0000774

A17 nnn -42 1 32 0"S430 . 1 0242 -0000627

4ftn nnn -454 16 03972 . 1 0288 -000051 5

4Rfi .000 10. 1798 .48609 .0451

8

.10325 .0000427

AQfi onn 1 1 0071 51712 05068 10^^56 0000"^ 54 ^n4 nnn 1 1 ft'^fi7 54 727 n5fi2

1

nnnn9Q4

s 1 9 nnn 1 2 fififi2 57fi5fi Ofi 1 77 10404 onno?4"^ 5?0 .000 13.501

2

.60502 .06735 .1 0421 .00001 99

J528-000 C\J %\J\J\J 14.3355 .63267 .07295 . 10436 .0000161

5"56.000 15. 1708 .65954 .07856 .10447 .00001 28 544 .000 1 6.0070 .68566 .084 19 . 10456 .0000099

552.000 16.8437 .71 105 .08983 .1 0463 .0000073

560.000 17.6810 .73573 .09548 . 10468 .0000050

568.000 18.5186 .75973 .101 14 . 1 0471 .0000030

576.000 19.3563 .78307 . 10680 . 10473 .0000012

584 .000 20. 1942 .80578 .1 1247 . 1 0473 -.0000004

592.000 2 1 .0320 .82787 .1 1814 . 10472 -.00000 19 600.000 21 .8697 .84936 .12381 .10470 -.0000032

608.000 22.7072 .87028 . 1 2949 . 10467 -.0000044

616.000 23. 5444 .89065 . 1351

7

. 1 0463 --0000055

624 .000 24 .381

3

.91048 . 1 4084 .10458 - 0000065

fi^9 nnn 95 2177 Q9C}R0 1 4fi59 1 045^^ - (\C\(\C\(\1A fi40 noo Q4ftfi2 1 52 19 10447 m\J\J\J\J\J\J L. 648.000 26.8892 .96695 .1 5786 . 1 0440 -.OOOOORQ

656.000 27.7241 .98481 .16353 .10432 -.0000096

664.000 28.5583 1.00222 .16919 .10424 -.0000102

672.000 29.3920 1.01920 .17485 .10416 -.0000107

680.000 30.2249 1.03575 .18050 .10407 -.00001 12 688.000 31.0571 1.05190 .18615 .10398 -.00001 17 696.000 31.8886 1.06764 .19180 .10389 -.0000121

105
Table 17. (Continued).

Normal Butane 1 sochore at 350 kg/m1 sotherm 1 sochore 1 sochor©

Temp • pppc c 1 1 rp Der i vat i ve Der i vat i ve P.ij V./ kJ rva 1 V U "furp 1 Ul ^ MPa MPa . m3/kg M^a/K ^/lPa/1^2

4 1 6. 274 3 .7745 • 1 571

1

.01512 . 1 3054

474 H ^ H . nnn VJWVJ 4.3018 .20265 .07334

4"57.nnn *+ _^ • vju 5.3921 .24930 .03142 . 1 3749 000765?! 440.000 6.4997 .29505 .03937 . 1 393

1

.0001961

448.000 7.6200 .33973 .04728 . 14070 .000 1 578

4 5fi 000 8.7501 .38327 .0551

5

.14179 .0001 778 464.000 9.8881 .42565 .06304 . 14268 .000 9\J\J\) 1005 \\J\J J 472 .000 1 1 .0326 .46686 .0709

1

.14341 .000083

1

480.000 ^ W W • v/W w 12. 1824 .50693 .07878 . 14402 .0000691

488.000 13.3366 .54586 .08664 .14453 .0000576

496.000 14.4946 , 58368 .09451 .14495 .0000480

504.000 1 5.6556 .62043 . 1 0238 .14530 .0000398

51 2.000 16.8192 .65613 . 1 1024 . 14559 .0000328

520.000 17.9849 .69081 .11810 .14583 .0000267

528.000 19.1 523 .72450 . 1 2595 .14602 .0000214

536 .000 20.3211 .75724 .13380 .14617 .0000167

544.000 21 .4909 .78906 . 1 4 1 64 .14628 .0000125

552 .000 22.661

5

.8 1998 .14947 .1 4637 .0000088

560.000 23.8327 .85004 . 1 5730 . 14643 .0000055

568.000 25.0043 .87927 .1651

2

.14646 .0000026

576.000 26. 1760 .90768 . 1 7293 . 14647 -.0000001

584 000 27 .3478 .93532 . 18073 . 14646 -.0000074

5Q7.000 28. 51 93 .96221 . 18851 . 14643 -.0000046

600.000 29 .6906 .98837 .19629 . 14639 -.0000065

608.000 30-861

5

1 .01 383 .20406 . 14633 -.0000083

6 1 6 .000 32.0318 11 .03861 • w w w 1 .21 181 . 1 4625 -.0000099

624.000 W^ " • w WW 33.2015 1 .06274 .2 1956 .14617 -.00001 1

3

632.000 34.3705 1.08623 .22729 .14607 -.0000126

640.000 35.5386 1.10911 .23501 .14597 -.0000138

648.000 36.7059 1.13140 .24271 .14585 -.0000149

656.000 37.6723 1.15311 ,25040 .14573 -.0000159

664.000 39.0376 1.17427 .25808 .14560 -.0000167

672.000 40.2018 1.19490 .26574 .14546 -.0000176

680.000 41.3650 1.21500 .27339 .14532 -.0000183

688.000 42.5269 1.23461 .28103 .14517 -.0000190

696.000 43.6877 1.25373 .28865 .14502 -.0000196

106
Table 17. (Continued).

Normal Butane I sochore at 400 kg/m^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Der i vat i ve Der i vati ve Curvature

K (wpa MPa.m3/kg MPaA MPa/K^

402.840 2.6135 . 1 1 338 .04987 .19052 .0004716

408.000 3.6023 .15431 .05801 .19265 .0003636

416.000 5.1540 .21653 .07021 .19513 .0002653

424.000 6.7228 .27710 .08210 .19699 .0002049

432.000 8.3048 .33597 .09378 .19846 .0001630

440.000 9.8973 .39312 .10532 .19963 .0001320

448.000 11.4983 ^ .44856 .1 1676 .20059 .0001078

456.000 13.1062 .50231 . 1 28 1 0 .20137 .0000884

464.000 14.7198 .55443 .13937 .20201 .0000725

472.000 16.3380 .60495 .15057 .20253 .0000591

480.000 17.9601 .65393 . 16172 .20296 .0000477

488.000 19.5852 .70141 .17281 .20330 .0000379

496.000 21 .2127 .74744 .18386 .20357 .0000295

504.000 22.8421 .79208 .19486 .20378 .0000221

512.000 24.4730 .83537 .20581 .20393 .0000155

520.000 26.1048 .87736 .21673 .20403 .0000098

528.000 27.7373 .91810 .22760 .20408 .0000047

536.000 29.3701 .95764 .23844 ^ .20410 .0000001

544.000 31 .0029 .99601 .24924 .20409 -.0000039

552.000 32.6354 1.03326 .26000 .20404 -.0000076

560.000 34.2674 1.06944 .27073 .20397 -.0000108

568.000 35.8988 1.10457 .28142 .20387 -.0000138

576.000 37.5293 1.13870 .29208 .20375 -.0000164

584.000 39.1587 1.17186 .30271 .20361 -.0000188

592.000 40.7869 1 .20410 .31330 .20345 -.0000210

600.000 42.4138 1.23543 .32387 .20327 -.0000229

608.000 44.0392 1 .26590 .33440 .20308 -.0000247

616.000 45.6631 1.29553 .34490 .20288 -.0000263

624.000 47.2852 1 .32435 .35537 .20266 -.0000277

632.000 48.9056 1.35239 .36580 .20243 -.0000290

640.000 50.5241 1.37959 .37621 .20220 -.0000302

648.000 52.1407 1.40625 .38659 .20195 -.0000313

656.000 53.7553 1.43212 .39694 .20170 -.0000322

664.000 55.3679 1.45731 .40726 .20144 -.0000331

672.000 56.9783 1 .48184 .41755 .201 17 -.0000338

680.000 58.5865 1.50574 .42781 .20089 -.0000345

688.000 60.1926 1 .52903 .43804 .20062 -.0000351

696.000 61 .7964 1.55173 .44825 .20033 -.0000357

107
Table 17. (Continued).

Normal Butane I sochore at 450 kg/in^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Der i vat i ve Der i vat i ve Curvature

K MPa MPa-m3/kg MPa/K MPa/K^

38 1 . 922 1.8022 .07331 .12106 .27769 .0002405

384.000 2.3797 .09627 .12558 .27817 .0002239

392.000 4.61 17 .18276 .14270 .27975 .0001731

400.000 6.8547 .26622 .15946 .28097 .0001358

408.000 9.1065 .34674 . 17592 .28194 .0001069

416.000 1 1 .3652 .42442 .19215 .28270 .0000837

424.000 13.6293 .49936 .20819 .28329 .0000646

432.000 15.8975 .57168 .22405 .28374 .0000486

440.000 18.1688 .64148 .23975 .28407 .0000350

448.000 20.4424 .70886 .25532 .28431 .0000233

456.000 22.7175 .77394 .27077 .28445 .0000131

464.000 24.9934 .83679 .28609 .28452 .0000042

472.000 27.2697 .89753 .30132 .28452 -.0000036

480.000 29.5457 .95623 .31644 .28447 -.0000105

488.000 31.8210 1 , 0 1 298 .33146 .28436 -.0000166

496.000 34.0952 1.06788 .34640 .28420 -.0000220

504.000 36.3681 1.12098 .36125 .28401 -.0000269

512.000 38.6392 1.17238 .37602 .28377 -.0000312

520.000 40.9084 1.22213 .39072 .28351 -.0000351

528.000 43. 1753 1.27031 .40533 .28321 -.0000385

536.000 45.4397 1.31698 .41988 .28289 -.0000416

544.000 47.7015 1.36220 .43436 .28255 -.0000444

552.000 49.9605 1.40604 .44877 .28218 -.0000469

560.000 52.2164 1.44853 .4631

1

.28180 -.0000491

568.000 54.4692 1.48974 .47739 .28140 -.0000511

576.000 56.7187 1.52972 .49161 .28098 -.0000529

584.000 58.9649 1.56852 .50576 .28055 -.0000545

592.000 61 .2076 1.60617 .51986 .28011 -.0000559

600.000 63.4466 1.64273 .53390 .27966 -.0000571

608.000 65.6821 1.67823 .54789 .27920 -.0000583

616.000 67.9138 1.71272 .56182 .27873 -.0000592

624.000 70.1417 1.74623 .57569 .27825 -.0000601

108
Table 17.

Normal Butane I

Temp. Pressure Z K MPa

353,249 1 .0155 .04019

356.000 2. 1 169 .08314

360.000 3.7181 .14440

364.000 5.3193 .20432

368.000 6.9203 .26292

372.000 8.5210 .32026

376.000 10.1214 .37636

380.000 11.7213 .43127

384.000 13.3208 .48501

388.000 14.9196 .53762

392.000 16.5178 .58914

396.000 18. 1 153 .63959

400.000 19.7120 .68900

404.000 21.3078 .73741 408.000 22.9027 .78484

41 2.000 24.4967 .83131 416.000 26.0897 .87685

420.000 27.6816 .92150

424.000 29.2724 .96526

428.000 30.8621 1 .00817

432.000 32.4505 1.05024

436.000 34.0378 1.09151

440.000 35.6237 1.13198

444.000 37.2084 1.17168

448.000 38.7918 1.21063

452.000 40.3737 1 .24886

456.000 41.9543 1.28636

460.000 43.5335 1.32317

464.000 45.1112 1.35931 468.000 46.6874 1.39478

472.000 48.2621 1.42961

476.000 49.8353 1.46380

480.000 51.4070 1.49738

484.000 52.9771 1.53036

488.000 54.5457 1.56276

492.000 56. 1126 1.59458

496.000 57.6779 1.62585

500.000 59.2416 1.65656

504.000 60.8036 1.68675

508.000 62.3640 1.71641

512.000 63.9228 1.74557

516.000 65.4798 1.77423

520.000 67.0352 1.80240

524.000 68.5888 1.83009

528.000 70.1407 1.85733

532.000 71.6910 1.88410

( Cont i nued )

.

sochore at 500 kg/m1 sotherm 1 sochore 1 sochore

Der i vat i ve Der i vat i ve Curvature

MPa.m3/kg MPa/K MPa/K^

.24622 .40030 .0000067

.25413 .40031 .0000020

.26554 .40030 -.0000045

.27686 .40027 -.0000106

.28810 .40022 -.0000164

.29925 .40014 -.0000218

.31033 .40004 -.0000270

.32134 .39993 -.0000319

.33227 .39979 -.0000366

.34315 .39963 -.0000410

.35396 .39946 -.0000452

.36471 .39927 -.0000492

.37540 .39907 -.0000529

.38604 .39885 -.0000565

.39662 .39862 -.0000599

.40715 .39837 -.0000631

.41764 .3981

1

-.0000661

.42807 .39784 -.0000690

.43846 .39756 -.0000718

.44880 .39727 -.0000743

.45910 .39697 -.0000768

.46936 .39665 -.0000791

.47958 .39633 -.0000813

.48975 .39600 -.0000834

.49989 .39567 -.0000854

.50999 .39532 -.0000872

.52005 .39497 -.0000890

.53007 .39461 -.0000906

.54006 .39424 -.0000922

.55002 .39387 -.0000937

.55994 .39349 -.0000950

.56983 .3931

1

-.0000964

.57968 .39272 -.0000976

.58951 .39233 -.0000987

.59930 .39193 -.0000998

.60906 .39153 -.0001008

.61879 .391 13 -.0001018

.62849 .39072 -.0001027

.63816 .39031 -.0001035

.64781 .38989 -.0001043

.65742 ,38947 -.0001050

.66701 ,38905 -.0001057

.67657 ,38863 -.0001063

.68610 ,38820 -.0001069

.69561 .38777 -.0001074

.70509 ,38734 -.0001079

109
Temp.

K

316.955

320.000

324.000

328.000

332.000

335.000

340.000

344.000

348.000

352.000

356.000

360.000

364.000

368.000

372.000

376.000

380.000

384.000

388.000

392.000

396,000

400.000

404.000

408.000

412.000

416.000

420.000

424.000

428.000

432.000

436.000

440.000

444.000

273.655

276.000

280.000

284.000

288.000

292.000

296.000

300.000

304.000

308.000

312.000

316.000

320.000

324.000

328.000

332.000

335.000

340.000

344.000

348.000

352.000

356.000

360.000

364.000

Table 17. (Continued),

Normal Butane 1 sochore at 550 kg/m^

1 sotherm 1 sochore 1 sochore

Pressure Z Der i vat i ve Der i vat i ve Curvature

MPa MPa* m->/Kg MPa/K MPa/K^

.42 1

5

.01 690 ,44649 .57026 -.0003 178

2,

1

5dd .Uo5oD •4578

1

.5693

1

-.0003082

4,4314 . 1 7384 .47261 .56810 -.0002970

C "7A 1 C 0.701

5

.25959 ,48/32 ,56693 -.0002875

8.9670 .34329 ,50195 ,55580 -.0002792

1 1 ,2279 .42474 ,51650 .56470 -.0002720

13.4846 .50410 ,53096 .56362 -.0002657

15,7370 .58146 .54535 .55257 -.0002603

17,9852 .65689 ,55966 .56154 -.0002555

20,2293 .73046 .57389 .55053 -.000251

4

22.4694 .80223 .58805 .55953 -.0002477

24.7055 ,87227 ,60214 .55854 -.0002444

25.9378 .94063 .61616 .55757 -.0002416

29. 1661 1 .00737 ,6301

1

.55651 -. 0002390

31 .3907 1 .07255 ,64399 .55566 -.0002357

33.51 14 1 . 13521 .65781 .55472 -.0002347

35.8284 1 . 19840 .67156 .55378 -.0002328

38.0417 1 .25918 .68525 .55285 -.0002312

40.2513 1 .31858 .59888 .55193 -.0002297

42.457

1

1 ,37665 .71244 .55102 -.0002283

44.5594 1 .43343 .72595 ,5501

1

-.0002270

46,8580 1 .48896 .73940 .54920 -.0002258

49,0530 1 .54327 ,75279 .54830 -.0002247

51 .2444 1 .59641 ,75513 .54740 -.0002237

53,4322 1,64841 ,77941 .54651 -,0002228

55,6165 -1 .69930 .79254 .54552 -,0002219

bl ,1912 1 .7491

1

.80582 .54473 -,0002210

59,9744 1.79787 .81894 .54385 -.0002202

62.1480 1.84552 .83202 .54297 -.0002193

54.3181 1.89238 .84504 .54210 -.0002186

66.4848 1.93818 ,85802 .54122 -.0002178

68,6479 1.98305 .87095 .54035 -.0002171

70.8076 2.02701 .88383 .53949 -.0002163

Normal Butane I sochore at 600 kg/m-^

.1053

1.9925

5.2016

8.3980

1 1,5821

14,7546

17,9158

21.0662

24.2061

27.3359

30.4559

33,5664

35,5675

39.7597

42.8430

45.9177

48.9839

52.0418

55.0917

58,1335

51,1675

64, 1938 67,2125

70,2237

,00448

,0841

1

,21645

,34453

.45856

.58873

.70520

.81815

.92773

1.03408

1.13733

1.23762

1.33506

1.42978

1.52187

1.61 143

1.69857

1.78338

1.86594

1.94633

2.02464

2.10094

2.17529

2.24777

.74460

.75571

.77460

.79341

.81216

.83082

.84940

.86790

.88632

.90465

.92290

.94107

.95915

,97716

' .99508

1,01291

1 .03067

1.04835

1.06595

1.08347

1.10091

1.11327

1,13556

1,15278

,80593

,80394

,80066

,79754

,79456

.79169

,78893

.78627

.78370

.78121

.77880

.77644

.77416

.77192

.76974

.76751

.76551

.76346

.76145

.75948

.75753

.75562

.75374

.75188

-.0008644

-.0008386

-.0007986

-.0007630

-.0007311

-.0007024

-.0005766

-.0006534

-.0006323

-.0006131

-.0005957

-.0005797

-.0005652

-.0005517

-,0005394

-.0005280

-,0005174

-,0005075

-.0004985

-.0004900

-.0004820

-.0004745

-.0004675

-.0004609

110
Table 17. (Continued),

Normal Butane I sochore at 650 kg/rn-^

Temp,

K

224,71

1

226.000

228,000

230.000

232.000

234.000

236.000

238.000

240.000

242.000

244.000

246.000

248.000

250.000

252.000

254.000

256.000

258.000

260.000

262.000

264.000

266.000

268.000

270.000

272.000

274.000

276.000

278.000

280.000

282.000

284.000

286.000

288.000

290.000

Pressure

MPa

.0104

1.4747

3,7413

6,0005

8,2526

10,4978

12.7362

14.9681

17.1936

19,4128

21.6260

23.83 52 26.0347

28.2304

30.4206

32.6054

34.7849

36.9591

39.1283

41 .2924

43.4516

45,6059

47.7555

49.9005

52.0408

54.1766

56,3080

58,4350

60.5577

62.6761

64.7903

66.9004

69.0064

71 .1084

.00050

.07018

.17648

.28059

.38257

.48249

.58041

.67639

.77048

,86274

,95322

1,04197

1,12904

1,21447

1,29830

1,38059

1.46136

1,54067

1,61855

1 .69503

1.77015

1.84394

1.91645

1.98769

2.05771

2.12652

2.19416

2.26067

2.32605

2.39035

2,45358

2,51577

2.57694

2.63713

1 sotherm

Der i vat i ve MPaTTt3/kg

1.16166

1 . 16929

1.18115

1.19300

1,20484

1 .21668

1.22851

1 .24033

1.25214

1.26394

1.27572

1.28748

1.29923

1.31096

1.32268

1.33437

1.34604

1.35770

1.36933

1,38094

1,39253

1 .40410

1,41564

1.42716

1.43866

1 .45013

1,46158

1 .47300

1.48441

1 .49578

1.50713

1.51846

1.52976

1.54103

I sochore

Der i vat i ve MPa/K

13762

13515

13143

12781 12430

12089

I 1756

11432

I I 1 17

1. 10809

1.10509

1,10215

1.09929

1.09648

1 .09374

1,09105

1.08842

1 ,08584

1 ,08331

1,08082

1,07838

1.07598

1.07363

1.07131

1.06903

1.06679

1,06458

1.06241

1,06027

1 ,05816

1 ,05607

1,05402

1,05199

1,04999

I sochore

Curvature

MPa/K^

-.0019286

-.0018906

-.0018345

-.0017816

-.0017316

-.0016845

-.0016399

-.0015977

-.0015578

-.0015199

-.0014811

-.0014500

-.0014177

-.0013869

-.0013577

-.0013298

-.0013033

-.0012781

-.0012539

-.0012309

-.0012089

-.001 1879

-.001 1678 -.001 1485

-.001 1301 -.001 1 124 -.0010954

-.0010791

-.0010635

-.0010485

-.0010340

-.0010201

-.0010066

-.0009937

Normal Butane I sochore at 700 kg/m-^

172.361

174.000

176.000

178.000

180.000

182.000

184.000

186.000

188.000

190.000

192.000

194.000

196.000

198.000

200.000

202.000

204.000

206.000

208.000

210.000

212.000

214.000

216.000

218.000

,0002

2,6501

5.8684

9.0705

12.2570

15.4285

18.5855

21 .7284

24.8578

27.9741

31.0776

34.1687

37.2478

40.3153

43.3714

46.4165

49.4508

52.4746

55,4881

58.4917

61.4855

64.4697

67.4446

70.4103

.00001

.15210

.33299

.50890

.68004

.84660

1 .00874

1. 16665

1.32047

1,47037

1,61648

1 ,75894

1,89788

2,03343

2.16569

2.29480

2.42084

2.54393

2.66416

2.78162

2,89641

3.00861

3.11829

3.22555

1 .72229

1.73404

1.74843

1.76287

1.77737

1 .79191

1 .80648

1.82107

1.83569

1.85033

1.86498

1.87964

1.89430

1 .90897

1 .92363

1 .93828

1 .95293

1.96757

1.98219

1 .99680

2.01139

2.02596

2.04051

2.05504

1 .62029

1.61329

1 ,60505

1,5971

1

1 .58946

1.58208

1.57495

1.56805

1.56137

1.55490

1.54863

1 .54254

1 .53662

1.53087

1,52527

1,51982

1,51450

1 ,50932

1,50426

1,49931

1,49448

1 ,48976

1,48514

1.48061

-.0043399

-.0042017

-.0040433

-.0338954

-.0037570

-.0036275

-.0035061

-.0033923

-,0032853

-,0031847

-.0030901

-.0030009

-.0029168

-.0028374

-.0027624

-.0026914

-.0026243

-.0025606

-.0025002

-.0024429

-.0023884

-.0023366

-.0022873

-.0022403

111
Table 17. (Continued).

Normal Butane Isochore at 735.272 kg/m1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Der i vat i ve Der i vat 1 ve Curvature

K MPa MPa.m3/kg MPa/K MPa/K^

134.860 .0000 .00000 2.23494 2. 1 1009 -.0082374

136.000 2.4002 .16780 2.24373 2. 10083 -.0080029

137.000 4.4971 .31209 2.25150 2.09293 -.0078062

138.000 6.5861 .45376 2.25932 2.08522 -.00761 75 139.000 8.6676 .59286 2.26720 2.07759 -.0074365

140.000 10.74 16 .72948 2.27513 2.07034 -.0072627

141. 000 12.8083 .86367 2.28310 2.06316 -.0070958

142.000 14.8679 .99549 2.291 12 2.0551

5

-.00693 54 143.000 16.9207 1 . 12500 2.29918 2.04929 -.0067813

144.000 18.9666 1 .25228 2.30727 2.04258 -.0066332

145.000 2 1 .0059 1 .37736 2.31540 2.03602 -.0064907

146.000 23.0387 1 .50030 2.32356 2.02960 -.0063535

14 7.000 25.0651 1 . 62 1 1

6

2.33175 2.02331 -.0062716

148.000 27.0853 1 .73999 2.33998 2.01715 -.006094 5 149.000 29.0995 1 .85683 2.34823 2.01 1 12 -.00 59770

1 50.000 31 . 1075 1 .971 74 2.35651 2.0052

1

-. 0058 540

1 51.000 33. 1 099 2.08475 2.36481 1 .9994

1

-.0057403

1 52.000 35. 1065 2. 19592 2.373 1

3

1 .99373 -. 0056306

1 53.000 37.0974 2.30529 2.38147 1 .988 1

5

-.0055248

1 54.000 39 .0828 2.41290 2. 38983 1 .98268 -.0054727

1t ^55.000 ^ 9 \J \J\J 4 1 .0628 2.51878 2.39821 1 .97730 -.005324

1

1 56.000 43. 0375 2.62298 7.40660 1 .97203 -.0057 789

1 57.000 4" 5.0069 ^9 \J\J\J7 2.72554 2.4 1 501 1 .96685 -.0051 370

11 Sft 9 000 \J\J\J 46. 97 1

2

2.82549 1 .961 75 - 0050481

1 59.000 48.9304 2.92587 2.43136 1 .95675 -.0049677

160.000 1 \J\J 9 \J\J\J 50.8847 3.0237

1

2.44030 1 .951 83 -.0048791

161. 000 52.834

1

3. 12005 2.44876 1 .94699 -.0047987

162.000 54.7787 3.21492 2.45722 1.94223 -.0047209

163.000 56.7186 3.30835 2.46569 1.93755 -.0046456

164.000 58.6538 3.40037 2.47416 1.93294 -.0045727

165.000 60.5845 3.49101 2.48265 1.92840 -.0045021

166.000 62.5107 3.58030 2.491 13 1.92393 -.0044336

167.000 64.4324 3.66827 2.49962 1.91953 -.0043673

168.000 66.3498 3.75494 2.50812 1.91520 -.0043030

169.000 68.2628 3.84035 2.51561 1 .91093 -.0042406

170.000 70. 1716 3.92451 2.5251

1

1.90672 -.0041801

112
Table 18. Calculated P( p) isotherms of normal butane.

Normal Butane Isotherm at 140 K

1 sotherm 1 sochore 1 sochore

Dens i ty Pressure z Der i vat 1 ve Der i vat i ve Curvature

kg/m-5 MPa MPa •m3/kg MPa/K MPa/K^

.00 .0000 .99999 .02003 .00000 -.0000000

730.42 .0000 .00000 2. 15683 2.03252 -.0075018

730.62 .4335 .02962 2. 16164 2.03406 -.0074912

731 .25 1.7892 . 12217 2. 17666 2.03886 -.0074536

731 .88 3.1543 .21521 2.19176 2.04369 -.0074266

732.50 4.5290 ' .30874 2.20693 2.04854 -.0073952

733.12 5.9131 .40274 2.22217 2.05341 -.0073643

733.75 7.3067 .49724 2.23749 2.05831 -.0073341

734.38 8.7099 .59223 2.25289 2.06323 -.0073044

735.00 10.1228 .68771 2.26336 2.06818 -.0072752

735.63 1 1.5453 .78369 2.28391 2.07315 -.0072466

736.25 12.9777 .88017 2.29954 2.07814 -.0072185

736.87 14.4198 .97715 2.31524 2.08316 -.0071910

737.50 15.8718 1.07463 2.33102 2.08820 -.0071641

738.12 17.3337 1.17261 2.34688 2.09327 -.0071376

738.75 18.8053 1 .27109 2.36282 2.09836 -.0071 1 17 739.38 20.2871 1.37009 2.37883 2.10347 -.0070864

740.00 21.7789 1.46960 2.39493 2.10860 -.0070615

740.63 23.2808 1.56961 2.41 1 10 2.1 1376 -.0070372

741 .25 24.7928 1 .67015 2.42736 2. 1 1894 -.0070134

741 .87 26.3150 1 .771 19 2.44369 2.12414 -.0069901

742.50 27.8474 1 .87276 2.4601 1 2. 12937 -.0069673

743. 13 29.3901 1 .97485 2.47660 2. 13461 -.0069450

743.75 30.9432 2.07746 2.49318 2. 13988 -.0069232

Norma 1 1Butane 1 sotherm at 150 K

.00 .0000 .99997 .02146 .00000 -.0000000

721 .01 .0000 .00000 2.01286 1 .89224 -.006291

1

721 .25 .4770 .03082 2.01827 1 .89403 -.0062820

722.50 3.01 78 . 19466 2.04699 1 .90352 -.0062354

723.75 5.5946 .36026 2.07598 1 .91309 -.0061 905

725.00 8.2078 .52762 2. 10524 1 .92275 -.0061474

726.25 1 0.8578 .69677 2. 13479 1 .93249 -.0061059

727.50 13.5449 .8677

1

2. 16461 1 .94232 -.0060661

728.75 1 6.2695 1 .04046 2. 19472 1 .95222 -.0060779

730.00 1 9 . 03 1

9

1 .21503 2.2251

1

1 .9622

1

00599 1

3

731 .25 21 .8324 1 .39144 2.25580 1 .97228 -.0059563

732.50 24.6716 1 .56971 2.28677 1 .98242 -.0059228

733.75 27.5495 1 .74983 2.3 1803 1 .99265 -.0058909

735.00 30.4667 1 .93183 2.34959 2.00296 -.0058605

736.25 33.4236 2. 1 1 572 2.38145 2.01334 -.005831

5

737.50 36.4205 2.301 52 2.41361 2.02379 -.0058041

738.75 39.4577 2.48923 2.44607 2.03433 -.0057781

740.00 42.5357 2.67888 2.47885 2.04494 -.0057535

741.25 45.6549 2.87047 2.51 193 2.05562 -.0057304

742.50 48.8157 3.06403 2.54533 2.06638 -.0057086

743.75 52.0184 3.25957 2.57904 2.07721 -.0056883

745.00 55.2634 3.45710 2.61308 2.0881

1

-.0056692

746.25 58.5512 3.65664 2.64744 2.09908 -.0056516

747.50 61.8822 3.85820 2.68212 2.11012 -.0056352

748.75 65.2567 4.06180 2.71714 2.12123 -.0056202

750.00 68.6751 4.26745 2.75249 2.13241 -.0056064

113
Table 18. (Continued).

Normal Butane Isotherm at 160 K

Isotherm 1 sochore 1 sochore

Dens i ty Pressure Z Derivative Der i vat i ve Curvature

kg/m3 MPa MPa.m3/kg MPa/l< MPa/K2

.00 .0000 .99990 .02288 .00000 -.0000000

71 1 .62 .0000 .00000 1.87808 1.76421 -.00531 12 712.50 1 .6660 .10216 1.89736 1.77075 -.0052872

713.75 4.0549 .24822 1.92488 1.78008 -.0052543

715.00 6.4783 .39587 1 .95266 1,78948 -.0052228

716.25 8.9366 .54514 1 .98069 1,79895 -.0051925

717.50 1 1.4301 .69603 2.00897 1 ,80850 -.0051635

718.75 13.9592 .84856 2.03752 1,81812 -.0051358

720.00 16.5240 1.00273 2.06633 1,82781 -.0051093

721.25 19. 1251 1.15856 2.09540 1,83757 -.0050841

722.50 21.7626 1.31606 2.12474 1,84741 -.0050600

723.75 24.4370 1.47524 2.15434 1,85731 -.0050371

725.00 27.1486 1.6361

1

2.18422 1,86728 -.0050154

726.25 29.8977 1.79868 2.21437 1,87733 -.0049948

727.50 32.6847 1.96297 2,24479 1,88744 -.0049753

728.75 35.5098 2.12898 2.27550 1.89762 -.0049570

730.00 38.3735 2.29673 2.30648 1.90787 -.0049398

731.25 41 .2761 2.46624 2.33774 1.91818 -.0049237

732.50 44.2181 2.63751 2,36930 1 .92857 -.0049086

733.75 47. 1995 2.81055 2.401 13 1.93901 -.0048947

735.00 50.2210 2.98538 2.43326 1 .94953 -.0048817

736,25 53.2828 3. 16201 2.46568 1 .9601 1 -.0048699

737.50 56.3854 3.34046 2.49840 1.97075 -.0048590

738.75 59.5289 3.52072 2.55142 1 .98146 -.0048492

740.00 62.7140 3.70283 2.56474 1 .99223 -.0048404

741 .25 65.9409 3.88679 2.59836 2.00306 -.0043325

742.50 69.2100 4.07262 2.63230 2.01395 -.0048257

Normal Butane 1 sotherm at 180 K

.01 .0003 .99937 ,02572 .00000 -.0000000

692.81 .0003 .00002 1,63122 1.53821 -.0038429

693.75 1.5495 .08674 1,64998 1.54483 -.0038301

695.00 3.6276 .20271 1,67501 1.55364 -.0038139

696.25 5.7371 .32002 1,70026 1.56250 -.0037986

697.50 7.8783 .43867 1,72574 1.57143 -.0037840

698.75 10.0515 ,55867 1,75144 1 .58042 -.0037701

700.00 12.2570 .68004 1,77 73/ 1.58946 -.0037570

701.25 14.4950 ,80278 1,80353 1.59856 -.0037447

702.50 16.7659 .92689 1 ,82992 1.60772 -.0037331

703.75 19.0699 1.05240 1,85654 1.61694 -.0037222

705.00 21 .4074 1.17930 1 ,88340 1.62621 -.0037120

706.25 23.7785 1.30760 1,91049 1.63555 -.0037025

707.50 26.1837 1,43732 1 ,93782 1.64493 -.0036937

708.75 28.6232 1,56846 1 ,96538 1.65438 -.0036856

710.00 31.0972 1,70103 1 ,99319 1 ,66388 -.0036781

71 1.25 33.6062 1,83504 2,02124 1,67344 -.0036714

712.50 36.1504 1,97051 2,04954 1,68305 -.0036653

713.75 38 . 7302 2, 10743 2,07808 1,69272 -.0036598

715.00 41 .3457 2,24581 2,10686 1,70244 -.0036550

716.25 43.9974 2,38568 2.13590 1,71222 -.0036508

717.50 46.6856 2,52703 2. 16519 1,72206 -.0036473

718.75 49.4105 2,66987 2.19473 1.73195 -.0036444

720.00 52.1725 2,81422 2.22453 1 .74189 -.0036421

721.25 54.9720 2,96009 2.25459 1.75188 -.0036404

722.50 57.8091 3, 10747 2.28491 1 .76194 -.0036394

723.75 60.6843 3,25640 2.31548 1.77204 -.0036389

725.00 63.5979 3,40686 2.34633 1.78220 -.0036391

726.25 66.5503 3,55887 2.37743 1 .79241 -.0036398

727.50 69.5416 3,71245 2.40881 1.80267 -.003641

1

114
Table 18. (Continued).

Normal Butane Isotherm at 200 K

1 sotherm 1 sochore 1 sochore

Density Pressure Z Der i vat i ve Der 1 vat 1 ve Curvature

kg/m3 MPa MPa-m3/kg MPa/K MPa/K^

.07 .0019 .99751 .02847 .00001 -.0000000

673.85 .0019 .00010 1.40894 1.34406 -.0028162

675.00 1.6332 .08457 1.42965 1.35158 -.0028097

676.25 3.4345 .17752 1.45235 1.35981 -.0028031

677.50 5.2642 .27159 1.47527 1.36808 -.0027970

678.75 7.1227 ^ .36680 1.49838 1.37641 -.0027914

680.00 9.0102 .46315 1.52170 1.38478 -.0027863

681.25 10.9271 .56065 1.54522 1.39320 -.0027816

682.50 12.8734 .65930 1.56895 1.40167 -.0027773

683.75 14.8495 .75911 1.59289 1.41019 -.0027735

685.00 16.8557 .66010 1.61704 1.41875 -.0027702

686.25 18.8922 .96226 1.64140 1.42736 -.0027672

687.50 20.9593 1.06560 1 .66597 1.43603 -.0027647

688.75 23.0572 1.17014 1.69076 1.44474 -.0027627

690.00 25.1863 1.27587 1.71576 1.45349 -.0027610

691.25 27.3467 1.38281 1.74097 1.46230 -.0027598

692.50 29.5388 1.49096 1.76640 1.471 15 -.0027589

693.75 31.7628 1.60032 1.79205 1.48005 -.0027585

695.00 34.0190 1.71092 1.81792 1.48900 -.0027585

696.25 36.3077 1.82274 1.84401 1.49800 -.0027589

697.50 38.6292 1.93581 1.87033 1.50704 -.0027597

698.75 40.9836 2.05012 1.89686 1.51613 -.0027608

700.00 43.3714 2.16569 1.92363 1 .52527 -.0027624

701.25 45.7928 2.28253 1.95062 1.53445 -.0027643

702.50 48.2481 2.40063 1.97783 1.54369 -.0027667

703.75 50.7375 2.52001 2.00528 1.55297 -.0027694

705.00 53.2614 2.64067 2.03296 1.56229 -.0027725

706.25 55.8200 2.76263 2.06087 1.57167 -.0027759

707.50 58.4136 2.88589 2.08902 1.58108 -.0027798

708.75 61 .0426 3.01045 2.1 1740 1.59055 -.0027840

710.00 63.7072 3.13633 2. 14602 1.60006 -.0027886

71 1.25 66.4078 3.26353 2.17488 1.60962 -.0027936

712.50 69.1445 3.39207 2.20398 1.61923 -.0027989

713.75 71 .9178 3.52194 2.23332 1.62888 -.0028046

115
Table 18. (Continued).

Normal Butane Isotherm at 220 K

1 sotherm Isochore 1 sochore

Density Pressure Z Derivative Der i vat ive Curvature

kg/m-J MPa MPa •m-J/kg MPa/K MPa/K^

.25 .0078 .99302 .03105 .00004 -.0000000

654.60 .0078 .00038 1 .20671 1. 174 55 -.0020734

655.00 .4948 .02400 1.21 322 1 . 1 7698 -.0020729

656.25 2.0240 .09800 1 .23355 1 . 18457 -. 002071

7

657. 50 3. 5788 . 1 7296 1 .25406 1 . 1 9220 -.0020708

658.75 5. 1 593 .24887 1 .27477 1 .19987 -.0020702

660.00 6.7658 .32574 1 .29566 1 .20758 -.0020699

661 .25 8.3985 .403 59 1.31673 1 .21533 -,0020699

662.50 10.0577 .48240 1 .33800 1 .22312 -.0020701

663.75 1 1 .7436 .56221 1 .35946 1 .23095 -.0020707

665.00 13.4564 .64299 1 .381 1

1

1 .23883 -.0020715

666.25 15. 1965 .72478 1 .40296 1 .24674 -.0020726

667.50 16.9639 .80756 1 .42499 1 .25470 -.0020739

668.75 18.7590 .89134 1 .44723 1 .26270 -.0020755

670.00 20.5821 .97614 1 .46965 1 .27074 -.0020774

671 .25 22.4333 1 .06196 1 .49228 1 .27882 -.0020795

672.50 24.3129 1 . 14880 1.51510 1 .28694 -.0020818

673.75 26.221 1 1 .23666 1.53812 1.2951

1

-.0020845

675.00 28.1583 1.32556 1.56134 1.30331 -.0020873

676.25 30. 1246 1 .4 1551 1.58477 1.31 156 -.0020905

677.50 32. 1203 1.50650 1.60839 1 .31985 -.0020938

678.75 34. 1456 1.59854 1 .63222 1 .32818 -.0020975

680.00 36.2009 1 .69165 1.65625 1 .33655 -.0021013

681 .25 38.2863 1 .78581 1 .68049 1 .34497 -.0021054

682.50 40.4022 1 .88105 1 .70494 1 .35342 -.0021098

683.75 42.5488 1 .97737 1 .72959 1 .36192 -.0021 144 685.00 44.7263 2.07478 1 .75445 1 .37046 -.0021 192 686.25 46.9350 2. 17327 1 .77952 1.37904 -.0021243

687.50 49. 1752 2.27286 1 .80481 1 .38766 -.0021296

688.75 51 .4471 2.37355 1 .83030 1.39633 -.0021351

690.00 53.7510 2.47535 1.85601 1.40503 -.0021409

691.25 56.0872 2.57827 1.88194 1.41378 -.0021469

692.50 58.4560 2.68230 1.90808 1.42257 -.0021531

693.75 60.8575 2.78747 1.93444 1.43140 -.0021596

695.00 63.2921 2.89377 1.96102 1.44027 -.0021663

696.25 65.7601 3.00121 1.98781 1.44918 -.0021733

697.50 68.2618 3.10980 2.01483 1.45814 -.0021805

698.75 70.7973 3.21954 2.04207 1.46714 -.0021879

116
Table 18. (Continued).

Normal Butane Isotherm at 240 K

1 sotherm 1 sochore 1 sochore

Dens i ty Pressure Z Der i ydt i ve Der i vat i ve Curvature

kg/m-5 MPa MPa •rrP/kg MPa/K MPa/K^

.71 .0241 .98456 .03532 .00010 -.0000000

634.87 .024

1

.001 10 1 .02168 1 .02453 -.001 5203

635.00 . 1 576 .00723 1 .02356 1 .02526 -.00 1 5205

637. 50 2.7618 . 1261

9

1 .05990 1 .03922 -.001 5250

640.00 5.4577 .24839 1 .09693 1 .05332 -.001 5302

642.50 8.2471 .37388 1 . 13467 1 .06757 -.001 5361 645.00 1 1.1317 .50270 1 . 1 731

1

1 .08 196 -.00 15427

647.50 14. 1 132 .63489 1 .21226 1 .09649 -.001 5499

650.00 17. 1936 .77048 1 .25214 1.11117 -.0015578

652.50 20.3745 .90953 1 .29274 1 . 12600 -. 001 5663

655.00 23.6578 1 .05207 1 .33409 1 .14097 -.0015754

657.50 27.0455 1 . 1981

5

1 .37617 1 .15609 -.0015851

660.00 30.5394 1 .34780 1.41901 1 . 1 7135 -.0015954

662.50 34.1412 1.50108 1.46260 1.18677 -.0016063

665.00 37.8530 1 .65802 1 .50696 1 .20233 -.0016178

667.50 41.6767 1 .81866 1.55210 1.21805 -.0016299

670.00 45.6142 1 .98306 1.59802 1 .23391 -.0016426

672.50 49.6674 2.15124 1.64472 1.24993 -.0016558

675.00 53.8385 2,32327 1 .69223 1 .26609 -.0016697

677.50 58.1292 2.49917 1.74054 1.28241 -.0016842

680.00 62.5418 2.67900 1.78967 1.29887 -.0016992

682.50 67.0783 2.86279 1 .83962 1.31549 -.0017149

685.00 71,7406 3.05060 1 .89040 1 .33226 - .0017312

Norma 1 I3utane Isotherm at 260 K

1 .69 .0610 .97089 .0351

1

.00025 -.0000001

614.46 .0610 .00267 .85208 .8901

8

-.0010979

61 5.00 .5249 .02295 .85896 .89293 -.0010998

617.50 2.7122 .11810 .89 105 .90569 -.001 1084

620.00 4.9806 .21 599 .92379 .91858 -.001 1 174 622.50 7.331

7

.31668 .95717 .931 59 -.001 1268

625.00 9.7671 .42018 .99122 .94473 -.001 1366

627 . 50 12.2883 .52654 1 .02592 .95799 -.001 1467

630.00 14.8972 .63579 1 .06130 .971 39 -.001 1572

632.50 17.5954 .74798 1 .09736 .98491 -.001 1681 635.00 20.3846 .86313 1 . 1341

0

.99857 -.001 1793

637. 50 23.2665 .98 1 29 1 . 1 7 1 53 1 .01 236 -.001 1909 640.00 26.2429 1 . 10250 1 .20967 1 .02628 -.0012028

642.50 29.31 54 1 .22679 1 .24851 1 .04033 -.001 2150

645.00 32.4860 1 .35421 1 .28806 1 .05452 -.0012277

647. 50 35.7563 1 .48478 1 .32833 1 .06885 -.001 2406

650.00 39.1283 1.61855 1.36933 1.08331 -.0012539

652.50 42.6036 1 .75555 1.41 106 1.09790 -.0012676

655.00 46.1841 1.89583 1.45354 1 . 1 1 263 -.0012817

657.50 49.8719 2.03943 1.49676 1.12751 -.0012961

660.00 53.6686 2.18637 1.54074 1.14251 -.0013109

662.50 57.5762 2.33671 1.58549 1.15766 -.0013261

665.00 61.5967 2.49049 1.63100 1.17295 -.0013416

667.50 65.7319 2.64773 1.67729 1.18838 -.0013575

670.00 69.9838 2.80848 1,72437 1.20395 -.0013739

117
Table 18. (Continued).

Normal Butane Isotherm at 280 K

Isotherm 1 sochore 1 sochore

Dens ity Pressure Z Der i vat i ve Der i vat i ve Curvature

kg/m-J MPa MPa •m3/kg MPa/K MPa/K^

2.50 .0965 .96392 .03728 .00037 -.0000002

3.49 .1330 .95069 .03620 .00053 -.0000004

593. 1

1

. 1330 .00560 .69689 .76860 -.0007679

595.00 1.4717 .06175 .71 778 .77732 -.0007762

597.50 3.301

1

. 13794 .74589 .78894 -.0007873

600.00 5.2016 .2 1 64 5 .77460 .80066 -.0007986

602.50 7. 1746 .29731 .80390 .81250 -.0008101

605.00 9.2217 .38055 .83382 .82446 -.0008218

607.50 1 1 .3442 .46622 .86435 .83653 -.0008336

610.00 13.5440 .55434 .89551 .84872 -.0008456

612.50 1 5.8223 .64495 .92730 .86102 -.0008577

615.00 18. 1810 .73808 .95972 .87344 -.0008701

617.50 20.6215 .83377 .99279 .88598 -.0008826

620.00 23. 1455 .93205 1 .02651 .89864 -.0008953

622.50 25.7546 1 .03295 1 .06089 .91 143 -.0009082

625.00 28.4505 1. 13651 1 .09593 .92433 -.00092 12 627.50 31 .2348 1 .24276 1 . 1 3 1 64 .93736 -.0009345

630.00 34 . 1 092 1 .351 75 1 . 16803 .95051 -.0009480

632.50 37.0755 1 .46349 1.20511 .96378 -.0009616

635.00 40. 1354 1 . 57804 1 .24288 .97718 -.0009755

637.50 43.2905 1.69542 1.28135 .99071 -.0009896

640.00 46.5427 1 .81566 1.32052 1.00436 -.0010039

642.50 49.8937 1.93881 1.36041 1.01815 -.0010185

645.00 53.3453 2.06491 1.40101 1.03206 -.0010332

647.50 56.8994 2.19397 1.44234 1.04610 -.0010482

650.00 60.5577 2.32605 1.48441 1.06027 -.0010635

652.50 64.3220 2.461 18 1.52721 1.07457 -.0010790

655.00 68. 1943 2.59938 1.57076 1.08900 -.0010948

118
Table 18. (Continued).

Normal Butane Isotherm at 298.150 K

1 sotherm Isochore 1 sochore

Dens i ty Pressure Z Der 1 vat 1 ve Der i vat i ve Curvature

kg/m3 MPa MPa.m3/kg MPa A MPa/K^

2.50 .1032 .96802 .04006 .00037 -.0000001

5.00 .2003 .93919 .03757 .00076 -.0000007

6. 18 .2438 .92534 .03634 .00096 -.0000012

572.65 .2438 .00998 .56807 .66742 -.0005261

575.00 1.6070 .06553 .59049 .67726 -.0005378

577.50 5.1136 . 1 264

1

.61484 .68781 -.0005502

580.00 4.6817 .18926 .63973 .69847 -.0005627

582.50 6.3127 .25410 .66517 .70923 -.0005752

585.00 8.0080 .32096 .691 17 .72009 -.0005877

587.50 9.7690 .38988 .71774 .73105 -.0006002

590.00 11.5972 .46088 .74489 .74213 -.0006128

592.50 13.4939 .53400 .77261 .75330 -.0006255

595.00 15.4608 .60926 .80093 .76459 -.0006382

597.50 17.4991 .68670 .82984 .77599 -.0006510

600.00 19.6105 .76634 .85935 .78749 -.0006638

602.50 21.7964 .84823 .88948 .7991

1

-.0006768

605.00 24.0584 .93239 .92022 .81084 -.0006898

607.50 26.3980 1.01885 .95158 .82268 -.0007029

610.00 28.8168 1.10765 .98358 .83463 -.0007160

612.50 31.3164 1.19882 1.01621 .84670 -.0007293

615.00 33.8984 1.29238 1.04949 .85889 -.0007428

617.50 36.5644 1.38838 1.08341 .871 19 -.0007563

620.00 39.3160 1.48684 1.1 1800 .88361 -.0007699

622.50 42.1549 1.58780 1.15325 .89615 -.0007837

625.00 45.0828 1.69129 1.18917 .90881 -.0007976

627.50 48.1013 1.79734 1.22576 .92158 -.00081 17 630.00 51.2122 1.90598 1.26304 .93448 -.0008259

632.50 54.4171 2.01726 1.30102 .94750 -.0008402

635.00 57.7178 2.13119 1.33969 .96064 -.0008547

637.50 61.1 161 2.24782 1.37906 .97391 -.0008694

640.00 64.6137 2.36718 1.41915 .98729 -.0008843

642.50 68.2125 2.48930 1.45995 1.00081 -.0008993

645.00 71.9141 2,61421 1.50148 1.01444 -.0009145

119
Table 18. (Continued).

Normal Butane Isotherm at 300 K

1 sotherm 1 sochore 1 sochore

Density Pressure Z Der ivat 1 ve Der Ivat Ive Curvature

kg/m^ MPa MPa 'm^/kg MPa/K MPa/K^

2.50 .1039 .96839 .04034 .00037 -.0000001

5.00 .201 7 .93998 .03788 .00076 -.0000006

6.52 .2582 .92233 .03630 .00102 -.0000014

570.49 .2582 .01055 .55557 .65753 -.0005039

572.50 1 .3934 .05671 .57438 .66585 -.0005140

575.00 2.8591 . 1 1 587 .59826 .67628 -.0005265

577.50 4.3851 . 17694 .62268 .68681 - .0005391

580.00 5.9729 .23997 .54764 .69744 AAA C C 1 ^ -•000551

D

582.50 7.6238 .30498 .673 16 .70817 AAA C y1 O 585.00 9.3392 .37201 .69924 .71 901 AAA C*?^: Q U0U5 / DO 587.50 1 1 . 1205 .44 108 .72589 .72995 A A A CQ A>t 590.00 12.9691 .51 222 .7531

1

.74 1 00 AAA^r AO 1 UUUoUZ

1

592.50 14.8865 .58547 .78092 .75216 AAA C 1 >1 Q 595.00 16.8742 .66085 .8093

1

.76342 AAA^O

597.50 18.9336 .73840 .83830 .77479 A A A^ Vl A >l -.0005404

600.00 21 .0662 .81815 .86790 .78627 AAA z; CZ A -.0006534

602.50 23.2736 .90013 .8981

1

.79787 AAAil CdL'Z -.0006553

605.00 25.5572 .98437 .92893 .80957 A AAC TAyl -.0005794

607.50 27.9187 1 .07090 .96038 . 82 1 39 AAA£ AO

C

-.0005925

610.00 30.3597 1 . 1 5976 .99246 .83332 A AAT A C O -.0007058

612.50 32.8816 1.25097 1 .02517 .84536 AAA T 1 A

1

-.00071 91 615.00 35.4861 1.34457 1 .05854 .85752 -.0007325

617.50 38. 1748 1.44059 1.09255 .86980 -.0007461

620.00 40.9494 1.53906 1.12722 .88220 A AA T C A O -.0007598

622.50 43.81 15 1 .64002 1 . 16256 .89471 AAA"7"7Ttf^ -.UUU / /3d

625.00 46.7627 1.74349 1.19857 .90734 -.0007875

627.50 49.8048 1.84952 1.23525 .92009 -.0008016

630.00 52.9395 1.95812 1 .27262 .93296 -.0008158

632.50 56.1685 2.06935 1 .31069 .94595 -.0008302

635.00 59.4936 2.18322 1.34945 .95907 -.0008447

637.50 62.9164 2.29977 1.38891 .97231 -.0008594

640.00 66.4387 2.41903 1.42909 .98567 -.0008743

642.50 70.0624 2.54104 1 .46998 .99915 -.0008893

120
Table 18. (Continued).

Normal Butane Isotherm at 320 K

1 sotherm 1 sochore 1 sochore

Dens ity Pressure Z Derivative Der ivative Curvature

kg/m-' MPa f^a •m3/kg MPa/K MPa/K^

2.50 .1112 .97194 .04336 .00037 -.0000001

5.00 .2168 .94743 .041 12 .00075 -.0000004

7.50 .3168 . 92270 ,03881 .001 17 -.000001

1

10.00 .41 08 .89751 .03643 .001 62 -.0000025

1 1 .30 .4575 .884 18 .03516 .00187 - .0000035

546. 16 .4575 .01830 .42794 .55518 -.0002873

547.50 1 .0367 . 04 1 36 .43823 .56008 -.0002945

550.00 2. 1 566 .08566 .45781 .5693 1 -.0003082

552. 50 "Z "Z 1 3.3261 1 "Z 1 CO

. 1 3 1 52 .47788 . 57863 -.0003z 1

5

555.00 4 . 54 64 .17896 .49843 .58804 -.0003348

557. 50 5.8187 ' .22801 .51 946 .59754 -.0003479

560.00 7. 1442 .27870 .54 1 00 .5071

4

-.0003509

562. 50 8.5241 .33 1 05 .56304 .61683 -.0003739

565.00 9.9598 .3851

0

.58560 .62661 -.0003867

567.50 1 1 .4525 .44087 .60867 .63649 -.0003995

570.00 13.0036 .49838 .63227 .64647 -.0004123

572.50 1 4 . 6 1 43 . 55767 .65641 .65654 -.0004250

575.00 16.2861 .61 876 .68108 .66672 -.0004377

577.50 18.0202 .68 168 .70631 .67700 -.0004 504 580.00 19.8181 .74646 .73209 .68737 -.000463

1

582.50 21 .681

1

.81312 .75843 .69785 -.0004757

585.00 23.6107 .88171 .78534 .70844 -.0004884

587.50 25.6083 .95224 .81283 .71912 -.000501

1

590.00 27.6753 1 .02474 .84090 .72992 -.00051 39 592.50 29.8133 1 .09924 .86956 .74081 -.0005266

595.00 32.0236 1. 17578 .89882 .75182 -.0005394

597.50 34.3079 1 .25438 .92868 .76293 -.0005523

600.00 36.6675 1 .33506 .95915 .77416 -.0005552

602.50 39. 1042 1 .41787 .99025 .78549 -.0005781

605.00 41 .6193 1 . 50283 1 .02196 .79693 -.000591

1

607.50 44.2145 1 .58997 1.05431 .80848 -.0006042

610.00 46.8914 1.67932 1.08729 .82015 -.0006174

612.50 49.6515 1.77092 1.12092 .83193 -.0006307

615.00 52.4965 1.86478 1.15521 .84382 -.0006441

617.50 55.4281 1.96094 1.19014 .85582 -.0006575

620.00 58.4478 2.05944 1.22575 .86794 -.000671

1

622.50 61 .5574 2.16029 1.26202 .88018 -.0006847

625.00 64.7585 2.26354 1.29898 .89253 -.0006985

627.50 68.0528 2.36921 1.33661 .90500 -.0007124

630.00 71 .4421 2.47734 1.37494 .91759 -.0007265

121
Table 18. (Continued).

Normal Butane Isotherm at 340 K

1 sotherm 1 sochore 1 sochore

Dens ity Pressure Z Der i vat i ve Der i vat i ve Curvature

kg/m3 MPa MPaTti3/k<j MPa/K MPa/K2

5.00 .2318 .95339 .04429 .00075 -.0000002

10.00 .4428 .91037 .04005 .00158 -.0000014

15.00 .6322 .86662 .03572 .00252 -.0000044

18.56 .7538 .83513 .03260 .00328 -.0000088

519.47 .7538 .02984 .31403 .46003 -.0001035

520.00 .9207 .03641 .31724 .46172 -.0001066

525.00 2.5845 .10122 .34853 .47787 -.0001355

530.00 4.4088 .17104 .38148 .49434 -.0001632

535.00 6.4022 .24605 .41614 .51114 -.0001898

540.00 8.5732 .32643 .45257 .52828 -.0002157

545.00 10.9309 .41238 .49082 .54577 -.0002409

550.00 13.4846 .50410 .53096 .56362 -.0002657

555.00 16.2438 .60178 .57304 .58184 -.0002902

560.00 19.2183 .70562 .61712 .60043 -.0003145

565.00 22.4184 .81583 .66325 .61940 -.0003385

570.00 25.8543 .93261 .71 148 .63877 -.0003625

575.00 29.5368 1.05618 .76189 .65852 -.0003864

580.00 33.4769 1.18675 .81451 .67868 -.0004104

585.00 37.6858 1.32454 .86942 .69925 -.0004345

son no Hi. « \ t vU 1

1 . &Mlfi HOV /

D

. / ^\J^.J — • UUU'f JO 1 595.00 46.9563 1.62263 .98628 .74163 -.0004830

600.00 52.0418 1.78338 1.04835 .76346 -.0005076

605.00 57.4439 1.95223 1.1 1291 .78573 -.0005325

610.00 63.1752 2.12941 1.18002 .80843 -.0005577

615.00 69.2485 2.31514 1.24974 .83158 -.0005832

Normal Butane 1 sotherm at 360 K

5.00 .2467 .95829 .04741 .00074 -.0000002

10.00 ,474 1 .92065 .04352 .00156 -.0000009

15.00 .6819 .88284 .03962 .00245 -.0000027

20.00 .8703 .84502 .03573 .00345 -.0000059

25.00 1 .0393 .80729 .03187 .00456 -.0000115

29.39 1.1718 .77422 .02847 .00565 -.0000200

489.36 1.1718 .04650 .21405 .37071 .0000609

490.00 1.3100 .05192 .21699 .37246 .0000567

495.00 2.4534 .09625 .24058 .38624 .0000250

500.00 3.7181 .14440 .26554 .40030 -.0000045

505.00 5.1111 .19654 .29192 .41466 -.0000321

510.00 6.6397 .25281 .31977 .42932 -.0000584

51 5.00 8.31 14 .31339 .34915 .44429 -.0000836

520.00 10.1338 .37843 .3801

1

.45959 -.0001080

525.00 12.1 152 .44812 .41270 .47521 -.0001317

530.00 14.2637 .52261 .44699 .491 18 -.0001549

535.00 16.5880 .60209 .48302 .50748 -.0001777

540.00 19.0969 .68673 .52085 .52414 -.0002001

545.00 21.7996 .77673 .56054 .541 16 -.0002224

550.00 24.7055 .87227 .60214 .55854 -.0002444

555.00 27.8243 .97353 .64571 .57630 -.0002664

560.00 31 .1660 1.08072 .69130 .59443 -.0002884

565.00 34.7408 1.19402 .73898 .61294 -.0003103

570.00 38.5593 1.31363 .78878 .63184 -.0003323

575.00 42.6323 1.43976 .84078 .651 14 -.0003544

580.00 46.9709 1.57261 .89502 .67083 -.0003766

585.00 51.5864 1.71237 .95157 .69094 -.0003990

590.00 56.4905 1 .85927 1.01047 .71 145 -.0004216

595.00 61.6952 2.01351 1 .07179 .73238 -.0004444

600.00 67.2125 2.17529 1.13556 .75374 -.0004675

122
Table 18.

Normal Butane

Dens ity Pressure Z

kg/in3 MPa

5.00 .2616 .96242

10.00 .5051 .92915

15.00 .7306 .89600

20.00 .9383 .86310

25.00 1.1286 .83052

30.00 1.3018 .79829

35.00 1.4581 . .76639

40.00 \,5911 .73482

45.00 1.7210 .70357

45.78 1.7387 .69873

453.83 1 . 7387 .07048

455.00 1.8910 .07646

460.00 2.5923 .10367

465.00 5.1111 .13363

470.00 4.2529 . 1 6647

475.00 5.2234 .20230

480.00 6.2952 .24127

485.00 7.4743 .28351 490.00 8.7673 .32916

495.00 10.1806 .37836

500.00 11.7213 .43127

505.00 13.3964 .48802

510.00 15.2134 .54877

515.00 17.1798 .61369

520.00 19.3036 .68293

525.00 21.5930 .75664

530.00 24.0564 .83501

535.00 26.7025 .91820

540.00 29.5403 1.00637

545.00 32.5791 1.09972

550.00 35.8284 1 . 1 9840

555.00 39.2980 1.30261

560.00 42.9981 1.41253

565.00 46.9389 1.52835

570.00 51.1311 1.65025

575.00 55.5857 1.77842

580.00 60.3139 1.91306

585.00 65.3271 2.05436

590.00 70.6371 2.20252

(Continued)

.

Isotherm at 380 K

Isotherm 1 sochore 1 sochore

Derivative Der i vat i ve Curvature

MPa .m3/kg MPa/K Mra/K

.05050 .00074 -.0000001

.04689 .00154 -.0000007

.04332 .00241 -.00000 18 .03980 .00336 -.0000038

.03634 .00439 -.0000068

.03294 .00550 -.00001 1

2

.02959 .00672 -.0000 177 .02629 .00804 -.0000272

.02303 .00948 -.0000422

.02252 .00972 -.0000453

.12849 .28570 .0002238

.13216 .28832 .0002143

. 14849 .29965 .0001769

.16588 .31 122 .0001 438

. 1 8437 .32305 .0001 137 .20403 .33514 r\i\(^ r\c> ^ o .0000860

.22488 .34751 .0000601

.24699 .36017 .0000355

.27041 .37312 .00001 23 .29517 .38637 -.00001 Ql

.32134 .39993 -.uouu^ ly .34896 .4 1 380

.37808 .42799 -.oouu /jy

.40876 .44251 r\r\r\r\CiA -.uuuuy4

J

.44 104 >1 C "7*2 "7 .45737 r\r\r\ i 1 / R -.UUU 114 5 .47499 .472 56 -. UUU 1 j44

.51066 .48809 -.UUU 1 134z .54809 .50398 r\r\r\ 1 "7*zn -. UUU 1 /jy

.58735 . 52022 Ann 1

R

-.UUU 1 yjp

.62849

.67156 .55378 -.0002328

.71662 .571 12 -.0002526

.76373 .58883 -.0002724

.81295 .60692 -.0002923

.86432 .62541 -.0003124

.91790 .64428 -.0003327

.97375 .66355 -.0003532

1.03192 .68322 -.0003739

1.09248 .70330 -.0003948

123
Table 18. (Continued).

Normal Butane Isotherm at 400 K

I SO therm 1 sochore I sochore

Den s i ty Pressure z \J\^\ 1 V <J 1 1 VJsD 1 1 V u 1 1 0o 1u1 p \/ ^ 11 r" 1 V a 1 u( c

kq/m-5 MPa MPa •m3 /kg MPa/K (i^Pa/K 2

5.00 .2764 .96595 .05356 .00074 - nnnnnni

in on 5357 .93637 0'5n7n nni s'^ - nnnnnns

1 5.00 ,11 nn7'^R - nnnnni

20.00 1 . 0048 .87802 .04366 nn^79

25.00 1 .2 1 52 .84948 .04050 .00427 • \J\J\J\J\JH\J 30.00 1.4099 .82136 .03742 .00532 -.0000073

35.00 1.5894 .79366 .03440 .00644 -.0000108

40.00 1.7540 .76638 .03146 .00763 - nnnni S4 45.00 1 .9041 . 73951 07859 nnRQn - nnnn7 17 50 on 2. 0401 .7 1 308 n7Sftn - nnnn7Hft 55.00 2 . 1 623 .687 10 .0231

1

.01 165 - nnnn'^RS 60 . 00 2 . 27 1

3

.661 59 .02050 .01315 -.0000514

65.00 2.3675 .63655 .01798 .01474 -.0000691

70.00 2.4513 .61 200 .01 555 .01643 -.000094 7 72.54 2.4892 .59973 .01435 . 0 1 734 -.0001 128

408 .02 2.4892 . 1 0662 .05843 .20249 .0004306

410.00 2.6082 .11118 .061 93 .20585 .0004060

415.00 2.9409 .12385 .07129 .21447 .0003528

420.00 3.3223 .13824 .08138 .22328 .0003089

425.00 3.7560 .15445 .09223 .23230 .0002716

430.00 4.2460 .17257 . 10390 .24 1 55 .0002389

435.00 4.7964 .19270 . 1 1 64 1 .25103 .0002097

440.00 5.4 1 16 .21495 . 12982 .26075 .0001832

445.00 6. 0961 .23942 .14415 .27073 .0001 587

450.00 6.8547 .26622 . 15946 .28097 .0001358

455.00 7.6924 .29547 .17577 . 29 1 48 .0001 141 460.00 8.6142 .32726 .19314 .30227 .0000935

465.00 9.6256 .361 77 .21161 .31333 .0000736

470.00 10.7322 .39907 .23121 .32468 .0000544

475.00 1 1 .9397 .43930 .25201 .33632 .0000357

480.00 1 3.2543 .48259 .27403 .34825 .0000175

485.00 14.6822 .52907 .29734 .36050 -.0000005

490.00 1 6.2299 .57887 .32197 .37304 -.0000181

495.00 17 .904

1

.63214 .34797 .38590 -.00003 56 500 on 1 9. 7 120 .68900 .37540 .39907 -.0000529

5n5 on 9 1

1 • fifinfi \JKJ\J\J .74962 .40430 .4 1256 -.0000702

sin nn 9"^ 7S7R - 0000ft7"S

5 1 5.00 .46673 .44052 -.0001045

s^n nn 4 55ni - 0001716

nn ^1 0170 .53568 .46983 -.0001 388

s^n nn • 1 O f J \ 1 1 4 1

A

- OOOISfiO

535.00 36.7473 1.20042 .61 158 .50051 -.0001733

540.00 39.9062 1.29154 .65227 .51638 -.0001907

545.00 43.2732 1.38766 .69486 .53261 -.0002082

550.00 46.8580 1 .48896 .73940 .54920 -.0002258

555.00 50.6705 1.59560 .78595 .56616 -.0002436

560.00 54.7210 1.70776 .83457 .58350 -.0002616

565.00 59.0198 1.82562 .88532 .60121 -.0002798

570.00 63.5778 1.94936 .93824 .61931 -.0002982

575.00 68.4059 2.07916 .99339 .63779 -.0003168

124
Table 18.

Norma I Butane

Dens ity Pressure Z

kg/fti^ MPa

5.00 .2837 .96753

10.00 .5510 .93950

1 5.00 .8022 . 9 1 1 83 20.00 1 .0376 .88457

25.00 1 .2577 .85776

30.00 1 .4628 .83 139 35.00 1 .6534 .80544

40.00 1.8297 .77992

45.00 1.9921 .75481

50.00 2. 141

1

.7301

4

55.00 2.2771 .70592

60.00 2.4005 .68217

65.00 2.51 19 .65890

70.00 2.61 17 .63614

75.00.. 2 . 7004 .61391

80.00 2.7786 .59221

85.00 2.8468 .57105

90.00 2.9055 .55045

94.40 2.9496 .53278

376.69 2.9496 .13351 380.00 3.0554 .13709

385.00 3.2388 .14344

390.00 3.4536 . 1 5099

395.00 3.7024 . 1 5982

400.00 3.9883 .17001

405.00 4.3145 .18164

410.00 4.6843 .19480

415.00 5. 1012 .20959

420.00 5.5689 .22608

425.00 6.0912 .24437

430.00 6.6722 .26457

435.00 7.3162 .28677

440.00 8.0274 . 3 1 1 07 445.00 8.8107 .33759

450.00 9.6706 .36642

455,00 10.61 24 .39768

460.00 1 1 . 64 1

1

.43149

465.00 12.7622 .46796

470.00 1 3.9813 .50721

4 /5.00 1 5.3044 .54937

480.00 16.7375 .59455

485.00 18.2869 .64289

490.00 19.9592 .69452

493 .00 O 1 ~7 C 1 O

21 •751

z

.74957

500.00 23.6999 .808 19 505.00 25.7826 .87051

51 0.00 28.0 168 .93667

51 5.00 30.4 1 05 1 .00682

520.00 32.9715 1.08112

525.00 35.7083 1.15971

530.00 38.6294 1.24274

535.00 41.7438 1.33038

540.00 45.0605 1.42279

545.00 48.5889 1.52012

550.00 52.3388 1.62255

555.00 56.3200 1.73024

560.00 60.5429 1.84337

565.00 65.0180 1.9621

1

570.00 69.7560 2.08663

(Continued)

.

Isotherm at 410 K

1 sotherm Isochore 1 sochore

Derivative Der i vat i ve Curvature

MPa •m3/kg MPa/K MPa/K

.05508 AAAT A .00074 AAAAAA

1

-.000000

1

.05183 A A 1 no .001 52 AAAAAA

/

-. 0000004

.04864 .00237 r\r\r\r\r\ 1 0 -.000001

2

.04554 .00327 UUUUUZ

J

.04251 A A ^ OT .00423 -•UUUUU

.03956 A A COiT .00526 r\r\r\r\r\c i •03667 AA £ZX A .00034 -•UuUUUoy

.U3jod A A-7/I A .00 /4y UUUU 1 /.^ .031 13 .00871 -.0000168

.02848 .00998 -.0000221

.02592 .01 132 AA A A OOC -•UUUU/oo

.02346 .01272 AAA A'Z C C -.000036!)

.021 10 A 1 J1 1 0 .01418 A AA A /I C 1 -•000U4D

1

.01883 .01 570 A A AA C 0 A -. 0000580

.01668 .01 729 A AAA ~7"Z A -•0000730

.01462 A 1 0 AC .01 895 A A AAAO "Z -• uouoyz3

.01 267 AOA^ 0 .020DO r\r\r\ 1 1 0 "z -•UUU

1

\OJ

.01 082 .02250 r\ r\ r\ 1 c C T -.0001 553

.00927 .024 19 -.0002043

.03006 . 1 5957 A AA ^ 1 AC .00051 05

.03375 . 1 64 1

6

A AA C A Ct C .0005485

.03973 .17120 AAA A ~l a C .0004756

.04626 . 17839 AAA A ^ 0 C .0004 185 .05337 .18577 A A A "7 *7 0 A .0003724

.061 10 .19335 .0003335

.06948 .201 14 .0002999

.07855 .2091

5

r\r\ f\^~i f^T .0002703

.08833 .2 1740 A AA 0 7 .0002436

.09887 .22588 .0002193

.11020 .23462 .0001968

. 1 2235 .24360 .0001757

.13537 .25284 AA A 1 d C "7 .0001 557

. 14929 .26234 A A A 1 T tl 1 .0001367

.16416 .272 1

1

.0001 183

. 18000 .2821

5

.0001006

. 1 9587 .29246 A AA AO "Z j1 .0000834

.2 1480 .30306 .0000665

O "Z O /! .23384 "Z 1 ZA C .3 1 395 A AAA C A

A

.0000500

.254UZ zo c 1 0 .^2512 AAAAZ Z"? .OOOOjJ

/

0-7 Cyl 1 X X^ c:q AAAA 1 ~7C .0000 1 /o

. ^^oUj XA QX c: AAAAA 1 -7 .00000 1

/

.JZ 193 z A ^ 0 .30042 AAAA 1 yl 0 -.0000142

.34/19 Z "700 A .3 /2o0 AAAA'ZAA -.0000300

.J/3o3 ZQ CACl .30 549 AAAA yl -.0000430

.40 1 o9 ZAO CA .39850 AAAA C 1 C -.OOOOol

3

A X i A A .4 J 1 44 /I 1 1 Q 0 .4 1 lo2 AAAA"7"7"Z -.0000 / /3 .4DZ52 .4254

/

AAAAAZ

1

-.000093

1

.4yj 1

y

A xnA ^ .4 jy4D A A A 1 AAA -. 000 1 oyo

.5<i9P0 A C Z~7T .453 /

/

A AA 1 0 y1 A -.000 1 249

.56550 .46843 -.0001410

.60325 .48343 -.0001571

.64279 .49878 -.0001734

.68419 .51448 -.0001899

.72750 .53053 -.0002065

.77278 .54696 -.0002232

.82007 .56374 -.0002402

.86944 .58090 -.0002574

.92094 .59844 -.0002748

.97463 ,61635 -.0002924

125
Table 18. (Continued).

Normal Butane Isotherm at 420 K

1 sotherm 1 sochore 1 sochore

Density Pressure Z Der i vat i ve Der i vat i ve Curvature

kg/m3 MPa MPa •m3/kg MPaA MPa/K^

10.00 .5662 .94246 .05346 .00152 -.0000004

20.00 1.0702 .89062 .04739 .00325 -.0000020

30.00 1.5151 .84060 .04164 .00520 -.0000052

40.00 1.9040 .79229 .03619 .00738 -.0000103

50.00 2.2399 .74564 .03104 .00978 -.0000178

60.00 2.5260 .70074 .02624 .01240 -.0000281

70.00 2.7661 .65772 .02183 .01521 -.0000418

80.00 2.9641 .61670 .01784 .01821 -.0000602

90.00 3. 1243 .57780 .01427 .02137 -.0000849

100.00 3.2509 .54109 .01 1 12 .02469 -.0001 192

1 10.00 3.3481 .50661 .00839 .02816 -.0001701

120.00 3.4199 .47436 .00604 .03180 -.0002547

130.00 3.4701 .44429 .00405 .03566 -.0004309

133.47 3.4830 .43436 .00342 .0371

0

-.0005514

328.06 3.4830 .17672 .00760 .11119 .001 1287

330.00 3.4985 .17646 .00840 .1 1304 .0010246

340.00 3.6053 . 17650 .01315 .12277 .0007067

350.00 3.7658 .17909 .01918 .13303 .0005459

360.00 3.9940 .18466 .02671 . 14398 .0004450

370.00 4.3058 .19370 .03595 .15571 .0003732

380.00 4.7195 .20672 .04712 . 16829 .0003176

390.00 5.2554 .22429 .06045 . 1 8 1 74 .0002717

400.00 5.9365 .24703 .07618 .19612 .0002320

410.00 6.7880 .27557 .09457 .21 146 .0001964

420.00 7.8377 .31061 .1 1588 .22778 .0001636

430.00 9.1 162 .35287 .14039 .24513 .0001326

440.00 10.6571 .40314 .16839 .26353 .0001028

450.00 12.4967 .46223 .20019 .28301 .0000737

460.00 14.6746 .53098 .23612 .30362 .0000451

470.00 17.2339 .61032 .27651 .32537 .0000167

480.00 20.2209 .70118 .32172 .34830 -.00001 16 490.00 23.6855 .80456 .3721

1

.37245 -.0000402

500.00 27.6816 .92150 .42807 .39784 -.0000690

510.00 32.2668 1.05307 .49000 .42452 -.0000983

520.00 37.5029 1.20042 .55832 .45251 -.0001280

530.00 43.4558 1.36472 .63343 .48185 -.0001583

540.00 50.1957 1.54720 .71579 .51258 -.0001892

550.00 57.7972 1.7491

1

.80582 .54473 -.0002210

560.00 66.3391 1.97176 .90396 .57835 -.0002536

126
Table 18. (Continued).

Norma I Butane

Dens i ty Pressure z kg/m3 MPa

10.00 .5741 .94390

20.00 1 .0869 .89557

30.00 1 .5419 .64507

40.00 1.9420 .79827

50.00 2.2902 .75312

60.00 2.5896 .70967

70.00 2.8440 .66804

80.00 3.0573 .62837

90.00 3.2335 .59074

100.00 3.3768 .55523

1 10.00 3.4914 .52189

120.00 3.5812 .49069

130.00 3.6498 .46163

140.00 3.7009 .43465

150.00 3.7375 .40969

160.00 3.7625 .38665

170.00 3.7786 .36547

180.00 3.7881 .34603

190.00 3.7930 .32825

200.00 3.7952 .31201 210.00 3.7959 .29721

220.00 3.7960 .28371 230.00 3.7960 .27137

240.00 3.7960 .26007

250.00 . 3.7964 .24969

260.00 3.7979 .24018

270.00 3.8021 .23154

280.00 3.81 12 .22381 290.00 3.8287 .21708

300.00 3.8590 .21 151 310.00 3.9079 .20728

320.00 3.9827 .20464

330.00 4.0921 .20389

340.00 4.2466 .20537

350.00 4.4586 .20946

360.00 4.7422 .21660

370.00 5. 1138 .22726

380.00 5.5918 .24196

390.00 6.1966 .26125

400.00 6.9514 .28575

410.00 7.8816 .31608

420.00 9.0151 .35293

430.00 10.3827 .39702

440.00 12.0182 .4491

1

450.00 13.9579 .51001 460.00 16.2419 .58056

470.00 18.9130 .66166

480.00 22.0179 .75423

490.00 25.6068 .85927

500.00 29.7335 .97779

510.00 34.4560 1.1 1087

520.00 39.8362 1.25963

530.00 45.9401 1.42523

540.00 52.8381 1.60888

550.00 60.6051 1.81 182 560.00 69.3201 2.03535

Isotherm at 425. 160 K

1 sotherm 1 sochore 1 sochore

Der ivat 1 ve Der ivat ive Curvature

MPa.m3/kg MPa/K MPa/K2

.05429 .00152 -.0000004

.04833 .00324 -.0000018

.04271 .00517 -.0000048

.03736 .00733 -.0000094

.03233 .00970 -.0000161

.02763 .01226 -.0000250

.02331 .01501 -.0000365

.01940 .01792 . -.0000510

.01591 .02098 -.0000691

.01283 .02415 -.0000918

.01015 .02743 -.0001201

.00786 .03078 -.0001560

.00593 .03419 -.0002022

.00433 .03763 -.0002635

.00303 .04108 -.0003476

.00201 .04451 -.0004680

.00124 .04791 -.000651

1

.00069 .05123 -.0009514

.00033 .05445 -.0014992

.00012 .05752 -.0026725

.00003 .06036 -.0060057

.00000 .06285 -.0251804

.00000 .06455 .3759035

.00001 .06684 .01 13369

.00008 .06985 .0044633

.00025 .07348 .0025343

.00062 .07770 .0016947

.00127 .08253 .0012437

.00230 .08798 .0009687

.00385 .09408 .0007860

.00605 .10086 .0006567

.00905 .10835 .0005603

.01301 .1 1657 .0004855

.0181

1

.12556 .0004251

.02453 .13534 .0003748

.03248 .14595 .0003317

.04215 .15742 .0002937

.05378 . 16977 .0002593

.06758 .18303 .0002277

.08380 .19723 ,0001979

.10269 .21240 .0001695

.12452 .22857 .0001420

.14957 .24576 .0001 151 .17812 .26402 .0000886

.21050 .28336 .0000621

.24701 .30382 .0000357

.28800 .32543 .0000091

.3338: .34823 -.0000177

.38485 .37223 -.0000449

.44146 .39748 -.0000725

.50407 .42400 -.0001007

.57307 .45184 -.0001294

.64889 .48103 -.0001588

.73197 .51 161 -.0001890

.82274 .54360 -.0002199

.92165 .57704 -.0002518

127
Table 18.

Norma i Butane

Dens i ty Pressure Z kg/m3 MPa

10.00 .5814 .94521

20.00 1 . 1 025 .89623

30.00 1 . 5668 .84910

40.00 1 .9773 .80366

50.00 2.3369 .75984

60.00 2.6487 .71 769

70.00 2.9163 .67730

80.00 3. 1434 .63880

90.00 3.3342 .60229

100.00 3.4927 .56782

1 1 0.00 3.5228 . 53544

120.00 3. 7285 C A C 1 7 .5051

3

130.00 3.0 132 .4 /DO

/

140.00 3.8804 .45061

1 50.00 3.9331 .42628

160.00 3.9740 .40379

1 70.00 4.0056 .38307

180.00 4.0303 .36402

190.00 4.0500 .34654

200.00 4.0665 .33056

210.00 4.0813 .31 596

220.00 4.0956 .30266

230.00 4. 1 103 .29053

240.00 4. 1257 .27947

250.00 4. 1426 .26939

260.00 4. 1623 .26027

270.00 4. 1868 .25210

280.00 4.2189 .24496

290.00 4.2621 .23893

300.00 4.3212 .23417

310.00 4.4022 .23087

320.00 4.5126 .22926

330.00 4.6612 .22964

340.00 4.8588 .23233

350.00 5.1177 .23771

360.00 5.4523 .24622

370.00 5.8790 .25832

380.00 6.41 63 .27451

390.00 7.0850 .29534

400.00 7.9082 .32 142

4 1 0.00 8.91 15 .35336

420.00 10. 1229 .39184

430.00 1 1 . 5735 .43757

440.00 13.2970 .491 31 45U.UU 1 3.3301

460.00 17.7128 .62601 470.00 20.4882 .70869

480.00 23.7031 .80282

490.00 27.4078 .90935

500.00 31.6564 1.02931

510.00 36.5070 1.16375

520.00 42.0216 1.31378

530.00 48.2664 1.48055

540.00 55.3121 1.66525

550.00 63.2335 1.86912

(Conti nued)

.

Isotherm at 430 K

1 sotherm 1 sochore 1 sochore

Der i vat i ve Der i vat i ve Curvature

MPa •mJ/kg MPa/K MPa/K^

.05507 .00152 -.0000003

.04922 .00323 -.0000017

.04369 .00515 -.0000044

.03845 .00729 -.0000087

.03351 .00962 -.0000147

AOO A 1 .02891 A 1 O 1 C .01215 -. 0000226

.02467 .01 484 -.0000325

.02083 .01 769 A A AA X A C -.0000445

A 1 ~7 >1 A

.0 1 /4U .0206 / AAAA CO A -•0000589

A 1 >1 "Z ~7 AO "Z T C .02375 A AA A ~7 C^T -.0000755

.011/3 All m A A 1 .02591 AAAAAyl O -•0000948

AAA >1 it .00946 A Z A 1 Z .0301

3

AAA 1 1 £ 1 -•000 1 161 AA "7 1^/1 .00/54 .03330 AAA 1 "ZAO -•uoo 1 jyz

.00594 .03554 AAA 1 £ "Z A -.0001530

.00463 .03988 AA A 1 O C yl -.0001854

.00359 .04308 AAA O A "Z C -. 0002035

.00278 .04623 AAAO 1 "20 -.0002132

.00219 .04932 AAAO 1 A T -.0002103

.00178 .05238 A A A 1 A 1 ^ -.0001916

. 00 1 54 .05544 A AA 1 C "7 A -.0001 570

AA \ A A .00 144 A C O CO .05852 AAA 1 AO 1 -•0001 087

.00144 .061 69 AA AA C AA -.0000508

.00 1 50 .06499 .0000139

.001 60 .06847 .0000832

.00180 .072 16 AAA ^ C A A .000 1544 .00217 .0761

5

A A A O O O 1 .0002221

.00277 .08050 .0002802

.00369 .08531 .0003238

.00503 .09064 .0003508

.00690 .09658 .0003620

.00943 . 1 03 1

7

.0003605

.01279 . 1 1047 .0003498

.01712 . 1 1850 .0003331

.02260 . 12732 .0003128

.02942 . 13694 .0002905

.03778 .14739 .0002672

.04788 .15871 .0002435

.05994 . 17092 .0002198

.074 19 . 18405 .0001960

.09087 .19812 .0001 723

. 1 1024 .21317 A A A 1 A Q C .0001485

.13257 .2292

1

AA A 1 O jl A .0001248

. 1581

2

.24629 AAA 1 AAA .0001 009

.18719 .26442 A AAAT£ O .0000768

.2201

0

.28364 A AAA CO A .0000524

ml.0 1 lb "Z A "^OQ .3U3yo AAAAo-7-7 .29871 .32546 .0000026

.34511 .34813 -.0000229

.39673 .37200 -.0000490

.45396 .39712 -.0000756

, .51719 .42351 -.0001028

.58683 .45121 -.0001307

.66331 .48026 -.0001593

.74707 .51069 -.0001887

.83854 .54253 -.0002190

128
Table 18. ( Cont i nued )

.

Normal Butane Isotherm at 440 K

1 sotherm 1 sochore 1 sochore

r\ y-\ r\ i Uwii b 1 1 y Pressure L Der i vat i ve Der i vat i ve Curvature

kg/tTi3 rlr a MPa .rfi3/kg MPa/K fMPa/K^

Z'J •uu OA \ A^ .yU 145 ,05 1 02 .00321 -,0000015

A n nn 4U» UU O A/1 QQ O 1 .1 1 o •o 1 4 1 y .04067 ,00721 -,0000075

O "7£: A 1 z. /oy

1

.73326 .03148 .01 194 -,0000187

on An J . 3 1 0.5 .6530

1

.02369 .01 730 -,0000351

1 nn nn Z T OC O 3 . / ZOO .5921

1

.01742 ,02310 -,0000554

I zU.UU 4 . 0248 .53288 .01 262 ,02919 -,0000769

1 ^ r\ rvA

1 4U»U(J 4.2401 .481 19 ,00912 ,03542 -,0000943

1 f^n nn A "ZA TA 4. jy /U .43662 ,00674 ,04 168 -,0001009

ion nn A 1 CA 4.5 loU .39861 ,00532 .04800 -,0000908

OAA AA 4.61 54 .36665 ,00475 ,05449 -.0000628

oon nn A "7 1 AO 4 . / 1 08 ,34021 ,00488 ,06139 -,0000207

240.00 4.8132 .31863 .00542 ,06895 ,0000307 A AA 4 . 93 1

5

.30135 .00656 ,07748 ,0000870

5.0836 ,26346 ,00891 ,08736 ,0001399

A AA jUU.OU 5.3009 ,28073 .01321 ,09907 ,0001797 TOO AA 5.o3 1!) .27960 .02043 , 1 1 308 .0002001

340.00 6.1453 .28717 ,03175 .12981 .0002014

7/r A AA JOU . UU C A*Z O A 6.9380 .30620 ,04857 . 14963 .0001876

380.00 8.1355 .34015 .07250 .17281 ,0001633

400.00 9.8973 .39312 ,10532 . 19963 .0001 320

420.00 12.4208 .46986 .14901 .23031 .0000959

>1 1 A AA 44U . UU 1 5 .y44

/

.57575 ,20575 .26508 .0000561

A ^A AA '^ou.uu ZUt 1051 .7 1681 ,27794 .30418 .0000132

/lOA AA ^ou • UU Q A A~7 .syy /6 ,36825 .34785 -.0000326 KAA AA 3UU.UU 1 1 "2 1 AO 1 . 1 3 198 ,47958 .39633 -,0000813

KOA AA J^\J • UU A A RO 7 1 1 >10 1 c:q

1 ,4z 1 5o ,61 506 .44990 -,0001331

A AA f^A Du.4uyo ^ AQA 1 "7~7"7'20

1 , / / /3o ,77805 .50881 -,0001882

Norma 1 [Butane 1 sotherm at 450 K

A C O O 1 ,U5zol .00320 -.0000014

dn . nnUU Z.9 1 9 1 IZ 1 1} QO "2 ,oz jy

J

,04284 ,0071

4

-.0000065

ftn OU. nnUU Z.OC) /O » I'i loo ,03398 ,01 177 -,0000158

RnOU . nnUU _>.4oyo »o 1 / 1)3 .02645 ,01698 -.0000287

1 AA AA 1 uu.uu IZ ^ A A c ,Ol445 ,02036 ,02261 -.0000435

1 OA AA 1 Z U . UU 4. J 1 J

J

,55839 .01 566 .02853 -.0000574

1 >1 A AA 1 'JU.UU >l C: AA 1

' ,50934 .01222 .03463 -.0000670

1 f^A AA 1 DU .UU A O AA A 4.0094 ,46696 .00988 ,04086 -.0000685

1 Q A AA 1 ou.uu A A AO 1 4.yyzi ,43084 .00855 ,04727 -.0000599

OAA AA /UU.UU 5. 15/6 ,40062 ,00816 ,05399 -.0000412

OOA AA ZZU. UU 5.3238 ,37593 ,00857 ,06122 -.0000145

O ^ A AA 5.5040 ,35627 ,00953 ,06919 .0000180 OC A A A /:o0.00 5.7100 ,341 17 ,01 125 ,07816 .0000539

^80 . 00 5.9633 .33085 ,01437 ,08847 .0000892

300.00 6.2994 .32620 ,01967 .10052 .0001 188 320.00 6.771

1

.32871 ,0281

1

.11473 .0001382

XAr\ AA u.uu ~I A ROA 1 .4DZ4 "Z /I A C 1 ,34051 .04085 . 1 3 1 52 .0001454

360.00 8,4428 .36433 .05926 .15125 .0001406

380.00 9.8711 .40354 ,08492 . 17425 .0001256

400.00 1 1.8997 .46215 .1 1960 .20080 .0001026

420.00 14.7283 .54477 ,16527 .23115 .0000734

440.00 18.5980 .65663 .22410 .26555 .0000393

460.00 23.7959 .80363 .29851 .30425 .0000010

480.00 30.6598 ,99229 .391 15 .34748 -.0000409

500.00 39.5829 1 ,22984 .50494 .39549 -.0000863

520.00 51 .0194 1.52420 .64303 .44855 -.0001351

540.00 65.4883 1,88399 ,80875 ,50693 -.0001876

129
Table 18. (Continued).

Normal Butane Isotherm at 500 K

i sotherm 1 sochore 1 sochore

Dens i ty Pressure Z Derivative Der i vat i ve Curvature

kg/ni3 MPa MPa.m3/kg MPa/K MPa/K^

20.00 1 .3253 .92648 .06157 .00315 -.0000008

40.00 2.4716 .86392 .05323 .00689 -.0000036

60.00 3.4603 .80634 .04580 .01 120 -.0000082

80.00 4.3107 ,75338 .03943 .01599 -.0000138

100.00 5.0452 .70539 .03422 .021 18 -.0000194

120.00 5.6878 .66269 .03023 .02671 -.0000239

140.00 6.2624 .62541 .02743 .03258 -.0000264

160.00 6.7931 .59360 .02583 .0388

1

-.0000261

180.00 7.3040 .56734 .02548 .04549 -.0000230

200.00 7.8210 .54675 .02645 .05273 -.00001 72

220.00 8.3704 .53195 .02869 .06069 -.0000091

240.00 8.9754 .52287 .03199 .05954 .0000007

260.00 9.6594 .51943 .03669 .07949 .00001 15 280.00 10.4575 .52218 .04355 .09078 .0000224

300.00 11.4216 .53230 .05344 .10370 .0000323

320.00 12.6222 .55149 .06738 .11854 .0000397

340.00 14.1514 .58193 .08651 .13564 .0000435

360.00 16.1263 .62630 .11219 .15531 .0000428

380.00 18.6924 .68775 ,14590 .17789 .0000369

400.00 22.0272 .76993 .18936 .20368 .0000256

420.00 26.3446 .87699 .24449 .23298 .0000092

440.00 31 .8990 1 .01362 .31344 .26606 -.0000121

460.00 38.9903 1.18509 .39861 .30320 -.0000380

480.00 47.9691 1.39724 .50265 .34467 -.0000683

500.00 59.2416 1.65656 .62849 .39072 -.0001027

Normal 1Butane Isotherm at 550 K

20.00 1 .4817 .94166 .07009 .0031

1

-.0000005

40.00 2.8124 .89368 .06312 .00675 -.0000023

60.00 4.0117 .84983 .05693 .01088 -.0000050

80.00 5.0956 .80959 .05162 .01545 -.0000083

100.00 6.0837 .77327 ,04738 .02043 -.00001 15 120.00 6.9985 .74128 ,04430 .02580 -.0000140

140.00 7.8641 .71397 ,04247 .03157 -.0000155

160.00 8 . 7064 .69 1 64 .04200 .03781 -.00001 57 180.00 9.5541 .67465 .04303 .04458 -.0000146

200.00 10.4386 .66340 .04571 .05202 -.0000122

220.00 1 1 .3935 ,65826 .05005 .06024 -.0000088

240.00 12.4505 .65938 .05590 .06942 -.0000047

260.00 1 3.6422 .66692 .06367 .07973 -.000000'' 280.00 JL~\J\J 9 \J\J 15.01 54 .68161 .07419 ,09138 .0000042

300.00 16.6345 .70477 .08842 . 10462 .0000079

320.00 18.5839 .73815 .10742 .1 1969 .0000103

340.00 20.9709 .78397 .13238 .13687 .0000105

360.00 23.9279 .84481 .16465 .15647 .0000081

380.00 27.6158 .92370 .20574 .17876 .0000025

400.00 32.2273 1.02405 .25731 .20406 -.0000067

420.00 37.9908 1.14971 .32128 .23263 -.0000197

440.00 45.1750 1.30498 .39975 .26478 -.0000364

460.00 54.0936 1.49467 ' .49513 .30077 -.0000571

480.00 65.1105 1.72412 .61006 .34088 -.0000815

130
Table 18. (Continued),

Normal Butane Isotherm at 600 K

1 sotherm 1 sochore 1 sochore

Density Pressure Z Der 1 vat i ve Der i va t i ve Curvature

kg/tn-> MPa MPa •nrP/kg MPa/K MPa/K^

20.00 1 .6368 ,95353 .07847 ,00309 -.0000004

40.00 3. 1474 .91677 .07272 ,00665 -.0000016

60.00 4.5501 .88356 .06766 .01067 -.0000034

80.00 5.8591 .85332 .06340 .0151

1

-.0000055

100.00 7.0927 .82639 ,0601

5

.0 1996 -.0000077

120.00 8.2731 .80326 ,0581

0

.02522 -.0000095

140.00 9.4258 .78444 ,05740 .03093 -.0000107

160.00 10. 5795 .77040 ,05824 .037 1

5

-.00001 12 180.00 1 1 .7669 .76165 .06082 .04395 -.00001 10 200.00 13.0252 .75880 ,06535 .05145 -.00001 02 220.00 14.3945 .76234 .07191 .05980 -.0000089

240.00 15.9143 .77259 ,08039 .0691 1 -.00000 72 260.00 17.6259 .78985 ,09124 .07957 -.0000055

280.00 19. 5858 .81499 ,10538 .09136 -.0000041

300.00 21.8697 .84936 ,12381 .10470 -.0000032

320.00 24.5744 .89475 ,14755 .11982 -.0000034

340.00 27.8202 .95335 ,17814 .13697 -.0000050

360 . 00 31 .7535 1 .OZ /DO ,Z 1553 1 CiC A 1 . 1 554

1

AAAA AO C 380.00 36.5489 1 . 1 2063 ,26455 . 1 /84z AA A A ^ A A -.00001 44 400.00 42.4138 1 .23543 ,32387 .20327 AAA AOO

A

-. 0000229

4y.5yuo 1 .3 /5oy ,39010 0"Z 1 OA - nAAAT/l "Z .UUOUjA J 440.00 58.3624 1 . >4 344 .4837

1

.z5/:5 1 -.000048 / 460.00 59.0562 1 .74910 CO O O 1 .58881 .zy /55 -.0000553

Norma 1 Butane 1 soTnerm ax 650 K

20.00 1 .7909 .96307 .08674 .00307 A AA A A A "I -.0000003

40.00 3.4784 .93524 .082 1

2

.00559 /^ A/\ AA 1 1 -. 000001

1

60.00 5.0798 .91055 .07813 .01053 -.0000025

80.00 6.6084 .88842 ,07489 .01487 -.0000040

100.00 8.0821 .86923 ,07257 .01953 -.0000055

120.00 9,5236 .85355 ,071 71 .02482 -.0000070

140.00 10.9604 .84199 ,07223 .03047 -.0000081

160.00 12.4241 .83513 ,07446 .03656 -.0000087

180.00 13.9519 .83362 ,07868 .04345 -.0000091

200.00 15.5862 .83814 ,08515 .05099 -.000009

1

220.00 17.3735 .84933 ,09398 .05936 -.0000089

240.00 19.3603 .85758 ,10510 .06871 -.0000086

260.00 21.5961 .89333 ,1 1903 .07922 -.0000084

280.00 24, 1467 .92749 .13674 .09104 -.0000084

300.00 27,0980 .97145 , 1 5928 .10438 -.0000091

320.00 30.5577 1 .02702 ,18780 .11945 -.0000106

340.00 34.6584 1.09632 ,22359 .13649 -.0000133

360.00 39,5589 1 .18182 ,26803 .15574 -.0000174

380.00 45.4475 1.28528 ,32266 .17745 -.0000234

400.00 52.5446 1.41278 ,38918 .20189 -.0000315

420.00 6 1 . 1 064 1.55475 .46947 .22932 -.0000419

440.00 71 ,4292 1,74595 .56555 .25001 -.0000548

131
Table 18. (Continued).

Normal Butane Isotherm at 700 K

1 sotherm 1 sochore 1 sochore

Density Pressure Z Der i vat 1 ve Der i vat i ve Curvature

kg/m3 MPa MPa •m3/kg MPa/K MPa/K2

20.00 1.9444 .97089 .09495 .00306 -.0000002

40.00 3.8064 .95035 .09138 .00654 -.0000009

60.00 5.6032 .93264 .08840 .01042 -.0000019

80.00 7.3475 .91723 .08618 .01470 -.0000031

100.00 9.0573 .90453 .08500 .01939 -.0000043

120.00 10.7565 .89518 .08516 .02451 -.0000055

140.00 12.4746 .88986 .08694 .03011 -.0000065

160.00 14.2467 .88924 .09062 .03626 -.0000073

180.00 16.1141 .89404 .09652 .04304 -.0000079

200.00 18.1245 .90502 .10496 .05055 -.0000083

220.00 20.3304 .92288 . 1 1608 .05892 -.0000087

240.00 22.7850 .94812 .12985 .06827 -.0000092

260.00 25.5458 .98123 .14684 .07876 -.0000098

280.00 28.6870 1.02318 .16807 .09055 -.0000108

300.00 32.3040 1.07537 .19462 .10384 -.0000123

320.00 36.5153 1.13959 .22770 .1 1882 -.0000145

340.00 41.4642 1.21792 .26862 .13570 -.0000178

360.00 47.3217 1.31275 .31880 .15473 -.0000223

380.00 54.2884 1.42675 .37981 .17615 -.0000282

400.00 . 62.5974 1.56286 .45334 .20019 -.0000360

132
Table 19. The Joule-Thomson Inversion locus for normal butane.

Temp. Den si ty Pressure

K kg/m3 MPa

350 51 1.2 2.707

360 505.9 5.584

370 500.6 7.91 1 380 495.4 10.297

390 490.2 12.551 400 485.0 14.680

410 479.9 16.693

420 474.7 18.595

430 469.7 20.394

440 464.7 22.095

450 459.7 23.703

460 454.8 25.224

470 449.9 26.661

480 445.0 28.020

490 440.2 29.304

500 435.5 30.517

510 430.8 31.662

520 426.

1

32.743

530 421.5 33.762

540 416.9 34.723

550 412.3 35.627

560 407.8 36.477

570 403.4 37.275

580 398.9 38.025

590 394.5 38.726

600 390.2 39.381

610 385.8 39.991

620 381 .5 40.560

630 377.3 41 .087 640 373.0 41 .575

650 368.8 42.024

660 364.6 42.436

670 360.5 42.812

680 356.4 43.154

690 352.3 43.462

700 348.2 43.738

710 344.1 43.981

720 340.1 44.196

730 336.1 44.380

740 332.1 44.537

750 328.1 44.666

760 324.1 44.768

770 320.2 44.845

780 316.3 44.898

790 312.4 44.927

800 308.5 44.934

810 304.6 44.919

820 300.8 44.884

830 297.0 44.828

840 293.2 44.754

850 289.4 44.662

860 285.6 44.553

133
Tab 1 e 20. Thermophys i ca 1 properties of saturated 1 iquid normalI butane.

1 sochore 1 sotherm

Temp. Pil , y dPa/dT dPJt/dT Der i vat i ve Der i vat i ve

K MPa kg/fTP kg/m3 kg/(nfi3.K) MPa/l< MPa.m3/kg

1

1 JH"^4• Rfin oou fi7'^SftF-nft . D / -J JO C UO 7^5 77 .34916E-04 .00000 1 .00000 . 1282E--06 - 044 1 9z 1 1 n 1 . 1 1 u 1 99'^RF-»/1

1

1 hU«UUU .

1

1 77/z 11 nF-nR uc—uj? 1 S)\J»H^ .85937E-04 .00000 .99999 .3012E--06 — Q4 94 9Z .UjZ9 n"^9R 9 1 R7P4.n 1 . Z 1 -) / c +U 1

1 4 D . uuu . Jyy zQQ 11 7P_nR / ll~UI? 77/ Z -JR . 77/ Z . 1924 5E-03 .00000 .99998 .6456E--06 —— . 04y4 1

1 nu 1 » 70 J J . ZU04 t+U

1

1 Rn nnn pcQ/i zp_nR . ouy^ jti^u J 77 1 n 1 / Z 1 . U 1 .40521E-03 .00000 .99997 .1303E.-05 —~ Q4n 1 . y4u

1

1

1 .oyzz RQ99 9n 1 XP-t-H 1 •ZU 1 jL+U

1

1\DDR s nfin

•

uuu 1 7SQ7P-n4 7/

1

1 D . J?^l1 .80723E-03 .00000 .99994 .2490E--05 . yjy J 1 R9fifl 1 . OZDO 1 044 F-l-n 1 . 1 y44 PtU 1

1 Du« uuu • D DU \ Z C UH 71/I 1 fi7 1 . oz . 15299E-02 .00000 .99990 .4532E--05 ~

.

yJy^ 1 7fi49 1

.

1 D4Z . 1 0 /O t+U

1

i o J • nnn uuu . fiR4 OJH 1I 1

1 P-n4 i_ US- 7nfi / UD •yc. Q7 .27718E-02 .00000 .99983 .7895E--05 . yJyO 1 . 1 U4Z .1014 1 ft 1 4 F+nU 1

1

1

1 7n/ u • nnn uuu .

1

1 1

1 77/ zl 11 F-n'^ C. U_J 107 / uz • 77z z .4821 1E~02 .00001 .99973 .1321E--04 — . Q4n"^ y^\jD 1 fsAfn 1 7 R 1 F+n

1

. 1 / -J 1 PTU !

1

1 / J • nnn uuu 7n77nF—n'^

. ZU.£ZUtl~U_J 0^CQ7/ . R9JZ ,80807E-02 .00001 .99958 .2133E--04 - . Q4yH 1

1 4H 11 SO 1 4

.

Jy 1

4

1 con F+n

1

iftn 1 o u • nnn uuu ^"^fiQ7F—n'^ fiQ7z ft 1 . 0 1 .13095E-01 .00002 .99937 .3332E--04 — 04 "^n 1

1 R"^R9 . 9 JoZ 1 fi^ 1 P+n

1

. I od I iiT^u 1 iss 1 o J • nnn uuu R44 1 1 P-n'^ fiftft DOO . noU^ .20580E-01 .00003 .99907 .5053E.-04 — 04 sn 1

1 .404ft7n/

U

1 R 74 p+n 1 . 1 -) /4 t+U I ion 1 yu» nnn uuu .0R'=i'^R7<^-n"^ J_5Z^ / u~U^ COT 00 ^ • J D .31447E-01 .00005 .99868 .7454E--04 — . 04y^ 741 *+ 1 4 "^77 1 R 1 7P+n 1 iQ'i nnn . i"'in4nF-n7 UUHUC u/. fi7ft D / 0 fil . U 1 .46834E-01 .00007 .99816 .1073E--03 1 ^onn 1 4fi9F+n

1

. 1 4uZ PT^J I 7nn ^uu« nnn uuu 1 Q447F-n7 fi7'^ ft 5 .68126E-01 .00010 .99751 .1508E--03 — OS'^ft • y JDO 1 "^44

1

1 .-)44 1 1 4nor+n

1

. 1 4 U 7 Lt^U 1 ?ns nnn 7R^4 SF-n7 fifiQy %\j071 . 96980 E-01 .00014 .99669 .2077E--03 - . 0S7ft y y 1 0 1 90Qfi 1 R7F+n 1 ^in ^ i u • nnn uuu 4n47QF-n7 fs«CL 77 .13534E+00 .00020 .99568 .2806E--03 . y uZ-j 1 . Z -JuD 1 '^nfiP+n 1 . 1 -?UOP~U 1 o 1 z 1 ^

c; • nnn uuu Rfi7 1 fiP-n7 fiSQ 4R . 18544 E+00 .00028 .99447 .3723E.-03 . yO 1

D

1

1 • 9c.

1

\ 40^y . i C -JO CTU t 99n i.L.\)% nnn uuu . 7ftn7fiF-n7 / ou / oc—uz (=iR4 U-JH .DUfin .24984E+00 .00038 .99302 .4860E--03 _ • 0790 y 1 i-y 1

1 .

1

1 74fi /4D 1 9n7P+n

1

. 1 ZU / P ' u

1

£-£-j* nnn uuu 1 ns74 t'-ni fi4Q 77 .331 39E+00 .00051 .99133 .6249E'-03 - *yty 070 1

1 11 1 '^R4 . 1 -? J4 1 1 RQF+n

1

9'';n ^-D\J9 nnn uuu 1 4 1 n4F-n

1

. 1 *t 1 UH C U 1 fi44 OH '4 ftn . 0 U .43328E+00 .00066 .98937 .7923E--03 - Qftfin 1

1 . n074 \jy 1 4 1 1 1 9P+n

1

. f 1 1 Z P ' U 1 nnn fi'^Q \j-jy ftfi . ou . 55901 E+00 .00086 .98712 .9916E--03 . J '-J-r 1

i . 0fin4 UUUH lOfifiF+n 1 . 1 uuu t_ rU 1 740 nnn 74n7QF-ni ^^4 R7 .71237E+00 .001 10 .98456 .1226E'-02 _ 11 . nnuu 161 u 1 0745 in97F+n

1

74 '3. nnn .. ^nR77F-ni -'WU III— \J 1 629.84 .89748E+00 .00140 .98168 . 1500E--02 -11 . nin4 u 1 UM . 9896 7U ^u .977QF+nn % y 1 1

y

UTuu

9150.000 ^ --"J • \J\J\J • ^y"SQ147F-ni I ^ 1 1- \j 1 624.76 .1 1 188E+01 .00175 .97845 .1815E--02 -11 . n9ni UZ.U 1 • y J -Ju .QXROF+nn . ^_/-JUL_T^UU 755. nnn .4QinfiF-ni 6 1 9 . 64 . 13809E+01 .0021

7

.97486 .2176E'-02 -1 .0304 .9225 .893 1 E+nn

7fin nnn . u\j yu y L. V 1 ftU 1

1 4M . 4fi *+ u . 16890E+01 .00267 .97089 .2586E--02 -11 .04 . UM 17I / .89n9 .8 59 1 F+nn

7fi5 nnn 75n47F-ni fiOQ uu y % 77 .20483E+01 .00325 .96651 .3046E--02 -1 .0538 .8 587 .81 7nF+nn

i- 1 \) m nnn UUU Q 1 R4'^F-n 1 f\C\'\ OU_J •yQ7L. .24646E+01 .00392 .96170 .3562E--02 -11 . nfifio uuu R77Q1 y 9 / f 6- / \—l\J\J 272.638 .mi '^'SF+nn fiO uu 11 . 09u? .27092 E+01 .00432 .95898 .3856E--02 -1 .0741 .8 1 20 .7574F+nn

7Rn nnn 1 "S7QRF+nn 'SQ'S 1 1 .34923E+01 .00560 .95069 .4765E--02 - 11 .OQfil . U 7 u 1 .7686 .6969F+nO

7ft £~0 Js . nnn UUU .1

1 -JO RRR-J 11 F+nn c~uu -JO 'Tft7/ . SQJy .41 169E+01 .00662 .94443 .5459E--02 - 1 1 1 74 % 1 Dyy . fiftn3h+nn UUU_J l~'\J u 7Qn ^ -7U. nnn UUU 1 ft7fi7F+nn -JO Sft 1

1 . Qft 70 .48249E+01 .00777 .93764 .6216E--02 -1I . 1709 \ ^.y y 7 1 IQ .fi745F+nn • uz. t -J _ ' u u

7Q'i nnn 77n7ftF+nn JS7fi 1 \j % 7Qi.y .56240E+01 .00908 .93028 .7039E--02 -11 . 14RR 1 MU u .6844 .5896 . -JU 7 U F+nn I- " uu

^nn nnn 7SR 1 7 F+nn S7n 4Q .65226E+01 .01055 .92233 .7929E--02 -11 . IfiQ"^ 1 u yD . U -J / -J . RRRfiP+On

ju"inRJ . nnn uuu . _?uu ^nn 1

1 QF+nn i?c~uu Sfi4 -JUH . -J^ RQ .75297E+01 .01219 .91377 .8888E--02 - 1t . 101^ \ y \ D . PC^ U-J 11 9^- . -JZ.ZH R774F+nn C~UU

_)^int u . nnn uuu "214 71 7P+nn RRQ c;7

-J JO . -J / ,86549E+01 .01402 .90457 .9918E--02 - 1 7 1 R

1

1 . z 1 J 1 .OU-J4 . 4QnnF+nn 4yUUCl ' uu

nnn ^QQ4QF+nn -J-JZ SS7 . 44H*t .99090 E+01 .01605 .89471 . 1 102E--01 -1 74nQ sftnn 4RDf;p+nn

j^u ?9n • nnn uuu 4 R74QP+nn R4fi 1 fi .1 1303E+02 .01830 .88418 .1219E--01 —1 7fiftft 1 . ZDOO R R R9 . 4770F+nn 4 Z / y P • uu ^7sJ . nnn uu u . R7J/L 1

P JJC ssF+nn rVU JDy • iH . 12851E+02 .02078 .87297 . 1344E--01 _1 900^^ 1 . £.yyD s'^nft • JD\)0 %DyOL. "^Qft7 F+nn CI "UU

j-)u. ^^n nnn uuu . J^/lUHl_.~UU 'SQ7n4F4-nn -J_J_? R'^'^ .

1

1 7J .14565E+02 .02352 .86107 .1477E--01 -1 "';'^9R 1 . JJ JJZ -J snfift . JUUO "^fiQ'';F+nn . DO yD c^KjyJ

-J^^1J J . nnn uuu fifiq''.4F+nn . UVJ^_>H CTUU R7fi 4 1 -JZ D . H 1 . 16462E+02 .02653 .84846 . 1617E--01 -1 '^ftftft . 4R'^9 40-JZ ^4 1 7 F+nn

_?HU. ^4n nnn uuu . 7/ -'JO^C.T^UU R'^R4F+nn SI Q 47 .18560E+02 .02984 .83513 .1765E--01 -1 4nR7 .4uUU 4finn 9DT 1t 4nF+nn 4UPTTJU

"^4R . nnn uuu . RAROsP+nn 0^ Jy R 1 7 "^7

-J 1 Z . -)Z .2G876E+02 .03346 .82107 . 1920E--01 —1~ I . 4R9R 4 JZO 4'^79 . 4J / Z • ZO7ft 7/ 7/ F+nn Pt^UU J)^U.UUU TKn nnn .y4DU QAf,n 1

I p+nn t+uu cn4 Q"^ .23436E+02 .03742 .80625 .2084E--01 _ 1 en 1 ft .414/ 4 147 . 9fi9'^F+nn ZDZ JP T^UU

j_) J . nnn uuu 1 nRA RF+n

1

407 4y / . 9Qzv . 26264 E+02 .04176 .79065 .2257E--01 — 1.7 jO J ?09fi . jyzo . 9'^7

ZJ> / 7F+nn / P+UU

_3Du Tcn • nnn uuu 1171 RP+n

1

.11/1 OCtU I 4R0 'toy "^fi . ju .29391 E+02 .04650 .77422 .2438E--01 — 1 1 fin 1 . 0 1 ou ._>^7n7 (U / . 9Z

1144 1

1 FP +|V) • uu

_jDi? ^ftR . nnn uuu 1 9QR4P+n

1

4R40 1

t .

1

1 n

U

.32855E+02 .05169 .75690 .2628E--01 —1— fift7R 1 .00 /u "^40 1 . D^y \ .

1

1 0y 11 jjpTuu F+nn

_>T7n/ u . nnn uu U 1 4X4R P+n

1

. 1 HJ>HO C^U 1 477 4fi .36701 E+02 .05738 .73862 .2828E--01 -1 IfyHl ^97ft . JZ / 0 . ifi04P+nn lDy4P'UU

-J"'i?/ Js m nnn UUU 1 RR 1 4F+n

1

. 1 -JO 1 HCTU 1 40J3T

. 4n4U .40985E+02 .06362 .71928 .3038E--01 —1 ftfinfi 1 .OUUU . JjUO ^nft7I •

1

1 4ft 40 Js F+nn PTUU

_/ou ^ftn • nnn uuu 1 7'^R7F+n 1 . 1 1 DO 1 [1 T^U 1 4H J

R'^ ft''; J? . 0 jj .45778E+02 .07048 .69873 .3259E--01 _11 QfiOR

.

yOyO • 9RR7 L.O J 1 .

1

1 9ft ^0 -JR F+nn £- » uu

_?o "^RR . nnn uu u . iQn7sp+ni 1 yU 1 J uT^u 1 44 C7 .51 175E+02 .07807 .67680 .3493E--01 —9~Z . innR lUUo 9fi40 . ZD4y .

1

t no\JyJR F+nn PT^UU

-)y \Qr\u. nnn uuu 9nQR"^P4.n 1 /4 X9 77 3Z • /

/

.57302E+02 .08649 .65325 .374 IE--01 -Z.ZD 1

7

9y1 A 1 .Z44 1 014 1 F_n

1

. y 1 4 1 p—u 1 Dyj TQc;

. nnn uuu 79R 1 QF-4-n 1 . ZZo 1 7 t+U

1

-1hzu9n OP . yo .64336E+02 .09593 .62772 .4006E--01 9 A R —Z . 404

J

99*^4 . ZZ J4 74 ^R F—n

1

. /4 Jo p—u 1 4nn Huu. nnn uuu 94RQ9F+n

1

4nft 4UO .uzn9 .72539E+02 .10662 .59973 .4290E--01 _9 7'^14 —Z . / J 1 4 .ZUZ9 9n9R RR4'^F-n 1 . 904JP—U

1

405. onn . 77 1 1 "^F+m -jy J 9 ^y .82323E+02 . 1 1 894 .56850 .4599E--01 -"^D . in9fi 1 Ui-U 1ft 1 3 .43fi7F-ni

410.000 .29496E+01 376.69 .94398E+02 .13351 .53278 .4939E--01 -3.6648 .1596 .3006E-01

415.000 .32060E+01 356. 17 . 11019E+03 .15163 .49012 .5323E--01 -4.6508 . 1367 .1794 E-01 420.000 .34830E+01 328.06 .13347E+03 .17672 .43436 .5774E--01 -7.0294 .1112 .7604E-02

425.160 . 37960 E+01 227.85 .22785E+03 .27394 .27394 .6427E--01 .0643 0.

134
Table 20. ( Cont i iiue'l) Heat of Temp. Vap.

K J /mo I 134.860 28789.2

140.000 28520.6

145.000 28265.6

150.000 28016.2

155.000 27772.2

160.000 27532.9

165.000 27298.0

170.000 27067.1

nS.OOO 26839.7

180.000 26615.3

185.000 26393.4

190.000 26173.7

195.000 25955.7

200.000 25738.9

205.000 25522.8

210.000 25307.0

215.000 25091.1

220.000 24874.5

225.000 24656.8

230.000 24437.6

235.000 24216.2

240.000 23992.3

245.000 23765.3

250.000 23534.8

255.000 23300.2

260.000 23061.1

265.000 22816.8

270.000 22566.9

272.638 22432.6

280.000 22047.9

285.000 21777.7

290.000 21499.5

295.000 21212.8

300.000 20916.9

305.000 20611.0

310.000 20294.4

315.000 19966.5

320.000 19626.4

325.000 19273.1

330.000 18905.8

335.000 18523.4

340.000 18124.8

345.000 17708.7

350.000 17273.6

355.000 16817.9

360.000 16339.6

365.000 15836.5

370.000 15305.8

375.000 14744.1

380.000 14147.3

385.000 13509.7

390.000 12824.0

395.000 12079.8

400.000 11262.1

405.000 10346.6

410.000 9291.7

415.000 8012.0

420.000 6273.2

425.160 0.0

Internal

Energy Enthalpy

J /mo I J /mo I .0 .0 602.8 602.8

1187.8 1187.8

1771.6 1771.6

2354.7 2354.7

2937.3 2937.3

3519.8 3519.8

4102.5 4102.5

4686.0 4686.0

5270.5 5270.5

5856.5 5856.5

6444.4 6444,5

7034.6 7034.8

7627.6 7627.7

8223.6 8223.9

8823.1 8823.4

9426.5 9427.0

10033.9 10034.6

10646.0 10646.9

11262.7 11264.0

11884.7 11886.4

12512.1 12514.3

13145.3 13148.1

13784.4 13788.0

14429.8 14434.4

15081.7 15087.5

15740.5 15747.6

16406.1 16415.0

16760.3 16770.1

17759.4 17772.4

18447.2 18462.9

19142.8 19161.5

19846.3 19868.5

20557.9 20584.2

21277.7 21308.6

22005.9 22042.0

22742.6 22784.6

23488.1 23536.8

24242.7 24298.8

25006.4 25070.9

25779.6 25853.6

26562.7 26647.1

27356.0 27452.0

28159.9 28268.8

28975.0 29098.2

29801.5 29940.7

30640.3 30797.2

31491.9 31668.4

32357.3 32555.6

33237.3 33460.0

34133.4 34383.3

35047.2 35327.6

35981.2 36296.3

36939.3 37293.9

37927.9 38328.4

38959.2 39414.3

40060.4 40583.6

41315.5 41932.6

44431.5 45399.9

Entropy Cy

J/(mol.K) J/(mol.|

133.544 88.51

137.932 87.86

142.036 87.29

145.992 86.78

149.812 86.34

153.507 85.99

157.089 85.71

160.565 85.51

163.945 85.40

167.237 85.37

170.447 85.42

173.582 85.56

176.549 85.77

179.652 86.05

182.596 86.41

185.486 86.84

188.326 87.33

191.120 87.88

193.872 88.48

196.584 89.13

199.260 89.84

201.902 90.58

204.513 91.37

207.096 92.19

209.652 93.05

212.183 93.93

214.692 94.85

217.180 95.78

218.485 96.29

222.098 97.73

224.532 98.73

226.950 99.75

229.353 100.78

231.744 101.83

234.122 102.89

236.490 103.95

238.847 105.04

241.196 106.13

243.536 107.22

245.870 108.31

248.198 109.40

250.521 110.48

252.842 111.55

255.160 112.60

257.478 113.62

259.797 114.62

262.119 115.57

264.446 115.46

266.779 117.30

269.122 118.05

271.479 118.70

273.854 119.23

275.254 119.60

278.689 119.75

281.178 119.57

283.753 118.84

286.487 116.84

289.504 110.53

297.647

Cg Cp

J/(mol .K) J/(mol .K)

1 1 7 . 39 1 1 7 . 39

1 17.07 1 17.07

1 16.82 1 16.82

1 16.61 1 16.61

1 '6.48 1 16.48

.42 1 16.42

1 10.44 1 16.44

1 16.54 1 16.54

1 16.72 1 15.72

1 16.99 1 16.99

1 17.34 1 17.34

1 17.77 1 17.77

118.28 118.28

1 18.88 1 18.88

119.54 1 19.55

120.29 120.29

121.10 121.11 121.98 121 .99 122.92 122.94

123.92 123.95

124.98 125.02

126.10 126.14

127.26 127.32

128.48 128.55

129.74 129.83

131.05 131.16

132.40 132.53

133.79 133.96

134.54 134.73

135.70 136.95

138.22 138.51 139.78 140.13

141 .38 141 .80 143.02 143.53

144.71 145.31 146.44 147.15

148.22 149.06

150.05 151.04

151 .94 153. 10 153.88 155.24

155.87 157.48

157.94 159.83

150.08 162.31 152.29 154.92

164.61 167.71 167.03 170.71 159.58 173.97

172.29 177.56

175.21 181 .58 178.40 186.17

181 .96 191.57

186.05 198.14

190.91 206.50

196.99 217.75

205. 10 234.17

217.06 261.09

237.72 314.81

287.81 479.31

Fugacity/ Vel . of

Pressure Sound

Ratio m/s

1 .00000 1721

1 .00000 1695

1 .00000 1669

1 .00000 1644 .99998 1519 .99994 1 594 .99986 1569

.99975 1544 .99959 1520 .99935 1495 .99902 1470 .99858 1445

.99799 1420

.99722 1 395

.99636 1359 .99521 1 344

.99392 1319 .99228 1294 .99045 1268 .98826 1 243

.98581 1218

.98298 1 1 92

.9 /yo5 115/

.y / 034 1 1 >i 1 114 1 .9 1.14 /

1 1 1 £

1 1 16

1 uyu

nc: T c o 1065

.y5o /2 1 039

.95595 1 026

.94773 988

.94 165 962

.93523 936

.92843 9 1

0

.92130 834

.91379 858

.90593 832

.89772 805

.88919 780

.88035 754

.87120 727

.851 75 700

.85204 574

.84207 547

.83 187 519

.82147 592 .81085 564 .80007 536

.7891

1

508 .77799 479

.75672 450

.75532 420

.74375 389

.73200 358

.72005 325

.70785 292

.69533 257

.63240 219

.66883 181 .65361 0

Di el ectr ic Constant

2.03857

2.03023

2.02212

2.01402

2.00592

1 .99783

1 .98975

1.98167

1 .97359

1 .96551

1 .95742

1.94932

1 .94122

1.93310

1 .92496

1 .91680

1 .90862

1 .90041

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192
NBS-n4A IREV. 2-8C)

U.S. DEPT. OF COMM. BIBLIOGRAPHIC DATA

SHEET (See instructions)

1. PUBLiCATION OR

REPORT NO. NBS Monogr. 169

2. Performing Organ. Report No, 3. PubM cation D ate

April 1982

4. TITLE AND SUBTITLE

THERMOPHYSICAL PROPERTIES OF NORMAL BUTANE FROM 135 TO 700 K AT

PRESSURES TO 70 MPa

5. AUTHOR(S)

William M. Haynes and Robert D. Goodwin

6. PERFORMING ORGANIZATION (If joint or other than NBS. see instructions)

NATIONAL BUREAU OF STANDARDS

DEPARTMENT OF COMMERCE

WASHINGTON, D.C. 20234

7. Contract/Grant No.

8. Type of Report & Period Covered

Final

9. SPONSORING ORGANIZATION NAME AND COMPLETE ADDRESS (Street. City. State. ZIP)

Same as No. 6

10. SUPPLEMENTARY NOTES

Library of Congress Catalog Card Number: 82-600512

Document describes a computer program; SF-185, FlPS Software Summary, is attached.

11. ABSTRACT (A 200-word or less factual summary of most si gnifi cant information. If document includes a si gnificant

bi bliography or literature survey, mention it here) Using a modified version of the nonanalytic equation of state, thermophysical

properties of normal butane are derived from physical properties data and are tabulated at integral temperatures from 135 to 700 K along isobars at pressures to

70 MPa. These isobar tables, along with a table for the saturated liquid, give

values for densities, compressibility factors, internal energies, enthalpies,

entropies, heat capacities, fugacities, sound velocities, dielectric constants, and

isochore and isotherm derivatives. Equations, whose coefficients are determined from

a least squares fit to selected experimental data, are also presented for vapor

pressures, orthobaric liquid and vapor densities, ideal gas properties, second virial

coefficients, dielectric constants, heats of vaporization, melting pressures, and

orthobaric liquid specific heats, enthalpies, and entropies. Comparisons between

experimental and calculated values for all properties considered here are reported in

detail.

12. KEY WORDS (Six to twelve entries; alphabetical order; capjtalize only proper names; and separate key words by semicolon s) Densities; dielectric constants; enthalpies; entropies; equation of state;

fugacities; internal energies; isobars; isochores; isotherms; Joule-Thomson

inversion; latent heats of vaporization; melting line; normal butane; orthobaric

dens-it ies; spe r.ifir heats; vapor pressure.g; vel or.-j ti es nf snnnd.

13. AVAILABILITY

Unlimited

I I For Official Distribution. Do Not Release to NTIS

[ 1 Order From Superintendent of Documents, U.S. Government Printing Office, Washington, D.C. 20402.

[X] Order From National Technical Information Service (NTIS), Springfield, VA. 22161

14. NO. OF

PRINTED PAGES

197

15. Price

$16.50

USCOmm-DC 6043-PeO