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REFERENCE

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PUBLICATIONS

U.S. DEPARTMENT OF COMMERCE / National Bureau of Standards

Thermophysical

Properties of Isobutane from

114 to 700 K at Pressures to 70 MPa
NATIONAL BUREAU OF STANDARDS

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Thermophysical Properties of Isobutane

from 114 to 700 K at Pressures to 70 MPa

R. D. Goodwin

W. M. Haynes

Thermophysical Properties Division

National Engineering Laboratory

National Bureau of Standards

Boulder, Colorado 80303

e

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

NATIONAL BUREAU OF STANDARDS, Ernest Ambler, Director

Issued January 1982
National Bureau of Standards Technical Note 1051

Nat. Bur. Stand. (U.S.), Tech. Note 1051, 196 pages (January 1982)

CODEN: NBTNAE

U 8. GOVERNMENT PRINTING OFFICE

WASHINGTON: 1982
Contents

Page

1. Introduction 1

2. Physical Properties and Their Formulation 2

2.1 Fixed-Point Values 3

2.2 Melting Line and Vapor Pressures 3

2.3 The Orthobaric Densities 4

2.4 The Virial Equation 6

2.5 The Equation of State 6

2.6 The Ideal Gas Functions 8

2.7 Thermal Loop Computations 9

2.8 The Heats of Vaporization 10

2.9 Saturated Liquid Enthalpies and Entropies 10

2.10 Dielectric Constants 11

3. Computational Methods . c 12

3.1 The Homogeneous Domain 12

3.2 The Saturated Liquid 13

3.3 The Compressed Liquid 13

3.4 Fugacity Coefficients 13

3.5 Simplified Computation 14

4. Tests and Conclusions 14

5. Tables of Physical and Thermodynamic Properties 15

5.1 Calculated P-p-T Isochores and Isotherms 15

5.2 The Joule-Thomson Inversion Locus 16

5.3 Thermophysical Properties of the Saturated Liquid 16

5.4 Thermophysical Properties Along Selected Isobars 16

6. Acknowledgments 16

7. References 18

APPENDIX A. Symbols and Units 24

APPENDIX B. Conversion of Units 26

APPENDIX C. Fixed-Point Values for Isobutane 27

APPENDIX D. Isobutane Properties Reference Index 28

APPENDIX E. Computer Program 31

m
List of Figures

Page

Figure 1. Density-temperature diagram of isobutane 50

Figure 2. P-T locus of P-p-T data for isobutane 51

Figure 3. P-T locus of nev/ P-p-T data for isobutane 52

List of Tables

Table 1. Comparisons of vapor pressure data with eq (2) 53

Table 2. Comparisons of saturated liquid density data with eq (3) . . 55

Table 3. Comparisons of saturated vapor density data with eq (4) . . 58

Table 4. Comparisons of second virial coefficients with eq (5). . . . 60

Table 5. Behavior of coefficients of equation of state for

isobutane (eq (6)) 61

Table 6. Calculated P(p) critical isotherm of isobutane 62

Table 7. Comparisons of experimental ^^-p-j data of isobutane with

eq (6) 63

Table 8. Comparisons of data for ideal gas functions with eq (7). . , 78

Table 9. Interpolated ideal gas functions from eq (7) 79

Table 10. Comparisons of heat of vaporization data with eq (9) . . . . 80

Table 11. Enthalpies of saturated liquid isobutane from eq (10) ... 83

Table 12. Entropies and specific heats of saturated liquid isobutane

from eq (11) 84

Table 13. Comparisons of dielectric constant data with eq (12) .... .85

Table 14. Comparisons with saturated liquid specific heats ...... 90

Table 15. Comparisons '^ with C and C data 91

V p Table 16. Comparisons with enthalpy data 94

Table 17. Calculated P(T) isochores of isobutane 95

Table 18. Calculated P(p) isotherms of isobutane 110

Table 19. The Joule-Thomson inversion locus for isobutane 131

Table 20. Thermophysical properties of saturated liquid isobutane . . 132

Table 21. Thermophysical properties of isobutane along isobars .... 134

IV
THERMOPHYSICAL PROPERTIES OF ISOBUTANE FROM 114 TO 700 K AT

PRESSURES TO 70 MPa

Robert D. Gouawin and William M. Haynes

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 isobutane are derived from physical

properties data and are tabulated at integral temperatures over the

entire range of fluid states from 114 to 700 K along isobars at

pressures to 70 MPa. Results include dielectric constants, densities,

enthalpies, entropies, equation of state, internal energies, isobars,

isochores, isotherms, Joule-Thomson inversion, heats of vaporization,

melting line, orthobaric densities, specific heats, sound velocities,

vapor pressures, and virial coefficients. In addition to the equation

of state, equations are given for vapor pressures, orthobaric vapor and

liquid densities, ideal gas properties, second virial coefficients,

dielectric constants, heats of vaporization, melting pressures, and

orthobaric liquid specific heats, enthalpies, and entropies. Several

new sets of data have been used in this correlation; comparisons

between experimental and calculated values are given.

Keywords: densities; dielactric constants; enthalpies; entropies;

equation of state; fugacitles; internal energies; isobars; isobutane;

isochores; isotherms; Joule-Thomson inversion; latent heats of

vaporization; melting line; orthobaric densities; specific heats;

sound velocities; vapor pressures; viriel coefficients.

1 . Introduction

Isobutane not only is a component of liquefied natural gas (LNG), but also

has become an important heat-exchange fluid for geothermal cycles. The present

report is a revision and extension of earlier, provisional work [23] and is based

on additional, new compressibility [27,63], vapor pressure [63,64] and dielectric

constant [27,30] data.

Earlier correlations on isobutane have been presented by Hanson [26], Das

and Kuloor [13], Das, et al. [14], Milora and Combs [41] and by Starling, et al . [55,56]. Functions for ideal gas states recently were computed from spectroscopic data by Chen, et al . [7]. A survey of available data has been prepared

quite recently by Kestin, et al . [34] and by Kumar [37], which also includes
comparisons between existing correlations. A major objective of this report is

to orovide a more accurate thermodynamic network for isobutane, by inclusion of new compressibility data of Waxman [63,64] and Haynes [27]. It should be noted

that Waxman [63,64] is also currently developing an equation of state for

isobutane that uses a completely different approach from that presented here, but

which is based on the same experimental data.

New compressibility isotherms to pressures of 21 MPa have been measured by

Waxman [63,64] in the temperature range, 378 through 448 K, including vapor

pressures in the range, 298 through 398 K, For compressed liquid states, P-p-T

and dielectric constant data have been obtained recently by Haynes [27] on isotherms from 120 through 300 K at pressures to 35 MPa. These new data have

been included here in a revision of the nonanalytic equation of state [20-23]

used to compute thermodynamic functions for isobutane. A new procedure for

numerical integrations is used here, in which the convergence error is

predetermined.

Units used in all of the computations in computer programs (Appendix E)

include pressures in bar and densities in mol/L. However, SI units are used

throughout this report in tables and equations. Pressures are given in MPa,

densities in kg/m-^ and temperatures in K. For thermal properties, the mol is

used for amounts of substance. Appendix A presents symbols and units as used in

the computations and Appendix B presents a conversion of units. Fixed-point

values used in this work are in Appendix C. A summary of references for the

principal physical properties of isobutane, along with ranges of data available,

is presented in Appendix D. Computer programs for the calculation of thermophysical properties of isobutane are found in Appendix E. Figure 1 is the

density-temperature phase diagram for isobutane, in which the upper, left-hand corner shows the freezing liquid line.

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

netv/ork. 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 is adopted from Das, et al . [14],

The pressure is obtained from eq (2), the vapor pressure equation. The liquid

density is assigned for consistency with data in eq (3). The vapor density is

obtained from eq (4), used for saturated vapor densities.

(b) The Boiling Point. The temperature is from 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 critical point parameters (T = 407.85 K,

3

P = 3.640 MPa, p = 224.36 kg/m' (3.86 mol/L)) in present work are adopted on the basis of fitting orthobaric densities, vapor pressures, and P-p-T data, and

examining the behavior of the calculated critical isotherm. Beattie, et al . [2]

reported a critical temperature of 408.14 +_ 0.05 K, a critical pressure of

3.648 +0.005 MPa, and a critical density of 221 kg/m^ (3.80 mol/L) from an analysis of their detailed set of critical region data. Recently Levelt

Sengers [64] analyzed this data set of Beattie, et al . [2] using a simple scaled

equation of state and obtained the following critical point parameters,

T^ = 407.865 + 0.009 K, P^ = 3.6306 + 0.0006 MPa, p = 227.0 + 0.1 kg/m^

(3.906 + 0.002 mol/L). More recently Levelt Sengers [53] has measured the

critical temperature and density of isobutane. The measured values are in

agreement '^fith the values obtained in this study to within experimental error of

0.02 K in temperature and 1 kg/m^ in density.

2.2 Melting Line and Vapor Pressures

(a) The Melting Line. Measurements were described by Reeves, Scott, and

Babb [47]. Unpublished lower-pressure data for isobutane, obtained from

Babb [47], are as follows:

T, K P, MPa

140.6 114.0

160.3 304.7

164.7 372.0

-8

By graphical approximations (for T. = 113.55 K and P. = 1.9481 x 10" MPa),

the constants for the Simon equation.
p, ^ Po-[(T/T,: - 1] (1)

have been estimated to be P = 43 MPa and c = 6.08. These constants differ

greatly from those for other substances; e.g., c is approximately two and Pg

varies from approximately 200 to 700 MPa for other low molecular weight alkanes

(methane, ethane, propane, normal butane) [21-24,23].

(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 identified as ID = 80 have been derived via revised thermal

loops, as described by Goodwin [23], by use of the saturated liquid specific heat

data of Aston, et al . [1] and of Parks, et al . [45] 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 here in

section 2.6; the virial equation formulated here 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.

Equation (2) is similar to previous forms [20-23].

The argument for eq (2) is T e '^ /'^ n> then, vapor pressures (P ) in MPa are given by the relation,

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

where e = 1 .30 and, from least squares analysis,

a = - 9.1617 1029

b = 20.1547 7713

c = -14.9868 2080

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. The

slope at the critical point 'ais dP /dT = 0.063512 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 table, are shown for the sake of comparison. If the variable for eq (3) is defined by

d

= 9.8235 4747

e

= -2.2352 2474

f

= 1.1621 4052
x(T) E (T^ - T)/(T^ - T^) , (3)

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

e 2 3

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

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

a = 0.7888 17981 c = -0.0352 35274

b = -0.0160 84282

(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 (6)) to yield a compressibility factor approaching unity in the limit

of low densities, as described earlier [20,2?]. Data in table 3 used in the fit

have been selected for consistency. Values identified by ID = 40 are derived

from the vapor-pressure and virial equations. The values identified by ID = 10 are derived by extrapolating isotherms of Waxman [63,64] to the vapor-pressure

curve. 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 unity as p -»0, (hence

T (p) — 0). Let A = (Z - 1), where Z is value of the compressibility

factor at the critical point, and define the arguments

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

The saturated vapor densities, P^ = P /(Z 'R'T), then are given by

Z = 1 + AQ.n-T;:^f(T) , (4)

where

f(T) E 1 + a-u^ + b-u + c.exp[n-(l - 1/u)] , (4a)

e = 0.35, n

= 1.20, and, from least squares analysis,

a = -0.7915 03145 c = 1.8853 35494

b = 0.8047 32724
The next-to-last column in table 3 gives the experimental residuals,

F(Z) E (Z - 1)-T-/[A. -nl ,

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, p = p/p and T =

"^/"'"r*

''"'^^ follovnng relation,

B (T) = 3, + B^/i + 3^/T^ , (5b) ^\ I 1 2 r 3 r

' ^ '

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,

3^ = 0.5087 5533 B^ = -0.6593 9715

B^ = -1 .1185 3523

have been determined. The second virials have been used to estimate P-p-T

values, to calculate saturated vapor densities via the vapor pressure equation,

and to make thermal loop computations.

2.5 The Equation of State

Figure 2 shows the P-T regions covered by P-p-T data of Beattie, et al . [3];

Morris, et al . [42]; and Sage and Lacey [50]. Pxegions covered by the new data

of Waxman [63,64] and Haynes [27] are seen in figure 3. Equal weightings of

unity have been given to the data of Beattie, et al., Haynes, and Waxman. The

data of Sage and Lacey, which fall in a region between Haynes and Beattie, et al

.

show systematic differences of 0.5 to 1.5 percent when compared to the data of

Beattie, et al., Waxman, and Haynes. Thus, they are given a low weighting of

0.02. The data of lorris, et al . ivere not used for fitting because those of

Beattie, et al . cover about the same range and also extend to higher temperatures. Data from the virial equation along a low density isochore are included

(with zero weighting) for comparison. Comparisons with the data of Morris,

et al . also are presented.
The nonanalytic equation of state used here has only three least-squares

coefficients as described in detail by Goodwin [20,22]. The equation has been

modified from earlier forms. 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)] + pVt^-FIp.T) , (6)

where

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

The reduced density, p , is defined as p/p^, while the constant R is defined

•^ ' c by R E (0.0083145)-p^, MPa/K.

The temperature-dependent functions in (5a) are defined as follows.

HpJ) = T^-exp[b-(l - T^/T] - (T^)'^ (6b)

r

where b e (1 - 6) + (1 - B)^^^ T^ e T/T^ and (T^) e T^(p)/T . r

y(p,T) E ^(p,T)/,!j^(p) - 1 , (5c)

where 4J(^(p) is obtained from i|j(p,T) merely by replacing T with T (p), and

^(p,T) E 1 - (u) - ro'^/n)/(l - 1/n) . (5d)

Values for 3 and n are found by trial.

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

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

0(p) = T^(p)"exp[-a-f(p)] , and (6f)

f(p) -= IP^ - 1|^/((P^) - 1)^^ . r

(p|.) = Pf'^'^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 B^ + B^-P^ (6g)

and

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

where Cg and y are to be found by trial.

Parameters and coefficients of eq (6) for isobutane are

a = 1, B

= 0.70, y = 0.13, n= 1 .1 ,

B^ = 0.4666 6891 283 C^ = 2.2

B2 = 0.1658 3380 415 C^ = -0.2641 2858 359

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

and table 6 gives behavior of pressure, etc. along the critical isotherm. (In

table G, the symbol, p . , is defined as the density reduced by the triple

r , L point density.) These 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. Despite some relatively large P-p-T deviations (see section 4), a smooth

and consistent representation of the P-p-T data has been developed by means of

the highly-constrained equation of state used here, which, in addition, yields a maximum in the specific heats, C (p,T), at the critical point.

Some recommendations have been made in section 4 concerning the need for

additional data in regions in which data are presently unavailable and in which

existing data sets are inconsistent. The functional form of the equation of

state used here for isobutane has also been used in current work for propane [24]

and normal butane [28], fluids for which the data bases are significantly better.

Identical nonlinear parameters (a, 3, Yj n) except for small differences in Y5

have been obtained for all three fluids in optimizing 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 . [7] has been developed. Using x = T/lOO,
7 , . Cp/R - 4 = exp(-£:/x^). E A-.x^""" . (7)

e 5.40 ^ = 43.59076

'•2 - - 40.54350

Ao = 739.7^837

where R = 8.31434 J/(mol.K) and

A^ = -3137.57293

A^ = 7742.58382

Ag = -7583.91994

A^ = 3251.25208

Table 8 shows the fit of derived values used. In this table, the values for

(H -H ) 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 [23], and more generally by Yarbrough and Tsai [65] uses virial eq (5a), ideal gas functions

eq (7), the heat of vaporization of Aston, et a1 . [1] at the normal boiling

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

et al . [1] and of Parks, et al . [45] for the saturated liquid from the triple- to

the normal boiling-point. Define x (T) = T/lOO, then the saturated liquid

specific heats, C (T) , are described by

C^(T) = a + b.x^ + c.x^ , (8)

in J/(mol»K) , where

a = 89.71230 c = 4.572016

b = 3.34517

The coefficients have units of J/(mol'K). The rms relative deviation is 0.31

percent for 44 data points. In fitting this equation the data of Parks,

et al . [45] were weighted 0.1 relative to unity for Aston, et al . [1].

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^^p,' ^^^"^ ^"^ kJ/mol uses argument

x(T) E (T^ - T)/(T^ - TJ;

vap

t'

(9)

where

0.43

28.117144

32.239895

-3.0186000

-3.3534669

Least squares coefficients have units of kJ/mol . The uncertainty of at least one percent in Q at the higher temperatures will affect compressed liquid

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

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

variable,

X E (T^ - T)/(T^ - T^) ;

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

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

^ a c t c

8

E

i = l

i-1

(10)

where e = 0.48, H^ = 0.001 J/mol, H = 43430.103 J/mol, and

A.

0.4190 52003

0.0955 65888

0.5120 32199

0.3011 49628 A.

-4.3108 63286

8.3850 53823

-6.7091 04812

1.9750 52516

The saturated liquid entropies in J/(mol«K) are shown in table 12. Let

x = (T - T)/(T - T ); then the entropies, S (T), are given in J/(mol»'K) by

10
(S^ - Sc)/(St - S^) = X + (x^ - x). i; A.'X

1

i-1

(11)

where e = 0.39, S^ = 108.80035 J/(mol»K)

A^ = 0.1513 53821

A^ = -0.7213 49078

A3 = 0.5916 51346

A. = -0.8071 40353

S = 278.16100 J/(mol-K), and

A^ = -0.6495 76938

A^ = 1.5685 90395

A. = -0.9190 17569

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

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

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

2.10 Dielectric Constants

Dielectric constants, e, for the saturated vapor of isobutane are estimated

from the refractive indices, n, of Sliwinski [54] via e = n . (These low

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

Haynes [27,30] recently has measured e for the saturated liquid at temperatures

from 115-300 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,

CMF E [(e - l)/(£ + 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 pressures up to 70 MPa. Define the variables,

T T/T and p

c ^r p/p • then, with P in units of MPa, the Clausius-Mossotti

function, in units of cm-^/mol , is given by

where

CMF = A^ + A^-p^ + A3-p^ + k^'ln (1 + 1/T^) + A^-P/IO

19.867026

0.6793 6208

-0.2274 7774

0.9947 2904

-0.0056 3750

(12b)

11
The coefficients have units of cin^/mol . Data at high pressures have a diminished weighting as seen in table 13. The rns relative deviation for 207

points is 0.059 percent in the CMF and O.Ol"! percent for the dielectric

constant.

Comparisons with dielectric constant data for liquid isobutane not used in

the fit to eq (1?) are not presented in table 13. The dielectric constants from

Thompson and Miller [59] and Luo and Miller [38] at temperatures between 22U and

250 K and from Pan, et al . [44] at temperatures from 114 to 120 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 = at the liquid triple-point, obtained by use of the arbitrary value,

E° = 23747.7595 J/mol . Specific heats of Aston, et al . [1] and of Parks,

et al . [45] could be integrated to give the solid at T = 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 > Tc.

Computations 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,

AE = / [P - T.0P/3T)].dp/p^ , (13)

AC^ = - T ./(9^P/3T^).dp/p^ , (14)

A

.0 P o R.£n[P^/(pRT)] + r [R - 0P/3T)/p]-dp/p . (15)

•'o

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 = - J(3P/3T)-dp/p^ . (15a)

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

12
H = E + P-v . (16)

Cp = C^ + T.OP/3T)^/OP/3p)/p^ . (17)

and

'/ = Cp-0P/3p)/C^ . (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, ^ Q , is used to compute

vap

AH = - g . 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, C (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.0P/3T).(dp^/dT)/p^ , (20)

where p^ is density of the saturated liquid. Values for C (p,T) and W(p,T) on this boundary follow from eqs (17) and (18). For liquid at the normal boiling

point, the following values have been obtained,

J^ = 261.517 K, H^ = 16774.7 J/mol

,

E^ = 16764.7 J/mol, S^ = 201 .388 J/(mol. K)

.

3.3 The Compressed Liquid

Starting with above values for E, S, and C 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),

13
(f/P) - (P°/P)-exp [AG/RT] . (21)

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

AG - (H - E°) - H° - T (S - S°) , (22)

in v/hich the arbitrary value of E was added to tabulated values o-'' H(P,T)

such that E(P,T) = for liquid at the trinle 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,'( and P,bar, it is necessai^y 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, Goodwin [23] made some comparisons of thermodynamic properties with results of other workers, namely Sage and Lacey [50], Das,

et al . [14], and Starling, et al , [55], to ensure freedom from gross

inaccuracies. These now are omitted because present properties are roughly

comparable with the earlier work [23].

The P-p-T comparisons in table 7 show relatively large inconsistencies among

the various data sets. Between room temperature and the critical temperature,

the liquid and vapor densities of Sage and Lacey [50] and the liquid densities of

Morris, et al . [42] exhibit systematic differences of as much as 0.5 to 1 percent

from the equation of state and from data from other sources. Of these two data

sets, only the data of Sage and Lacey [50] were used in the fit, but with a low

weighting (0.02). At temperatures above the critical point, the present work has

not realized a representation as precise as desired for the data of Beattie,

et al . [3] and Waxman, et al . [63,64]. This leads to a diminished accuracy (for

the density), but not to irregularities or inconsistencies with the nonanalytic

equation of state used here, as seen by inspecting derivatives of the P(p,T)

surface in tables 6, 17, 18, 20, and 21. Other equations of state with a large

14
number of adjustable least-squares coefficients fitted to inconsistent P-p-T data

from different laboratories may yield inaccuracies in the all-important

derivatives . Comparisons of calorimetric specific heats with calculated results are given

in tables 14 and 15. The data of Sage and Lacey [50] are not consistent with the

ideal gas state specific heats of other investigators, as vvas also noted in a paper by Dai ley and Felsing [11]. Otherwise, the agreement is generally good for

this difficult computation. Comparisons between the experimental enthalpies of

Koppany and Lenon [35] and calculated values are presented in table 16 for both

gas and liquid at temperatures from 350 to 3^5 K. The average difference is less

than 100 J/mol.

In summary, the P(p,T) surface has been extended for compressed liquid down

to the triple-point via the new compressibility data of Haynes [27], and has been

improved by inclusion of the new vapor pressures and gaseous densities of Waxman,

et al . [63,64]. However, there are still regions in which accurate data are needed for isobutane. A self-consistent and accurate set of P-p-T data, vapor

pressures, and orthobaric densities at temperatures from 300 K to the critical

temperature would probably be the most valuable contribution for improving the

P(p,T) surface for isobutane. It would also be beneficial to have accurate

specific heat and sound velocity data to check the derivatives of the surface.

Concurrently with the development of the nonanalytic equation of state for

Isobutane at this laboratory, Waxman, et al . [63,64] also have been developing an equation of state for isobutane with a completely different approach. Both

efforts use the same data base, including the new data sets. Preliminary

comparisons of calculated thermodynamic properties for the two different

equations show excellent agreement. The results from these two equations should

supersede other correlations, which have been based on inaccurate and

insufficient data. Hov/ever, it should be emphasized that additional accurate

data (in regions as noted above) are still needed to better define the P(p,T)

surface for isobutane.

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)

15
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 C (p,T) at the critical point.

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

monotonically with density along isotherms.

5.2 The Joule-Thomson Inversion Locus

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

obtained from equation of state (6) under the condition, T»(3P/3T) = p*(3P/3p).

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 Thermophysical 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 = 407.85 K along isobars at

P > P = 3.640 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. Acknowledgments

Many staff members of the Thermophysical Properties Division of the National

Bureau of Standards (MBS) 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

16
and in obtaining documents. The authors are grateful to Meyer Waxman of the

Thermophysics Division of NBS who participated in many fruitful discussions and

contributed prepubl ication vapor sressure and P-p-T data and to J. M. H. Levelt

Sengers, also of the Thermophysics Division, who provided analysis and data for

critical point properties of isobutane before publication of her results.

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.

17
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18
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19
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80 mole percent isobutane in isopentane. Electric Power Research Institute,

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20
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Clausius-Mossotti functions for simple liquid mixtures: systems containing

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pressure-transmitting fluids, J. Chem. Phys. 40, No. 12, 3662 (Jun 1964).

Also, private communication on isobutane from Prof. S. E. Babb, Jr.,

October 2, 1978.

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for testing and improving correlations for liquefied natural gas, AIChE J.

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21
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n-butane, isobutane, and n-pentane, Ind. Eng. Chem. _29, 1309 (1937).

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22
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23
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 nelting 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.

(3P/3T) isochore derivative, MPa/K

(3P/3p)j isotherm derivative, MPaMii^/kg

(9^P/3T^) isochore curvature, MPa/K^

a,^,y,T] nonlinear parameters in the equation of state

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

Aq Zj, - 1 in saturated vapor density equation

A^ coefficients defined in various equations

b (1 - S) + (1 - S)^/^ 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),C|„(T) reduced second and third virial coefficients

c exponent in Simon equation

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

Cp(p,T) molal heat capacity at constant pressure, J/(mol«K)

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

CMF Clausius-Mossotti function, cm-^/mol

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

E° 23,747.7595 J/mol (arbitrary)

e exponent in various equations

e dielectric constant

f/P fugacity/pressure ratio

f(p) used in definition of 9(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 =

24
APPENDIX A. (Continued)

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

J the joule, 1 Nth

JT Joule-Thomson

L the liter, 10"-^ m^

mol 58.1243 grams of isobutane (C^ = 12 scale)

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

P pressure, MPa

P^ melting pressure, MPa

P^(T) the vapor pressure, MPa

Pj^(p) Pg[T^(p)], vapor pressure as a function of density

n(T) Pa("^)/Pc

^(p,!) function in the equation of state

'i'(p,T) 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* 0.0083145 Pc, MPa/K

p density, kg/m^

Pp P/Pc' '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

Tp T/T(,, reduced temperature

T^(p) liquid-vapor coexistence temperature, K (Tg) Tq(p)/Tc, reduced temperature at coexistence for the equation

r of state

0(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)/(Tt - TJ

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 [49].

25
APPIINDIX 3. Conversion of Units

In the follov/ing table the nolecjlar weight of isobutane is given by

mol . vvt. = 58.1243 g/mol . Also, 1 cal,, = 1 cal (therrnochemical ) = 4.134 J and I 3TU.^ - 1 3T'i (International Table) - 1055.056 J.

To convert from ^To Multiply by

Pressure, MPa bar 10.

9.36923

10.1972

145.038

Volume, m^ liter (L) 1000.

35.3147

Density, kg/in^ g/cm"^ 0.001

bar

atn

kg/cm^

^\-)/^r?-

liter (L)

ft3

g/cm-^

;]iol/L

Ib/ft^

MPa-m^/kg

bar 'L/rnol

cal^t^/mol

BTUjj/1d

3TUjy/(lb.°r;

1 ./(mol . ivt .) 0.062428

Molar energy, J/mol MPa'm-^/kg 0.001/(mol. v/t.)

0.01

0.239006

0.429923/ (mol. vvt.)

Molar entropy, J/(mol.;() 3TUtt/( lb •°r) 0.238846/(mol . wt .)

26
APPENDIX C. Fixed-Point Values for Isobutane

Critical °oiit

^c ^ 3.640 MP

Pc

--- 224.36 kg/in- ( 3.86 niol/L)

Tc =

= 407.85 K

Normal Boil ing Poi it

P = 0.101325 MPa

T = 261.517 K Py = 2.841 kg/ir (0.04888 mol/L)

p^ = 593.71 kg/m-' (10.2145 mol/L)

Triple Point

P^ - 1.9481 X 10"^ MPa

T^ = 113.55 K

Py = 1.1994 X 10"^ kg/iii^ (2.0633 x 10'^ nol/L)

p^ = 741.38 kg/m^ (12.755 mol/L)

27
Melting Line

Reeves [47]

APPENDIX D. Isobutane Properties Reference Index

Date Pressure Range, MPa

1964 150 - 1000

Vapor Pressures

Burrell [5]

Seibert [52]

Dana [12]

Sage [50]

Morris [42]

Aston [1]

Gi Hi land [18]

Wackher [62]

Beattie [2]

Connolly [9]

Hirata [31]

Gilnour [19]

I'laxman [63,54]

Thermal loops (This report'

Date

1926

1938

1939

1940

1940

1945

1949

1962

1966

1967

1980

1982

Temperature Range, K 153 - 260

303 - 393

249 - 353

290 - 394

344 - 373

183 - 262

352 - Tc

206 - 263

303 - 398

344 - Tc

295 - T

' c 261

298 _ 398

't 260

Saturated Liquid Densities

Dana [12]

Coffin [8]

Van der Vet [60]

Sage [50]

Morris [42]

Benoliel [4]

Carney [6]

NCAA [58]

Wackher [62]

Beattie [2]

Gilmour [19]

Sliwinski [54]

Kahre [33]

Rodosevich [48]

Date

1926

1928

1937

1938

1939

1941

1942

1942

1945

1949

1967

1969

1973

1973

Temperature Range, K 273 - 329

245 - 298

233 - 323

294 - 394

311 - 373

213 - 293

223 - 333

228 - 333

224 - 273

303 - 398

261

283 - 368

278 - 328

114 - 120

28
APPENDIX D. (Confinued)

Saturated Liquici Densi ties Date Temp erature Range, K McClune [40] 1976 123 - 173

Haynes [29] 1977 115 - 300

Orrit [43] 1978 129 - 249

Saturated Vapor Densit:ies Date Temp erature Range, K Dana [12] 1926 25U - 333

Sage/Lacey [50] 1938 294 - 394

Sliwinski [54] 1969 283 - 368

Waxman [63,64] 1980 378 - 304

Vi rial /vapor pressure equations (This 1982 115 - 260

report)

Virial Coefficients Date Temp erature Range, K Jessen [32] 1938 273 - 303

Sage [50] 1938 294 - 394

Morris [42] 1939 411 - 511

Beattie [3] 1950 423 - 573

Kretschmer [36] 1951 303

Gunn [25] 1953 344 - 511

Connolly [9] 1962 344 - 444

Strein [57] 1971 296 - 494

Compressibil ity Data Date Range of T, K Range of P, MP

a

Sage [50] 1938 294 - 394 0.07 - 20.7

Morris [42] 1939 311 - 511 0.7 - 34.5

Beattie [3] 1950 423 - 573 2.6 - 30.8

Waxman [63,64] 1981 378 - 448 0.3 - 20.8

Haynes [27] 1982 120 - 300 1.7 - 34.7

Virial equation (This 1982 270 - 570 0.1 - 0.2

report)

29
APPENDIX D. (Cont inued)

Specific Hea ts Date Type Range of T, K Dana [12] 1926 Ca (T) 259 - 291

Parks [45] 1937 r (T) 115 - 253

Sage [51] 1937 r^P (T) 294 - 444

Sage [50] 1938 r (T) 294 - 394

Aston [1] 1940 Ca (T) 117 - 275

Dailey [11] 1943 r^P (T) 348 - 693

Wacker [61] 1947 r-P

(T) 243 - 353

Ernst [16] 1970 Cp (T) 293 - 353

Chen [7] 1975 CO

P :t) Spectroscopic

Heats of Vap orization Date Temperature Range, K Dana [12] 1926 270 - 330

Sage [5U] 1933 290 - 390

Aston [1] 1940 261

Hanson [26] 1946 244 - 405

Das [13] 1957 261 - 400

Das [14] 1973 261 - 400

Thermal loop s (This report) 1982

^t

- 260

Clapeyron eq uation (This report) 1982 115 - 405

Dielectric C onstant^ Date Temperature Range, K Sliwinski [54] (index of refraction) 1969

Pan [44] 1975

Thompson [59] 1980

Luo [38] 1981

Haynes [27,30] 1982

283 - 368

114 - 120

228

220 - 250

115 - 300

30
APPENDIX E. Computer Program

PROGRAM IBTHRM8 ( INPUT , OUTPUT)

C REVISION OF I8UTANE THERMOFUNCTIONS , RDG/NBS, START JAN. 26, 1981

COMMON GK,GKK, Bl ,B2 ,63 ,B4,B5, C1,C2,C3, E1,E2,E3, ER, IX COMMON/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

COMMON/3/ 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,0ZDT, 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 F0RMAT(I5, 2F10.0)

2 F0RMAT(I5, 3F10.0)

3 F0RMAT(8I10)

5 FORMAT! IX)

9 F0RMAT{8F10.0)

14 FORMATdHl 13X * IBUTANE 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, FIG. 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=12,70 $ TI = 10*J $ CALL IDEAL $ HZA(J) = HZ

86 SZA(J) = SZ

87 PRINT 20 $ DO 88 J=12,70 $ T = 10*J

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

89 CALL JTLOCUS $ CALL TABLIO

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

, 1 = 1 ,NI

)

91 DO 300 I=IN,NI $ IK - I $ LS = 92 P = PP(I) $ IF(I.EQ.25) P = PORT

93 PK = P/10 $ 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

31
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

CASES FOR P LESS THAN PORT.

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

CASE FOR SATURATED LIQUID AND VAPOR.

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

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 S DPDIS = DPGDD/10/WM

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

128 T = JT

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 = $ 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

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

180 TPS(IK) = TCRT $ K = L = 181 DO 250 J=l,99 $ T = JT = 10*(IT+J)

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

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

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 = $ 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

32
226 PRINT 17, T,DEN,DIS,Z, DPTIS,DPDIS, E,H,S,CV,CP, FOP, IW, DIE

250 CONTINUE

300 CONTINUE

999 STOP $ END

SUBROUTINE COEXIST

C GIVEN 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), (G=0. 083145)

1 FORMATdHO 9X *J 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 = 6 EG = EZZ + EZ + EDELF(L,M,T,DA,DB) $ HG = EG + 100*PS/DB

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

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

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

10 CPG = CVG = WG = $ 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*DPDO/CVG)

13 DPGPT = DPDT $ DPGDD = DPDD

C NOW TRAVERSE THE ,D0ME, USING QVAP ,DATA,.

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

16 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*(DP0T/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,OTHDR, 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 FORMATdHO 9X *T G.E. TCRT IN COMPRES. * / ) 2 IF(T.GE.TCRT) 3,4

33
3 PRINT 1 S STOP

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

5 CALL COMPRLQ S RETURN

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

7 CALL COMPRLQ

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

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

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) S H = E + 100*P/DB

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

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

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

1 FORMATdHO 9X *T NOT UNDER TCRT IN COMPRLQ.*/)

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

3 PRINT 1 S STOP

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

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

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

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

C 8 CVS = CVSATF(T) S 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) S DX = DB - DL $ IF(DX.GT.O) 11,20

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

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

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

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

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

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

30 RETURN S 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

C0MM0N/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 S DPDIS = DPDD/10/WM

9 RETURN S END

FUNCTION CSATXF(T)

34
C IBUTANE 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*v^ +...).

DIMENSION AS(7)

DATA {NFS=7),{ES=0.39),{TTRP=113.55),{TCRT=407.85)

DATA (STRP = 108. 80035), (SORT = 278.16100)

DATA (AS = 0.1513538214, -0.7213490782, 0.5916513456,

1 -0.8071403525, -0.6495769380, 1.568590395, -0.9190175694)

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,D2PDT2,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 ISOBUTANE CONSTANTS VIA REVISED THERMALOOPS, SEPT. 23, 1980.

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,PCRT, 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=1. 20), {GKK=0. 083145)

DATA(AV = -0.7915031451, 0.8047327238, 1.885335494)

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

3 PRINT 1 $ STOP

4 DENGASF = DCRT $ DDSDT = I.OE+IO $ 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 = $ GO TO 12

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

35
12 F = 1 + AV{1)*UE + AV{2)*U + AV(3)*XP $ ZFX = F

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 IBUTANE SAT. LIQUID DEN, MOL/L, (0CRT=3.86), RDG, FEB. 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=113.55),(TCRT=407.85),(DCRT=3.86),{DTRP=12.755)

DATA(AW = 0.788817981, -0.016084282, -0.085235274)

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

3 PRINT 1 $ 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 S 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 5; RETURN $ END

FUNCTION DIELF(D,T,P)

C IBUTANE CONSTS., RDG, MARCH 7, 1981, VIA HAYNES DATA.

C CM,RMSPCT = 0.059, E,RMSPCT = 0.015.

C CM = Al + A2*R + A3*R2 + A4*LN(1+B/X) + A5*PI.

DIMENSION A(5)

DATA ( B=l .0 ) , ( DCRT=3 . 86 ) , ( TCRT=407 .85

)

DATA(A = 19.867026, 0.67936208, -0.22747774,

1 0.99472904, -0.0056375024)

1 R = D/DCRT $ X = T/TCRT S G = AL0G(1+B/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 )/(l .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)

36
DATA {LD=2) ,(DI=0. 00001) ,(G=0. 083145)

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 *EDELF NG AT TCRT FOR CV AT DEN NEAR OR GT C.P.*/)

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) = 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

CC 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

37
60 CONTINUE S N = M $ NM = M-1 S NP = N+1

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

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

64 PRINT 3, NP,E(NP),S(NP) ,C(NP) S PRINT 2, ED, SD, CD

99 STOP S END

FUNCTION FINOENF(T,P)

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

C0MM0N/1/AL,BE,GA,DE,EP,ET, OCRT,TCRT,PCPT, DGAT,DTRP ,TTRP,PTRP

C0MM0N/3/DPDT,D2PDT2,DPSDT,DPMDT,0PDD,DP0P,DTSDR,DTHDP,DDSDT

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 *FINOENF = 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) S DL=DENLIQF(T) S 3S=PSATF(T) S IF(P-PS) 3,32,4

3 D = DG/2 S GO TO 11

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

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

6 D = DCRT/2 S GO TO 11

7 D = 2*DCRT S GO TO 11

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

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

10 D = DCRT

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

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

13 DD = DP/DPDD S IF(ABS ( DD/D)-1 .OE-7) 31,31,14

14 D = D + DD S IF(D.GT.O.O) 15,15

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

16 IF(D.GT.DM) 17,13

17 D = DM S 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 S GO TO 30

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

23 D = DL S GO TO 30

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

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

26 D = DCRT - 0.02 S GO TO 30

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

28 D = DCRT + 0.02

30 CONTINUE S PRINT 41 S STOP

31 FINDENF = D S RETURN

32 PRINT 43 S STOP

33 FINDENF = DCRT S RETURN

34 FINDENF = DCRT S PRINT 42 $ RETURN

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

36 RETURN S END

FUNCTION FINDTMF(P)

C GIVEN P ON THE MELTING LINE, FIND T FOR I3UTANE.

38
C0MM0N/1/AL,BE,GA,0E,EP,ET, DCRT,TCRT,PCRT, DGAT,DTRP ,TTRP,PTRP

DATA (A=430.0),(E=6.08)

1 X = (P-PTRP)/A + 1 S FINDTWIF = TTRP*X**(1 .0/E) <R RETURN $ END

FUNCTION FINOTSF(P)

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

COWON/l/AL,RE,GA,nF,EP,ET, DCRT,TCRT,PCRT, DGAT,DTRP,TTRP,PTRP

C0MM0M/3/nPDT,D2PDT2,DPSnT,0PMDT,DPDD,DPDR,0TSDR,DTHDR,DDS0T

1 FORMAT (1 HO 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 S IF{T-TCRT) 9,9,8

8 T = TCRT

9 CONTINUE $ PRINT 1 $ STOP

10 FINDTSF = T $ RETURN

11 FINDTSF = TCRT $ RETURN

12 PRINT 2 S STOP $ END

SUBROUTINE GENEOUS

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

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/99/ TI,E7Z, EZ,SZ,CVZ, HZ,CPZ

DATA (g=l. 01325), (G=0. 083145)

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

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

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

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

7 CV = CVZ + DELCV % PX = PVTF(T,DP,1)

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

9 W = SORT{WK*CP*DPDD/CV) $ RETURN

10 DEN=S=0 $ E = EZZ + EZ $ H = E + 100*G*T $ 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,DPS0T,DPMDT,DPDD,DPDR,DTSDR,0THDR,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 IFCIK.FO.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 U!^ TO NEW DEN ON GIVEN ISOTHERM.

39
9 DA = DK(J) $ DK(J) = DEN = DB = FINDENF{T,P) $ N = 14

11 EK(J) = E = EK(J) + E0ELF(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*(DPDT/DB)**2

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

FUNCTION HSATF(T)

C IBUTANE 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 .48 ), ( TTRP=113 .55 )

, fTCRT=407 .85)

DATA (HTRP = 0.001),(HCRT = 43430.103)

DATA (AH = 0.4190520028, 0.09556588803, 0.5120321990,

1 0.3011496278, -4.310863286, 8.385053823, -6.709104812,

2 1.975052516)

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

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

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

DIMENSION A(7)

DATA (E=6.40) ,( R=8. 3145) ,( HI = 7. 26243166) ,( SI=35 .59759)

DATA{A = 43.59076, -40.54350, 739.72837, -3137.57293,

1 7742.58382, -7583.91994, 3251.25208)

1 NK = 7 $ 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 S 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 S 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

40
DATA (WM = 58.1243)

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

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

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

3 6X4HD/DC 9X5HTS/TC 9X5HPS/PC 10X4HP/PC 9X5HDP/DR 4X6HDTS/DR

4 4X6HDTH/DR 4X6HDPS/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 PRINT 1, TCRT, DCS, PCS, DPST, DPT $ DO 8 J=l,41

5 DR = 0.895 + 0.005*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, nTSDR,DTHDR, DPSDR, DX3DR,DXEDR

9 RETURN S END

SUBROUTINE JTLOCUS

C THE JOULE-THOMSON P-V-T LOCUS FOR IBUTANE.

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,nRP,PTRP

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

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

1 FORMATdHl 16X *THE JOULE-THOMSON INVERSION LOCUS FOR IBUTANE* //

2 17/. 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 = 320 $ 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

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

19 SS = SP $ DI = DI

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) = 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.

41

DX $ GO TO 20

DX

T $ DNd) == DI
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 ,83 ,84 ,B5 , C1,C2,C3, E1,E2,E3, ER,IX

C0MM0N/1/AL,BE,GA,DE,EP,ET, DCRT,TCRT,PCRT, D6AT,DTRP,TTRP,PTRP

C0MM0N/3/DPDT.D2PDT2,DPSDT,DPMDT,DPDD,DPDR,DTSDR,DTHDR,DDS0T

COMMON/6/ TSAT, THETA, PSAT

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

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

1 15X 6HTTRP =F7,3, 8H, TBLP =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, 83 =F14.11/

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

8 TB=FINDTSF(1. 01325) $ DGB=DENGASF{T8) $ DLB=DEMLIQF(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 $ DCR = DCRT*Wf4

DGA = DGAT*WM $ 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, 81,82,83, 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 = 81 + 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 I8UTANE MELT LINE. PRIVATE( S.E .RABB,JR.) , 10/2/78.

C THREE DATA ADJUSTED FOR TTRP = 113.55 BY R.D.G.

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

C0MM0N/1/AL,8E,GA,DE,EP,ET, DCRT, TCRT, PCRT, DGAT,DTRP,TTRP ,PTRP

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

DATA (A = 430.0) ,(E = 6.08)

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 IBUTANE VAPOR PRESSURE, BAR, RDG, FEB. 19, 1981. (DCRT=3.86).

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 = 1.30)

DATA (TTRP=113.55) ,(TCRT=407.85) ,(DCRT-3.86) ,( DTRP=12 .755)

DATA(PJ = -9.16171029, 20.15477713, -14.98682080,

42
1 9.82354747, -2.23522474, 1.16214052)

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

STOP

GO TO 10

Zl = -EPP*Z/V

$ 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 DPSDT = PL1*PSATF/TCRT $ RETURN $ END

7 PRINT 1 $

8 Z = Zl = $

9 Z = V**EPP $

10 PL = PJ(5)*Z

SUBROUTINE PVTDATA

IBUTANE EOS CONSTANTS, RDG/NBS, FEB. 19, 1981. (0CRT=3.86).

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,PCRT, 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 S TTRP = 113.55 $ TCRT = 407.85

12 OCRT = 3.860 S DTRP = 12.7550

13 PTRP = PSATF(TTRP) $ PCRT = PSATF(TCRT)

20 GKK = 0.083145 $ GK = GKK*DCRT $ ZCRT = PCRT/DCRT/GKK/TCRT

21 IX = 2 $ AL = 1.0 $ BE = 0.7 $ GA = 0.13 $ DE = 22 EP = S ER = 2.20 $ ET = 1.1

23 Bl = 0.46666891283 $ B2 = 0.16583380415

B3=B=E2=E3=0

$ WK = 100000/WM

24 El = 0.26412858369

25 OGAT = DENGASF(TTRP)

99 RETURN $ END

$ EZZ = 23747.7595

FUNCTION PVTF(T,D,M)

C IBUTANE 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,DF,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

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)

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 $

12 F = B*XB + E*XE $ Fl = B*XB1 + E*XE1 $

13 PVTF = PS + RG*(T-TS) + GKT*F $ FRT=F/S2

14 DPDT = RG + GK*F1 $ D2PDT2 = GK*F2/TC ; 15 BD = (2*B1 + 4*B2*S2)*S*DSDR

$ THETA=THETAF(D)

E = E1*SM*XP

$ F2 = B*XB2 + E*XE2

$ DFRTDT=F1/S2/TC

IF(M) 15,30

43
16 XPl = -IX*GA*SX/S $ SMI = (SN+SR)*S2 + V

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)

QVAP = A1*X + (XE-X)*(A2 + A3*X + A4*X2 +

X # (TC-T)/(TC-TT), XE # X**E.

DIMENSION AQ(4)

DATA (NFQ=4),(EQ=0.43),(TTRP=113.55),(TCRT=407.85)

DATA (AQ = 28.117144, 32.239895, -3.0186000, -3.3534669)

FORMATdHO 9X *T EXCEEDS TCRT IN QVAPXF{T).

IF(TCRT-T) 3,4,5

PRINT 1 $ STOP

QVAPXF = $ RETURN

XN = TCRT - TTRP $ X F = $ DO 7 K=2,NFQ

F = F + AQ(K)*X**(K-2)

Q = AQ(1)*X + (XE-X)*F

/ )

= (TCRT-T)/XN $ XE = X**EQ

12

3

4

56

79

10 QVAPXF = Q*1000 $ RETURN % END

SUBROUTINE SIMPLE

FOR ANY GIVEN T,K AND P,MPA, CONVERT TO P,BAR, AND USE SUBROUTINE

THERMO (OR ENTRIES THEREIN) TO GET THERMOPHYSICAL PROPERTIES.

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 5X1HU 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)

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 = 110 + 10*J

22 CALL THERMO $ IW = W $ Z = P/DEN/R/T

GET DIEL. CONST., AND FUGACITIES.

25 GIB = H-EZZ-HZ -T*(S-SZ) $ FOP = EXP(GIB/GJ/T)*PA/P

26 IF(T.GT.450) 27,28

27 DIE = $ GO TO 30

28 DIE = DIELF{DEN,T,P)

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

FUNCTION SSATF(T)

IBUTANE SATLIQ ENTROPY, J/MOL/K.

CONSTRAINED AT TRIPLE AND CRITICAL POINTS.

44
C Y # (S-SCRT)/(STRP-SCRT), X # (TC-T)/(TC-TT)

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

DIMENSION AS(7)

DATA (NFS=7),(ES=0.39),(TTRP=113.55),(TCRT=407.85)

DATA (STRP = 108. 80035), (SCRT = 278.16100)

DATA (AS = 0.1513538214, -0.7213490782, 0.5916513456,

1 -0.8071403525, -0.6495769380, 1.563590395, -0.9190175694)

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

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 /6/ 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(60) ,TSA(60) ,PSA(60) ,DLT(60) ,DPT(60) ,DPD(60)

DATA (G=0. 083145), (WM=58. 1243)

4 FORMATdHl 13X ^PROPERTIES OF SATURATED LIQUID IBUTANE* //

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 6X5HMPA/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 IBUTANE * //

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 = 52 $ PRINT 4

121 DO 150 J=1,NP $ IF{J.EQ.l) 122,123

122 T = TTRP $ GO TO 139

123 IF(J.EQ.23) 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 = 127 VG = VL = 1.0/DCRT $ ZG = ZCRT $ GO TO 141

128 T = 100 + 10*J

129 IF(J.GT.IO) T = 150 + 5*J

139 DSA(J) = DL = DENLIQF(T) $ 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

45
147 PSA(J) = PS = PSAT $ Z = PS/DL/G/T

148 PS=PS/10 S DPSDT=DPSDT/10 S DPDT=DPDT/10 S DPDD=DPDD/10

149 DL=DL*WM $ DG=DG*WM $ DDlDT=DDLDT*WM S DPDD = DPDD/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 PRINT 11 S DO 180 J=1,NP $ T = TSA(J) $ P = PSA(J)

161 CALL COEXIST $ DL = DEN S IW = W 162 DIEL = DIELF(DL,T,P) S 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 GJ = lOO^G S XP = EXP(GIBS/GJ/T) S 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 S 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 TORT.

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,PCRT, DGAT,OTRP,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/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 = TORT. * / ) 10 IF(T-TCRT) 11,20,25

C SUBCRITICAL ISOTHERMS.

11 PM = PMELTF(T) S IF(P.GE.PM) 12,13

12 PRINT 1 S CALL COMPRLQ S TI=T $ CALL IDEAL $ RETURN

13 PS = PSATF(T) S IF(P-PS) 14,15,16

14 CALL GENEOUS $ RETURN

15 PRINT 2 S RETURN

16 CALL COMPRLQ $ TI = T $ CALL IDEAL S RETURN

C THE CRITICAL ISOTHERM.

20 CALL GENEOUS S IF(DEN.LT.DCRT) RETURN

21 CP = CV = W = S 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) S PM = PMELTF(T) S CALL COMPRLQ

41 TI = T $ CALL IDEAL S 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

46
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 = FINDTSFiP) $ CALL COEXIST $ DEN=DMG $ 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,

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/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.

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

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 = $ 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 = DENLIQFCT)

47
11 DD = D - DC $ IF(ABS(Dn/D).LT.1.0E-7) 25,12

12 DT = DD/DDSDT S IF( ABS(DT/T) .LT.l .OE-7) 25,13

13 T = T + DT S IF(T) 14,14,15

14 T = TTRP S GO TO 13

15 IF(T.LT.TCRT) 18,16

16 T = TCRT - 0.05

18 IF{K.EQ.l) PRINT 2, DC, DD , DDSDT, DT, T 20 CONTINUE S K = K+1 S IF(K.NE.l) STOP

21 PRINT 1, DEN S GO TO 4

25 TSATF = T S DTSDR = DTRP/DDSDT S RETURN

30 TSATF = TCRT S DTSDR = S RETURN S 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/3/0PDT,D2P0T2,DPSDT,DPMDT,DPDD,DPDR, DTSDR, DTHDR, DDSDT

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

COMMON/6/ TSAT, THETA, PSAT

1 B = BE S BN = 1-P S A = BN + SORT(PN)

2 TC=TCRT $ TS=TSAT $ X=T/TC S XS=TS/TC $ XS1=DTSDR/TC

3 U = X**B S Ul = B*U/X $ U2 = -BN*U1/X

4 US = XS**B $ USl = B*US*XS1/XS

5 V = 1-TS/T S VIR = -DTSDR/T S VIX = TS/T/X S V2X = -2*V1X/X

6 P = EXP(A*V) $ PI = A*P $ P2 = A*P1

7 PIR = P1*V1R S PIX = Pl^VlX S P2X = P1*V2X + °2*V1X*V1X

8 XBF = U*"^ - US S XPl = U*D1X + 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 - (Vi-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,DPDR, DTSDR, DTHDR, DDSDT

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

COMMON/6/ TSAT, THETA, PSAT

1 E = ET $ EK = E/(E-1) $ TC = TCRT

2 TS = TSAT $ TH = THETA S X = T/TC

3 V! = 1.0 - TH/T $ IF(W) 30,30,4

4 CONTINUE

5 WIR = -DTHDR/T S WIX = TH/T/X $ W2X = -2*W1X/X

6 WE = W**E S WEI = E*WE/W S WEIR = WE1*W1R

7 WEIX = WE1*W1X $ WE2X = WE1*W2X + ( E-1)*WE1*W1X*W1X/W

8 H = 1 - EK*(W-WE/E) S HIR = -EK*( WIR-WEIR/E)

9 HIX = -EK*(W1X-WE1X/E) $ H2X = -EK*(W2X-WE2X/E)

10 WS = 1.0 - TH/TS S IF(WS) 11,11,12 J

11 HS = 1 $ HSl = $ GO TO 16 '

12 WSl = (TH*nTSDR/TS - DTHDR) /TS

13 WSE = WS**E S WSEl = E*WSE*WS1/WS j

48
14 HS = 1 - EK*{WS-WSE/E) $ HSl = -EK*(WS1-WSE1/E)

16 U = 1.0/HS $ UlR = -U*HS1/HS

17 P = H*U $ OXEDR = H*U1R + H1R*IJ

18 XEl = H1X*U $ XE2 = H2X*1J $ XEF = P - 1 $ RETURN

30 XEF = XEl = XE2 = DXEDR =0 $ RETURN $ END

49
1 1 1 /

I

(0 i/

Q- /

S /

o / m /

0)

c

0.

eg o

^rf ^^^ - 3

^ - n

o \\

j2 \

\

-

**c 1 o

^ J

i 0. ^ CO

/ o ^

/

0-?

"^

i^i .

1

o

o

CO

o

o

o M

o 0) "^ 3^irf CO^

0)

a

o

o E

CO 0)

O)c

ro

4->13O

«/)

CD

TO

CD

5-

4->

IT3 s_GJCl

-M

1 >~. +J

•r—COc

cu D

o

o

CVJ

O)

So

o

GO

O

o

o

o

CO

o

o

o

o

o

o

CO

o o

o o CVJ To

CUJ/B)| 'A^jSUeQ

50
o

o

o

o

o

4-) :3O

00

o

o

^ Q. o (0 ^-o

0) CO a =3

(J E

o

0) 1— o 1- D- o • CO

C7)

o

o

OCM

edI/V 'd

51
oo

inoo

fa ^ o

00o ^ o *« 0) 1— ^ Q. 3 o oo (0 5

CO 0) M- a O E

C/l =3U o o H 1—1 Q.• CO o 13 o

CMOOO^

edI/V 'd

52
Table 1. Comparisons of vapor pressure data with eq (2). Data sources and ID numbers: (l)Aston, (2)Beattie, (3)Connolly, (4)Dana, (5)Morris, (6)Sage,

Diff.

(7)Wackher, (8)Gi II i land, (9)Gilmour, (lO)Waxman, (80)Thermal Loops.

Weight

80

80

8080

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

80

1010

1010

1010

1010

1010

10

101010

1010

.078 .080

.087

.094

.102

.110

.118

.126

.135

.144

.154

.164 .174

.184 .195

.206

.217 .229

.240

.253 .265

.278

.291 .304

.318 .332

.346

.361 .376

.391 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

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

0.000

Temp.

K T/Tc

113.550 .27841

115.000 .28197

120.000 .29423

125.000 .30649

130.000 .31874

135.000 .33100

140.000 .34326

145.000 .35552

150.000 .36778

155.000 .38004

160.000 .39230

165.000 .40456

170.000 .41682

175.000 .42908

180.000 .44134

185.000 .45360

190.000 .46586

195.000 .47812

200.000 .49038

205.000 .50264

210.000 .51490

215.000 .52715

220.000 .53941 225.000 .55167

230.000 .56393

235.000 .57619

240.000 .58845

245.000 .60071

250.000 .61297

255.000 .62523

260.000 .63749

298.150 .73103

303.150 .74329

308.150 .75555

313.150 .76781

318.150 .78007

323.150 .79233

328.150 .80459

333.150 .81684

333.150 .81684

343.150 .84136

353.150 .86588

363.150 .89040

373.150 .91492

383.150 .93944

393.150 .96396

398.150 .97622

188.070 .46113

201.4 56 .49395

216.729 .53139

216.729 .53139

229.053 .56161

245.584 .60214

251.089 .61564

254.399 .62376

259.922 .63730

261.551 .64 1 29 303.150 .74329

323.150 .79233

348.150 .85362

373.150 .91492

398.150 .97622

344.260 .84408

360.930 .88496

377.590 .92581

Py(expt)

MPa .19395E-07

.28238E-07

.95543E-07

.29046E-06

.80357E-06

.20453E-05

.48345E-05

.10697E-04

.22308E-04

.441 14E-04

.83147E-04

.15007E-03

.26039E-03

.43592E-03

.70635E-03

.ni09E-02

.17000E-02

.25371 E-02

.37001 E-02

.52829E-02

.73965E-02

.10170E-01

.13752E-01

.18309E-01

.24030E-01

.31120E-01

.39805E-01

.50333E-01

.62964E-01

.77983E-01

.95684E-01

.35000E+00

.40430E+00

.46410E+00

.53040E+00

.60320E-K)0

.68360E+00

.77250E+00

.86830E+00

.86760E+00

.10867E+01

.13432E+01

.16408E+01

.19855E+01

.23819E+01

.28361 E+01 .30879E+01

.15159E-02

.42610E-02

.11579E-01

.11579E-01

.23233E-01

.52132E-01

.66405E-01

.76350E-01

.95476E-01

.10178E+00

.39932E+00

.67898E+00

.12090E+01

.19832 E+01 .30843E+01

.1 1 146E+01

.15726E+01

.21572E+01

Pa(calc)

MPa .19481E-07

.28330E-07

.95570E-07

.29002E-06

.80164E-06

.20398E-05

.48217E-05

.10671E-04

.22265E-04

.44050E-04

.83070E-04

.15000E-03

.26041E-03

.43614E-03

.70698E-03

.1 1123E-02

.17026E-02

.25415E-02

.37071 E-02

.52933E-02

.74113E-02

.10190E-01

.13777E-01

.18339E-01

.24061 E-01

.31 147E-01

.39820E-01

.50320E-01

.62903E-01

.77842E-01

.95423E-01

.35032E+00

.40435E+00

.46436E+00

. 53074 E+00

.60388E+00

.68421 E+00

.77215E+00

.86813E+00

.86813E+00

.10860E+01

.13418E+01

.16396E+01

.19842E+01

.23810E+01

.28370E+01

.30902E+01

.14490E-02

.41210E-02

.11331E-01

.11331 E-01 .22879E-01

.51677E-01

.65947E-01

.75912E-01

.95127E-01

.10146E+00

.40435E+00

.68421 E+00

.12089 E+01 .19842 E+01 .30902E+01

.1 1 125E+01

.15696E+01

.21535E+01

-.44

-.32

-.03

.15

.24 .27

.27

.24

.19 .15

.09 .04 -.01 -.05

-.09

-.12

-.15

-.17

-.19

-.20

-.20

-.20

-.18

-.16

-.13

-.09

-.04

.03

.10

.18

.27 -.09

-.01

-.06

-.06

-.11 -.09

.05

.02 -.06

.06 .10

.07

.07 .04

-.03

-.07

4.61

3.40

2.19

2.19

1.55 .88

.69 .58

.37 .32 -1.24 -.76

.00 -.05

-.19

.19 .19

.17

dPg/dT

MPa/K

.510E-08

.722E-08

.222E-07

.616E-07

.156E-06

.365E-06

.797E-06

.163E-05

.3t5E-05

.579E-05

.102E-04

.171E-04

.278E-04

.435E-04

.661E-04

.977E-04

.141E-03

.198E-03

.272E--03 .366E-03

.485E-03

.631E-03

.809E-03

.102E-02

.127 E-02

.157E-02

.191 E-02

.230E-02

.274 E-02

.324E-02

.380 E-02

.102E-01

.114E-01

.126E-01

.139E-01

.153E-01

.168E-01

.184E-01

.200E-01

.200E-01

.236E-01

.276E-01

.320E-01

.370E-01

.425E-01

.489E-01

.525 E-01

.122E-03

.29 7E-03

.689E-03

.689E-03

.122E-02

.235E-02

.285E-02

.318E-02

.379E-02

.399E-02

.114E-01

.168E-01

.256E-01

.370 E-01 .525E-01

.240E-01

.310E-01

.393E-01

53
Table 1. (Continued).

Data sources and ID numbers: (l)Aston , (2)Beattie, (3)Connolly, (4)Dana, (5)Morri s. (6)Sage,

(7)Wackher, (8)Gi 1 1 i land. (9)Gi Imour, (lO)Waxman, (80)Thermal Loops.

D Weight Temp. T/Tc P(^(expt) Pa(calc) Diff. dPg/dT

K MPa MPa % MPa/K

3 0.000 394.260 .96668 .28938E+01 .28917E+01 ,Qil .496E-01

3 0.000 406.870 .99760 .35788E+01 .35798E+01 -.03 .605E-01

3 0.000 407.770 .99980 .36325E+01 .363 50 E+01 -.07 .624E-01

4 0.000 249.140 .61086 .62090E-01 .60579E-01 2.49 .266E-02

4 0.000 255.090 .62545 .79740E-01 .78134E-01 2.06 .325E-02

4 0.000 259.310 .63580 .94580E-01 .92829E-01 1.89 .372E-02

4 0.000 261.000 ^63994 .10121E+00 .99282E-01 1.94 .392E-02

4 0.000 263.240 .64543 .1 1430E+00 .10837E+00 5.47 .419E-02

4 0.000 270.910 .66424 .14736E+00 .14443E+00 2.03 .523E-02

4 0.000 279.810 .68606 .19993E+00 .19709E+00 1.44 .664E-02

4 0.000 287.780 .70560 .2590 5E+00 .25562E+00 1.34 .808E-02

4 0.000 295.230 .72387 .32531E+00 .32137E+00 1.23 .960E-02

4 0.000 299.480 .73429 .36877E+00 .36413E+00 1.27 .105E-01

4 0.000 304.130 .74 569 .42143E+00 .41563E+00 1.39 .1 16E-01

4 0.000 309.030 .75771 .48268E+00 .47557E+00 1.49 .129E-01

4 0.000 313.070 .76761 .53782E+00 .52962E+00 1.55 .139E-01

4 0.000 317.730 .77904 .60502E+00 .59747E+00 1.26 .152E-01

4 0.000 317.730 .77904 .60462E+00 .59747E+C0 1.20 .152E-01

4 0.000 328.660 .80584 .79167E+00 .78156E+00 1.29 .185E-01

4 0.000 335.320 .82217 .91526E+00 .91240E+OG .31 .208E-01

4 0.000 345.070 .84607 .11364E+01 .11321 E+01 .38 .244E-01

4 0.000 352.640 .86463 .13395E+01 .13278 E+01 .88 .274E-01

4 0.000 352.640 .86463 .13310E+01 .13278E+01 .24 .274E-01

5 0.000 344.261 .84409 .11128E+01 .11125E+01 .03 .240E-01

5 0.000 377.594 .92582 .21567E+01 .21537E+01 .14 .393E-01

6 0.000 290.372 .71196 .27579E+00 .27722E+00 -.52 .859E-02

6 0.000 294.261 .72149 .31006E+00 .31217E+00 -.68 .939E-02

6 0.000 310.928 .76236 .49580E+00 .50043E+00 -.93 .133E-01

6 0.000 327.594 .80322 .75704E+00 .76198E+00 -.65 .ie2E-01

6 0.000 344.261 .84409 .11 107E+01 .11125E+01 -.16 .2 OE-01

6 0.000 360.928 .88495 .15810E+01 .15696E+01 .73 .3 )E-01 6 0.000 377.594 .92582 .21629E+01 .21537E+01 .43 .Z:y3E-01

6 0.000 394.261 .96668 .28937 E+01 .28917E+01 .07 .496E-01

7 0.000 206.450 .50619 .64395E-02 .58474E-02 10.13 .398E-03

7 0.000 215.150 .52752 .11172E-01 .10285E-01 8.62 .636E-03

7 0.000 228.750 .56087 .23851E-01 .22510E-01 5.96 .121 E-02

7 0.000 237.350 .58195 .36170E-01 .35012E-01 3.31 .172E-02

7 0.000 242.150 .59372 .45596E-01 .44097E-01 3.40 .207E-02

7 0.000 250.450 .61407 .65488E-01 .64147E-01 2.09 .279E-02

7 0.000 258.150 .63295 .88886E-01 .88591E-01 .33 .359E-02

7 0.000 261.250 .64055 .10106E+00 .10027E+00 .79 .395E-02

7 0.000 262.750 .64423 .10654E+00 .10633E+00 .20 .413E-02

8 0.000 352.039 .86316 .13652E+01 .131 14E+01 4.10 .271E-01

8 0.000 372.594 .91356 .19995E+01 .19637E+01 1.82 .367E-01

8 0.000 389.261 .95442 .27234E+01 .26521 E+01 2.69 .463E-01

8 0.000 403.150 .98848 .33991 E+01 .33625E+01 1.09 .566E-01

8 0.000 407.594 .99937 .36887E+01 .36241 E+01 1.78 .618E-01

9 0.000 261.400 .64092 .10133E+00 .10086E+00 .46 .397E-02

um ber of data po ints used in f it = 47; rms pressure deviation = 0.1 16^.

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

Data sources and ID numbers: (l)Beattie, (2)Carney, (3)Coffin, (5)Dana, (7)Gilmour, (8)Haynes,

(9)McClune, (lO)Morris, (ll)Orrit, (12)Sage, ( 13) S I i winski , (14)NGAA, (15)Van der Vet,

(16)Wackher, (17)Benoliel, (18)Kahre, ( 19)Rodosevich.

ID Weight Te np. (Tc-T)/(Tc-Tt) Densi ty (expt ) Dens i ty ( ca 1 c

)

Diff. dPj/dT

^< mo I/L kg/m3 kg/ Tl3 ? kg/(m3.K)

8 1.000 115 .075 .99482 12 .731 739 .95 739 .89 .01 -.9709

8 1.000 120 .075 .97783 12 .649 73 5 .21 735 .05 .02 -.9687

9 1.000 123 .150 .96738 12 .583 731 .38 732 .07 -.09 -.9675

8 1.000 125 .075 .96084 12 .569 730 .55 730 .21 .05 -.9668

9 1.000 128 .150 .95039 12 .501 726 .61 727 .24 -.09 -.9658

1 1 1.000 129 .478 .94 588 12 .483 725 .55 72 5 .95 -.06 -.9654

8 1.000 130 .075 .94385 12 .485 725 .68 725 .38 .04 -.9652

1 1 1.000 133 .032 .93380 12 .428 722 .36 722 .52 -.02 -.9645

9 1.000 133 .150 .93340 12 .420 721 .90 722 .41 -.07 -.9645

8 1.000 135 .075 .92686 12 .402 720 .83 720 .55 .04 -.9641

n 1.000 135 .728 .92464 12 .379 719 .52 719 .92 -.06 -.9640

9 1.000 138 .150 .91641 12 .341 717 .31 717 .59 -.04 -.9636

11 1.000 138 .596 .91490 12 .335 716 .95 717 .16 -.03 -.9635

8 1.000 140 .075 .90987 12 .322 716 .18 715 .74 .06 -.9634

11 1.000 141 .445 .90522 12 .294 714 .55 714 .42 .02 -.9632

9 1.000 143 .150 .89942 12 .260 712 .60 712 .77 -.02 -.9631

11 1.000 144 .033 .89642 12 .247 711 .85 71 1 .92 -.01 -.9631

8 1.000 145 .075 .89288 12 .235 71 1 .17 710 .92 .04 -.9630

11 1.000 146 .745 .88721 12 .202 709 .21 709 .31 -.01 -.9630

9 1.000 148 .130 .88250 12 .178 707 .84 707 .98 -.02 -.9630

8 1.000 150 .075 .87589 12 .153 706 .41 706 .10 .04 -.9631

1 1 1.000 152 .693 .86700 12 .106 703 .64 703 .58 .01 -.9633

9 1.000 153 .150 .86544 12 .095 703 .01 703 .14 -.02 -.9634

11 1.000 155 .443 .8 5765 12 .058 700 .87 700 .93 -.01 -.9637

11 1.000 158 .124 .84854 12 .016 698 .41 698 .35 .01 -.9641

9 1.000 158 .150 .8484 5 12 .013 698 .25 698 .32 -.01 -.9641 n 1.000 160 .760 .83959 11 .973 69 5 .90 695 .81 .01 -.9647

9 1.000 163 .150 .83146 11 .930 693 .42 693 .50 -.01 -.9653

11 1.000 163 .448 .83045 11 .928 693 .32 693 .21 .02 -.9654

1 1 1.000 166 .140 .82130 11 .884 690 .74 690 .61 .02 -.9663

9 1.000 168 .150 .81448 11 .848 688 .66 688 .67 -.00 -.9670

1 1 1.000 171 .559 .80289 11 ,793 685 44 685 .37 .01 -.9684

9 1.000 173 .150 .79749 1 1 .766 683 .89 683 .83 .01 -.9691

1 1 1.000 174 .459 .79304 11 .745 682 .64 682 .56 .01 -.9698

11 1.000 177 .042 .78426 11 .703 680 .22 680 .05 .02 -.9711

11 1.000 179 .875 .77463 1 1 .656 677 .47 677 .30 .02 -.9728

11 1.000 182 .638 .76525 11 .609 674 .74 674 .61 .02 -.9745

11 1.000 185. 429 .75576 1 1. 560 671. 94 671. 89 .01 -.9764

n 1.000 188. 223 .74627 1 1. 512 669. 10 669. 16 -.01 -.9785

11 1.000 194. 542 .72480 11. 407 663. 04 662. 96 .01 -.9839

11 1.000 199. 485 .70800 1 1. 325 658. 25 658. 08 .03 -.9887

1

1

1.000 205. 110 .68889 1 1. 225 652. 47 652. 50 -.01 -.9948

11 1.000 210. 673 .66999 1 1. 132 647. 05 646. 95 .02 -1.0017

11 1.000 216. 223 .65113 11. 033 641. 31 641. 37 -.01 -1.0093

11 1.000 221. 684 .63257 10. 937 635. 73 635. 84 -.02 -1.0176

1

1

1.000 227. 155 .61398 10. 842 630. 17 630. 25 -.01 -1.0267

8 1.000 228. 000 .61111 10 827 629. 33 629. 38 -.01 -1.0282

14 1.000 228. 428 .60966 10. 827 629. 31 628. 94 .06 -1.0290

11 1.000 229. 970 .60442 10. 790 627. 14 627. 35 -.03 -1.0318

14 1.000 232. 261 .59663 10. 756 625. 18 624. 98 .03 -1.0361

11 1.000 232. 686 .59519 10. 741 624. 30 624. 54 -o04 -1.0369

11 1.000 235. 557 .58543 10. 688 621. 24 621. 55 -.05 -1.0425

11 1.000 238. 707 .57473 10. 633 618. 02 618. 26 -.04 -1.0490

14 1.000 238. 983 .57379 10. 636 618. 21 617. 97 .04 -1.0496

11 1.000 241. 431 .56547 10. 583 615. 12 615. 39 -.04 -1.0549

11 1.000 244. 259 .55586 10. 531 612. 08 612. 40 -.05 -1.0613

14 1.000 246. 150 .54944 10. 503 610. 48 610. 39 .01 -1.0658

11 1.000 246. 962 .54668 10. 479 609. 09 609. 52 -.07 -1.0677

11 1.000 249. 415 .53835 10. 439 606. 73 606. 90 -.03 -1.0738

14 1.000 249. 817 .53698 10. 438 606. 70 606. 47 .04 -1.0748

14 1.000 255. 372 .51810 10. 336 600. 77 600. 46 .05 -1.0894

14 1.000 255. 483 .51773 10. 335 600. 71 600. 33 .06 -1.0897

7 1.000 261. 000 .49898 10. 225 594. 32 594. 28 .01 -1.1056

55
Table 2. (Continued),

Data sources and ID numbers: (DBeattie, (2)Carney, (3)Coffin, (5)Dana, (7)Gilmour, (8)Haynes,

(9)McClune, (lO)Morris, (IDOrrit, (12)Sage, ( 13)S I

i

winski , (14)NGAA, (15)Van der Vet,

(16)Wackher, ( 17)Benol iel , (18)Kahre, ( 19)Rodosevich.

ID Weight Temp. (Tc-T)/(Tc-Tt) Density (expt) Density (calc) Diff. dPj,/dT K mol/L kg/m3 kg/m3 % kg/(m3.K)

14 1.000 266.483 .48035 10.127 588.62 588.17 .08 -1.1227

14 1.000 277 . 1 50 .44410 9.913 576.19 576.00 .03 -1.1604

18 1.000 277.550 .44275 9.901 575.50 575.54 -.01 -1.1619

13 1.000 283.200 .42355 9.782 568.55 568.91 -.06 -1.1847

8 1.000 288.706 .40484 9.668 561.92 562.32 -.07 -1.2089

14 1.000 288.706 .40484 9.679 562.59 562.32 .05 -1.2089

18 1.000 288.750 .40469 9.680 562.65 562.27 .07 -1.2091

8 1.000 290.000 .40044 9.641 560.38 560.75 -.07 -1.2149

13 1.000 293.190 .38960 9.578 556.72 556.85 -.02 -1.2303

•2 1.000 299.817 .36708 9.438 548.60 548.59 .00 -1.2648

14 1.000 299.817 .36708 9.438 548.58 548.59 -.00 -1.2648

8 1.000 300.000 .36646 9.430 548.11 548.35 -.04 -1.2658

13 1.000 303.150 .35576 9.363 544.23 544.34 -.02 -1.2837

14 1.000 310.928 .32933 9.196 534.51 534.17 .06 -1.3323

18 1.000 310.950 .32926 9.194 534.40 534.14 .05 -1.3324

13 1.000 313.120 .32188 9.138 531.13 531.23 -.02 -1.3472

13 1.000 323.120 .28790 8.899 517.25 517.39 -.03 -1.4239

13 1.000 333.110 .25396 8.649 502.69 502.71 -.01 -1.5175

13 1.000 343.080 .22008 8.380 487.08 487.02 .01 -1.6346

13 1.000 353.090 .18607 8.087 470.02 469.94 .02 -1.7866

13 1.000 363.110 .15202 7.761 451.10 451.06 .01 -1.9927

13 1.000 368.100 .13507 7.582 440.71 440.79 -.02 -2.1263

0.000 303.150 .35576 9.445 548.98 544.34 .85 -1.2837

0.000 323.150 .28780 8.912 518.00 517.35 .13 -1.4241

0.000 348.150 .20285 8.258 479.99 478.56 .30 -1.7063

0.000 373.150 .11791 7.364 428.03 429.65 -.38 -2.2927

0.000 398.150 .03296 6.073 352.99 351.40 .45 -4.8156

2 0.000 227.594 .61249 10.841 630.10 629.79 .05 -1.0275

2 0.000 233.150 .59361 10.743 624.40 624.06 .05 -1.0378

2 0.000 238.706 .57473 10.643 618.60 618.26 .05 -1.0490

2 0.000 244.261 .55586 10.541 612.70 612.40 .05 -1.0613

2 0.000 249.817 .53698 10.438 606.70 606.47 .04 -1.0748

2 0.000 255.372 .51810 10.337 600.80 600.46 .06 -1.0894

2 0.000 266.483 .48035 10.127 588.60 588.17 .07 -1.1227

2 0.000 277.150 .44410 9.913 576.20 576.00 .03 -1.1604

2 0.000 288.706 .40484 9.679 562.60 562.32 .05 -1.2089

2 0.000 310.928 .32933 9.195 534.50 534.17 .06 -1.3323

2 0.000 322.039 .29158 8.945 519.90 518.92 .19 -1.4148

2 0.000 333.150 .25382 8.663 503.50 502.65 .17 -1.5179

3 0.000 245.350 .55216 10.548 613.10 611.24 .30 -1.0639

3 0.000 252.450 .52803 10.417 605.48 603.63 .31 -1.0816

3 0.000 257.350 .51138 10.331 600.48 598.30 .37 -1.0949

3 0.000 259.550 .50391 10.288 597.98 595.88 .35 -1.1013

3 0.000 261.950 .49575 10.249 595.72 593.23 .42 -1.1084

3 0.000 264.650 .48658 10.192 592.40 590.22 .37 -1.1168

3 0.000 266.950 .47876 10.149 589.90 587.65 .38 -1.1242

3 0.000 267.650 .47638 10.139 589.32 586.86 .42 -1.1265

3 0.000 270.450 .46687 10.077 585.72 583.69 .35 -1.1360

3 0.000 271.850 .46211 10.056 584.50 582.10 .41 -1.1409

3 0.000 273.850 .45532 10.015 582.11 579.81 .40 -1.1481

3 0.000 277.450 .44309 9.956 578.69 575.65 .53 -1 .1615

3 0.000 281.650 .42881 9.856 572.87 570.74 .37 -1.1783

3 0.000 284.850 .41794 9.791 569.10 566.95 .38 -1.1917

3 0.000 285.650 .41522 9.776 568.22 565.99 .39 -1.1952

3 0.000 293.350 .38906 9.619 559.10 556.65 .44 -1.2311

3 0.000 298.450 .37173 9.514 552.99 550.31 .49 -1.2574

5 0.000 273.150 .45770 10.013 582.00 580.61 .24 -1.1455

5 0.000 28 1 . 1 50 .43051 9.858 572.99 571.33 .29 -1.1762

5 0.000 289.150 .40333 9.686 562.99 561.78 .22 -1.2110

5 0.000 297.150 .37615 9.514 552.99 551.94 .19 -1.2505

5 0.000 305.150 .34896 9.342 543.00 541.76 .23 -1.2956

5 0.000 313.150 .32178 9.170 533.00 531.19 .34 -1.3475

56
Table 2. (Continued).

Data sources and ID numbers: (l)Beattie, (2)Carney, (3)Coffin, (5)Dana, (7)Gllmour, (8)Haynes,

(9)McClune, (lO)Morris, (ll)Orrit, (12)Sage, ( 13)Sllwmski , (14)NGAA, (15)Van der Vet,

(16)Wackher, ( 17)Benol i el , (18)Kahre, ( 19)Rodosevich.

ID Weight Temp. (Tc-T)/(TcrTt) Density (expt) Density (calc) Diff. dPj/dT

K mol/L kg/m3 kg/m3 % kg/(m3.K)

5 0.000 321.150 .29460 8.981 522.01 520.18 .35 -1.4076

5 0.000 329.150 .26741 8.792 511.03 508.64 .47 -1.4780

10 0.000 310.928 .32933 9.245 537.35 534.17 .60 -1.3323

10 0.000 344.261 .21607 8.392 487.77 485.08 .55 -1.6504

10 0.000 377.594 .10281 7.254 421.65 419.07 .62 -2.4759

11 0.000 150.360 .87492 12.162 706.90 705.83 .15 -.9631

12 0.000 294.261 .38596 9.626 559.50 555.53 .72 -1.2356

12 0.000 310.928 .32933 9.245 537.36 534.17 .60 -1.3323

12 0.000 327.594 .27270 8.839 513.76 510.93 .55 -1.4634

12 0.000 344.261 .21607 8,389 487.60 485.08 .52 -1.6504

12 0.000 360.928 .15944 7.861 456.92 455.35 .34 -1.9417

12 0.000 377.594 .10281 7.254 421.63 419.07 .61 -2.4759

14 0.000 322.039 .29158 8.945 519.92 518.92 .19 -1.4148

14 0.000 333.150 .25382 8.662 503.47 502.65 .16 -1.5179

15 0.000 283.150 .42372 9.798 569.50 568.97 .09 -1.1845

15 0.000 288.710 .40483 9.686 563.00 562.31 .12 -1.2089

15 0.000 293.150 .38974 9.592 557.50 556.90 .11 -1.2301

15 0.000 298.150 .37275 9.485 551.30 550.69 .11 -1.2558

15 0.000 303.150 .35576 9.377 545.00 544.34 .12 -1.2837

15 0.000 308.150 .33877 9.266 538.60 537.84 .14 -1.3142

15 0.000 313.150 .32178 9.155 532.10 531.19 .17 -1.3475

15 0.000 318.150 .30479 9.038 525.30 524.37 .18 -1.3839

15 0.000 323.150 .28780 8.917 518.30 517.35 .18 -1.4241

16 0.000 223.650 .62589 10.923 634.86 633.83 .16 -1.0207

16 0.000 233.650 .59191 10.748 624.71 623.54 .19 -1.0387

16 0.000 243.650 .55793 10.566 614.15 613.05 .18 -1.0599

16 0.000 253.650 .52396 10.382 603.44 602.33 .18 -1.0847

16 0.000 263.650 .48998 10.185 591.99 591.34 .11 - 1 . 1 1 37

16 0.000 273.150 .45770 9.995 580.96 580.61 .06 -1.1455

17 0.000 213.150 .66157 11.093 644.77 644.47 .05 -1.0050

17 0.000 223.150 .62759 10.909 634.08 634.34 -.04 -1.0199

17 0.000 233.150 .59361 10.732 623.79 624.06 -.04 -1.0378

17 0.000 243.150 .55963 10.553 613.39 613.58 -.03 -1.0588

17 0.000 253.150 .52565 10.367 602.57 602.87 -.05 -1.0834

17 0.000 263.150 .49168 10.176 591.47 591.90 -.07 -1.1121

17 0.000 273.150 .45770 9.982 580.20 580.61 -.07 -1.1455

17 0.000 283.150 .42372 9.786 568.80 568.97 -.03 -1.1845

17 0.000 293.150 .38974 9.586 557.18 556.90 .05 -1.2301

18 0.000 299.850 .36697 9.438 548.60 548.54 .01 -1.2650

18 0.000 327.550 .27285 8.776 510.10 511.00 -.18 -1.4630

19 0.000 114.000 .99847 12.754 741.29 740.94 .05 -.9715

19 0.000 115.000 .99507 12.741 740.53 739.97 .08 -.9710

19 0.000 120.000 .97808 12.665 736.12 735.12 .14 -.9687

Number of data points used in fit = 85; rms density deviation = 0.038^.

57
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59
Table 4. Comparisons of second virial coefficients with eq (5)

Data sources and ID numbers: (l)Beattie, (2)Gunn, (3)Jessen, (4)Kretschmer,

(5)Morris, (6)Sage, (7)Strein, (8)Connolly.

D Weigtit Temp.

K T/Tc B cm^/mo

1

B^-Cexpt) B^(calc) Diff. Diff.

%

3 1.000 273.16 .670 -889.00 -3.432 -3.356 -.075 -2.25

7 1.000 296.10 .726 -691.00 -2.667 -2.755 .088 3.19

3 1.000 303.16 .743 -699.00 -2.698 -2.602 -.097 -3.71

4 1.000 303.16 .743 -644.00 -2.486 -2.602 .116 4.45

7 1.000 308.10 .755 -634.00 -2.447 -2.501 .054 2.17

6 1.000 327.60 .803 -541.34 -2.090 -2.156 .067 3.09

7 1.000 333.90 .819 -532.50 -2.055 -2.059 .004 .18

6 1.000 344.27 .844 -524.24 -2.024 -1.913 -.111 -5.80

7 1.000 353.90 .868 -476.70 -1.840 -1.790 -.050 -2.82

7 1.000 373.90 .917 -427.60 -1.651 -1.567 -.083 -5.32

2 1.000 410.90 1.007 -310.60 -1.199 -1.246 .047 3.80

5 1.000 410.94 1.008 -329.72 -1.273 -1.246 -.027 -2.14

1 1.000 423.16 1.038 -289.38 -1.117 -1.160 .043 3.68

5 1.000 444.27 1 .089 -256.50 -.990 -1.028 .038 3.71

2 1.000 444.30 1.089 -267.80 -1.034 -1.028 -.006 -.55

1 1.000 448.16 1.099 -253.65 -.979 -1.006 .027 2.69

1 1.000 473.16 1.160 -223.20 -.862 -.878 .016 1.84

2 1.000 477.60 1.171 -230.20 -.889 -.857 -.032 -3.68

5 1.000 477.60 1.171 -223.06 -.861 -.857 -.004 -.46

1 1.000 498.16 1.221 -197.06 -.761 -.769 .008 1.07

2 1.000 510.90 1.253 -191.60 -.740 -.720 -.020 -2.77

5 1.000 510.94 1.253 -191.28 -.738 -.719 -.019 -2.62

1 1.000 523.16 1.283 -174.14 -.672 -.676 .003 .52

1 1.000 548.16 1.344 -153.27 -.592 -.595 .003 .58

1 1.000 573.16 1.405 -133.76 -.516 -.525 .008 1.61

6 0.000 294.27 .722 -620.77 -2.396 -2.797 .401 14.33

5 0.000 310.94 .762 -585.29 -2.259 -2.446 .187 7.65

8 0.000 344.26 .844 -457.20 -1.765 -1.913 .148 7.74

2 0.000 344.30 .844 -414.00 -1.598 -1.912 .314 16.43

8 0.000 360.93 .885 -412.70 -1.593 -1.707 .114 6.66

6 0.000 360.94 .885 -502.65 -1.940 -1.707 -.234 -13.70

8 0.000 377.59 .926 -374.00 -1.444 -1.530 .087 5.67

2 0.000 377.60 .926 -358.00 -1.382 -1.530 .148 9.70

6 0.000 377.60 .926 -488.54 -1.886 -1.530 -.355 -23.23

8 0.000 394.26 .967 -34 1 . 1 -1.317 -1.378 .062 4.47

6 0.000 394.27 .967 -466.83 -1.802 -1.378 -.424 -30.75

7 0.000 394.60 .968 -384.00 -1.482 -1.375 -.107 -7.77

8 0.000 406.87 .998 -318.30 -1.229 -1.277 .048 3.76

8 0.000 410.93 1.008 -311.50 -1.202 -1.246 .044 3.51

7 0.000 413.80 1.015 -349.90 -1.351 -1.225 -.126 -10.25

7 0.000 433.80 1.064 -320.00 -1.235 -1.091 -.144 -13.23

8 0.000 444.26 1.089 -259.60 -1.002 -1.028 .026 2.55

7 0.000 453.60 1.112 -291.80 -1.126 -.976 -.150 -15.37

7 0.000 470.20 1.153 -267.20 -1.031 -.892 -.140 -15.65

7 0.000 494.00 1.21 1 -243.40 -.940 -.786 -.154 -19.56

Number of data points = 25; rms deviation = 2.99$.

60
Table 5. Behavior of coef ficients of equation of state for isobutane (eq (6)).

P/Pc To e Pa B(p) C{p)

K K MPa

.10 333.276 314.002 .8707 .46833 -.49855

.20 363.148 348.267 1.6395 .47330 -.42041

.30 380.115 369.609 2.2547 .48159 -.34720

.40 390.935 384.095 2.7305 .49320 -.27939

.50 398.060 394.014 3.0854 .50813 -.21733

.60 402.711 400.610 3.3377 .52637 -.16131

.70 405.592 404.698 3.5035 .54793 -.11152

.80 407.153 406.887 3.5970 .57280 -.06805

.90 407.761 407.728 3.6344 .60099 -.03090

1.00 407.850 407.850 3.6400 .63250 0.00000

1.10 407.776 407.743 3.6354 .66733 .02483

1.20 407.319 407.053 3.6072 .70547 .04381

1.30 406.183 405.288 3.5385 .74693 .05725

1.40 404.123 402.015 3.4180 .79170 .06551

1.50 400.946 396.871 3.2399 .83979 .06900

1.60 396.500 389.562 3.0046 .89120 .06817

1.70 390.674 379.876 2.7182 .94593 .06349

1.80 383.391 367.681 2.3913 1.00397 .05547

1.90 374.601 352.937 2.0384 1.06533 .04460

2.00 364.276 335.691 1.6760 1 . 1 3000 .03141

2.10 352.405 316.086 1.3214 1.19800 .01638

2.20 338.997 294.353 .9912 1.26930 .00000

2.30 324.074 270.814 .6999 1.34393 -.01726

2.40 307.679 245.874 .4584 1.42187 -.03498

2.50 289.878 220.006 .2730 1.50313 -.05274

2.60 270.764 193.741 .1437 1.58771 -.07020

2.70 250.463 167.641 .0642 1.67560 -.08703

2.80 229.136 142.271 .0230 1.76681 -.10295

2.90 206.978 118.167 .0061 1.86133 -.11772

3.00 184.208 95.805 .0010 1.95917 -.13116

3.10 161.062 75.565 .0001 2.06033 -.14312

3.20 137.775 57.713 .0000 2.16481 -.15350

3.30 114.567 42.389 .0000 2.27260 -.16222

3.40 91.631 29.609 .0000 2.38371 -.16926

61
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62
Table 7. Comparisons of experimental P-p-T data of isobutane

with eq (6).

Summary of P-P-T data comparisons.

Range of Data No. of PointsDevi at

Ap/p, rms

ions

Authors T(K) P(MPa) P( kg/m3

)

AP/P, mean

(1) {%)

Beattie [3) 423-573 2.6 - 30.8 58-465 75 0.71 0.39

Morris [421 311-511 0.7 - 34.5 10-593 171 1.00 4.74

Sage (501 294-394 0.07- 20.7 1-593 164 0.93 7.26 Waxman (63,641 378-448 0.3 - 20.8 6-458 35 0.83 0.42

Haynes [271 120-300 1.7 - 34.7 551-749 156 0.04 3.82

Virial equation

(this report) 270-570 0.11- 0.24 2.9 31 0.49 0.46

Total number of points used in fit = 480

Overall rms density deviation = 0.56^

Overall mean pressure deviation = 2.15?

53
Table 7. (Continued).

Data sources and ID numbers: (l)Virial Equat ion, (2)Bea-htie, (3)M(Drris, (4)Siage, (10)Wcixman. (XXXX)Halynes.

D Data Weight Temp. Density Density Dens ity °expt Pcalc Pressure

Point ex P+ calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa %

10 1 1.000 377.594 .100 5.81 5.85 -.64 .3022 .3003 .62

10 2 1.000 377.594 .200 11.62 11.66 -.32 .5814 .5796 .30

10 3 1.000 377.594 .300 17.44 17.44 .01 .8382 .8383 -.01

10 4 1.000 377.594 .400 23.25 23.19 .24 1.0733 1.0755 -.20

10 5 1.000 377.594 .500 29.06 28.96 .36 1.2874 1.2911 -.29

10 6 1.000 377.594 .600 34.87 34.73 .41 1.4809 1.4855 -.31

10 7 1.000 377.594 .700 40.69 40.51 .42 1.6545 1.6593 -.29

10 8 1.000 394.261 .100 5.81 5.85 -.64 .3166 .3147 .62

10 9 1.000 394.261 .200 11.62 11.66 -.33 .6114 .6096 .30

10 10 1.000 394.261 .300 17.44 17.44 .01 .8850 .8851 -.01

10 11 1.000 394.261 .400 23.25 23.19 .24 1.1382 1.1406 -.21

10 12 1.000 394.261 .500 29.06 28.95 .38 1.3717 1.3760 -.31

10 13 1.000 394.261 .600 34.87 34.72 .45 1.5861 1.5917 -.35

10 14 1.000 394.261 .700 40.69 40.50 .47 1.7822 1.7884 -.34

10 15 1.000 394.261 .800 46.50 46.29 .45 1 .9607 1 .9669 -.31

10 16 1.000 394.261 .900 52.31 52.10 .41 2.1223 2.1280 -.27

10 17 1.000 394.261 1.000 58.12 57.92 .36 2.2677 2.2726 -.21

10 18 1.000 394.261 1.100 63.94 63.76 .27 2.3978 2.4015 -.15

10 19 1.000 394.261 1.200 69.75 69.61 .20 2.5128 2.5154 -.10

10 20 1.000 394.261 1.300 75.56 75.48 .11 2.6139 2.6153 -.05

10 21 1.000 423.150 .100 5.81 5.85 -.65 .3417 .3395 .64

10 22 1.000 423.150 .200 11.62 11.67 -.39 .6635 .6610 .37

10 23 1.000 423.150 .300 17.44 17.45 -.09 .9661 .9653 .09

10 24 1.000 423. 150 .400 23.25 23.22 .12 1.2501 1.2515 -.11

10 25 1.000 423.150 .500 29.06 28.99 • .27 1.5163 1.5198 -.23

10 26 1.000 423.150 .600 34.87 34.75 .35 1.7653 1.7704 -.29

10 27 1.000 423.150 .700 40.59 40.52 .40 1.9977 2.0041 -.32

10 28 1.000 423.150 .800 46.50 46.30 .43 2.2144 2.2217 -.33

10 29 1.000 423.150 .900 52.31 52.08 .45 2.4159 2.4238 -.32

10 30 1.000 423.150 1.000 58.12 57.86 .46 2.6030 2.6113 -.32

10 31 1.000 423.150 1.100 63.94 63.64 .46 2.7764 2.7848 -.30

10 32 1.000 423.150 1.200 69.75 69.43 .46 2.9367 2.9452 -.29

10 33 1.000 423.150 1.300 75.56 75.22 .45 3.0847 3.0931 -.27

10 34 1.000 423.150 1.400 81.37 81.01 .45 3.2210 3.2293 -.26

10 35 1.000 423.150 1.500 87.19 86.80 .45 3.3464 3.3544 T.24

10 36 1.000 423.150 1.600 93.00 92.59 .44 3.4615 3.4693 -.23

10 37 1.000 423.150 1.700 98.81 98.37 .45 3.5669 3.5746 -.21

10 38 1.000 423.150 1.800 104.62 104.15 .46 3.6634 3.6710 -.21

10 39 1.000 423.150 1.900 110.44 109.91 .47 3.7515 3.7591 -.20

10 40 1.000 423.150 2.000 116.25 115.67 .50 3.8320 3.8397 -.20

10 41 1.000 423.150 2.100 122.06 121.41 .53 3.9054 3.9132 -.20

10 42 1.000 423.150 2.200 127.87 127.15 .57 3.9723 3.9803 -.20

10 43 1.000 423.150 2.300 133.69 132.86 .61 4.0333 4.0416 -.21

10 44 1.000 423.150 2.400 139.50 138.58 .66 4.0891 4.0977 -.21

10 45 1.000 423.150 2.500 145.31 144.28 .71 4.1401 4.1489 -.21

10 46 1.000 423.150 2.664 154.83 153.66 .75 4.2153 4.2239 -.20

10 47 1.000 423.150 3.035 176.41 174.52 1.07 4.3519 4.3627 -.25

10 48 1.000 423.150 3.375 196.17 193.16 1.53 4.4522 4.4675 -.34

10 49 1.000 423.150 3.931 228.49 222.11 2.79 4.5997 4.6340 -.74

10 50 1.000 423.150 4.237 246.24 238.40 3.18 4.6898 4.7368 -.99

10 51 1.000 423.150 4.425 257.21 249.07 3.16 4.7545 4.8087 -1.13

10 52 1.000 423.150 4.743 275.71 270.36 1.94 4.9091 4.9561 -.95

10 53 1.000 423.150 5.405 314.14 310.07 1.29 5.4031 5.4801 -1.41

10 54 1.000 423.150 6.010 349.32 347.01 .66 6.4265 6.5212 -1.45

10 55 1.000 423.150 7.000 406.85 405.68 .29 10.8398 10.9855 -1.33

10 56 1.000 423.150 7.543 438.43 437.40 .24 15.9822 16.1982 -1.33

10 57 1.000 423.150 7.878 457.91 457.16 .16 20.7503 20.9602 -1.00

10 58 1.000 448.150 .100 5.81 5.85 -.64 .3632 .3609 .62

10 59 1.000 448.150 .200 11.62 11.67 -.40 .7080 .7053 .38

10 60 1.000 448.150 .300 17.44 17.46 -.12 1.0350 1.0338 .11

10 61 1.000 448.150 .400 23.25 23.23 .10 1.3448 1.3460 -.09

10 62 1.000 448.150 .500 29.06 28.99 .24 1 .6383 1.6417 -.21

10 63 1.000 448.150 .600 34.87 34.76 .33 1.9159 1.9213 -.28

64
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (2)Beattie, (3)Morris, (4)Sage, ( 10) Waxman,

(XXXX)Haynes.

D Data Weight Temp. Density Densi ty Densi ty °expt ^calc Pressure

Point ex P+ calc Diff. Diff.

No. K mol/L kg/nr> kg/m^ % MPa MPa %

10 64 1.000 448.150 .700 40.69 40.53 .39 2.1783 2.1854 -.32

10 65 1.000 448.150 .800 46.50 46.29 .44 2.4263 2.4348 -.35

10 66 1.000 448.150 .900 52.31 52.06 .48 2.6603 2.6702 -.37

10 67 1.000 448.150 1.000 58.12 57.83 .51 2.8812 2.8922 -.38

10 68 1.000 448.150 1.100 63.94 63.59 .54 3.0895 3.1015 -.39

10 69 1.000 448.150 1.200 69.75 69.36 .56 3.2859 3.2988 -.39

10 70 1.000 448.150 1.300 75.56 75.12 .58 3.4710 3.4846 -.39

10 71 1.000 448.150 1.400 81.37 80.89 .59 3.6455 3.6597 -.39

10 72 1.000 448.150 1.500 87.19 86.66 .60 3.8101 3.8247 -.38

10 73 1.000 448.150 1.600 93.00 92.43 .61 3.9654 3.9802 -.37

10 74 1.000 448.150 1.700 98.81 98.21 .61 4.1120 4.1268 -.36

10 75 1.000 448.150 1.800 104.62 104.00 .60 4.2507 4.2652 -.34

10 76 1.000 448.150 1.897 110.25 109.57 .61 4.3769 4.3918 -.34

10 77 1.000 448.150 1.897 110.27 109.57 .63 4.3769 4.3922 -.35

10 78 1.000 448.150 2.524 146.71 145.84 .59 5.0598 5.0738 -.28

10 79 1.000 448.150 2.826 164.25 163.28 .59 5.3276 5.3417 -.26

10 80 1.000 448.150 3.378 196.32 194.78 .78 5.7698 5.7912 -.37

10 81 1.000 448.150 3.378 196.36 194.78 .80 5.7698 5.7916 -.38

10 82 1.000 448.150 4.495 261.25 257.06 1.60 6.7568 6,8389 -1.20

10 83 1.000 448.150 5.032 292.48 288.87 1.24 7.4805 7.5813 -1.33

10 84 1.000 448.150 6.014 349.58 347.89 .48 10.0243 10.1365 -1.11

10 85 1.000 448.150 6.015 349.64 347.89 .50 10.0242 10.1405 -1.15

65
Data sources and ID numbers;

Table 7. (Continued)

(l)Virial Equation, (2)3eattie, (3)Morris, (4)Sage, (lO)Waxman,

(XXXX)Hay nes.

D Data Weight Temp. Density Density Dens i ty '^expt Pcalc Pressure

Point ex P+ calc Diff. Diff.

No. K mol/L kg/m-J kg/m^ % MPa MPa %

2 85 1.000 423.150 .999 58.08 57.89 .32 2.6041 2.6098 -.22

2 87 1.000 448.150 .999 58.08 57.87 .36 2.8827 2.8905 -.27

2 88 1.000 473.150 .999 58.08 57.85 .39 3.1542 3.1639 -.31

2 89 i.OOO 498.150 .999 58.08 57.88 .33 3.4228 3.4322 -.27

2 90 1.000 523.150 .999 58.08 57.91 .29 3-6872 3.6964 -.25

2 91 1.000 548 . 1 50 .999 58.08 57.96 .20 3.9507 3.9576 -.18

2 92 1.000 573.150 .999 58.08 57.92 .27 4.2060 4.2163 -.24

2 93 1.000 423.150 1.499 87.12 86.91 .23 3.3488 3.3530 -.13

2 94 1 .000 448.150 1.499 87.12 86.76 .41 3.8129 3.8227 -.26

2 95 1.000 473.150 1.499 87.12 86.68 .50 4.2617 4.2767 -.35

2 96 1.000 498.150 1.499 87.12 86.76 .41 4.7055 4.7199 -.30

2 97 1.000 523.150 1.499 87.12 86.84 .32 5.1422 5.1551 -.25

2 98 1.000 548.150 1.499 87.12 86.94 .20 5.5749 5.5842 -.17

2 99 1.000 573.150 1.499 87.12 87.02 .11 6.0025 6.0084 -.10

2 100 1.000 423.150 1.998 116.15 115.83 .28 3.8341 3.8384 -.11

2 lOi 1.000 448.150 1.998 116.15 115.69 .40 4.5079 4.5176 -.21

2 102 1.000 473.150 1.998 116.15 115.87 .25 5.1645 5.1726 -.16

2 103 1.000 498.150 1.998 116,15 115.90 .22 5.8029 5.8118 -.15

2 104 1.000 523.150 1.998 1 16.15 115.98 .15 6.4321 6.4395 -.12

2 105 1.000 548.150 1.998 116.15 116.15 .00 7.0583 7.0585 -.00

2 106 1.000 573.150 1.998 1 16.15 116.28 -.11 7.6774 7.6704 .09

2 107 1.000 423.150 2.498 145.19 144.63 .39 4.1432 4.1479 -.11

2 108 1.000 448.150 2.498 145.19 144.68 .35 5.0409 5.0492 -.16

2 109 1.000 473.150 2.498 145.19 144.83 .25 5.9133 5.9220 -.15

2 110 1.000 498.150 2.498 145.19 145.13 .05 6.7746 6.7767 -.03

2 1 11 1.000 523.150 2.498 145.19 145.30 -.07 7.6227 7.6184 .06

2 112 1.000 548.150 2.498 145.19 145.59 -.27 8.4687 8.4500 .22

2 113 1.000 573.150 2.498 145.19 145.82 -.43 9.3077 9.2734 .37

2 1 14 1.000 423.150 2.998 174.23 172.79 .83 4.34 18 4.3502 -.19

2 1 15 1.000 448.150 2.998 174.23 173.60 .36 5.4756 5.4845 -.16

2 1 16 1.000 473.150 2.998 174.23 174.00 .13 6.5882 6.5934 -.08

2 117 1.000 498.150 2.998 174.23 174.47 -.14 7.6936 7.6861 .10

2 118 1.000 523.150 2.998 174.23 174.75 -.30 8.7879 8.7670 .24

2 119 1.000 548.150 2.998 174.23 175.11 -.50 9.8812 9.8383 .44

2 120 1.000 573.150 2.998 174.23 175.39 -.66 10.9684 10.9016 .61 2 121 1.000 423.150 3.497 203.27 200.17 1.52 4.4877 4.5032 -.35

2 122 1.000 448.150 3.497 203.27 201.87 .69 5.8687 5.8885 -.34

2 123 uooo 473.150 3.497 203.27 202.70 .28 7.2458 7.2594 -.19

2 124 1.000 498.150 3.497 203.27 203.40 -.06 8.6248 8.6204 .05

2 125 1.000 523 . 1 50 3.497 203.27 203.81 -.26 9.9967 9.9732 .24

2 126 1.000 548.150 3.497 203.27 204.32 -.52 1 1.3758 11.3189 .50

2 127 1.000 573.150 3.497 203.27 204.65 -.68 12.7467 12.6580 .70

2 128 1.000 423.150 3.997 232.31 225.99 2.72 4.6204 4.6551 -.74

2 129 1.000 448.150 3.997 232.31 229.40 1.25 6.2771 6.3236 -.73

2 130 1.000 473.150 3.997 232.31 230.88 .62 7.9560 7.9949 -.49

2 131 1.000 498.150 3.997 232.31 231.85 .20 9.6482 9.6659 -.18

2 132 1.000 523.150 3.997 232.31 232.46 -.07 1 1.3423 11.3345 .07

2 133 1.000 548.150 3.997 232.31 233.09 -.34 13.0486 12.9997 .38

2 134 1.000 573.150 3.997 232.31 233.56 -.54 14.7539 14.6606 .54

2 135 1.000 423.150 4.496 261.35 253.37 3.05 4.7825 4.3383 -1.15

2 136 1.000 448.150 4.496 261.35 257.51 1.47 6.7655 6.8408 -1.10

2 137 1.000 473.150 4.496 261.35 259.27 .80 8.7980 8.8669 -.78

2 138 1.000 498.150 4.496 261.35 260.46 .34 10.8620 10.9038 -.38

2 139 1.000 523.150 4.496 261.35 261.16 .07 12.9341 12.9455 -.09

2 140 1.000 548.150 4.496 261.35 261.92 -.22 15.0316 14.9881 .29

2 141 1.000 573.150 4.496 261.35 262.40 -.40 17.1239 17.0291 .56

2 142 1.000 423.150 4.996 290.39 283.79 2.27 5.0359 5.1 105 -1.46

2 143 1.000 448.150 4.996 290.39 287.04 1.15 7.4312 7.5223 -1.21

2 144 1.000 473.150 4.996 290.39 288.53 .64 9.8964 9.9774 -.81

2 145 1.000 498.150 4.996 290.39 289.55 .29 12.4042 12.4545 -.40

2 146 1.000 523.150 4.996 290.39 290.23 .05 14.9313 14.9431 -.08

2 147 1.000 548.150 4.996 290.39 290.92 -.19 17.4877 17.4366 .29

2 148 1.000 573.150 4.996 290.39 291.42 -.36 20.0472 19.9309 .58

66
Table 7. (Continued)

Data sources and ID numbers: (l)Virial Equation, (2)Beattie, (3)Morris, (4)Sage, (lO)Waxman,

(XXXX)Haynes.

ID Data Weight Temp. Density Density Density expt ca 1 c Pressure

Point ex P+ calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ MPa MPa %

2 149 1.000 423.150 5.995 348.46 346.13 .67 6.3916 6.4854 -1.45

2 150 1.000 448.150 5.995 348.46 347.08 .40 9.9714 10.0620 -.90

2 151 1.000 473.150 5.995 348.46 347.73 .21 13.6323 13.6986 -.48

2 152 1,000 498,150 5.995 348.46 348.33 .04 17.3519 17.3675 -.09

2 153 1.000 523.150 5.995 348.46 348.66 -.06 21.0807 21.0531 .13

2 154 1.000 548 . 1 50 5.995 348.46 349.25 -.23 24.8763 24.7455 .53

2 155 1.000 423.150 6.994 406.54 405.42 .28 10.8073 10.9462 -1.27

2 156 1.000 448.150 6.994 406.54 406.05 .12 16.2566 16.3352 -.48

2 157 1.000 473.150 6.994 406.54 406.27 .07 21.7058 21.7591 -.24

2 158 1.000 498.150 6.994 406.54 406.81 -.07 27.2615 27.1971 .24

2 159 1.000 423.150 7.993 464.62 464.07 .12 22.7687 22.9385 -.74

2 160 1.000 448.150 7.993 464.62 464.1

1

.1 1 30.7815 30.9631 -.59

67
Tab le 7. (Conti nued)

Data sources and ID numbers:

(XXXX)Haynes.

(l)Virial Equation, (2)Beattie, (3)Morris, (4)Sage, (lO)Waxman,

) Data Weight Temp. Dens ity Dens ity Density '^expt Pcalc Pressure

Point ex P+ calc Diff. Diff.

No. K mol/L kg/rrH kg/m^ % MPa MPa %

4 161 .020 294.261 .029 1.67 1.68 -.63 .0689 .0685 .62

4 162 .020 294.261 .043 2.47 2.49 -.79 .1013 .1006 .76

4 163 .020 294.261 .058 3.40 3.43 -.88 .1379 .1367 .85

4 164 .020 294.261 .090 5.21 5.25 -.78 .2068 .2053 .73

4 165 .020 294.261 .123 7.12 7.16 -.46 .2758 .2746 .42

4 166 .020 294.261 9.677 562.45 558.36 .73 1.7237 3.8857 -55.64

4 167 .020 294.261 9.735 565.82 561.64 .74 3.4474 5.7846 -40.40

4 168 .020 294.261 9.794 569.24 564.75 .79 5.1711 7.8135 -33.82

4 169 .020 294.261 9.846 572.29 567.72 .80 6.8948 9.7178 -29.05

4 170 .020 294.261 9.896 575.17 570.55 .80 8.6184 11.5969 -25.68

4 171 .020 294.261 9.949 578.28 573.26 .87 10.3421 13.7247 -24.65

4 172 .020 294.261 10.000 581.22 575.87 .92 12.0658 15.8230 -23.75

4 173 .020 294.261 10.051 584.19 578.38 .99 13.7895 18.0352 -23.54

4 174 .020 294.261 10.095 586.76 580.80 1.02 15.5132 20.0262 -22.54

4 175 .020 294.261 10.136 589.13 583.13 1.02 17.2369 21.9315 -21.41

4 176 .020 294.261 10.173 591.31 585.39 1.00 18.9606 23.7328 -20.11

4 177 .020 294.261 10.211 593.50 587.59 1.00 20.6843 25.6023 -19.21

4 178 .020 310.928 .027 1.57 1.58 -.55 .0689 .0686 .54

4 179 .020 310.928 .040 2.33 2.35 -.65 .1013 .1007 .63

4 180 .020 310.928 .055 3.20 3.22 -.75 .1379 .1369 .72

4 181 .020 310.928 .084 4.89 4.92 -.67 .2068 .2055 .63

4 182 .020 310.928 .114 6.64 6.67 -.43 .27 58 .2747 .40

4 183 .020 310.928 .146 8.48 8.49 -.11 .3447 .3444 .10

4 184 .020 310.928 .179 10.42 10.39 .28 .4137 .4147 -.25

4 185 .020 310.928 9.292 540.07 537.25 .52 1.7237 2.8947 -40.45

4 186 .020 310.928 9.367 544.48 541.35 .57 3.4474 4.8510 -28.93

4 187 .020 310.928 9.438 548.58 545.17 .62 5.1711 6.8081 -24.05

4 188 .020 310.928 9.503 552.36 548.75 .65 6.8948 8.7337 -21.06

4 189 .020 310.928 9.566 556.00 552.14 .69 8.6184 10.701-19.46

4 190 .020 310.928 9.623 559.30 555.35 .71 10.3421 12.5828 -17.81

4 191 .020 310.928 9.680 562.64 558.41 .75 12.0658 14.5860 -17.28

4 192 .020 310.928 9.735 565.82 561.34 .79 13.7895 16.5888 -16.87

4 193 .020 310.928 9.787 568.84 564.13 .83 15.5132 18.5755 -16.49

4 194 .020 310.928 9.835 571.68 566.82 .85 17.2369 20.5300 -16.04

4 195 .020 310.928 9.878 574.14 569.41 .82 18.9606 22.2857 -14.92

4 196 .020 310.928 9.928 577.03 571.90 .89 20.6843 24.4325 -15.34

4 197 .020 327.594 .026 1.49 1.50 -.41 .0689 .0687 .40

4 198 .020 327.594 .038 2.21 2.22 -.50 .1013 .1008 .49

4 199 .020 327.594 .052 3.03 3.04 -.57 .1379 .1371 .55

4 200 .020 327.594 .079 4.61 4.63 -.49 .2068 .2059 .47

4 201 .020 327.594 .107 6.25 6.26 -.30 .2758 .2750 .28

4 202 .020 327.594 .137 7.94 7.95 -.04 .3447 .3446 .04

4 203 .020 327.594 .167 9.70 9.68 .24 .4137 .4146 -.22

4 204 .020 327.594 .231 13.46 13.34 .85 .5516 .5557 -.75

4 205 .020 327.594 .302 17.56 17.32 1.37 .6895 .6974 -1.14

4 206 .020 327.594 8.890 516.72 514.12 .50 1.7237 2.5519 -32.45

4 207 .020 327.594 8.989 522.45 519.40 .58 3.4474 4.5233 -23.79

4 208 .020 327.594 9.077 527.62 524.22 .64 5.1711 6.4808 -20.21

4 209 .020 327.594 9.159 532.35 528.65 .69 6.8948 8.4352 -18.26

4 210 .020 327.594 9.229 536.45 532.78 .69 8.6184 10.2568 -15.97

4 211 .020 327.594 9.292 540.07 536.64 .64 10.3421 11.9674 -13.58

4 212 .020 327.594 9.358 543.92 540.27 .67 12.0658 13.8992 -13.19

4 213 .020 327.594 9.419 547.45 543.71 .68 13.7895 15.7748 -12.59

4 214 .020 327.594 9.477 550.84 546.97 .70 15.5132 17.6710 -12.21

4 215 .020 327.594 9.533 554.08 550.08 .72 17.2369 19.5749 -11.94

4 216 .020 327.594 9.582 556.97 553.05 .70 18.9606 21.3510 -11.20

4 217 .020 327.594 9.636 560.09 555.90 .75 20.6843 23.3504 -1 1.42

4 218 .020 344.261 .024 1.42 1.42 -.30 .0689 .0687 .29

4 219 .020 344.261 .036 2.10 2.10 -.39 .1013 .1009 .38

4 220 .020 344.261 .049 2.87 2.88 -.41 .1379 .1373 .40

4 221 .020 344.261 .075 4.37 4.38 -.30 .2068 .2062 .29

4 222 .020 344.261 .102 5.90 5.91 -.16 .2758 .2754 .15

4 223 .020 344.261 .129 7.49 7.48 .11 .3447 .3451 -.11

68
Table 7. (Continued)

Data sources and ID numbers:

(XXXX)Haynes.

(l)Virial Equation, (2)3eattie, (3)Morris, (4)Sage, (lO)Waxman,

Data Weight Temp. Density- Dens ity Density pexpt Pcalc Pressure

Point ex P+ calc Diff. Diff.

No. K mol/L kg/m-^ kg/m^ p MPa MPa %

4 224 .020 344.261 .157 9.11 9.08 .34 .4137 .4150 -.31

4 225 .020 344.261 .216 12.53 12.43 .81 .5516 .5556 -.73

4 226 .020 344.261 .279 16.20 15.99 1.27 .6895 .6972 -1.10

4 227 .020 344.261 .365 21.19 20.84 1.69 .8618 .8739 -1.38

4 228 .020 344.261 .461 26.77 26.28 1.86 1.0342 1 .0488 -1.39

4 229 .020 344.261 8.441 490.61 487.92 .55 1.7237 2.3396 -26.33

4 230 .020 344.261 8.572 498.24 495.12 .63 3.4474 4.2744 -19.35

4 231 .020 344.261 8.683 504.68 501.43 .64 5.1711 6.1399 -15.78

4 232 .020 344.261 8.780 510.30 507.08 .63 6.8948 7.9591 -13.37

4 233 .020 344.261 8.870 515.56 512.21 .65 8.6184 9.8268 -12.30

4 234 .020 344.261 8.951 520.25 516.93 .64 10.3421 11.6378 -11.13

4 235 .020 344.261 9.033 525.02 521.31 .71 12.0658 13.6298 -11.47

4 236 .020 344.261 9.104 529.19 525.39 .72 13.7895 15.4938 -11.00

4 237 .020 344.261 9.168 532.88 529.23 .69 15.5132 17.2528 -10.08

4 238 .020 344.261 9.229 536.45 532.85 .67 17.2369 19.0472 -9.50

4 239 .020 344.261 9.292 540.07 536.28 .70 18.9606 20.9653 -9.56

4 240 .020 344.261 9.361 544.11 539.55 .84 20.6843 23.2281 -10.95

4 241 .020 360.928 .023 1.35 1.35 -.26 .0689 .0688 .25

4 242 .020 360.928 .034 2.00 2.00 -.28 .1013 .1010 .28

4 243 .020 360.928 .047 2.73 2.74 -.28 .1379 .1375 .27

4 244 .020 360.928 .071 4.15 4.16 -.16 .2068 .2065 .16

4 245 .020 360.928 .096 5.60 5.60 .02 .2758 .2758 -.02

4 246 .020 360.928 .122 7.09 7.07 .26 .3447 .3456 -.25

4 247 .020 360.928 .148 8.61 8.57 .48 .4137 .4156 -.46

4 248 .020 360.928 .203 11.77 11.67 .87 .5516 .5560 -.80

4 249 .020 360.928 .260 15.11 14.93 1.22 .6895 .6970 -1.09

4 250 .020 360.928 .337 19.58 19.26 1.61 .8618 .8739 -1.38

4 251 .020 360.928 .420 24.43 23.96 1.92 1.0342 1.0506 -1.56

4 252 .020 360.928 .511 29.71 29.14 1.92 1.2066 1.2244 -1.46

4 253 .020 360.928 .612 35.56 34.99 1.59 1.3790 1.3944 -1.11

4 254 .020 360.928 .726 42.22 41.82 .95 1.5513 1.5605 -.59

4 255 .020 360.928 7.876 457.80 456.46 .29 1.7237 1.9150 -9.99

4 256 .020 360.928 8.056 468.24 467.28 .21 3.4474 3.6209 -4.79

4 257 .020 360.928 8.222 477.88 476.07 .38 5.1711 5.5653 -7.08

4 258 .020 360.928 8.351 485.41 483.56 .38 6.8948 7.3596 -6.32

4 259 .020 360.928 8.477 492.72 490.13 .53 8.6184 9.3568 -7.89

4 260 .020 360.928 8.580 498.71 496.01 .54 10.3421 11.1908 -7.58

4 261 .020 360.928 8.675 504.20 501.36 .56 12.0658 13.0455 -7.51

4 262 .020 360.928 8.763 509.33 506.27 .60 13.7895 14.9337 -7.66

4 263 .020 360.928 8.839 513.74 510.83 .57 15.5132 16.6840 -7.02

4 264 .020 360.928 8.916 518.23 515.07 .61 17.2369 18.5915 -7.29

4 265 .020 360.928 8.986 522.28 519.06 .62 18.9606 20.4299 -7.19

4 266 .020 360.928 9.054 526.23 522.83 .65 20.6843 22.3278 -7.36

4 267 .020 377.594 .022 1.29 1.29 -.18 .0689 .0688 .17

4 268 .020 377.594 .033 1.91 1.91 -.18 .1013 .1011 .18

4 269 .020 377.594 .045 2.61 2.61 -.16 .1379 .1377 .16

4 270 .020 377.594 .068 3.95 3.96 -.03 .2068 .2068 .03

4 271 .020 377.594 .092 5.33 5.32 .15 .2758 .2762 -.14

4 272 .020 377.594 .116 6.73 6.71 .36 .3447 .3459 -.34

4 273 .020 377.594 .140 8.16 8.12 .54 .4137 .4158 -.51

4 274 .020 377.594 .191 11.12 11.02 .90 .5516 .5562 -.84

4 275 .020 377.594 .244 14.20 14.04 1.18 .6895 .6970 -1.08

4 276 .020 377.594 .314 18.26 17.99 1.49 .8618 .8733 -1.31

4 277 .020 377.594 .389 22.59 22.20 1.73 1.0342 1.0497 -1.47

4 278 .020 377.594 .468 27.21 26.71 1.81 1.2066 1.2246 -1.47

4 279 .020 377.594 .554 32.18 31.61 1.78 1.3790 1.3981 -1.37

4 280 .020 377.594 .648 37.67 37.00 1.79 1.5513 1.5717 -1.30

4 281 .020 377.594 .755 43.90 43.03 1.99 1.7237 1.7469 -1.33

4 282 .020 377.594 .878 51.03 49.96 2.11 1.8961 1.9204 -1.27

4 283 .020 377.594 1.022 59.42 58.28 1.91 2.0684 2.0891 -.99

4 284 .020 377.594 7.493 435.52 433.23 .53 3.4474 3.7031 -6.91

4 285 .020 377.594 7.728 449.20 446.80 .53 5.1711 5.5316 -6.52

4 286 .020 377.594 7.910 459.77 457.34 .53 6.8948 7.3470 -6.16

69
Table 7. (Continued)

Data sources and ID numbers:

(XXXX)Haynes.

(DVirial Equation, (2)Beattie, (3)Morris, (4)Sage, (lO)Waxman,

D Data Weight Temp. Density Dens ity Dens ity ^expt Pcalc Pressure

Point ex pt calc Diff. Diff.

No. K rrol/L kg/mJ kg/m^ MPa MPa

4 287 .020 377.594 6.049 467.83 466.07 .38 8.6184 8.9998 -4.24

4 288 .020 377.594 8.178 475.33 473.60 .36 10.3421 10.7700 -3.97

4 289 .020 377.594 8.308 482.92 480.25 .55 12.0658 12.8133 -5.83

4 290 .020 377.594 8.407 488.67 486.23 .50 13.7895 14.5398 -5.16

4 291 .020 377.594 8.503 494.24 491.68 .52 15.5132 16.3758 -5.27

4 292 .020 377.594 8.591 499.33 496.70 .53 17.2369 18.1944 -5.26

4 293 .020 377.594 .8.677 504.36 501.36 .60 18.9606 20.1381 -5.85

4 294 .020 377.594 8.743 508.20 505.71 .49 20.6843 21.7231 -4.78

4 295 .020 394.261 .021 1.24 1.24 -.10 .0689 .0689 .10

4 296 .020 394.261 .031 1.82 1.83 -.10 .1013 .1012 .10

4 297 .020 394.261 .043 2.49 2.50 -.07 .1379 .1378 .07

4 298 .020 394.261 .065 3.78 3.77 .08 .2068 .2070 -.08

4 299 .020 394.261 .087 5.09 5.07 .26 .2758 .2765 -.25

4 300 .020 394.261 .110 6.42 6.39 .42 .3447 .3461 -.41

4 301 .020 394.261 .134 7.77 7.72 .64 .4137 .4162 -.61

4 302 .020 394.261 .182 10.55 10.45 .97 .5516 .5567 -.91

4 303 .020 394.261 .231 13.43 13.27 1.22 .6895 .6974 -1.13

4 304 .020 394.261 .296 17.18 16.93 1.48 .8618 .8735 -1.33

4 305 .020 394.261 .363 21.12 20.77 1.64 1 .0342 1 .0493 -1.44

4 306 .020 394.261 .434 25.21 24.83 1.50 1.2066 1.2221 -1.27

4 307 .020 394.261 .511 29.71 29.14 1.92 1.3790 1 .4009 -1.57

4 308 .020 394.261 .592 34.43 33.75 2.00 1.5513 1.5760 -1.57

4 309 .020 394.261 .681 39.57 38.71 2.17 1.7237 1.7521 -1.62

4 310 .020 394.261 .778 45.24 44.12 2.46 1.8961 1.9296 -1.74

4 311 .020 394.261 .886 51.49 50.09 2.72 2.0684 2.1063 -1.80

4 312 .020 394.261 1.141 66.30 64.50 2.72 2.4132 2.4496 -1.49

4 313 .020 394.261 1.474 85.66 85.68 -.02 2.7579 2.7576 .01 4 314 .020 394.261 6.702 389.55 384 . 1 5 1.39 3.4474 3.7067 .00

4 315 .020 394.261 7.112 413.38 410.84 .61 5.1711 5.4005 - .25

4 316 .020 394.261 7.388 429.45 427.17 .53 6.8948 7.1852 -4,04

4 317 .020 394.261 7.596 441.52 439.40 .48 8.6184 8.9607 -3.82

4 318 .020 394.261 7.765 451.35 449.33 .45 10.3421 10.7313 -3.63

4 319 .020 394.261 7.903 459.38 457.77 .35 12.0658 12.4224 -2.87

4 320 .020 394.261 8.032 466.87 465.15 .37 13.7895 14.2230 -3.05

4 321 .020 394.261 8.146 473.50 471.73 .37 15.5132 16.0070 -3.08

4 322 .020 394.261 8.239 478.88 477.69 .25 17.2369 17.5992 -2.06

4 323 .020 394.261 8.334 484.38 483.15 .25 18.9606 19.3700 -2.11

4 324 .020 394.261 8.420 489.41 488.19 .25 20.6843 21.1224 -2.07

70
Data sources and

(XXXX)Haynes.

Table 7. (Continued)

D numbers: (l)Virial Equation, (2)Beattie, (3)iMorris, (4)Sage, {10)Waxman,

ID Data Weight Temp, Density Density Density ^expt Pcalc Pressure

Point ex pt calc Diff, Diff,

No. K mol/L kg/nr^ kg/m^ 10 MPa MPa %

1301 325 1.000 120,000 12,884 748.89 749.04 -,02 34.7208 34.3216 1,16

1302 326 1.000 120.000 12,862 747.60 747.75 -,02 31.2775 30.8871 1.26

1303 327 1.000 120,000 12,840 746.29 746.44 -,02 27.8345 27.4387 1,44

1304 328 1.000 120,000 12,817 744,97 745.11 -,02 24,3914 24.0384 1,47 1305 329 1.000 120.000 12.794 743,63 743,76 -,02 20,9480 20.6117 1,63

1306 330 1.000 120.000 12.771 742,29 742.40 -,01 17.5050 17.2339 1,57

1307 331 1.000 120,000 12,748 740,95 741.01 -,01 14.0618 13,9045 1,13

1308 332 1.000 120.000 12.725 739.61 739,60 ,00 10.6189 10,6369 -,17

1309 333 1.000 120.000 12.706 738.51 738,46 ,01 7.8644 7,9868 -1.53

1310 334 1.000 120,000 12.686 737.36 737,30 .01 5.1102 5,2578 -2,81

1311 335 1.000 120.000 12.671 736.52 736,43 ,01 3,0443 3,2570 -6,53

1312 336 1.000 120.000 12.662 735.97 735,84 ,02 1.6672 1,9786 -15,74

1701 337 1.000 130.000 12.735 740.21 740,34 -,02 34.7197 34,3905 .96 1702 338 1.000 130,000 12.71

1

738.81 738,97 -.02 31.2765 30.8714 1,31 1703 339 1.000 130,000 12.687 737.39 737,57 -.02 27.8330 27.3908 1,61 1704 340 1.000 130.000 12.662 735.99 736,16 -.02 24.3898 23,9770 1,72 1705 341 1.000 130.000 12,638 734.58 734,72 -.02 20.9465 20.6147 1,61 1706 342 1.000 130.000 12,614 733,17 733,26 -.01 17.5035 17.3032 1,16 1707 343 1.000 130.000 12,589 731.74 731,78 -.01 14.0603 13,9753 .61 1708 344 1.000 130,000 12.565 730.30 730,27 .00 10.6174 10,6993 -.77

1709 345 1.000 130,000 12.545 729.14 729,04 ,01 7,8629 8,0842 -2.74

1710 346 1.000 130.000 12.525 727.98 727.80 ,02 5,1086 5,5023 -7.16

1711 347 1.000 130.000 12.509 727.08 726.86 .03 3.0428 3,5367 -13.97

1712 348 1.000 130.000 12.499 726.47 726,22 .03 1.6657 2,1951 -24.12

1401 349 1.000 140,000 12.587 731.59 731.72 -.02 34.7206 34,3981 .94 1402 350 1.000 140,000 12.560 730.06 730.26 -.03 31.2773 30,81 18 1.51 1403 351 1.000 140,000 12.535 728,60 728.78 -.02 27.8337 27,4179 1.52 1404 352 1.000 140,000 12.510 727.13 727.27 -.02 24.3905 24,0648 1.35

1405 353 1.000 140,000 12.485 725.66 725.74 -.01 20.9471 20,7654 .88 1406 354 1.000 140.000 12.462 724.35- 724.18 .02 17.5039 17,8757 -2,08

1407 355 1.000 140.000 12.435 722.78 722.59 .03 14,0607 14,4502 -2.70

1408 356 1.000 140,000 12.407 721,15 720,98 .02 10.6179 10.9735 -3.24

1409 357 1.000 140,000 12.385 719,87 719,67 .03 7.8631 8.2857 -5.10

1410 358 1.000 140,000 12.363 718,59 718,33 .04 5.1089 5.6362 -9.36

1411 359 1.000 140.000 12.346 717,61 717,32 .04 3.0429 3.6267 -16.10

1412 360 1.000 140,000 12.335 716,97 716,64 .05 1.6658 2,3307 -28 . 53

1501 361 1.000 140,000 12.583 731,35 731,72 -.05 34.7188 33,8330 2.62

1502 362 1,000 140.000 12.560 730,02 730,26 -.03 31.2755 30.7168 1.82

1503 363 1.000 140,000 12.534 728,55 728,78 -.03 27.8319 27.3111 1.91 1504 364 1.000 140,000 12.509 727,08 727,27 -.03 24.3887 23.9597 1.79 1505 365 1.000 140,000 12.483 725,59 725,74 -.02 20.94 53 20.6102 1.63

1506 366 1.000 140,000 12.458 724,10 724,18 -.01 17.5022 17.3154 1.08

1507 367 1.000 140,000 12,432 722,58 722,59 -,00 14.0590 14.0247 .24 1508 368 1.000 140,000 12.405 721,00 720,98 ,00 10.6161 10.6661 -.47

1509 369 1.000 140,000 12.383 719,75 719,67 ,01 7.8616 8.0433 -2.26

1510 370 1.000 140,000 12.361 718,50 718,33 .02 5.1073 5.4450 -6.20

1511 371 1.000 140,000 12.345 717,56 717,32 .03 3.0416 3.5322 -13.89

1512 372 1.000 140,000 12.334 716,92 716,64 .04 1.6645 2.2368 -25.59

1601 373 1.000 160,000 12.293 714,54 714.68 -.02 34.7211 34.4251 .86 1602 374 1.000 160,000 12.265 712,91 713.04 -.02 31.2776 31.0150 .85 1603 37 5 1.000 160,000 12.236 711,23 71 1.37 -.02 27.8341 27.5477 1.04 1604 376 1.000 160,000 12,207 709,55 709,66 -.02 24.3910 24.1572 .97 1605 377 1.000 160,000 12.178 707,81 707,93 -,02 20.9476 20.7277 1.06

1606 378 1.000 160.000 12.148 706,09 706.15 -,01 17.5045 17.3762 .74 1607 379 1.000 160,000 12.117 704,30 704.35 -,01 14.0613 13.9808 .58

1608 380 1.000 160,000 12.086 702,50 702.50 -,00 10.6184 10,6116 .06 1609 381 1.000 160,000 12.062 701,08 700.99 ,01 7.8639 8.0173 -1.91

1610 382 1.000 160.000 12.037 699,65 699.46 ,03 5.1097 5.4553 -6.34

1611 383 1.000 160,000 12.018 698,54 698.29 .04 3.0438 3.4875 -12.72

1612 384 1.000 160,000 12.005 697,80 697.50 .04 1.6667 2.1831 -23.65

1901 38 5 1.000 160.000 12.298 714,82 714,68 .02 34.7198 35.0282 -.88

1902 386 1.000 160,000 12.270 713,16 713,04 .02 31,2765 31,5226 -.78

1903 387 1.000 160,000 12.242 711.54 71 1,37 .02 27.8330 28,1885 -1.26

71
Data sources and

(XXXX)Haynes.

Table 7. (Continued)

D numbers: (l)Virial Equation, (2)Beattie, (3)Morris, (4)Sage, (lO)Waxman,

ID Data Weight Temp. Dens ity Dens ity Dens ity '^expt Pcalc Pressure

Point ex P"^ calc Diff. Diff.

No. K mol/L kg/np kg/m^ % MPa MPa %

1904 388 1.000 160.000 12.212 709.82 709.66 .02 24.3899 24.7043 -1.27

1905 389 1.000 160.000 12.182 708.05 707.93 .02 20.9465 21.1841 -1.12

1906 390 1.000 160.000 12.151 706.27 706.15 .02 17.5034 17.7342 -1.30

1907 391 1.000 160.000 12.121 704.50 704.35 .02 14.0602 14.3534 -2.04

1908 392 1.000 160.100 12.096 703.05 702.78 .04 11.3059 11.8038 -4.22

1909 393 1.000 160.000 12.070 701.54 701.37 .02 8.5513 8.8632 -3.52

1910 394 1.000 160.000 12.045 700.09 699.85 .03 5.7971 6.2351 -7.02

1911 395 1.000 160.000 12.025 698.93 698.58 .04 3.7314 4.1645 -10.40

1912 396 1.000 160.000 12.006 697.82 597.50 .05 1.6655 2.2135 -24.76

2001 397 1.000 180.000 12.011 698.14 597.85 .04 34.7205 35.2598 -1.53

2002 398 1.000 180.000 1 1.980 696.32 696.01 .04 31.2771 31.8445 -1.78

2003 399 1.000 180.000 11.948 694.45 694.13 .05 27.8336 28.4148 -2.05

2004 400 1.000 180.000 11.915 692.53 592.21 .05 24.3905 24.9549 -2.30

2005 401 1.000 180.000 1 1.880 690.51 690.24 .04 20.9472 21.4092 -2.15

2006 402 1.000 180.000 1 1.844 688.44 688.23 .03 17.5041 17.8578 -1.98

2007 403 1.000 180.000 11.808 686.35 685.17 .03 14.0509 14.3540 -2.04

2008 404 1.000 180.000 11.779 684.66 684.49 .03 1 1.3065 1 1.5943 -2.48

2009 405 1.000 180.000 11.749 682.93 582.76 .02 8.5521 8.8071 -2.90

2010 406 1.000 180.000 11.720 581.19 681.01 .03 5.7978 6.0781 -4.61

2011 407 1.000 180.000 11.697 579.89 679.65 .03 3.7322 4.0714 -8.33

2012 408 1.000 180.000 1 1.674 678.53 678.30 .03 1 .6663 2.0179 -17.42

2101 409 1.000 200.000 11.725 681.48 68 1 . 1

9

.04 34.7199 35.2246 -1.43

2102 410 1.000 200.000 11.689 579.39 679.12 .04 31.2756 31.7098 -1.37

2103 41 1 1.000 200.000 11.652 677.29 677.01 .04 27.8331 28.2803 -1.58

2104 412 1.000 200.000 11.615 675.08 674.84 .04 24.3899 24.7705 -1.54

2105 413 1.000 200.000 11.576 572.84 572.62 .03 20.9455 21.2897 -1.61

2106 414 1.000 200.000 11.535 670.50 570.33 .03 17.5035 17.7552 -1.42

2107 415 1.000 200.000 11.494 668.06 567.98 .01 14.0603 14.1779 -.83

2108 416 1.000 200.000 11.460 665.10 666.04 .01 11.3061 11.3930 -.75

2109 417 1.000 200.000 1 1.426 564.13 564.06 .01 8.5516 8.6514 -1.15

2110 418 1.000 200.000 11.392 662.14 652.03 .02 5.7974 5.9463 -2.50

2111 419 1.000 200.000 1 1.365 650.58 660.47 .02 3.7317 3.8801 -3.83

2112 420 1.000 200.000 11.338 558.98 558.88 .02 1 .6559 1.8028 -7.59

2201 421 1.000 220.000 11.443 565.12 664.63 .07 34.7200 35.4580 -2.08

2202 422 1.000 220.000 1 1.400 662.62 552.32 .05 31.2767 31.7175 -1.39

2203 423 1.000 220.000 11.359 550.21 559.94 .04 27.8332 28.2211 -1.37

2204 424 1.000 220.000 11.316 657.76 657.49 .04 24.3901 24.7609 -1.50

2205 425 1.000 220.000 11.272 655.16 654.97 .03 20.9467 21.2082 -1.23

2206 426 1.000 220.000 11.225 652.45 652.36 .01 17.5037 17.6254 -.69

2207 427 1.000 220.000 11.177 649.64 649.66 -.00 14.0605 14.0395 .15 2208 428 1.000 220.000 1 1 . 1 38 647.35 547.43 -.01 11.3062 11.2159 .81 2209 429 1.000 220.000 11.098 645.03 545.14 -.02 8.5517 8.4271 1.48 2210 430 1.000 220.000 11.056 542.61 542.77 -.03 5.7974 5.6097 3.35

2211 431 1.000 220.000 11.024 640.78 640.95 -.03 3.7318 3.5412 5.38

2212 432 1.000 220.000 10.993 538.95 639.08 -.02 1.5659 1.5234 9.35

2301 433 1.000 240.000 11.155 548.35 648.13 .03 34.7206 35.0189 -.85

2302 434 1.000 240.000 1 1 . 1 08 645.65 545.54 .02 31.2773 31.4237 -.47

2303 435 1.000 240.000 11.061 542.90 642.86 .01 27.8339 27.8803 -.17

2304 436 1.000 240.000 1 1.013 640.10 640.09 .00 24.3908 24.4074 -.07

2305 437 1.000 240.000 10.963 537.19 537.21 -.00 20.9474 20.9190 .14 2306 438 1.000 240.000 10.911 634.17 634.23 -.01 17.5043 17.4345 .40 2307 439 1.000 240.000 10.855 530.96 631.12 -.02 14.0611 13.8902 1.23 2308 440 1.000 240.000 10.810 528.31 628.54 -.04 11.3058 11.0633 2.20

2309 441 1.000 240.000 10.763 525.59 625.86 -.04 8.5529 8.2723 3.39

2310 442 1.000 240.000 10.715 522.80 623.09 -.05 5.7980 5.5165 5.10

2311 443 1.000 240.000 10.678 620.67 620.93 -.04 3.7323 3.4856 7.05

2312 444 1.000 240.000 10.641 618.47 618.71 -.04 1.5665 1.4535 14.65

2401 445 1.000 260.000 10.872 531.93 631.65 .04 34.7194 35.0533 -.95

2402 446 1.000 260.000 10.820 528.90 628.74 .03 31.2761 31.4728 -.53

2403 447 1.000 260.000 10.767 625.80 625.71 .01 27.8327 27.9290 -.34

2404 448 1.000 260.000 10.711 622.58 62 2.56 .00 24.3897 24.4055 -.05

2405 449 1.000 260.000 10.654 619.25 519.28 -.00 20.9464 20.9197 .13 2406 450 1.000 260.000 10.594 515.77 615.84 -.01 17.5033 17.4309 .42

72
Data sources and ID numbers:

Table 7. (Continued)

(l)Virial Equation, (2)Beattie, (3)Morris, (4)Sage, (lO)Waxman,

(:XXXX)Hcjynes.

ID Data Weight Temp. Density Dens ity Density expt Pcalc Pressure Point ex P"'" calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ % . MPa MPa %

2407 451 1.000 260.000 10.532 612.16 612.24 -.01 14.0602 13.9839 .55 2408 452 1.000 260.000 10.480 609 . 1

4

609.23 -.01 11.3060 11.2323 .66 2409 453 1.000 260.000 10.425 605.97 606.07 -.02 8.5515 8.4612 1.07 2410 454 1.000 260.000 10.368 602.60 602.78 -.03 5.7973 5.6578 2.47

2411 455 1.000 260.000 10.322 599.96 600.19 -.04 3.7317 3.5544 4.99

2412 456 1.000 260.000 10.275 597.22 597.50 -.05 1.6658 1.4496 14.91 2501 457 1.000 280.000 10.580 614.96 615.15 -.03 34.7209 34.5197 .58 2502 458 1.000 280.000 10.522 611.59 61 1.87 -.05 31.2775 30.9922 .92 2503 459 1.000 280.000 10.461 608.03 608.44 -.07 27.8340 27.4330 1.46

2504 460 1.000 280.000 10.398 604.35 604.85 -.08 24.3908 23.9175 1.98 2505 461 1.000 280.000 10.332 600.52 601.09 -.09 20.9474 20.4431 2.47

2506 462 1.000 280.000 10.263 596.52 597.11 -.10 17.5043 17.0055 2.93

2507 463 1.000 280.000 10.190 592.30 592.91 -.10 14.0611 13.5858 3.50

2508 464 1.000 280.000 10.129 588.73 589.35 -.10 11.3069 10.8430 4.28

2509 465 1.000 280.000 10.065 585.03 58 5.59 -.10 8.5523 8.1542 4.88

2510 466 1.000 280.000 9.998 581.14 581.62 -.08 5.7981 5.4829 5.75

2511 467 1.000 280.000 9.945 578.03 578.46 -.07 3.7324 3.4590 7.90

2512 468 1.000 280.000 9.889 574.76 57 5.15 -.07 1.6665 1.4338 16.23

1801 469 1.000 300.000 10.299 598.61 598.60 .00 34.7216 34.7361 -.04

1802 470 1.000 300.000 10.234 594.84 594.90 -.01 31.2783 31.2308 .15

1803 471 1.000 300.000 10.166 590.88 591.01 -.02 27.8348 27.7242 .40 1804 472 1.000 300.000 10.093 586.64 586.91 -.05 24.3916 24.1716 .91 1805 473 1.000 300.000 10.016 582.16 582.56 -.07 20.9483 20.6415 1.49 1806 474 1.000 300.000 9.934 577.41 577.93 -.09 17.5052 17.1268 2.21

1807 475 1.000 300.000 9.848 572.38 572.98 -.10 14.0620 13.6671 2.89

1808 476 1.000 300.000 9.775 568.15 568.73 -.10 11.3077 10.9419 3.34

1809 477 1.000 300.000 9.698 563.71 564.19 -.09 8.5531 8.2722 3.40

1810 478 1.000 300.000 9.615 558.89 559.31 -.08 5.7989 5.5718 4.08

1811 479 1.000 300.000 9.547 554.91 555.37 -.08 3.7332 3.4996 6.68

1812 480 1.000 300.000 9.475 550.70 551.16 -.08 1.6674 1.4484 15.12

73
Data sources and

(XXXX)Haynes.

Table 7. (Continued)

ID numbers: (l)Virial Equation, (2)3eattie, (3)Morris, (4)Sage, (lO)Waxnnan,

ID Data Weight Temp. Density Density Density ^expt Pcalc Pressure

Point ex P+ calc Diff. Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa

3 481 .000 310.928 9.254 537.89 534.66 .60 .6895 1.9821 -65.22

3 482 .000 310.928 9.282 539.52 536.41 .58 1.3790 2.6625 -48.21

3 483 .000 310.928 9.342 543.00 539.75 .60 2.7579 4.1788 -34.00

3 484 .000 310.928 9.399 546.33 542.91 .63 4.1369 5.7204 -27.68

3 485 .000 310.928 9.451 549.33 545.90 .62 5.5158 7.1818 -23.20

3 486 .000 310.928 9.503 552.36 548.75 .65 6.8948 8.7337 -21.06

3 487 .000 310.928 9.566 556.00 552.14 .69 8.6184 10.7011 -19.46

3 488 .000 310.928 9.623 559.30 555.35 .71 10.3421 12.5828 -17.81

3 489 .000 310.928 9.677 562.45 558.41 .72 12.0658 14.4647 -16.58

3 490 .000 310.928 9.728 565.42 561.34 .72 13.7895 16.3320 -15.57

3 491 .000 310.928 9.776 568.23 564.13 .72 15.5132 18.1695 -14.62

3 492 .000 310.928 9.818 570.66 566.82 .67 17.2369 19.8205 -13.04

3 493 .000 310.928 9.864 573.32 569.41 .68 18.9606 21.6920 -12.59

3 494 .000 310.928 9.906 575.79 571.90 .68 20.6843 23.4992 -11.98

3 495 .000 310.928 9.945 578.08 574.31 .65 22.4080 25.2257 -11.17

3 496 .000 310.928 9.985 580.38 576.64 .65 24.1316 27.0218 -10.70

3 497 .000 310.928 10.025 582.70 578.89 .65 25.8553 28.8899 -10.50

3 498 .000 310.928 10.062 584.83 581.08 .64 27.5790 30.6532 -10.03

3 499 .000 310.928 10.099 586.97 583.20 .64 29.3027 32.4804 -9.78

3 500 .000 310.928 10.132 588.91 585.27 .62 31.0264 34.1814 -9.23

3 501 .000 310.928 10.166 590.87 587.28 .61 32.7501 35.9377 -8.87

3 502 .000 310.928 10.196 592.62 589.24 .57 34.4738 37.5466 -8.18

3 503 .000 344.261 8.410 488.81 486.34 .51 1.3790 1.9253 -28.38

3 504 .000 344.261 8.516 495.01 492.36 .53 2.7579 3.4191 -19.34

3 505 .000 344.261 8.607 500.26 497.73 .51 4.1369 4.8369 -14.47

3 506 .000 344.261 8.694 505.31 502.61 .54 5.5158 6.3368 -12.96

3 507 .000 344.261 8.774 509.98 507.08 .57 6.8948 7.8491 -12.16

3 508 .000 344.261 8.867 515.39 512.21 .62 8.6184 9.7653 -11.74

3 509 .000 344.261 8.951 520.25 516.93 .64 10.3421 11.6378 -11.13

3 510 .000 344.261 9.027 524.68 521.31 .64 12.0658 13.4811 -10.50

3 511 .000 344.261 9.101 529.01 525.39 .68 13.7895 15.4131 -10.53

3 512 .000 344.261 9.168 532.88 529.23 .69 15.5132 17.2528 -10.08

3 513 .000 344.261 9.229 536.45 532.85 .67 17.2369 19.0472 -9.50

3 514 .000 344.261 9.292 540.07 536.28 .70 18.9606 20.9653 -9.56

3 515 .000 344.261 9.348 543.37 539.55 .70 20.6843 22.8043 -9.30

3 516 .000 344.261 9.399 546.33 542.67 .67 22.4080 24.5338 -8.66

3 517 .000 344.261 9.448 549.14 545.65 .64 24.1316 26.2406 -8.04

3 518 .000 344.261 9.493 551.79 548.52 .59 25.8553 27.9118 -7.37

3 519 .000 344.261 9.539 554.46 551.27 .58 27.5790 29.6622 -7.02

3 520 .000 344.261 9.582 556.97 553.92 .55 29.3027 31.3615 -6.56

3 521 .000 344.261 9.626 559.50 556.48 .54 31.0264 33.1352 -6.36

3 522 .000 344.261 9.663 561.66 558.96 .48 32.7501 34.6965 -5.61

3 523 .000 344.261 9.700 563.83 561.35 .44 34.4738 36.3154 -5.07

3 524 .000 377.594 7.357 427.62 426.32 .30 2.7579 2.8785 -4.19

3 525 .000 377.594 7.571 440.07 439.16 .21 4.1369 4.2512 -2.69

3 526 .000 377.594 7.743 450.08 449.10 .22 5.5158 5.6691 -2.70

3 527 .000 377.594 7.885 458.33 457.34 .22 6.8948 7.0758 -2.56

3 528 .000 377.594 8.037 467.15 466.07 .23 8.6184 8.8502 -2.62

3 529 .000 377.594 8.168 474.76 473.60 .24 10.3421 10.6286 -2.70

3 530 .000 377.594 8.283 481.47 480.25 .25 12.0658 12.4023 -2.71

3 531 .000 377.594 8.387 487.48 486.23 .25 13.7895 14.1689 -2.68

3 532 .000 377.594 8.482 493.03 491.68 .27 15.5132 15.9614 -2.81

3 533 .000 377.594 8.569 498.09 496.70 .28 17.2369 17.7369 -2.82

3 534 .000 377.594 8.650 502.78 501.36 .28 18.9606 19.5106 -2.82

3 535 .000 377.594 8.724 507.07 505.71 .27 20.6843 21.2490 -2.66

3 536 .000 377.594 8.796 511.28 509.79 .29 22.4080 23.0611 -2.83

3 537 .000 377.594 8.864 515.23 513.65 .31 24.1316 24.8637 -2.94

3 538 .000 377.594 8.927 518.90 517.31 ,31 25.8553 26.6337 -2.92

3 539 .000 377.594 8.989 522.45 520.79 .32 27.5790 28.4355 -3.01

3 540 .000 377.594 9.051 526.06 524.11 .37 29.3027 30.3543 -3.46

3 541 .000 377.594 9.107 529.36 527.28 .39 31.0264 32.1975 -3.64

3 542 .000 377.594 9.162 532.53 530.32 .41 32.7501 34.0434 -3.80

3 543 .000 377.594 9.214 535.56 533.25 .43 34.4738 35.8807 -3.92

74
Data sources and ID numbers;

(XXXX)Haynes.

Table 7. (Continued)

(l)Virial Equation, (2)3eattie, (3)Morris, (4)Sage, (lO)Waxman,

D Data Weight Temp. Density Density Density f^expt Pcalc Pressur

Point ex P+ calc Diff. V Diff.

No. K mol/L kg/m3 kg/m^ % MPa MPa %

3 544 .000 410.928 .217 12.59 12.60 -.03 .6895 .6893 .03

3 545 .000 410.928 .471 27.35 27.18 .62 1.3790 1.3863 -.53

3 546 .000 410.928 1.195 69.46 69.36 .15 2.7579 2.7603 -.09

3 547 .000 410.928 1.557 90.50 90.55 -.05 3.1716 3.1708 .02

3 548 .000 410.928 1.720 99.99 99.98 .01 3.3095 3.3097 -.01

3 549 .000 410.928 1.918 111.47 111.65 -.16 3.4474 3.4455 .05

3 550 .000 410.928 2.196 127.64 127.42 .17 3.5853 3.5869 -.04

3 551 .000 410.928 2.392 139.05 138.33 .52 3.6542 3.6581 -.11

3 552 .000 410.928 2.694 156.58 153.78 1.79 3.7232 3.7327 -.26

3 553 .000 410.928 3.297 191.61 182.89 4.55 3.7921 3.8036 -.30

3 554 .000 410.928 4.632 269.22 248.92 7.54 3.8611 3.8947 -.86

3 555 .000 410.928 5.002 290.72 281.82 3.06 3.9300 3.9665 -.92

3 556 .000 410.928 5.320 309.24 296.79 4.02 3.9990 4.0911 -2.25

3 557 .000 410.928 5.624 326.91 313.92 3.97 4.1369 4.3060 -3.93

3 558 .000 410.928 6.179 359.16 350.18 2.50 4.8263 5.1309 -5.94

3 559 .000 410.928 6.492 377.35 368.25 2.41 5.5158 5.9929 -7.96

3 560 .000 410.928 6.756 392.71 390.74 .50 6.8948 7.0496 -2.20

3 561 .000 410.928 7.096 412.42 409.16 .79 8.6184 8.9938 -4.17

3 562 .000 410.928 7.293 423.88 422.76 .27 10.3421 10.5047 -1.55

3 563 .000 410.928 7.473 434.34 433.69 .15 12.0658 12.1788 -.93

3 564 .000 410.928 7.628 443.36 442.91 .10 13.7895 13.8802 -.65

3 565 .000 410.928 7.763 451.22 450.92 .07 15.5132 15.5835 -.45

3 566 .000 410.928 7.883 458.19 458.03 .04 17.2369 17.2795 -.25

3 567 .000 410.928 7.990 464.44 464.44 .00 18.9606 18.9610 -.00

3 568 .000 410.928 8.091 470.30 470.28 .00 20.6843 20.6897 -.03

3 569 .000 410.928 8.183 475.61 475.67 -.01 22.4080 22.3875 .09

3 570 .000 410.928 8.271 480.75 480.67 .02 24.1316 24.1598 -.12

3 571 .000 410.928 8.354 485.56 485.34 .05 25.8553 25.9389 -.32

3 572 .000 410.928 8.430 490.01 489.72 .06 27.5790 27.6967 -.42

3 573 .000 410.928 8.506 494.40 493.86 .11 29.3027 29.5346 -.79

3 574 .000 410.928 8.577 498.55 497.78 .16 31.0264 31.3784 -1.12

3 575 .000 410.928 8.645 502.46 501.50 .19 32.7501 33.2088 -1.38

3 576 .000 410.928 8.710 506.27 505.05 .24 34.4738 35.0857 -1.74

3 577 .000 444.261 .196 11.42 11.47 -.45 .6895 .6865 .43

3 578 .000 444.261 .415 24.15 24.18 -.13 1.3790 1.3774 .11

3 579 .000 444.261 .959 55.74 55.64 .18 2.7579 2.7616 -.13

3 580 .000 444.261 1.318 76.61 76.32 .37 3.4474 3.4558 -.25

3 581 .000 444.261 1.781 103.55 102.94 .59 4.1369 4.1505 -.33

3 582 .000 444.261 2.426 141.01 139.68 .94 4.8263 4.8472 -.43

3 583 .000 444.261 3.300 191.84 190.62 .63 5.5158 5.5309 -.27

3 584 .000 444.261 4.244 246.67 241.86 1.95 6.2053 6.2801 -1.19

3 585 .000 444.261 4.882 283.76 279.85 1.38 6.8948 6.9832 -1.27

3 585 .000 444.261 5.765 335.11 332.38 .81 8.6184 8.7524 -1.53

3 587 .000 444.261 6.248 363.15 360.65 .69 10.3421 10.5367 -1.85

3 588 .000 444.261 6.566 381.66 379.93 .45 12.0658 12.2486 -1.49

3 589 .000 444.261 6.820 396.40 394.67 .44 13.7895 14.0191 -1.64

3 590 .000 444.261 7.030 408.63 406.66 .48 15.5132 15.8280 -1.99

3 591 .000 444.261 7.207 418.89 416.82 .50 17.2369 17.6226 -2.19

3 592 .000 444.261 7.361 427.84 425.65 .51 18.9606 19.4244 -2.39

3 593 .000 444.261 7.485 435.05 433.48 .36 20.6843 21.0523 -1.75

3 594 .000 444.261 7.596 441.52 440.54 .22 22.4080 22.6630 -1.13

3 595 .000 444.261 7.704 447.82 446.96 .19 24.1316 24.3735 -.99

3 596 .000 444.261 7.800 453.40 452.87 .12 25.8553 26.0163 -.62

3 597 .000 444.261 7.897 458.98 458.34 .14 27.5790 27.7896 -.76

3 598 .000 444.261 7.988 464.30 463.44 .19 29.3027 29.6053 -1.02

3 599 .000 444.261 8.068 468.92 468.22 .15 31.0264 31.2876 -.83

3 600 .000 444.261 3.144 473.36 472.73 .13 32.7501 32.9988 -.75

3 601 .000 444.261 8.219 477.74 476.99 .16 34.4738 34.7853 -.90

3 602 .000 477.594 .181 10.52 10.55 -.23 .6895 .6880 .22

3 603 .000 477.594 .378 21.95 21.92 .13 1.3790 1.3806 -.12

3 604 .000 477.594 .830 48.22 48.13 .19 2.7579 2.7623 -.16

3 605 .000 477.594 1.096 63.72 63.55 .26 3.4474 3.4543 -.20

3 606 .000 477.594 1.398 81.27 81.04 .28 4.1369 4.1453 -.20

75
Table 7. (Continued)

Data sources and ID numbers:

(XXXX)Haynes.

(l)Virial Equation, (2)Beattie, (3)Morris, (4)Sage, (lO)Waxman,

) Data Weight Temp, Density Density Density '^expt Pcalc Pressure

Point ex Dt calc Diff.

w ^ Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa %

3 607 .000 477.594 1.740 101.13 101.09 .04 4.8263 4.8276 -.03

3 608 .000 477.594 2.136 124.17 124.16 .01 5.5158 5.5162 -.01

3 609 .000 477.594 2.583 150.13 150.35 -.15 6.2053 6.1996 .09

3 610 .000 477.594 3.064 178.10 178.63 -.29 6.8948 6.8821 .18

3 611 .000 477.594 4.192 243.66 243.09 .24 8.6184 8.6364 -.21

3 612 .000 477.594 4.965 288.57 288.79 -.08 10.3421 10.3319 .10

3 613 .000 477.594 5.491 319.16 319.90 -.23 12.0658 12.0166 .41 3 614 .000 477.594 5.866 340.96 342.38 -.42 13.7895 13.6656 .91 3 615 .000 477.594 6.164 358.27 359.74 -.41 15.5132 15.3520 1.05

3 616 .000 477.594 6.408 372.44 373.84 -.38 17.2369 17.0509 1.09 3 617 .000 477.594 6.614 384.41 385.70 -.34 18.9606 18.7600 1.07

3 618 .000 477.594 6.788 394.54 395.95 -.36 20.6843 20.4334 1.23

3 619 .000 477.594 6.926 402.58 404.99 -.60 22.4080 21.9279 2.19

3 620 .000 477.594 7.059 410.31 413.07 -.67 24.1316 23.5226 2.59

3 621 .000 477.594 7.173 416.93 420.39 -.83 25.8553 25.0203 3.34

3 622 .000 477.594 7.291 423.77 427.09 -.78 27.5790 26.7061 3.27

3 623 .000 477.594 7.402 430.26 433.27 -.70 29.3027 28.4463 3.01

3 624 .000 477.594 7.507 436.35 439.00 -.61 31.0264 30,2149 2.69

3 625 .000 477.594 7.598 441.64 444.36 -.61 32.7501 31,8635 2.78

3 626 .000 477.594 7.677 446.20 449.38 -.71 34.4738 33,3694 3.31

3 627 .000 510.928 .168 9.76 9.78 -.23 .6895 ,6879 .22

3 628 .000 510.928 .347 20.14 20.12 .12 1.3790 1.3805 -.11

3 629 .000 510.928 .741 43.08 42.99 .21 2,7579 2.7631 -.19

3 630 .000 510.928 .962 55.89 55.75 .25 3.4474 3.4548 -.21

3 631 .000 510.928 1.200 69.74 69.54 .29 4.1369 4.1465 -.23

3 632 .000 510.928 1.458 84.75 84.46 .34 4.8263 4,8392 -.26

3 633 .000 510.928 1.734 100.81 100.62 .19 5.5158 5,5236 -.14

3 634 .000 510.928 2.031 118.04 118.01 .03 6.2053 6,2065 -.02

3 635 .000 510.928 2.343 136.21 136.50 -.21 6.8948 6.8841 .15

3 636 .000 510.928 3.156 183.47 184.74 -.69 8.6184 8.5723 .54

3 637 .000 510.928 3.912 227.37 228.31 -.41 10.3421 10.3010 .40

3 638 .000 510.928 4.530 263.29 263.52 -.09 12.0658 12.0532 .10

3 639 .000 510.928 5.002 290.72 291.30 -.20 13.7895 13.7485 .30

3 640 .000 510.928 5.368 312.01 313.36 -.43 15.5132 15.3963 .76

3 641 .000 510.928 5.675 329.87 331.26 -.42 17.2369 17.0903 .86

3 642 .000 510.928 5.928 344.56 346.19 -.47 18.9606 18.7576 1.08

3 643 .000 510.928 6.150 357.48 358.93 -.41 20.6843 20.4748 1.02

3 644 .000 510.928 6.346 368.83 370.01 -.32 22.4080 22.2140 .87

3 645 .000 510.928 6.520 378.96 379.82 -.23 24.1316 23.9722 .67 3 646 .000 510.928 6.671 387.76 388.60 -.22 25.8553 25.6823 .67

3 647 .000 510.928 6.810 395.81 396,57 -.19 27.5790 27.4081 .62

3 648 .000 510.928 6.938 403.28 403.85 -.14 29.3027 29.1637 .48

3 649 .000 510.928 7.059 410.31 410,56 -.06 31.0264 30.9597 .22

3 650 .000 510.928 7.166 416.50 416.78 -.07 32.7501 32.6681 .25

3 651 .000 510.928 7.262 422.09 422.59 -.12 34.4738 34.3225 .44

75
Table 7. (Continued)

Data sources and 1 D numbers: (l)Viria 1 Equat ion, (2)Becattie, (3)Mc)rris, (4)S<age, ( 10)Waxman,

(XXXX)Ha ynes.

Data Weiglit Temp. Densi 1-y Density Density °expt Pcalc Pressure

Point expt calc Diff.

'^ r Diff.

No. K mol/L kg/m^ kg/m^ % MPa MPa %

1 652 .000 270.000 .050 2.91 2.91 -.01 .1072 .1072 .01

1 653 .000 280.000 .050 2.91 2.91 -.11 .1116 .1115 .10

1 654 .000 290.000 .050 2.91 2.91 -.19 .1160 .1158 .18

1 655 .000 300.000 .050 2.91 2.91 -.26 .1204 .1201 .25

1 656 .000 310.000 .050 2.91 2.92 -.32 .1248 .1244 .31

1 657 .000 320.000 .050 2.91 2.92 -.37 .1291 .1286 .36

1 658 .000 330.000 .050 2.91 2.92 -.41 .1334 .1329 .40

1 659 .000 340.000 .050 2.91 2.92 -.45 .1377 .1371 .44

1 660 .000 350.000 .050 2.91 2.92 -.48 .1420 .1414 .46

1 661 .000 360.000 .050 2.91 2.92 -.50 .1463 .1456 .49

1 662 .000 370.000 .050 2.91 2.92 -.52 .1506 .1499 .51

1 663 .000 380.000 .050 2.91 2.92 -.53 .1549 .1541 .52

1 664 .000 390.000 .050 2.91 2.92 -.54 .1592 .1583 .53

1 665 .000 400.000 .050 2.91 2.92 -.55 .1634 .1625 .54

1 666 .000 410.000 .050 2.91 2.92 -.56 .1677 .1668 .55

1 667 .000 420.000 .050 2.91 2.92 -.56 .1719 .1710 .55

1 668 .000 430.000 .050 2.91 2.92 -.56 .1762 .1752 .56

1 669 .000 440.000 .050 2.91 2.92 -.57 .1804 .1794 .56

1 670 .000 450.000 .050 2.91 2.92 -.57 .1847 .1836 .56

1 671 .000 460.000 .050 2.91 2.92 -.56 .1889 .1879 .56

1 672 .000 470.000 .050 2.91 2.92 -.56 .1931 .1921 .55

1 673 .000 480.000 .050 2.91 2.92 -.56 .1974 .1963 .55

1 674 .000 490.000 .050 2.91 2.92 -.55 .2016 .2005 .55

1 675 .000 500.000 .050 2.91 2.92 -.55 .2058 .2047 .54

1 676 .000 510.000 .050 2.91 2.92 -.55 .2100 .2089 .54

1 677 .000 520.000 .050 2.91 2.92 -.54 .2143 .2131 .53

1 678 .000 530.000 .050 2.91 2.92 -.53 .2185 .2173 .53

1 679 .000 540.000 .050 2.91 2.92 -.53 .2227 .2215 .52

1 680 .000 550.000 .050 2.91 2.92 -.52 .2269 .2257 .52

1 681 .000 560.000 .050 2.91 2.92 -.52 .2311 .2299 .51

1 682 .000 570.000 .050 2.91 2.92 -.51 .2353 .2341 .51

77
Table 8. Comparisons of data for ideal gas functions with eq (7).

Isobutane ideal gas functions from Chen, et al. [7]

Temp. f^-Hg, J/mol Diff. S°, J/( mol K) Diff. CO, J/(mo 1 K) Diff.

K expt. calc. al

10 expt. calc. % expt. calc. %

50.00 1674.4 1660.5 .83 194.012 193.782 .12 34.81 34.80 .04 100.00 3699.1 3704.2 -.14 221.585 221.608 -.01 47.28 47.28 -.01

150.00 6398.4 6399.3 -.01 243.258 243.283 -.01 60.29 60.30 -.01

200.00 9702.7 9704.5 -.02 262.211 262.221 -.00 71.84 71.82 .03 273.15 15603.5 15603.7 -.00 287.190 287.212 -.01 89.91 89.93 -.02

298.15 17936.0 17935.7 .00 295.390 295.377 .00 96.65 96.67 -.02

300.00 18115.0 181 15.0 -.00 295.976 295.976 -.00 97.15 97.17 -.02

400.00 29201.0 29201.8 -.00 327.691 327.683 .00 124.43 124.40 .02 500.00 42913.2 42909.0 .01 358.192 358.166 .01 149.24 149.17 .05 600.00 58924.1 58916.2 .01 387.313 387.292 .01 170.37 170.39 -.01 700.00 76881.0 76879.4 .00 414.927 414.947 -.00 188.28 188.38 -.05

800.00 96496.4 96503.8 -.01 441.119 44 1 . 1 29 -.00 203.64 203.71 -.04

900.00 117539.4 117549.7 -.01 465.888 465.902 -.00 216.94 216.89 .02 1000.00 139825.1 139824.3 .00 489.361 489.360 .00 228.45 228.34 .04 1100.00 163182.7 163171.7 .01 511.620 511.605 .00 233.49 238.39 .04 1200.00 187476.7 187463.9 .01 532.749 532.736 .00 247.15 247.28 -.05

78
Table 9. Interpol ate(j ideal gas fund'ions from eq (7).

Temp. E°-Eg H°-H§ S° pO C^

K J/mol J/mol J/(mol.K) J/(mol .K) J/(mol .K)

110.0 3275.8 4190.4 226.239 4 1.64 49.95

120.0 3705.6 4703.3 230.700 44.32 52.63

130.0 4162.0 5242.9 235.018 46.96 55.27

140.0 4644.5 5808.5 239.208 49.52 57.83

150.0 5152.1 6399.3 243.283 51.98 60.30

160.0 5683.8 7014.2 247.251 54.36 62.67

170.0 6239.0 7652.5 251.120 56.67 64.99

180.0 6817.2 8313.8 254.899 58.95 67.26

190.0 7418.0 8997.7 258.596 61.22 69.53

200.0 8041.6 9704.5 262.221 63.50 71.82

210.0 8688.1 10434.2 265.780 65.82 74.13

220.0 9358.1 11187.3 269.283 68.18 76.50

230.0 10051.9 11964.2 272.737 70.59 78.91

240.0 10770.2 12765.6 276.147 73.06 81.38

250.0 11513.4 13592.0 279.520 75.59 83.90

260.0 12282.1 14443.8 282.861 78.16 86.48

270.0 13076.8 15321.7 286.173 80.78 89.10

280.0 13897.9 16225.9 289.462 83.44 91.76

290.0 14745.8 17157.0 292.728 86.14 94.45

300.0 15620.7 18115.0 295.976 88.86 97.17

310.0 16522.9 19100.4 299.207 91.59 99.91

320.0 17452.6 20113.2 302.422 94.34 102.66

330.0 18409.8 21153.6 305.623 97.10 105.41 340.0 19394.5 22221.4 308.811 99.85 108.16

350.0 20406.8 23316.8 311.986 102.60 1 10.91 360.0 21446.4 24439.6 315.149 105.33 1 13.65

370.0 22513.4 25589.7 318.300 108.05 1 16.37

380.0 23607.4 26766.9 321.439 110.75 119.07

390.0 24728.4 27971.0 324.567 113.43 121.75

400.0 25876.0 29201.8 327.683 116.09 124.40

410.0 27050.0 30459.0 330.787 1 18.71 127.03

420.0 28250.2 31742.3 333.879 121.31 129.62

430.0 29476.1 33051.4 336.959 123.87 132.19

440.0 30727.5 34385.9 340.027 126.40 134.72

450.0 32004.1 35745.6 343.083 128.90 137.22

460.0 33305.5 37130.1 346.126 131.36 139.68

470.0 34631.3 38539.1 349.156 133.79 142.11 480.0 35981.2 39972.1 352.173 136.18 144.50

490.0 37354.8 41428.9 355.176 138.54 146.85

500.0 38751.8 42909.0 358.166 140.85 149.17

510.0 40171.7 44412.1 361.143 143.14 151.45

520.0 41614.4 45937.9 364.106 145.38 153.70

530.0 43079.3 47485.9 367.054 147.59 155.91 540.0 44566.1 49055.9 369.989 149.76 158.08

550.0 46074.4 50647.4 372.909 151.90 160.22

560.0 47604.0 52260.1 375.815 154.01 162.32

570.0 49154.4 53893.7 378.706 156.07 164.39

580.0 50725.4 55547.8 381.583 158.11 166.42

590.

C

52316.5 57222.1 384.445 160.1

1

168.42

600.0 53927.5 58916.2 387.292 162.08 170.39

610.0 55557.9 60629.8 390.125 164.01 172.33

620.0 57207.6 62362.6 392.942 165.92 174.23

630.0 58876.2 641 14.3 395.745 167.79 176.10

640.0 60563.3 65884.6 398.533 169.63 177.94

650.0 62268.7 67673.1 401.306 171.44 179.76

660.0 63992.0 69479.6 404.064 173.22 181.54

670.0 65733.0 71303.7 406.807 174.98 183.29

680.0 67491.4 73145.3 409.535 176.70 185.01 690.0 69266.9 75004.0 412.248 178.40 186.71 700.0 71059.3 76879.4 414.947 180.07 188.38

79
Table 10. Comparisons of heat of vaporization data with eq (9), Data sources and ID numbers: (l)Aston, (2)Dana, (3)Das/Ku loor,

(4)Das/Reed/Eubank, (5)Hanson, (6)Sage, (80)Thermal Loops,

(41 )C1 apeyron.

ID Weight Temp. Heat ol' Vaporization DIff.

K expt.

kj/mol

cal c.

%

80 1.000 113.550 28.161 28.117 .16

80 1.000 115.000 28.091 28.051 .14 80 .998 120.000 27.851 27.825 .09 80 .996 125.000 27.614 27.600 .05 80 .995 130.000 27.380 27.376 .01 80 .993 135.000 27.148 27.153 -.02

80 .991 140.000 26.920 26.931 -.04

80 .989 145.000 26.693 26.709 -.06

80 .987 150.000 26.468 26.488 -.08

80 .985 155.000 26.245 26.267 -.08

80 .983 160.000 26.024 26.046 -.08

80 .981 165.000 25.803 25.825 -.09

80 .979 170.000 25.583 25.604 -.08

80 .977 175.000 25.364 25.382 -.07

80 .974 180.000 25.145 25.160 -.06

80 .972 185.000 24.926 24.937 -.04

80 .969 190.000 24.707 24.713 -.02

80 .966 195.000 24.486 24.488 -.01

80 .963 200.000 24.265 24.261 .02

80 .960 205.000 24.042 24.033 .04

80 .957 210.000 23.817 23.802 .06

80 .954 215.000 23.590 23.570 .08 80 .950 220.000 23.360 23.335 .11 80 .947 225.000 23.127 23.098 .13

80 .943 230.000 22.891 22.858 .15

80 .939 235.000 22.651 22.614 .16

80 .935 240.000 22.406 22.367 .17 80 .930 245.000 22.157 22.117 .18

80 .925 250.000 21.902 21.862 .18 80 .920 255.000 21.642 21.602 .18 80 .915 260.000 21.375 21.338 .17

41 1.000 115.000 28.008 28.051 -.15

41 .996 125.000 27.580 27.600 -.07

41 .992 135.000 27.145 27.153 -.03

41 .988 145.000 26.707 26.709 -.01

41 .984 155.000 26.267 26.267 -.00

41 .979 165.000 25.827 25.825 .01

41 .974 175.000 25.387 25.382 .02

41 .968 185.000 24.946 24.937 .04

41 .962 195.000 24.500 24.488 .05

41 .956 205.000 24.046 24.033 .06

41 .949 215.000 23.580 23.570 .04

41 .941 225.000 23.099 23.098 .01

41 .932 235.000 22.601 22.614 -.06

41 .922 245.000 22.086 22.117 -.14

41 .912 255.000 21.554 21.602 -.23

41 .899 265.000 21.005 21.068 -.30

41 .886 275.000 20.440 20.510 -.34

41 .870 285.000 19.859 19.926 -.34

41 .851 295.000 19.255 19.309 -.28

41 .830 305.000 18.622 18.654 -.17

41 .805 315.000 17.948 17.954 -.03

41 .775 325.000 17.218 17.200 .10

41 .738 335.000 16.413 16.380 .20

41 .692 345.000 15.515 15.478 .23

41 .533 355.000 14.500 14.473 .19

41 .556 365.000 13,341 13.329 .09

41 .451 375.000 11.990 11.993 -.03

41 .305 385.000 10.351 10.358 -.07

41 .112 395.000 8.204 8.178 .32

41 .000 405.000 4.585 4.346 5.51

80
Table 10. (Continued).

Data sources and ID numbers: (l)Aston, (2)Dana, (3)0as/Ku loor,

(4)Das/Reed/Eubank, (5)Hanson, (6)Sage, (80)Thermal Loops,

(41 )Clapeyron.

D Weight Temp. Heat of Vapor i zat ion Diff.

K kj/mol

expt. calc.

i

5 0.000 244.261 22.157 22.154 .01

5 0.000 255.372 21.590 21.585 .03

3 0.000 261.320 21.297 21.267 .14

4 0.000 261.320 21.297 21.267 .14

1 0.000 261.440 21.295 21.261 .16

5 0.000 266.483 20.996 20.987 .04

2 0.000 270.000 20.852 20.792 .19

3 0.000 270.000 20.820 20.792 .15

4 0.000 270.000 20.769 20.792 -.11

5 0.000 277.594 20.547 20.562 -.07

2 0.000 280.000 20.246 20.222 .12 3 0.000 280.000 20.251 20.222 .14

4 0.000 280.000 20.154 20.222 -.55

5 0.000 288.705 19.685 19.701 -.08

2 0.000 290.000 19.627 19.621 .05

3 0.000 290.000 19.627 19.621 .05

4 0.000 290.000 19.555 19.621 -.44

6 0.000 290.000 19.575 19.621 -.25

5 0.000 299.817 18.996 18.998 -.01

2 0.000 300.000 18.970 18.986 -.09

3 0.000 300.000 18.970 18.986 -.09

4 0.000 300.000 18.916 18.986 -.37

6 0.000 300.000 19.029 18.986 .22

4 0.000 310.000 18.292 18.510 -.10

2 0.000 310.000 18.254 18.310 -.41

3 0.000 310.000 18.292 18.310 -.10

6 0.000 310.000 18.580 18.310 .38

5 0.000 310.928 18.226 18.245 -.10

2 0.000 320.000 17.405 17.584 -1.02

3 0.000 320.000 17.502 17.584 -.47

4 0.000 320.000 17.619 17.584 .20 5 0.000 320.000 17.651 17.584 .27

5 0.000 522.039 17.561 17.429 -.39

2 0.000 330.000 16.555 16.799 -1.57

3 0.000 330.000 16.698 16.799 -.60

4 0.000 330.000 16.857 16.799 .55

6 0.000 330.000 16.815 16.799 .10

5 0.000 333.150 16.415 16.537 -.74

3 0.000 340.000 15.807 15.940 -.84

4 0.000 340.000 16.008 15.940 .42 6 0.000 340.000 15.955 15.940 -.05

5 0.000 344.261 15.402 15.548 -.94

3 0.000 550.000 14.857 14.990 -.89

4 0.000 350.000 15.046 14.990 .57 6 0.000 550.000 14.954 14.990 -.24

5 0.000 555.372 14.294 14.435 -.96

3 0.000 360.000 13.782 15.921 -1.00

4 0.000 360.000 13.929 13.921 .06

6 0.000 560.000 15.811 13.921 -.79

5 0.000 566.485 12.984 15.145 -1.23

3 0.000 370.000 12.514 12.690 -1.59

4 0.000 370.000 12.615 12.690 -.59

6 0.000 370.000 12.559 12.690 -1.19

5 0.000 377.594 11.355 11.605 -2.51

3 0.000 580.000 10.950 11.225 -2.45

4 0.000 380.000 10.979 11.223 -2.17

6 0.000 380.000 10.908 11.223 -2.80

4 0.000 385.000 10.067 10.558 -2.81

6 0.000 38 5.000 9.891 10.558 -4.51

5 0.000 588.706 9.255 9.657 -5.96

3 0.000 590.000 8.970 9.564 -4.21

81
Table 10. (Continued).

Data sources and ID numbers: (l)Aston, (2)Dana, ( 3)Das/Ku loor,

(4)Das/Reed/Eubank, (5)Hanson, (6)Sage, (80)Thermal Loops,

(4 1 )Clapeyron.

Weight Temp. Heat of Vaporization Diff.

K expt.

kj/mol

calc.

%

4 0.000 390.000 9.017 9.364 -3.71

6 0.000 390.000 8.778 9.364 -6.26

4 0.000 395.000 7.807 8.178 -4.53

5 0.000 399.817 6.377 6.725 -5.18

3 0.000 400.000 6.276 6.661 -5.78

4 0.000 400.000 6.397 6.661 -3.96

5 0.000 405.372 3.891 4.095 -4.99

Number of data points used in fit = 61; rms deviation = 0.132?.

82
Table 11. Enthal pies of eq (10).

saturated liquid isobijtane fro

Temp. H.l H(j (eq ( 10)) Diff.

K J/ nol J/mol %

113.55 .0 .0 0.000

120.00 625.9 625.9 -.002

130.00 1614.4 1614.6 -.012

140.00 2625.3 2625.5 -.005

150.00 3659.0 3658.8 .004

160.00 4715.4 4715.

1

.006

170.00 5794.8 5794.6 .004

180.00 6897.5 6897.5 -.000

190.00 8023.7 8024.0 -.003

200.00 9173.5 9173.9 -.004

210.00 10346.9 10347.2 -.003

220.00 11543.9 11544.0 -.001 230.00 12764.9 12764.6 .002

240.00 14009.8 14009.5 .003

250.00 15279.8 15279.3 .003 260.00 16575.6 16575.3 .002

270.00 17898.7 17898.8 -.000

280.00 19250.8 19251.3 -.003

290.00 20634.1 20634.8 -.003

300.00 22050.6 22051 .2 -.003

310.00 23502.7 23502.7 .000

320.00 24992.4 24991.7 .003

330.00 26522.3 26521.3 .004 340.00 28096.2 28095.5 .003

350.00 29719.8 29720.2 -.001

360.00 31403.7 31405.0 -.004

370.00 33166.3 33167.1 -.003

380.00 35039.9 35039.1 .002

390.00 37093.8 37092.5 .003

400.00 39541.5 39542.5 -.002

407.85 43430.1 43430.1 0.000

Number of points = 29; rms deviation = 0.004$.

' Derived from ideal gas functions, the equation of state, and the formulated

heats of vaporization.

83
Table 12. Entropies and specific heats of saturated liquid

isobutane from eq (11).

Temp, <; 1 ^a So (eq (ID) Diff. Ca

K J/(mol.K) J/(mol .K) % J/(mol

.

113.55 108.800 108.800 0.000 96.65

120.00 114.179 114.177 .002 97.99

130.00 122.103 122.103 .000 100.10

140.00 129.598 129.600 -.001 102.26

150.00 136.730 136.731 -.001 104.49

160.00 143.547 143.547 -.000 106.77

170.00 150.090 150.089 .000 109.08

180.00 156.390 156.389 .000 111.40

190.00 162.476 162.475 .000 113.74

200.00 168.369 168.369 .000 116.08

210.00 174.089 174.089 -.000 118.43

220.00 179.653 179.653 -.000 120.79

230.00 185.075 185.075 -.000 123.19

240.00 190.370 190.370 .000 125.64

250.00 195.550 195.549 .000 128.16

260.00 200.626 200.625 -.000 130.76

270.00 205.611 205.612 -.000 133.48

280.00 210.516 210.517 -.000 136.31 290.00 215.351 215.351 -.000 139.27

300.00 220.125 220.125 -.000 142.38

310.00 224.847 224.847 .000 145.66

320.00 229.527 229.525 .001 149.13

330.00 234.173 234.171 .001 152.89

340.00 238.796 238.796 -.000 157.05

350.00 243.414 243.416 -.001 161.90

360.00 248.056 248.058 -.001 167.95

370.00 252.766 252.766 .000 176.21 380.00 257.623 257.620 .001 188.94

390.00 262.792 262.793 -.000 212.25

400.00 268.781 268.781 -.000 273.72

407.85 278.161 278.161 0.000 —

K)

Number of points = 29; rms deviation = 0.001*.

' Derived from ideal gas functions, equation of state, and formulated heats

of vaporization.

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89
Table 14. Comparisons with saturated liquid specific heats.

Data sources and ID numbers: (DAston, (2) Parks, (6) Dana.

ID Temp.

K

116.940

123.110

129.430

135.800

142.840

150.130

158.460

165.220

168.700

174.450

180.310

185.870

190.990

196.100

201.520

206.560

211.630

216.780

222.270

227.310

232.890

238.570

245.040

251.940

257.020

2 115.400

2 122.100

2 136.500

2 142.800

2 154.600

2 160.800

2 171.500

2 177.300

2 187.800

2 193.500

2 202.700

2 208.500

2 214.300

2 225.000

2 230.600

2 240.200

2 245.400

2 253.000

2 258.300

6 259.390

6 260.620

6 265.380

6 270.560

6 270.840

6 275.750

6 280.230

5 280.560

6 285.890

6 289.790

6 290.650

Ca> V moLK)

expt calc

99.90 97.35

100.94 98.64

101.36 99.97

102.53 101.34

103.58 102.89

104.88 104.52

106.59 106.41 108.22 107.97

108.51 108.78

109.56 110.11

111.11 111.48

112.11 112.77

113.07 113.97

113.87 115.17

114.96 116.44

115.50 117.62

116.55 118.81 118.51 120.03

119.10 121.33

120.73 122.54

122.19 123.89

124.12 125.29

125.79 126.90

127.59 128.66

128.26 129.98

99.33 97.04

100.23 98.43

103.07 101.50

103.83 102.88

105.65 105.53

107.04 106.95

108.71 109.43

110.10 110.77

11 1.90 113.23

113.41 114.56

115.08 116.71 116.20 118.08

117.30 119.44

119.56 121.99

120.92 123.34

123.16 125.69

124.66 126.99

127.19 128.93

128.46 130.31 120.12 130.60

129.36 130.93

125.47 132.21

126.20 133.63

132.52 133.71

136.41 135.09

141.27 136.38

143.22 136.47

152.70 138.04

155.13 139.21 150.02 139.47

Diff.

2.61

2.34

1.39

1.17

.67

.34 .16 .23 -.24

-.50

-.33

-.59

-.79

-1.13

-1.27

-1.80

-1.91

-1.26

-1.84

-1.48

-1.37

-.93

-.87

-.83

-1.32

2.36

1.83

1.55

.92

.11 .08 -.65

-.61 -1.17

-1.01

-1.40

-1.59

-1.80

-1.99

-1.96

-2.02

-1.83

-1.35

-1 .43 -8.03

-1.20

-5.10

-5.57

-.89

.98 3.59

4.94

10.62 11.44

7.57

Number of data points = 55; rms deviation = 3.15?.

90
Table 15 . Comparisons

Cp data of

with C^ and Cp

Ernst [ 16!

data.

Pressure Tentip. Density Cd, J/(mc I'K) Diff. MPa K kg/m3 ex Dt ca c %

0.0000 293. 150 0.0000 95 .21 95 .31 -.10

0.0000 313. 150 0.0000 100 .67 100 .77 -.10

0.0000 333. 150 0.0000 106 .37 106 .28 .09 0.0000 353. 150 0.0000 111 .74 111 .77 -.03

.0490 293. 150 1.1904 96 .09 95 .94 .15 .0490 313. 150 1.11 14 101 .36 101 .28 .08 .0490 333. 150 1.0424 106 .83 106 .69 .13 .0490 353. 150 .9817 112 .10 112 .12 -.02

.0981 293. 150 2.4181 97 .06 96 .71 .36

.0981 313. 150 2.2514 102 .11 101 .84 .26

.0981 333, 150 2.1074 107 .32 107 .13 .18

.0981 353. 150 1.9815 112 .48 112 .47 .01 .1961 293. 150 4.9842 99 .18 98 .73 .45

.1961 313. 150 4.6126 103 .68 103 .21 .46

.1961 333. 150 4.2991 108 .34 108 .13 .19 .1961 353. 150 4.0293 113 .42 113 .25 .15

.3432 313. 150 8.3751 106 .58 106 .04 .51 .3432 333. 150 7.7449 110 .58 110 .03 .50

.3432 353. 150 7.2193 115 .06 114. 64 .37 .4903 313. 150 12.4725 110 .57 110 .41 .14 .4903 333. 150 11.4118 113 .17 112 .58 .53

.4903 353. 150 10.5655 116 .88 116 .36 .44 .6374 333. 150 15.3603 116 .51 116 07 .38 .6374 353. 150 14.0979 119 .20 118 .53 .57 .7845 353. 150 17.8596 121 .83 121 .29 .45

Number of data points of Ernst [16! = 25; rms deviation = 0.32|.

Temp.

K

347.60

359.40

387.50

452.50

561.70

605.30

692.70

C^ data of Dai ley [111

eg, J/(mol.K)

ex pt ca I

c

109.66

112.55

119.62

137.03

1 6 1 . 29 169.70

185.18

110.25

113.48

121.08

137.84

162.67

171.42

187.17

D iff.

%

-.54

-.82

- 1.21 -.59

-.85

- 1.00

- 1.06

Number of data points of Dai ley [11! = 7; rms deviation = 0.^

91
Table 15. (Continued).

Cp data of Sage, et al. [51!

P = 0.101325 MPa (1 atm)

Temp. Cp, J/(mol'K) Diff.

K expt ca I

c

%

294.261 94.553 97.042 -2.63

310.928 96.985 101.302 -4.45

327.594 99.611 105.633 -6.10

344.261 102.432 110.122 -7.51

360.928 105.351 114.573 -8.75

377.594 108.415 119.006 -9.77

394.261 111.722 123.396 -10.45

410.928 115.127 127.725 -10.94

427.594 118.702 131.982 -11.19

444.261 122.326 136.155 -11.31

Number of data points of Sage, et al. [511 = 10; rms deviation = 8.80*.

Cp data of Wacker [ 61 I

Temp. Pressure [Density Cp, J/(mol •K) Diff.

K MPa kg/m3 expt ca Ic % 243.19 .01200 .3476 82.72 82.45 .32 243.18 .01253 .3632 82.76 82.47 .35 243.10 .01213 .3517 82.76 82.44 .39 243.20 .02400 .7003 83.27 82.80 .56 243.16 .02373 .6925 83.28 82.78 .51 243.15 .02386 .5965 83.25 82.78 .55 243.09 .02400 .7006 83.10 82.77 .40 243.12 .02346 .6847 83.16 82.75 .48 243.19 .02373 .6924 83.27 82.79 .58 243.16 .02400 .7004 83.21 82.79 .51 243.08 .02346 .6849 83.09 32.75 .40 243.16 .03106 .9104 83.43 83.02 .50 243.24 .03040 .8902 83 . 52 83.02 .61 243.24 .03026 .8852 83.41 83.01 .48 273.26 .02520 .6522 90.58 90.36 .24 273.24 .02520 .6523 90.63 90.35 .31 273.09 .05040 1.3138 91.25 90.79 .52 273.13 .05200 1.3614 91.27 90.83 .48 273.09 .05040 1.3188 91.19 90.79 .45 273.02 .05200 1.3520 91.17 90.80 .40 273.21 .05066 1.3253 91.15 90.82 .36 273.07 .05200 1.3617 91.19 90.82 .42 312.93 .02453 .5525 101.04 100.96 .08 312.98 .02520 .5575 101.05 100.98 .09 313.38 .05135 1.1755 101.45 101.37 .09 313.37 .05200 1.1785 101.50 101.37 .13 313.19 .05160 1.1701 101.45 101.31 .13 313.19 .05200 1.1793 101.40 101.32 .08 313.48 .05150 1.1690 101.55 101.39 .16 313.16 .05200 1.1794 101.42 101.31 .1 1 352.87 .02466 .4917 1 11.79 111.87 -.07

352.80 .02533 .5051 111.88 111.85 .02 352.79 .05213 1.0454 11 1.98 112.04 -.06

352.80 .05213 1.0454 112.01 112.05 -.03

353.45 .05160 1.0326 112.23 112.22 .01 352.88 .05226 1.0478 112.10 112.07 .03 352.87 .05213 1.0451 112.03 112.06 -.03

Number of data points of Wacker [611 = 37; rms deviation = 0.36$.

92
Table 15. (Continued)

Cp data of Sage and Lacey [50]

Temp. Pressure Dens ity Cp, J/{mol •K) Diff.

K MPa kg/m3 expt ca Ic %

294.261 0.0000 0.000 93.58 95,61 -2.12

310.928 0.0000 0.000 95.96 100,16 -4.19

327.594 0.0000 0.000 98.69 104,75 -5.79

344.261 0.0000 0.000 101.41 109,34 -7.25

360.928 0.0000 0.000 104.40 113,90 -8.34

377.594 0.0000 0.000 107.47 118,42 -9.25

394.261 0.0000 0.000 110.77 122,88 -9.85

294.261 .1013 2.491 94.75 97.04 -2.36

310.928 .1013 2.346 97.16 101.30 -4.09

327.594 .1013 2.218 99.61 105,68 -5.75

344.261 .1013 2.104 102.43 110,12 -6.98

360.928 .1013 2.002 105.35 114.57 -8.05

377.594 .1013 1.910 108.41 119.01 -8.90

394.261 .1013 1.826 111.72 123.40 -9.46

294.261 .1379 3.427 95.84 97.71 -1.91

310.928 .1379 3.223 97.54 101.79 -4.17

327.594 .1379 3.043 100.02 106.07 -5.70

344.261 .1379 2.884 102.80 110.43 -6.91

360.928 .1379 2.741 105.72 114.83 -7.94

377.594 .1379 2.613 108.78 119.22 -8.76

394.261 .1379 2.496 112.09 123.58 -9.30

294.261 ,2758 7.155 101.95 101.22 .72 310.928 .2758 6.673 100.75 104.15 -3.26

327.594 .2758 6.264 102.04 107.80 -5.34

344.261 .2758 5.910 104.38 111.77 -6.62

360.928 .2758 5.598 107.15 115.91 -7.56

377.594 .2758 5.321 110.14 120.11 -8.30

394.261 .2758 5.072 113.45 124.33 -8.75

310.928 .4137 10.392 106.10 107.64 -1.42

327.594 .4137 9.680 104.89 110.11 -4,74

344.261 .4 137 9.084 106.30 113.45 -6.31

360.928 .4137 8.570 108.73 117.20 -7.22

377.594 .4137 8.121 111.63 121.14 -7.86

394.261 .4137 7.723 114.91 125.17 -8.20

327.594 .5516 13.340 108.71 113.27 -4.03

344.261 .5516 12.432 108.66 115.58 -5.99

360.928 .5516 11.673 110.46 118.76 -6.99

377.594 .5516 1 1.021 113.18 122,34 -7.49

394.261 .5516 10.452 116.42 126,13 -7.70

327.594 .6895 17.321 114.11 117,81 -3.14

344.261 ,6895 15.994 111.50 118.32 -5.76

360.928 .6895 14.928 112.40 120,65 -6.83

377.594 ,6895 14.035 114.84 123,75 -7.20

394.261 ,6895 13.268 118.02 127,23 -7.23

344.261 ,8618 20.837 115.93 123,03 -5.77

360.928 ,8618 19.260 115.15 123,63 -6.86

377.594 ,8618 17.991 117.05 125,85 -7.00

394.261 ,8618 16.930 120,09 128,81 -6.77

344.261 1,0342 26.276 121.52 130,22 -6.68

360.928 1.0342 23.959 118.41 127,58 -7.19

377.594 1,0342 22.199 119.46 128,46 -7.01

394 . 26

1.0342 20.773 122,28 130,69 -6.44

360.928 1.2066 29.143 122.06 133,02 -8.24

377.594 1.2066 26.714 122,08 131,72 -7.32

394.261 1 .2066 24.829 124,59 132.92 -6.27

360.928 1.3790 34.990 126,46 141.02 -10.32

377.594 1.3790 31.612 125,00 135,89 -8.01

394.261 1,3790 29,138 126,99 135,60 -6.35

360.928 1,5513 41,820 132,08 154,25 -14.37

377.594 1,5513 36,997 128.28 141,40 -9.28

394.261 1,5513 33,746 129.52 138,84 -6.71

377.594 1.7237 43,026 132,00 149,04 -11.43

394.261 1.7237 38,714 132,22 142,83 -7.43

377.594 2,0684 58,280 142,02 180.18 -21.18

394.261 2.0684 50,090 138,38 154,40 -10.38

394.261 2.4132 64,501 146,40 176,25 -16.94

Number of data points of Sage and Lacey (501 = 66; rms deviation = 7.85^.

93
Table 16. Comparisons with enthalpy data.

Enthalpy data of Koppany 1351

Temp. Pressure Dens i ty H, J/ mol Diff.

K MPa kg/m3 expt calc J/mol

349.650 1.7237 478.487 761 1.6 8014.7 -403.1

350.094 1.7237 477.683 7895.5 8088.0 -192.5

349.983 1.7237 477.884 8030.7 8069.6 -38.9

349.761 1.7237 478.287 7922.6 8033.0 -110.5

354.983 1.7237 468.521 8747.3 8903.6 -156.4

354.817 1.7237 468.844 8544.5 8875.5 -331.0

354.594 1.7237 469.273 8733.7 8838.0 -104.3

354.317 1.7237 469.807 8598.5 8791.3 -192.7

361.539 1.7237 455.153 9882.9 10030.5 -147.6

361.872 1 . 7237 454.433 9734.2 10089.0 -354.8

362.261 1.7237 453.587 9855.9 10157.4 -301.5

363.928 1.7237 449.891 10450.7 10452.7 -2.0

363.928 1.7237 449.891 10450.7 10452.7 -2.0

364.150 1.7237 449.388 10585.9 10492.3 93.6

364.650 1.7237 448.250 11261.9 10581.8 680.1

364.706 1.7237 448.123 11343.0 10591.7 751.3

367.372 1.7237 46.868 23929.9 24282.4 -352.5

367.650 1.7237 46.743 24565.3 24327.1 238.2

370.483 1.7237 45.544 24551.8 24775.6 -223.8

373.039 1.7237 44.570 25619.9 25170.4 449.5

377.039 1.7237 43.203 25849.7 25774.7 75.0

388.261 1.7237 40.083 27066.5 27417.2 -350.8

378.761 1.7237 42.663 25227.8 26031.0 -803.2

383.428 1.7237 41.321 26458.1 26716.8 -258.7

388.872 1.7237 39.936 27350.4 27505.3 -154.9

394.761 1.7237 38.607 28161.6 28349.2 -187.6

Number of data points of Koppany [35) = 26; average difference = -91.6 J/mol,

94
Table 17. Calculated P(T) i sochores of isobutane.

Isobutane I sochore at 25 kg/m-^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Derivative Der ivat i ve Curvature

< MPa MPa.in5/kg MPa/K MPa/K^

337 .864 .9664 .79982 .02904 .00464 -.0000159

338 .000 .9670 .80002 .02907 .00464 -.0000158

346 .000 1 .0037 .81117 .03099 .00453 -.0000115

354 .000 1.0397 .82123 .03281 .00445 -.0000089

362 .000 1 .0750 .83040 .03456 .00439 -.0000072

370 .000 1 . 1 099 .83882 .03625 .00434 -.0000060

378 .000 1.1444 .84660 .03791 .00429 -.0000051

386 .000 1.1786 .85382 .03953 .00425 -.0000044

394 .000 1.2125 .86055 .04113 .00422 -.0000038

402 .000 1.2462 .86683 .04270 .00419 -.0000034

410 .000 1.2796 .87273 .04425 .00417 -.0000030

418 .000 1.3129 .87826 .04578 .00414 -.0000027

426 .000 1.3459 .88348 .04730 .00412 -.0000024

434 .000 1.3789 .88841 .04880 .00411 -.0000022

442 .000 1.4116 .89307 .05029 .00409 -.0000020

450. 000 1.4443 .89748 .05177 .00407 -.0000018

458 .000 1 .4768 .90167 .05324 .00406 -.0000016

466 .000 1.5093 .90566 .05469 .00405 -.0000015

474 .000 1.5416 .90945 .05614 .00404 -.0000014

482. 000 1.5739 .9 1 306 .05759 .00403 -.0000013

490 .000 1.6060 .91651 .05902 .00402 -.0000012

498. 000 1.6381 .91981 .06045 .00401 -.0000011

506 .000 1.6701 .92296 .06187 .00400 -.0000010

514, 000 1.7021 .92598 .06329 .00399 -.0000010

522 .000 1.7340 .92887 .06470 .00398 -.0000009

530 .000 1.7658 .93165 .06611 .00398 -.0000008

538 .000 1.7976 .93432 .06751 .00397 -.0000008

546. 000 1.8293 .93688 .06891 .00396 -.0000007

554 .000 1.8610 .93934 .07030 .00396 -.0000007

562 .000 1.8927 .94171 .07169 .00395 -.0000007

570 .000 1.9243 .94400 .07308 .00395 -.0000006

578 .000 1.9558 .94620 .07446 .00394 -.0000006

586 .000 1 .9873 .94832 .07584 .00394 -.0000006

594. 000 2.0188 .95037 .07722 .00393 -.0000005

602 .000 2.0503 .95235 .07859 .00393 -.0000005

610, 000 2.0817 .95426 .07996 .00393 -.0000005

618 .000 2.1131 .95611 .08133 .00392 -.0000005

626. 000 2.1444 .95790 .08270 .00392 -.0000004

634 .000 2.1758 .95963 .08406 .00391 -.0000004

642. 000 2.2071 .96131 .08543 .00391 -.0000004

650 .000 2,2383 .96293 .08679 .00391 -.0000004

658. 000 2.2696 .96451 .08814 .0039

1

-.0000004

666 .000 2.3008 .96603 .08950 .00390 -.0000004

674. 000 2.3320 .96751 .09085 .00390 -.0000003

682 .000 2.3632 .96895 .09220 .00390 -.0000003

690 .000 2.3944 .97034 .09356 .00389 -.0000003

698 .000 2.4255 .97170 .09490 .00389 -.0000003

95
Table 17. (Continued),

sobutane Isochore at 50 kg/m-^

i sotherm Isochore Isochore

Temp. Pressure Z Der ivat i ve Der ivative Curvature

K MPa MPa • m3/kg MPaA MPa/K2

367.788 1.7933 .68172 .01998 .01082 -.0000575

370.000 1.8171 .68664 .02057 .01070 -.0000505

378.000 1.9013 .70325 .02304 .01037 -.0000353

386.000 1.9832 .71834 .02524 .01012 -.0000270

394.000 2.0634 .73220 .02735 .00993 -.0000218

402.000 2.1421 .74502 .02939 .00977 -.0000181

410.000 2.2197 .75695 .03136 .00963 -.0000154

418.000 2.2963 .76809 .03329 .00952 -.0000132

425.000 2.3721 .77853 .03518 .00942 -.0000116

434.000 2.4471 .78834 .03703 .00933 -.0000102

442.000 2.5215 .79760 .03886 .00926 -.0000091

450.000 2.5953 .80634 .04067 .00919 -.0000081

458.000 2.6585 .81462 .04245 .00913 -.0000073

465.000 2.7413 .82248 .04421 .00907 -.0000067

474.000 2.8137 .82994 .04595 .00902 -.0000061

482.000 2.88 56 .83704 .04768 .00897 -.0000055

490.000 2.9573 .84381 .04940 .00893 -.0000051

498.000 3.0286 .85027 .05110 .00889 -.0000047

506.000 3.0996 .85645 .05279 .00886 -.0000043

514.000 3.1703 .86235 .05447 .00082 -.0000040

522.000 3.2407 .85801 .05614 .00879 -.0000037

530.000 3.3109 .87343 .05779 .00876 -.0000035

538.000 3.3809 .87863 .05945 .00874 -.0000033

546.000 3.4507 .88363 .06109 .00871 -.0000030

554.000 3.5203 .88843 .06272 .00869 -.0000029

562.000 3.5897 .89305 .06435 .00857 -.0000027

570.000 3.6590 .89750 .06597 .00864 -.0000025

578.000 3.7281 .90179 .06759 .00862 -.0000024

586.000 3.7970 .90592 .05920 .00851 -.0000023

594.000 3.8658 .90991 .07080 .00859 -.0000021

602.000 3.9344 .91376 .07240 .00857 -.0000020

610.000 4.0029 .91748 .07400 .00856 -.0000019

518.000 4.0713 .92108 .07558 .00854 -.0000018

626.000 4.1396 .92455 .07717 .00853 -.0000018

634.000 4.2077 .92792 .07875 .00851 -.0000017

842.000 4.2758 .931 17 .08033 .00850 -.0000016

650.000 4.3437 .93433 .08190 .00849 -.0000015

658.000 4.41 15 .93739 .08347 .00848 -.0000015

666.000 4.4793 .94035 .08503 .00846 -.0000014

674.000 4.5470 .94323 .08660 .00845 -.0000013

682.000 4.5146 .94602 .08815 .00844 -.0000013

590.000 4.5821 .94873 .08971 .00843 -.0000012

598.000 4.7495 .95135 .09126 .00842 -.0000012

96
Table 17. (Continued).

I sobutane I sochore at 100 kg/m^

Isotherm 1 sochore 1 sochore

Temp. Pressure Z Der i vati ve Der ivati ve Curvature

K MPa MPa.m3/kg MPa/K MPa/K2

394.560 2.9066 .51498 .00768 .02593 -.0002585

402.000 3.0941 .53806 .01040 .02463 -.0001245

410.000 3.2877 .56057 .01300 .02383 -.0000820

418.000 3.4760 .58133 .01547 .02326 -.0000614

426.000 3.6603 .60066 .01786 .02283 -.0000489

434.000 3.8414 .61877 .02019 .02247 -.0000405

442.000 4.0200 .63581 .02248 .02217 -.0000343

450.000 4.1963 .65190 .02473 .02192 -.0000297

458.000 4.3708 .66714 .02695 .02170 -.0000260

466.000 4.5435 .68160 .02916 .02150 -.0000230

474.000 4.7148 .69536 .03134 .02133 -.0000206

482.000 4.8848 .70847 .03350 .02117 -.0000185

490.000 5.0536 .72099 .03565 .02103 -.0000168

498.000 5.2213 .73295 .03778 .02090 -.0000153

506.000 5.3881 .74439 .03990 .02078 -.0000140

514.000 5.5539 .75536 .04201 .02068 -.0000129

522.000 5.7189 .76588 .04411 .02058 -.0000120

530.000 5.8831 .77599 .04620 .02048 -.00001 11 538.000 6.0467 .78570 .04828 .02040 -.0000103

546.000 6.2095 .79504 .05035 .02032 -.0000096

554.000 6.3718 .80403 .05241 .02024 -.0000090

562.000 6.5334 .81269 .05447 .02017 -.0000085

570.000 6.6946 .82105 .05652 .02011 -.0000080

578.000 6.8552 .82911 .05856 .02005 -.0000075

586.000 7.0153 .83690 .06060 .01999 -.0000071

594.000 7.1750 .84442 .06263 .01993 -.0000068

602.000 7.3342 .85169 .06465 .01988 -.0000064

610.000 7.4931 .85872 .06667 .01983 -.0000061

618.000 7.6515 .86553 .06869 .01978 -.0000058

626.000 7.8096 .87212 .07070 .01974 -.0000055

634.000 7.9673 .87851 .07270 .01969 -.0000053

642.000 8.1247 .88470 .07470 .01965 -.0000051

650.000 8.2817 .89070 .07670 .01961 -.0000049

658.000 8.4385 .89652 .07869 .01957 -.0000047

666.000 8.5949 .90217 .08068 .01954 -.0000045

674.000 8.7511 .90766 .08266 .01950 -.0000043

682.000 8.9070 .91299 .08464 .01947 -.0000042

690.000 9.0626 .91817 .08662 .01944 -.0000040

698.000 9.2179 .92321 .08859 .01940 -.0000039

97
Table 17. (Continued),

sobutane Isochore at 150 kg/m-^

1 sotherm Isochore Isochore

Temp. Pressure Z Derivative Der i vat i ve Curvature

K MPa MPa.m3/kg MPa/K MPa/K^

404.847 3.4598 .39828 .00181 .04248 -.0009884

410.000 3.6717 .41736 .00366 .04026 -.0002361

418.000 3.9880 .44464 .00624 .03896 -.0001185

425.000 4.2963 .47002 .00878 .03818 -.0000810

434.000 4.5994 .49390 .01130 .03762 -.0000618

442.000 4.8985 .51650 .01382 .03717 -.0000500

450.000 5.1944 .53796 .01634 .03681 -.0000419

458.000 5.4875 .55840 .01887 .03650 -.0000360

466.000 5.7784 .57790 .02139 .03623 -.0000315

474.000 6.0672 .59654 .02392 .03599 -.0000279

482.000 6.3543 .61440 .02645 .03578 -.0000250

490.000 6.6397 .63152 .02898 .03559 -.0000226

498.000 6.9238 .64795 .03151 .03542 -.0000206

506.000 7.2064 .66374 .03404 .03526 -.0000190

514.000 7.4879 .67893 .03658 .03511 -.0000175

522.000 7.7682 .69356 .03911 .03498 -.0000163

530.000 8.0475 .70765 .04164 .03485 -.0000152

538.000 8.3259 .72124 .04417 .03473 -.0000142

546.000 8.6033 .73435 .04670 .03462 -.0000134

554.000 8.8799 .74701 .04923 .03452 -.0000126

562.000 9.1556 .75925 .05176 .03442 -.0000119

570.000 9.4306 .77107 .05429 .03433 -.0000113

578.000 9.7049 .78252 .05682 .03424 -.0000108

586.000 9.9785 .79359 .05934 .03416 -.0000103

594.000 10.2514 .80432 .06186 .03408 -.0000098

602.000 10.5237 .81471 .06438 .03400 -.0000094

610.000 10.7954 .82478 .06690 .03392 -.0000091

618.000 11.0665 .83455 .06942 .03385 -.0000087

626.000 1 1 .3370 .84402 .07193 .03378 -.0000084

634.000 11.6070 .85322 .07444 .03372 -.0000081

642.000 11.8765 .86215 .07695 .03365 -.0000079

650.000 12.1455 .87083 .07946 .03359 -.0000076

658.000 12.4140 .87926 .08196 .03353 -.0000074

666.000 12.6820 .88745 .08446 .03347 -.0000072

674.000 12.9496 .89542 .08696 .03342 -.0000069

682.000 13.2167 .90317 .08946 .03336 -.0000068

690.000 13.4834 .91071 .09195 .03331 -.0000066

698.000 13.7497 .91805 .09444 .03326 -.0000064

98
Table 17. (Continued),

sobutane I sochore at 200 kg/m^

1 sotherm tsochore 1 sochore

Temp. Pressure Z Der i vat ive Der i vat ive Curvature

K MPa MPa.m3/kg MPa/K MPa/K^

407.736 3.6329 .31143 .00006 .05794 -.0089383

410.000 3.7609 .32062 .00073 .05603 -.0002601

418.000 4.2043 .35157 .00328 .05503 -.0000733

426.000 4.6425 .38092 .00601 .05457 -.0000457

434.000 5.0778 .40095 .00884 .05426 -.0000340

442.000 5.5108 .43580 .01174 .05401 -.0000275

450.000 5.9421 .46155 .01469 .05381 -.0000234

458.000 6.3719 .48629 .01769 .05364 -.0000205

466.000 6.8003 .51008 .02073 .05348 -.0000184

474.000 7.2276 .53297 .02379 .05334 -.0000168

482.000 7.6538 .55503 .02688 .05321 -.0000156

490.000 8.0790 .57630 .03000 .05309 -.0000146

498.000 8.5032 .59682 .03313 .05298 -.0000138

506.000 8.9266 .61663 .03628 .05287 -.0000131

514.000 9.3492 .63577 .03944 .05277 -.0000125

522.000 9.7709 .65427 .04261 .05267 -.0000121

530.000 10.1919 .67216 .04580 .05257 -.0000116

538.000 10.6121 .68946 .04899 .05248 -.0000113

546.000 11.0316 .70622 .05220 .05239 -.0000110

554.000 11.4504 .72244 .05541 .05231 -.0000107

562.000 11.8685 .73816 .05862 .05222 -.0000105

570.000 12.2860 .75340 .06184 .05214 -.0000103

578.000 12.7027 .76818 .06506 .05206 -.0000101

586.000 13.1189 .78251 .06829 .05198 -.0000099

594.000 13.5344 .79642 .07152 .05190 -.0000097

602.000 13.9493 .80993 .07475 .05182 -.0000096

610.000 14.3635 .82304 .07798 .05175 -.0000094

618.000 14.7772 .83579 .08122 .05167 -.0000093

626.000 15.1903 .84817 .08445 .05160 -.0000092

634.000 15.6028 .86021 .08768 .05152 -.0000091

642.000 16.0147 .87192 .09092 .05145 -.0000090

650.000 16.4260 .88330 .09415 .05138 -.0000089

658.000 16.8368 .89439 .09738 .05131 -.0000088

666.000 17.2470 .90517 .10061 .05124 -.0000087

674.000 17.6566 .91567 .10384 .05117 -.0000086

682.000 18.0657 .92590 .10707 .05110 -.0000085

690.000 18.4743 .93586 . 1 1 030 .05104 -.0000084

698.000 18.8823 .94557 .11352 .05097 -.0000083

99
Table 17. (Continued),

sobutane I sochore at 224.36 kg/rn^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Der i vat i ve Derivative Curvature

K MPa MPa.m3/kg MPa/K MPa/K^

407.850 3.6400 .27808 .00000 .06351 -.0000000

410.000 3.7766 .28700 .00063 .06351 -.0000002

418.000 4.2846 .31938 .00342 .06351 -.0000011

426.000 4.7926 .35054 .00645 .06349 -.0000019

434.000 5.3005 .38054 .00961 .06348 -.0000026

442.000 5.8082 .40945 .01286 .06345 -.0000032

450.000 6.3158 .43731 .01619 .06343 -.0000038

458.000 6.8230 .46418 .01957 .06339 -.0000044

466.000 7.3300 .49011 .02301 .06336 -.0000049

474.000 7.8367 .51515 .02648 .06331 -.0000053

482.000 8.3431 .53933 .02999 .06327 -.0000057

490.000 8.8490 .56270 .03352 .06322 -.0000061

498.000 9.3546 .58529 .03708 .06317 -.0000065

506.000 9.8598 .60715 .04067 .06312 -.0000068

514.000 10.3645 .62829 .04427 .06306 -.0000071

522.000 10.8688 .64877 .04789 .06301 -.0000073

530.000 11.3726 .66859 .05152 .06295 -.0000076

538.000 11.8759 .68780 .05516 .06289 -.0000078

546.000 12.3788 .70642 .05882 .06282 -.0000080

554.000 12.8811 .72447 .06248 .06276 -.0000082

562.000 13.3829 .74198 .06615 .06269 -.0000083

570.000 13.8842 .75896 .06983 .06262 -.0000084

578.000 14.3849 .77545 .07351 .06256 -.0000086

586.000 14.8851 .79146 .07720 .06249 -.0000087

594.000 15.3847 .80701 .08089 .06242 -.0000088

602.000 15.8837 .82212 .08458 .06235 -.0000089

610.000 16.3822 .83680 .08828 .06228 -.0000089

618.000 16.8802 .85107 .09198 .06220 -.0000090

626.000 17.3775 .86495 .09568 .06213 -.0000091

634.000 17.8743 .87845 .09938 .06206 -.0000091

642.000 18.3704 .89158 .10308 .06199 -.0000091

650.000 18.8660 .90437 .10678 .06191 -.0000092

658.000 19.3611 .91681 .1 1047 .06184 -.0000092

666.000 19.8555 .92893 .11417 .06177 -.0000092

674.000 20.3493 .94073 .1 1787 .06169 -.0000092

682.000 20.8426 .95223 .12156 .06162 -.0000092

690.000 21.3352 .96344 .12525 .06154 -.0000092

698.000 21.8273 .97436 .12894 .06147 -.0000092

100
Table 17. (Continued).

I sobutane I sochore at 250 kg/rrr

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Derivative Der i vat i ve Curvature

K MPa MPa.m3/kg MPa/K MPaA2

407.742 3.6332 .24917 .00009 .06998 .0100265

410.000 3.7952 .25884 .00092 .07235 .0003342

418.000 4.3802 .29302 .00418 .07364 .0000919

426.000 4.9717 .32635 .00770 .07420 .0000545

434.000 5.5668 .35867 .01138 .07456 .0000379

442.000 6.1644 .38998 .01517 .07482 .0000280

450.000 6.7637 .42030 .01903 .07502 .0000213

458.000 7.3645 .44963 .02297 .07517 .0000164

466.000 7.9663 .47803 .02696 .07528 .0000125

474.000 8.5689 .50551 .03099 .07537 .0000094

482.000 9.1721 .53211 .03506 .07543 .0000069

490.000 9.7758 .55787 .03917 .07548 .0000047

498.000 10.3797 .58282 .04331 .07551 .0000029

506.000 10.9839 .60700 .04747 .07553 .0000013

514.000 11.5881 .63042 .05165 .07553 -.0000001

522.000 12.1923 .65313 .05585 .07552 -.0000013

530.000 12.7965 .67514 .06006 .07551 -.0000023

538.000 13.4005 .69650 .06429 .07549 -.0000033

546.000 14.0042 .71721 .06853 .07546 -.0000041

554.000 14.6078 .73732 .07278 .07542 -.0000049

562.000 15.2110 .75684 .07704 .07538 -.0000055

570.000 15.8138 .77579 .08131 .07533 -.0000061

578.000 16.4163 .79420 .08558 .07528 -.0000067

586.000 17.0183 .81208 .08986 .07523 -.0000071

594.000 17.6199 .82947 .09414 .07517 -.0000076

602.000 18.2210 .84636 .09842 .07511 -.0000080

610.000 18.8216 .86280 .10271 .07504 -.0000083

618.000 19.4216 .87878 .10700 .07497 -.0000086

626.000 20.0211 .89433 . 1 1 1 29 .07490 -.0000089

634.000 20.6201 .90946 .11557 .07483 -.0000092

642.000 21.2184 .92419 .11986 .07476 -.0000094

650.000 21.8162 .93853 .12415 .07468 -.0000096

658.000 22.4133 .95249 . 1 2843 .07460 -.0000098

666.000 23.0098 .96610 .13272 .07452 -.0000099

674.000 23.6057 .97935 .13700 .07444 -.0000101

682.000 24.2009 .99227 .14128 .07436 -.0000102

690.000 24.7955 1.00486 .14555 .07428 -.0000103

698.000 25.3894 1.01713 .14982 .07420 -.0000104

101
Table 17. (Continued).

Isobutane I sochore at 300 kg/m^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Derivative Derivative Curvature

K MPa MPa.m3/kg l^a/K f^a/K^

405.537 3.5002 .20112 .00297 .09363 .0018158

410.000 3.9285 .22327 .00502 .09748 .0004944

418.000 4.7201 .26313 .01125 .10011 .0002329

426.000 5.5275 .30235 .01656 .10162 .0001535

434.000 6.3448 .34067 .02195 . 1 0267 .0001 131 442.000 7.1695 .37798 .02741 .10347 .0000877

450.000 7.9998 .41426 .03293 .10409 .0000700

458.000 8.8346 .44949 .03850 .10450 .0000558

466.000 9.6731 .48371 .04411 .10501 .0000465

474.000 10.5146 .51691 .04975 .10535 .0000382

482.000 11.3585 .54913 .05543 .10562 .0000314

490.000 12.2044 .58039 .06113 .10585 .0000257

498.000 13.0520 .61073 .05685 .10504 .0000208

506.000 13.9009 .64017 .07259 .10618 .0000166

514.000 14.750S .66874 .07335 .10630 .0000130

522.000 15.6017 .69547 .08412 .10539 .0000098

530.000 16.4531 .72339 .08990 .10645 .0000070

538.000 17.3050 .74953 .09558 .10551 .0000046

546.000 18.1572 .77492 .10148 .10653 .0000024

554.000 19.0095 .79958 .10728 .10655 .0000004

562.000 19.8619 .82354 .11308 .10554 -.0000013

570.000 20.7141 .84682 .1 1888 .10653 -.0000029

578.000 21.5662 .85945 .12459 .10550 -.0000043

586.000 22.4181 .89146 .13049 .10646 -.0000055

594.000 23.2695 .91285 .13630 .10541 -.0000057

602.000 24.1206 .93367 .14210 .10635 -.0000077

610.000 24.9711 .95391 .14790 .10629 -.0000085

613.000 25.8211 .97361 .15370 .10621 -.0000095

626.000 26.6705 .99279 .15949 .10613 -.0000102

634.000 27.5192 1.01146 .16528 .10605 -.0000109

642.000 28.3673 1.02963 .17105 .10595 -.0000115

650.000 29.2146 1.04734 .17684 .10587 -.0000121

658.000 30.0611 1.05458 .18251 .10577 -.0000125

566.000 30.9068 1.08139 .18838 .10566 -.0000131

674.000 31.7517 1.09776 .19414 .10556 -.0000135

682.000 32.5957 1.11372 .19989 .10545 -.0000139

690.000 33.4389 1.12928 .20564 .10534 -.0000142

698.000 34.2811 1.14446 .21138 .10522 -.0000145

102
Table 17. (Continued).

Isobutane I sochore at 350 kg/m-"

Isotherm 1 sochore 1 sochore

Temp. Pressure Z Derivative Der ivati ve Curvature

K MPa MPa.m3/kg NPa/K MPa/K^

398.439 3.1053 .15567 .01656 .13388 .0008360

402.000 3.5867 .17821 .02057 .13628 .0005517

410.000 4.6914 .22855 .02906 .13959 .0003197

418.000 5.8172 .27797 .03732 .14173 .0002241

426.000 6.9575 .32621 .04548 .14329 .0001696

434.000 8.1083 .37318 .05361 .14449 .0001336

442.000 9.2687 .41884 .06171 .14545 .0001077

450.000 10.4356 .46319 .06981 .14623 .0000879

458.000 11.6080 .50623 .07790 .14687 .0000723

466.000 12.7852 .54799 .08598 .14739 .0000596

474.000 13,9661 .58850 .09405 .14783 .0000490

482.000 15.1502 .62780 .10212 .14818 .0000401

490.000 16.3368 .66593 .1 1018 .14847 .0000325

498.000 17.5256 .70290 .1 1824 .14871 .0000260

506.000 18.7160 .73878 . 1 2629 .14889 .0000203

514.000 19.9077 .77359 .13433 .14903 .0000153

522.000 21.1004 .80737 .14236 .14914 .0000109

530.000 22.2938 .84016 .15038 .14921 .0000070

538.000 23.4876 .87199 .15839 .14925 .0000035

546.000 24.6817 .90289 .16639 .14926 .0000005

554.000 25.8758 .93291 .17438 .14926 -.0000023

562.000 27.0698 .96206 .18235 .14923 -.0000048

570.000 28.2634 .99038 .19031 .14918 -.0000070

578.000 29.4566 1.01791 .19826 .14912 -.0000090

586.000 30.6493 1.04466 .20620 .14904 -.0000108

594.000 31.8412 1.07067 .21412 .14895 -.0000124

602.000 33.0324 1.09597 .22203 . 1 4884 -.0000139

610.000 34.2226 1.12057 .22992 .14872 -.0000152

618.000 35.4119 1.14450 .23780 .14860 -.0000164

626.000 36.6002 1.16778 .24566 .14846 -.0000174

634.000 37.7873 1.19045 .25351 .14832 -.0000184

642.000 38.9733 1.21251 .26135 .14817 -.0000193

650.000 40.1580 1.23399 .26916 .14801 -.0000201

658.000 41.3414 1.25491 .27696 .14785 -.0000208

666.000 42.5236 1.27529 .28475 .14768 -.0000215

674.000 43.7043 1.29514 .29252 .14750 -.0000221

682.000 44.8836 1.31449 .30027 .14733 -.0000226

690.000 46.0615 1.33334 .30801 .14714 -.0000231

698.000 47.2379 1.35173 .31573 .14696 -.0000235

103
Table 17. (Continued).

I sobutane 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 MPa NPaTn3/k.9 MPa/K MPa/K^

384.746 2.4496 .11127 .05272 .19566 .0004687

386.000 2.6953 .12203 .05478 .19622 .0004360

394.000 4.2773 .18973 .06753 .19910 .0002995

402.000 5.8788 .25558 .07986 .20117 .0002236

410.000 7.4947 .31947 .09193 .20275 .0001740

418.000 9.1219 .38139 .10383 .20399 .0001384

426.000 10.7579 .44135 .11560 .20499 .0001113

434.000 12.4011 .49938 .12726 .20579 .0000899

442.000 14.0501 .55554 .13884 .20643 .0000725

450.000 15.7037 .60989 .15034 .20695 .0000580

458.000 17.3611 .66248 .16177 .20737 .0000458

466.000 19.0214 .71337 .17315 .20769 .0000354

474.000 20.6839 .76263 .18446 .20794 .0000265

482.000 22.3482 .81032 .19573 .20812 .0000187

490.000 24.0137 .85649 .20695 .20824 .0000119

498.000 25.6799 .90121 .21812 .20831 .0000059

506.000 27.3465 .94453 .22924 .20834 .0000006

514.000 29.0132 .98649 .24032 .20832 -.0000041

522.000 30.6796 1.02717 .25137 .20827 -.0000083

530.000 32.3455 1.06659 .26237 .20819 -.0000120

538.000 34.0106 1.10482 .27333 .20808 -.0000154

546.000 35.6747 1.14190 .28425 .20795 -.0000183

554.000 37.3376 1.17787 .29514 .20779 -.0000210

562.000 38.9992 1.21278 .30599 .20761 -.0000234

570.000 40.6593 1.24666 .31680 .20741 -.0000256

578.000 42.3178 1.27955 .32758 .20720 -.0000275

586.000 43.9745 1.31149 .33832 .20697 -.0000292

594.000 45.6294 1.34252 .34903 .20673 -.0000308

602.000 47.2823 1.37266 .35970 .20648 -.0000322

610.000 48.9331 1.40196 .37035 .20622 -.0000335

618.000 50.5817 1 .43043 .38095 .20595 -.0000346

626.000 52.2282 1.45812 .39153 .20567 -.0000356

634.000 53.8724 1.48504 .40207 .20538 -.0000365

642.000 55.5142 1.51123 .41258 .20508 -.0000373

650.000 57.1537 1.53671 .42306 .20478 -.0000380

658.000 58.7907 1.56151 .43351 .20447 -.0000387

666.000 60.4252 1.58564 .44393 .20416 -.0000393

674.000 62.0572 1.60914 .45432 .20385 -.0000397

682.000 63.6867 1.63202 .46468 .20353 -.0000402

690.000 65.3137 1.65431 .47500 .20320 -.0000406

698.000 66.9380 1.67602 .48530 .20288 -.0000409

104
Table 17. (Continued).

Isobutane I sochore at 450 kg/m-^

1 sotherm 1 sochore ! sochore

Temp. Pressure Z Der i vat i ve Der i vat i ve Curvature

K VPa MPa.m3/kg MPa/K MPa/K^

363.640 1.6554 .07072 .12619 .28536 .0002232

370.000 3.4745 .14588 .14026 .28663 .0001776

378.000 5.7728 .23725 .15758 .28787 .0001355

386.000 8.0797 .32518 .17456 .28883 .0001039

394.000 10.3934 .40980 .19127 .28956 .0000790

402.000 12.7121 .49125 .20775 .29010 .0000588

410.000 15.0347 .56966 .22405 .29051 .0000420

418.000 17.3599 .64518 .24017 .29078 .0000278

426.000 19.6869 .71792 .25614 .29096 .0000157

434.000 22.0150 .78802 .27197 .29104 .0000052

442.000 24.3433 .85559 .28768 .29104 -.0000039

450.000 26.6715 .92075 .30326 .29098 -.0000119

458.000 28.9988 .98361 .31874 .29086 -.0000189

466.000 31.3250 1.04427 .33411 .29068 -.0000250

474.000 33.6496 1.10283 .34939 .29046 -.0000305

482.000 35.9722 1.15939 .36457 .29019 -.0000354

490.000 38.2926 1.21402 .37966 .28989 -.0000397

498.000 40.6104 1.26683 .39467 .28956 -.0000435

506.000 42.9254 1.31787 .40960 .28920 -.0000469

514.000 45.2375 1.36724 .42445 .28881 -.0000499

522.000 47.5463 1.41500 .43922 .28840 -.0000526

530.000 49.8513 1.46122 .45392 .28797 -.0000550

538.000 52.1538 1.50596 .46855 .28752 -.0000571

546.000 54.4521 1.54928 .48311 .28706 -.0000590

554.000 56.7466 1.59125 .49761 .28658 -.0000607

562.000 59.0373 1.63192 .51204 .28609 -.0000622

570.000 61.3240 1.67134 .52640 .28558 -.0000635

578.000 63.6066 1.70956 .54070 .28 507 -.0000646

586.000 65.8851 1.74662 .55495 .28455 -.0000656

594.000 68.1593 1.7B258 .56913 .28402 -.0000665

602.000 70.4294 1.81747 .58326 .28349 -.0000672

105
Table 17. (Continued),

sobutane I sochore at 500 kg/m-^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Derivative Derivative Curvature

K NPa NPa.m3/kg MPa/K MPa/K^

334.887 .9034 .03772 .25462 .41183 -.0000375

338.000 2.1852 .09039 .26377 .41171 -.0000404

342.000 3.8317 . 1 5665 .27544 .41154 -.0000442

346.000 5.4775 .22134 .28701 .41 136 -.0000480

350.000 7.1226 .28452 .29850 .41116 -.0000518

354.000 8.7668 .34625 .30990 .41094 -.0000555

358.000 10.4101 .40656 .32122 .41071 -.0000592

362.000 12.0525 .46550 .33247 .41047 -.0000627

366.000 13.6938 .52311 .34365 .41021 -.0000662

370.000 15.3341 .57944 .35475 .40994 -.0000695

374.000 16.9733 .63452 .36579 .40966 -.0000727

378.000 18.61 14 .68840 .37677 .40936 -.0000757

382.000 20.2482 .741 10 .38769 .40905 -.0000787

386.000 21.8838 .79266 .39855 .40873 -.0000815

390.000 23.5180 .84312 .40935 .40840 -.0000842

394.000 25.1509 .89250 .42010 .40806 -.0000867

398.000 26.7825 .94085 .43080 .40771 -.0000892

402.000 28.4126 .98818 .44144 .40734 -.0000915

406.000 30.0412 1.03453 .45204 .40697 -.0000937

410.000 31.6683 1.07992 .46259 .40659 -.0000958

414.000 33.2940 1.12439 .47309 .40621 -.0000978

418.000 34.9180 1.16795 .48355 .40581 -.0000997

422.000 36.5404 1.21063 .49396 .40541 -.0001015

426.000 38.1613 1.25246 .50433 .40500 -.0001032

430.000 39.7804 1 .29346 .51466 .40458 -.0001047

434.000 41.3979 1.33365 .52495 .40416 -.0001062

438.000 43.0137 1.37304 .53521 .40373 -.0001077

442.000 44.6278 1.41168 .54542 .40330 -.0001090

446.000 46.2401 1.44956 .55559 .40286 -.0001102

450.000 47.8507 1.48671 .56573 .40242 -.0001 114 454.000 49.4595 1.52316 .57583 .40197 -.0001125

458.000 51.0665 1.55891 .58590 .40152 -.0001135

462.000 52.6716 1.59399 .59593 .40106 -.0001145

466.000 54.2750 1.62842 .60593 .40060 -.0001154

470.000 55.8765 1.66220 .61589 .40014 -.0001162

474.000 57.4761 1.69535 .62582 .39967 -.0001170

478.000 59.0739 1.72790 .63572 .39921 -.0001177

482.000 60.6697 1.75985 .64559 .39873 -.0001183

486.000 62.2637 1.79123 .65543 .39826 -.0001 189 490.000 63.8558 1.82203 .66524 .39778 -.0001195

494.000 65.4460 1.85228 .67501 .39730 -.0001200

498.000 67.0342 1.88200 .68476 .39682 -.0001205

502.000 68.6205 1.91118 .69448 .39634 -.0001209

506.000 70.2049 1.93985 .70417 .39585 -.0001212

510.000 71.7874 1.96802 .71383 .39537 -.0001216

106
Table 17. (Continued),

sobutane I sochore at 550 kg/m-'

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Der ivat 1 ve Der i vative Curvature

K MPa MPa.m3/kg MPa/K MPa/K^

298.696 .3559 .01515 .45889 .58797 -.0004143

302.000 2. 2964 .09665 .47144 .58663 -.0003976

306.000 4.6398 .19272 .48656 .58507 -.0003800

310.000 6.9771 .28607 .50159 .58359 -.0003647

314.000 9.3085 .37680 .51654 .58215 -.0003515

318.000 11.6344 .46502 .53140 .58077 -.0003399

322.000 13.9548 .55084 .54618 .57943 -.0003299

326.000 16.2699 .63435 .56088 .57813 -.0003210

330.000 18.5799 .71563 .57550 .57686 -.0003132

334.000 20.8848 .79477 .59004 .57563 -.0003062

338.000 23.1849 .87186 .60450 .57441 -.0003001

342.000 25.4802 .94697 .61889 .57322 -.0002946

346.000 27.7707 1.02016 .63320 .57206 -.0002897

350.000 30.0566 1.09152 .64744 .57091 -.0002853

354.000 32.3380 1.161 10 .66161 .56977 -.0002813

358.000 34.6148 1.22896 .67571 .56865 -.0002777

362.000 36.8872 1.29517 .68974 .56755 -.0002744

366.000 39.1552 1.35978 .70370 .56646 -.0002714

370.000 41.4189 1.42284 .71760 .56538 -.0002687

374.000 43.6783 1.48441 .73143 .56431 -.0002662

378.000 45.9334 1.54453 .74520 .56325 -.0002638

382.000 48.1843 1.60325 .75891 .56220 -.0002616

386.000 50.4310 1.66062 .77256 .561 16 -.0002596

390.000 52.6735 1.71667 .78615 .56012 -.0002577

394.000 54.9120 1.77145 .79968 .55909 -.0002559

398.000 57.1463 1.82 500 .81316 .55807 -.0002542

402.000 59.3766 1.87736 .82658 .55706 -.0002526

406.000 61.6028 1.92856 .83995 .55605 -.0002511

410.000 63.8250 1.97864 .85326 .55505 -.0002496

414.000 66.0432 2.02762 .86652 .55406 -.0002482

418.000 68.2574 2.07555 .87972 .55307 -.0002468

422.000 70.4677 2.12245 .89288 .55208 -.0002454

I sobutane I sochore at 600 kg/m-^

255.790 .0804 .00366 .76165 .83395 -.0010718

258.000 1.9207 .08674 .77231 .83162 -.0010375

262.000 5.2390 .23298 .79157 .82758 -.0009812

266.000 8.5417 .37414 .81076 .82376 -.0009313

270.000 11.8294 .51047 .82988 .82013 -.0008869

274.000 15.1029 .64221 .84893 .81666 -.0008473

278.000 18.3629 .76960 .86789 .81334 -.0008118

282.000 21.6098 .89284 .88678 .81016 -.0007799

286.000 24.8443 1.01212 .90559 .80710 -.0007511

290.000 28.0668 1.12762 .92431 .80415 -.0007251

294.000 31.2776 1.23953 .94294 .80130 -.0007015

298.000 34.4772 1.34799 .96149 .798 53 -.0006800

302.000 37.6660 1.45316 .97995 .79585 -.0006604

306.000 40.8442 1.55517 .99833 .79325 -.0006425

310.000 44.0121 1.65417 1.01662 .79071 -.0006260

314.000 47.1699 1.75027 1.03482 .78824 -.0006108

318.000 50.3180 1.84360 1.05294 .78582 -.0005968

322.000 53.4566 1.93426 1.07097 .78346 -.0005838

326.000 56.5858 2.02237 1.08892 .78115 -.0005718

330.000 59.7059 2. 10801 1.10679 .77889 -.0005605

334.000 62.8170 2.19129 1.12457 .77667 -.0005501

338.000 65.9192 2.27230 1.14228 .77449 -.0005402

342.000 69.0129 2.35112 1 . 1 5990 .77234 -.0005310

107
Table 17. (Continued).

sobutane I sochore at 650 kg/m-^

1 sotherm sochore 1 sochore

Temp. Pressure Z Derivative Derivative Curvature

K MPa MPaTn3/kg MPa A MPa/K^

207.623 .0063 .00033 1.18604 .18388 -.0024010

208.000 .4525 .02340 1. 18829 1.18297 -.0023851

210.000 2.8138 .1441 1 1.20026 .17829 -.0023040

212.000 5. 1658 .26207 1.21225 .17375 -.0022279

214.000 7.5089 .37737 1.22424 .15937 -.0021554

216.000 9.8434 .49012 1.23523 .15513 -.0020892

218.000 12.1695 .60038 1.24822 .15101 -.0020260

220.000 14.4875 .70824 1.26022 .15702 -.0019655

222.000 16.7977 .81378 1.27221 .15314 -.0019104

224.000 19.1002 .91705 1.28419 . 14938 -.0018574

226.000 21.3952 1.01816 1.29516 .14571 -.0018074

228.000 23.6831 1.11715 1.30813 .14214 -.0017502

230.000 25.9639 1.21409 1.32008 . 1 3857 -.0017154

232.000 28.2378 1.30904 1.33202 .13528 -.0015731

234.000 30.5051 1.40205 1.34394 .13198 -.0015330

236.000 32.7658 1.49320 1.35535 .12875 -.0015949

238.000 35.0201 1.58252 1.36774 .12559 -.0015588

240.000 37.2682 1.67007 1.37962 1.12251 -.0015244

242.000 39.5102 1.75591 1.39147 .11950 -.0014918

244.000 41.7462 1.84008 1.40330 .11554 -.0014507

246.000 43.9764 1.92262 1.41512 .11355 -.0014311

248.000 46.2009 2.00358 1.42691 .11082 -.0014030

250.000 48.4197 2.08301 1.43868 .10804 -.0013751

252.000 50.6331 2.16094 1.45042 .10531 -.0013504

254.000 52.8410 2.23741 1.46215 .10264 -.0013259

256.000 55.0436 2.31247 1.47385 .10001 -.0013024

258.000 57.2411 2.38514 1.48552 .09743 -.0012800

260.000 59.4334 2.45847 1.49717 .09489 -.0012585

262.000 61.5206 2.52949 1.50880 1 .09239 -.0012379

264.000 63.8030 2.59923 1.52040 .08994 -.0012182

266.000 65.9804 2.66773 1.53197 .08752 -.001 1992 268.000 68.1531 2.73501 1.54352 .08514 -.0011811

270.000 70.3210 2.80111 1.55505 .08279 -.0011636

I sobutane I sochore at 700 kg/m^

155.411 .0001 .00000 1.75605 1.70217 -.0055644

158.000 2,6978 .17052 1.77724 1.69348 -.0053578

150.000 6.0742 .37913 1.79141 1.58298 -.0051367

162.000 9.4300 .58133 1.80559 1.57293 -.0049223

154.000 12.7562 .77739 1.82006 1.66328 -.0047231

156.000 16.0834 .95759 1.83451 1.55402 -.0045377

168.000 19.3825 1.15219 1.84903 1.54512 -.0043651

170.000 22.6641 1.33142 1.86361 1.63656 -.0042040

172.000 25.9289 1.50550 1.87823 1.62830 -.0040536

174.000 29.1775 1.674 64 1.89290 1.52034 -.0039130

176.000 32.4105 1.83906 1.90761 1.51264 -.0037813

178.000 35.6283 1.99893 1.92234 1.50520 -.0035580

180.000 38.8314 2.15444 1.93710 1.59801 -.0035422

182.000 42.0204 2.30575 1.95187 1.59103 -.0034334

184.000 45.1957 2.45303 1.96665 1.58427 -.0033311

186.000 48.3576 2.59642 1.98144 1.57770 -.0032343

188.000 51.5066 2.73608 1.99523 1.57132 -.0031440

190.000 54.6430 2.87214 2.01103 1.56512 -.0030584

192.000 57.7672 3.004 72 2.02581 1.55909 -.0029775

194.000 60.8795 3.13395 2.04059 1.55321 -.0029010

196.000 63.9802 3.25996 2.05536 1.54748 -.0028286

198.000 67.0695 3.38285 2.07012 1.54189 -.0027599

200.000 70.1478 3.50274 2.08485 1.53644 -.0026949

108
Table 17. (Continued).

Isobutane I sochore at 741.375 kg/m^

1 sotherm 1 sochore 1 sochore

Temp. Pressure Z Derivative Der i vat i ve Curvature

K MPa MPa.m3/kg MPa/K MPa/K^

113.550 .0000 .00000 2.42683 2.35818 -.0125365

114.000 1.0599 .08767 2.42991 2.35258 -.0123604

115.000 3.4064 .27930 2.43686 2.34041 -.0119829

116.000 5.7409 .46666 2.44392 2.32861 -.0116236

117.000 8.0637 .64988 2.45110 2.31715 -.0112814

118.000 10.3753 .82909 2.45839 2.30604 -.0109553

119.000 12.6759 1.00442 2.46579 2.29524 -.0106444

120.000 14.9659 1.17599 2.47328 2.28474 -.0103478

121.000 17.2455 1.34392 2.48085 2.27454 -.0100646

122.000 19.5150 1.50832 2.48852 2.26461 -.0097943

123.000 21.7748 1.66929 2.49626 2.25495 -.0095360

124.000 24.0250 1.82694 2.50408 2.24553 -.0092890

125.000 26.2659 1.98137 2.51197 2.23636 -.0090528

126.000 28.4978 2.13267 2.51993 2.22743 -.0088268

127.000 30.7208 2.28093 2.52795 2.21871 -.0086104

128.000 32.9353 2.42625 2.53602 2.21020 -.0084031

129.000 35.1413 2.56869 2.54415 2.20190 -.0082045

130.000 37.3391 2.70835 2.55233 2.19379 -.0080141

131.000 39.5290 2.84530 2.56056 2.18587 -.0078314

132.000 41.7109 2.97961 2.56884 2.17812 -.0076561

133.000 43.8853 3.11136 2.57715 2.17055 -.0074877

134.000 46.0521 3.24062 2.58551 2.16315 -.0073261

135.000 48.2116 3.36745 2.59390 2.15590 -.0071707

136.000 50.3639 3.49192 2.60232 2.14880 -.0070213

137.000 52.5093 3.61409 2.61078 2.14185 -.0068776

1 38 . 000 54.6477 3.73402 2.61926 2.13505 -.0067393

139.000 56.7794 3.85176 2.62777 2.12837 -.0066062

140.000 58.9045 3.96738 2.63631 2.12183 -.0064780

141.000 61.0231 4.08093 2.64487 2.11542 -.0063545

142.000 63.1354 4.19245 2.65345 2.10912 -.0062354

143.000 65.2414 4.30200 2.66205 2.10294 -.0061206

144.000 67.3413 4.40963 2.67066 2.09688 -.0060098

145.000 69.4352 4.51539 2.67929 2.09092 -.0059029

146.000 71.5232 4.61931 2.68794 2.08507 -.0057997

109
Table 18. Calculated P( p) isotherms of isobutane.

Isobutane I sot he nm at 120 K

1 sotherm Isochore Isochore

Density Pressure Z Der i vat i ve Der i vat i ve Curvature

kg/m3 MPa MPa.m3/kg MPa/K MPa/K^

.00 .0000 1.00000 .01717 .00000 -.0000000

735.12 .0000 .00000 2.31157 2.23922 -.0109656

735.63 1.1754 .09309 2.32434 2.24279 -.0109115

736.25 2.6331 .20834 2.34016 2.24721 -.0108458

736.87 4.1006 .32419 2.35606 2.25167 -.0107813

737.50 5.5781 .44062 2.37206 2.25616 -.0107178

738.12 7.0657 .55765 2.38814 2.26069 -.0106554

738.75 8.5633 .67528 2.40432 2.26524 -.0105941

739.38 10.0711 .79351 2.42059 2.26983 -.0105338

740.00 11.5890 .91234 2.43695 2.27446 -.0104746

740.63 13.1173 1.03178 2.45340 2.27911 -.0104153

741.25 14.6558 1.15182 2.46994 2.28380 -.0103591

741.87 16.2047 1.27248 2.48658 2.28852 -.0103029

Isobutane Isotherm at 130 K

.00 .0000 1.00000 .01860 .00000 -.0000000

725.45 .0000 .00000 2.14582 2.07129 -.0089963

726.25 1.7257 .12778 2.16498 2.07703 -.0089355

727.50 4.4507 .32898 2.19515 2.08610 -.0088430

728.75 7.2137 .53230 2.22564 2.09527 -.0087538

730.00 10.0150 .73774 2.25646 2.10455 -.0086675

731.25 12.8550 .94533 2.28760 2.11394 -.0085843

732.50 15.7341 1.15508 2.31907 2.12343 -.0085041

733.75 18.6528 1.36702 2.35088 2.13303 -.0084267

735.00 21.61 IS 1.58116 2.38302 2.14274 -.0083521

736.25 24.6106 1.79752 2.41550 2.15254 -.0082803

737.50 27.6504 2.01612 2.44833 2.16245 -.0082113

738.75 30.7315 2.23699 2.48151 2.17246 -.0081449

740.00 33.8543 2.46014 2.51503 2.18256 -.0080812

741.25 37.0192 2.68559 2.54891 2.19276 -.0080201

742.50 40.2267 2.91337 2.58316 2.20306 -.0079615

743.75 43.4772 3.14350 2.61776 2.21344 -.0079054

74 5.00 46.7713 3.37599 2.65274 2.22392 -.0078517

746.25 50.1093 3.61087 2.68808 2.23450 -.0078005

747.50 53.4917 3.84816 2.72381 2.24516 -.0077517

110
Table 18. (Continued).

Isobutane Isotherm at 140 K

Isotherm Isochore Isochore

Density Pressure Z Der i vat i ve Der i vat i ve Curvature

kg/m3 MPa MPa.m3/kg MPaA MPa/K^

.00 .0000 .99998 .02003 ,00000 -.0000000

715.81 .0000 .00000 1.99329 1,92029 -,0074533

716.25 .8843 .06165 2.00333 1,92347 -,0074289

717.50 3.4063 .23706 2.03191 1,93250 -,0073617

718.75 5.9642 .41435 2,06076 1,94162 -,0072968

720.00 8.5583 .593 54 2.08992 1,95084 -.0072342

721.25 11.1891 .77465 2.1 1936 1.96015 -.0071738

722.50 13.8569 .95768 2.14910 1.96955 -.0071156

723.75 16.5620 1.14266 2.17914 1.97904 -.0070596

725.00 19.3048 1.32960 2.20948 1.98862 -.0070057

726.25 22.0858 1.51852 2.24013 1.99829 -.0069538

727.50 24.9053 1.70943 2.27108 2.00804 -,0069040

728.75 27.7636 1.90235 2.30235 2.01788 -,0068562

730.00 30.6613 2.09730 2.33393 2.02780 -,0068103

731.25 33.5986 2.29429 2.36582 2.03781 -,0067664

732.50 36.5760 2.49334 2.39804 2.04790 -.0067243

733.75 39.5938 2.69447 2.43058 2.05807 -.0066842

735.00 42.6527 2.89770 2.46345 2.06832 -.0066459

736.25 45.7527 3.10302 2.49665 2.07866 -.0066093

737.50 48.8944 3.31048 2.53018 2.08907 -.0065746

738.75 52.0732 3.52008 2.56405 2.09956 -.0065417

740.00 55.3046 3.73184 2.59826 2.11012 -.0065104

741.25 58.5740 3.94579 2.63282 2.12076 -.0064809

742.50 61.8868 4.16193 2.66773 2.13147 -.0064530

743.75 65.2435 4.38030 2.70299 2.14226 -.0064268

745.00 68.6445 4.60090

Isobutane

2.73861

Isotherm at 160 K

2.15312 -.0064022

.00 .0001 .99982 .02288 .00000 -.0000000

696.54 .0001 .00001 1.71961 1.65863 -,0052313

697.50 1.6609 .10404 1.73935 1.66533 -.0052040

698.75 3.8513 .24082 1.76526 1.67412 -.0051697

700.00 6.0742 .37913 1.79141 1.68298 -.0051367

701.25 8.3299 .51900 1.81781 1.69191 -.0051050

702.50 10.6188 .66044 1.84446 1.70091 -.0050746

703.75 12.9412 .80345 1.87136 1.70998 -.0050455

705.00 15.2973 .94804 1.89851 1.7191

-.0050175

706.25 17.6876 1.09424 1.92 592 1.72831 -.0049908

707.50 20.1122 1.24204 1,95359 1.73758 -.0049652

708.75 22.5717 1.39146 1.98151 1,74692 -.0049408

710.00 25.0661 1.54252 2.00969 1.75632 -.0049175

711.25 27.5959 1.69521 2.03814 1.76579 -.0048954

712.50 30.1616 1.84957 2.06685 1.77532 -.0048743

713.75 32.7632 2.00559 2.09583 1.78492 -.0048544

715.00 35.4013 2.16329 2.12508 1.79458 -.0048355

716.25 38.0760 2.32268 2.15460 1.80431 -.0048176

717.50 40.7879 2.48377 2,18439 1.81409 -.0048008

718.75 43.5371 2.64657 2.21447 1.82395 -.0047851

720.00 46.3242 2.81 110 2,24482 1.83386 -.0047703

721.25 49.1493 2.97737 2.27545 1,84383 -.0047565

722.50 52.0129 3.14539 2.30637 1,85387 -.0047438

723.75 54.9154 3.31518 2.33758 1,86397 -.0047319

725.00 57.8570 3.48674 2.36907 1.87412 -.004 721

726,25 60.8382 3.66009 2.40086 1.88434 -.00471 12 727.50 63.8593 3.83524 2.43295 1.89462 -.0047022

728.75 66.9206 4.01221 2.46533 1.90495 -.0046942

730.00 70.0227 4.19100 2.49801 1.91534 -.0046870

111
Table 18. (Cont i nued)

.

Isobutane sothemn at 180 K

1 sotherm Isochore Isochore

Density Pressure Z Der i vat i ve Der i vat i ve Curvature

kg/m3 MPa MPa«m3/kg MPa A MPa/K^

.03 .0007 .99890 .02569 .00000 -.0000000

677.18 .0007 .00004 1.47850 1.43840 -.0037472

677.50 .4769 .02734 1.48444 1.44052 -.0037426

678.75 2.3469 .13429 1.50769 1.44881 -.0037253

680.00 4.2462 .24252 1.53116 1.45715 -.0037088

681.25 6.1749 .35203 1.55485 1.46555 -.0036931

682.50 8.1334 .46283 1.57875 1.47400 -.0036782

683.75 10.1219 .57493 1.60288 1.48251 -.0036640

685.00 12.1407 .68834 1.62722 1.49107 -.0036505

686.25 14.1900 .80306 1.65179 1.49969 -.0036378

687.50 16.2702 .91912 1.67658 1.50836 -.0036258

688.75 18.3816 1.03650 1.70159 1.51708 -.0036145

690.00 20.5243 1.15523 1.72683 1.52586 -.0036038

691.25 22.6987 1.27531 1.75230 1.53470 -.0035939

692.50 24.9052 1.39675 1.77800 1.54358 -.0035846

693.75 27.1438 1.51956 1.80392 1.55252 -.0035759

695.00 29.4151 1.64374 1.83009 1.56151 -.0035679

696.25 31.7191 1.76932 1.85648 1.57056 -.0035606

697.50 34.0564 1.89628 1.88311 1.57965 -.0035538

698.75 36.4270 2.02465 1.90999 1.58880 -.0035477

700.00 38.8314 2.15444 1.93710 1.59801 -.0035422

701.25 41.2699 2.28565 1.96445 1.60726 -.0035373

702.50 43.7426 2.41829 1.99204 1.61656 -.0035329

703.75 46.2501 2.55237 2.01988 1.62592 -.0035292

705.00 48.7925 2.68790 2.04797 1.63533 -.0035261

706.25 51.3701 2.82489 2.07631 1.64479 -.0035235

707.50 53.9833 2.96335 2.10489 1.65429 -.0035215

708.75 56.6324 3.10328 2.13373 1.66385 -.0035201

710.00 59.3178 3.24471 2.16283 1.67346 -.0035192

711.25 62.0395 3.38762 2.19218 1.68312 -.0035189

712.50 64.7983 3.53206 2.22179 1.69283 -.0035191

713.75 67.5942 3.67801 2.25166 1.70259 -.0035199

715.00 70.4276 3.82548 2.28180 1.71240 -.0035212

112
Table 18. (Continued).

Isobutane Isotherm at 200 K

Isotherm Isochore Isochore

Density Pressure Z Der i vat i ve Der ivat i ve Curvature

kg/m3 MPa MPa.nT5/kg MPa/K MPaA^

.13 .0037 .99578 .02837 .00002 -.0000000

657.57 .0037 .00020 1.26266 1.24930 -.0027130

658.75 1.5019 .07969 1.28227 1.25657 -.0027061

660.00 3.1179 .16512 1.30327 1.26434 -.0025992

661.25 4.7602 .25162 1.32447 1.27215 -.0026928

662.50 6.4291 .33920 1.34587 1.28000 -.0026869

663.75 8.1250 .42787 1.36746 1.28790 -.0026815

665.00 9.8479 .51762 1.38925 1.29584 -.0025765

666.25 11.5982 .60848 1.41124 1.30383 -.0026720

667.50 13.3761 .70044 1.43343 1.31187 -.0025679

668.75 15.1818 .79351 1.45582 1.31995 -.0026642

670.00 17.0157 .88770 1.47841 1.32807 -.0025609

671.25 18.8779 .98302 1.50121 1.33524 -.0025581

672.50 20.7688 1.07947 1.52421 1.34446 -.0025555

673.75 22.6885 1.17706 1.54742 1.35272 -.0026535

675.00 24.6374 1.27580 1.57083 1.36102 -.0025519

676.25 26.6157 1.37570 1.59446 1.36937 -.0026506

677.50 28.6236 1.47675 1.61829 1.37777 -.0026497

678.75 30.6615 1.57898 1.64234 1.38621 -.0026492

680.00 32.7296 1.68238 1.66660 1.39469 -.0026491

681.25 34.8281 1.78696 1.69107 1.40322 -.0026493

682.50 36.9574 1.89274 1.71576 1.41 179 -.0026499

683.75 39.1176 1.99971 1.74067 1.42041 -.0026509

685.00 41.3091 2.10789 1.76579 1.42907 -.0026522

686.25 43.5322 2.21728 1.79114 1.43778 -.0026538

68 7.50 45.7871 2.32789 1.81670 1.44553 -.0025559

688.75 48.0740 2.43972 1.84249 1.45532 -.0026582

690.00 50.3934 2.55280 1.86850 1.46416 -.0026610

691.25 52.7454 2.66711 1.89474 1.47304 -.0026540

692.50 55.1303 2.78267 1.92121 1.48197 -.0026674

693.75 57.5485 2.89950 1.94790 1.49094 -.0026712

695.00 60.0002 3.01758 1.97483 1.49995 -.0025752

696.25 62.4857 3.13694 2.00198 1.50901 -.0025796

697.50 65.0052 3.25758 2.02937 1.51811 -.0025844

698.75 67.5592 3.37951 2.05700 1.52725 -.0026895

700.00 70.1478 3.50274 2.08486 1.53644 -.0026949

Isobutane Isotherm at 220 K

.44 .0138 .98845 .03076 .00006 -.0000000

637.55 .0138 .00069 1.06755 1.08428 -.0019672

640.00 2.6758 .13285 1.10407 1.09830 -.0019648

642.50 5.4832 .27118 1. 14202 1.11275 -.0019636

645.00 8.3865 .41316 1.18059 1.12735 -.0019635

647.50 11.3873 .55883 1.22009 1.14211 -.0019645

650.00 14.4875 .70824 1.25022 1.15702 -.0019665

652.50 17.6890 .86143 1.30109 1.17209 -.0019595

655.00 20.9936 1.01846 1.34272 1.18731 -.0019735

657.50 24.4032 1.17937 1.38510 1.20269 -.0019784

660.00 27.9198 1.34421 1.42826 1.21822 -.0019843

662.50 31.5452 1.51302 1.47219 1.23391 -.0019910

665.00 35.2814 1.68587 1.51591 1.24975 -.0019986

667.50 39.1304 1.85278 1.56242 1.25575 -.0020071

670.00 43.0942 2.04362 1.50874 1.28191 -.0020165

672 . 50 47.1748 2.22903 1.65588 1.29822 -.0020267

675.00 51.3743 2.41847 1.70384 1.31459 -.0020378

677.50 55.6947 2.61218 1.75253 1.33132 -.0020497

680.00 60.1381 2.81022 1.80226 1.34810 -.0020624

682.50 64.7067 3.01263 1.85275 1.36504 -.0020759

685.00 69.4026 3.21947 1.90411 1.38214 -.0020903

113
Table 18. (Continued).

isobutane I sothenn at 240 K

Isotherm Isochore Isochore

Density Pressure Z Derivative Der i vat i ve Curvature

kg/m3 MPa MPa.m3/kg MPa/K MPa/K^

1.19 .0398 .97514 .03269 .00017 -.0000001

616.90 .0398 .00188 .89025 .93827 -.0014136

617.50 .5749 .02712 .89804 .94139 -.0014146

620.00 2.8610 .13441 .93099 .95451 -.0014194

622.50 5.2304 .24474 .96460 .96776 -.0014249

625.00 7.6845 .35814 .99887 .981 15 -.0014311

627.50 10.2252 .47465 1.03380 .99467 -.0014379

630.00 12.8541 .59431 1.06942 1.00833 -.0014453

632.50 15.5729 .71717 1.10572 1.02212 -.0014532

635.00 18.3833 .84326 1.14271 1.03605 -.0014618

637.50 21.2870 .97262 1.18040 1.05011 -.0014709

640.00 24.2858 1.10531 1.21880 1.06431 -.0014806

642.50 27.3816 1.24135 1.25791 1.07865 -.0014907

645.00 30.5760 1.38080 1.29775 1.09313 -.0015015

647.50 33.8709 1.52369 1.33831 1.10775 -.0015127

650.00 37.2682 1.67007 1.37962 1.12251 -.0015244

652.50 40.7697 1.81998 1.42167 1.13741 -.0015367

655.00 44.3772 1.97346 1.46447 1. 15245 -.0015495

657.50 48.0927 2.13056 1.50804 1.16763 -.0015628

660.00 51.9180 2.29131 1.55238 1.18296 -.0015765

662.50 55.8552 2.45577 1.59751 1.19843 -.0015909

665.00 59.9062 2.62 398 1.64341 1.21403 -.0016057

667.50 64.0730 2.79598 1.69012 1.22979 -.0016210

670.00 68.3575 2.97182

Isobutane

1.73763

Isotherm at 260 K

1.24568 -.0016369

2.50 .0891 .95787 .03421 .00037 -.0000002

2.69 .0954 .95505 .03401 .00040 -.0000003

595.38 .0954 .00431 .72897 .80755 -.0009918

59 7.50 1.6633 .07485 .75300 .81760 -.0009993

600.00 3.5319 .16051 .78195 .82957 -.0010085

602.50 5.5736 .24873 .81 149 .84167 -.0010181

605.00 7.6399 .33953 c84165 .85388 -.0010280'

607,50 9.7823 .43296 .87243 .86621 -.0010382

610.00 12.0025 .52904 .90383 .87856 -.0010488

612.50 14.3020 .62783 .93586 .89123 -.0010597

615.00 15.6824 .72934 .96854 .90393 -.0010709

617.50 19.1452 .83363 1.00186 .91674 -.0010823

620.00 21.6922 .94072 1.03583 .92969 -.0010941

622.50 24.3249 1.05066 1.07047 .94275 -.0011062

625.00 27.0451 1.16347 1.10577 .95594 -.001 1185

627.50 29.8544 1.27921 1.14175 .96926 -.0011312

630.00 32.7544 1.39790 1.17841 .98270 -.0011441

632.50 35.7470 1.51959 1.21576 .99627 -.001 1574 635.00 38.8338 1.64431 1.25381 1.00997 -.001 1709 637.50 42.0165 1.77210 1.29256 1.02379 -.001 1847 640.00 45.2971 1.90300 1.33203 1.03775 -.001 1989 642.50 48.6773 2.03705 1.37222 1.05184 -.0012133

64 5.00 52.1588 2.17429 1.41313 1.06606 -.0012280

647.50 55.7436 2.31475 1.45478 1.08041 -.0012431

650.00 59.4334 2.45847 1.49717 1.09489 -.0012585

652.50 63.2301 2.60550 1.54031 1.10950 -.0012742

655.00 67.1356 2.75588 1.58422 1.12425 -.0012902

657.50 71.1518 2.90963 1.62888 1.13913 -.0013066

114
Table 18. (Continued).

Isobutane Isotherm at 280 K

Isotherm 1 sochore 1 sochore

Density Pressure Z Der i vat i ve Der i vat i ve Curvature

kg/m3 MPa MPa.m3/kg MPa/K MPa/K^

2.50 .0965 .96328 .03729 .00037 -.0000001

5.00 .1867 .93222 .03490 .00077 -.0000008

5.34 .1984 .92813 .03457 .00082 -.0000010

572.68 .1984 .00865 .58264 .68927 -.0006625

575.00 1.5775 .06850 .60508 .69918 -.0006732

577.50 3.1209 .13493 .62976 .70996 -.0006849

580.00 4.7268 .20347 .65499 .72084 -.0006967

582.50 6.3963 .27416 .68077 .73182 -.0007086

585.00 8.1310 .34702 .70711 .74291 -.0007206

587.50 9.9323 .42209 .73402 .75411 -.0007328

590.00 11.8016 .49941 .76150 .76541 -.0007450

592.50 13.7403 .57899 .78957 .77683 -.0007574

595.00 15.7500 .66089 .81823 .78835 -.0007700

597.50 17.8320 .74512 .84749 .79999 -.0007826

600.00 19.9879 .83173 .87735 .81174 -.0007954

602.50 22.2193 .92074 .90782 .82360 -.0008083

605.00 24.5275 1.01219 .93891 .83557 -.0008214

607.50 26.9143 1.10612 .97062 .84766 -.0008346

610.00 29.3812 1.20255 1.00297 .85987 -.0008479

612.50 31.9297 1.30152 1.03596 .87219 -.0008614

615.00 34.5615 1.40308 1.06959 .88463 -.0008751

617.50 37.2782 1.50724 1.10387 .89719 -.0008889

620.00 40.0814 1.61404 1.13882 .90987 -.0009028

622.50 42.9729 1.72353 1.17443 .92267 -.0009170

625.00 45.9542 1.83573 1.21072 .93559 -.0009313

627.50 49.0270 1.95068 1.24769 .94863 -.0009458

630.00 52.1932 2.06841 1.28535 .96179 -.0009605

632.50 55.4544 2.18897 1.32370 .97508 -.0009754

635.00 58.8123 2.31237 1.36276 .98848 -.0009905

637.50 62.2687 2.43867 1.40253 1.00202 -.0010058

640.00 65.8255 2.56790 1.44301 1.01567 -.0010213

642.50 69.4844 2.70009 1.48422 1.02946 -.0010371

115
Table 18. (Continued).

sobutane Isotherm at 298.15 K

isotherm Isochore Isochore

Density Pressure Z Derivative Der i vat i ve Curvature

kg/m3 MPa MPa -013 /kg MPa/K MPa/!<2

2.50 .1031 .96714 .04004 .00037 -.0000001

5.00 .2005 .94024 .03788 .00076 -.0000005

7.50 .2925 .91447 .03572 .001 18 -.0000014

9.15 .3503 .89744 .03423 .00148 -.0000027

550.69 .3503 .01492 .46233 .59082 -.0004209

552.50 1.2021 .05102 .47708 .59777 -.0004304

555.00 2.4207 .10226 .49783 .60743 -.0004436

557.50 3.6917 .15526 .51907 .61719 -.0004566

560.00 5.0164 .21004 .54081 .62704 -.0004697

562.50 6.3962 .26661 .56306 .63699 -.0004827

565.00 7.8321 .32503 .58582 .64704 -.0004956

567.50 9.3257 .38530 .60909 .65718 -.0005086

570.00 10.8781 .44747 .63290 .66743 -.0005215

572.50 12.4906 .51156 .65724 .67777 -.0005345

575.00 14.1647 .57760 .68211 .68821 -.0005474

577.50 15.9015 .64562 .70754 .69876 -.0005604

580.00 17.7029 .71565 .73352 .70941 -.0005734

582.50 19.5697 .78773 .76007 .72016 -.0005865

585.00 21.5037 .86187 .78718 .73102 -.0005995

58 7.50 23.5061 .93812 .81486 .74199 -.0006127

590.00 25.5785 1.01650 .84314 .75306 -.0006258

592.50 27.7223 1.09705 .87200 .76424 -.0006391

595.00 29.9389 1.17979 .90145 .77552 -.0006524

597.50 32.2300 1.26476 .93151 .78692 -.0006658

600.00 34.5970 1.35199 .96218 .79843 -.0006792

602.50 37.0414 1.44151 .99347 .81005 -.0006928

605.00 39.5649 1.53335 1.02539 .82178 -.0007064

607.50 42.1689 1.62754 1.05793 .83363 -.0007202

610.00 44.8551 1.72412 1.09111 .84558 -.0007340

612.50 47.6250 1.82312 1.12494 .85766 -.0007480

615.00 50.4803 1.92457 1.15942 .86984 -.0007621

617.50 53.4226 2.02850 1.19456 .88215 -.0007763

620.00 56.4536 2.13495 1.23036 .89457 -.0007906

622.50 59.5750 2.24394 1.26684 .90710 -.0008051

625.00 62.7884 2.35552 1.30399 .91976 -.0008197

627.50 66.0955 2.46971 1.34183 .93253 -.0008344

630.00 69.4981 2.58654 1.38037 .94542 -.0008493

116
Table 18 (Continued)

Isobutane Isotherm at 300 K

Isotherm Isochore Isochore

Density Pressure Z Der i vat i ve Derivative Curvature

kg/m3 MPa MPa.m3/kg MPa/K MPa/K^

2.50 .1038 .96749 .04032 .00037 -.0000001

5.00 .2019 .94095 .03818 .00075 -.0000004

7.50 .2947 .91558 .03604 .00117 -.0000013

9.54 .3696 .89393 .03414 .00156 -.0000029

548.35 .3696 .01571 .45072 .58120 -.0003987

550.00 1.1223 .04755 .46385 .58743 -.0004074

552.50 2.3073 .09731 .48419 .59698 -.0004207

555.00 3.5437 .14878 .50501 .60662 -.0004339

557.50 4.8327 .20200 .52632 .51636 -.0004470

560.00 6.1757 .25698 .54813 .62618 -.0004601

562.50 7.5738 .31375 .57045 .63611 -.0004731

565.00 9.0283 .37236 .59328 .64613 -.0004861

567.50 10.5406 .43281 .61663 .65625 -.0004991

570.00 12.1119 .49515 .64051 .66647 -.0005121

572.50 13.7436 .55940 .66492 .67679 -.0005251

575.00 15.4369 .62560 .68987 .68721 -.0005381

577.50 17.1934 .69376 .71537 .69773 -.0005511

580.00 19.0143 .76393 .74143 .70836 -.0005641

582.50 20.9010 .83613 .76805 .71909 -.0005771

585.00 22.8550 .91039 .79524 .72992 -.0005902

587.50 24.8777 .98674 .82301 .74086 -.0006034

590.00 26.9706 1.06522 .85136 .75191 -.0006166

592.50 29.1350 1.14585 .88030 .76306 -.0006298

595.00 31.3725 1.22866 .90984 .77433 -.0006431

597.50 33.6847 1.31370 .93998 .78570 -.0006565

600.00 36.0729 1.40098 .97073 .79718 -.0006700

602.50 38.5389 1.49053 1.00210 .80878 -.0006835

605.00 41.0840 1.58240 1.03410 .82048 -.0006972

607.50 43.7099 1.67662 1.06673 .83230 -.0007109

610.00 46.4181 1.77320 1.09999 .84423 -.0007248

612.50 49.2104 1.87219 1.13391 .85628 -.0007387

615.00 52.0882 1.97363 1.16847 .86844 -.0007528

617.50 55.0533 2.07753 1.20369 .88072 -.0007570

620.00 58.1072 2.18393 1.23958 .89311 -.0007813

622.50 61.2518 2.29287 1.27615 .90562 -.0007958

625.00 64.4885 2.40438 1.31339 .91825 -.0008104

627.50 67.8193 2.51849 1.35132 .93100 -.0008251

630.00 71.2457 2.63523 1.38994 .94386 -.0008400

117
Table 18. (Continued).

Isobutane Isotherm at 320 K

Density

kg/m3

5.00

10.00

15.00

16.26

Pressure

MPa

.2169

.4141 .5915

.6327

.94780

.90474

.85139

.85023

Isotherm

Der i vat i ve MPa.m3/kg

.04136

.03750

.03337

.03228

Isochore

Der i vat i ve MPa/K

.00075

.00159

.00255

.00281

Isochore

Curvature

MPa A2

-.0000003

-.0000017

-.0000056

-.0000074

521.79

525.00

530.00

535.00

540.00

545.00

550.00

555.00

560.00

565.00

570.00

575.00

580.00

585.00

590.00

595.00

600.00

60 5.00

610.00

615.00

.6327

1.7340

3.5851

5.6079

7.81 11 10.2038

12.7952

15.5950

18.6131

21.8595

25.3446

29.0793

33.0744

37.3412

41.8912

46.7363

51.8885

57.3601

63.1638

69.3125

.02649

.07216

.14777

.22899

.31600

.40901 .50823

.61385

.72611

.84521 .97137

1.10481

1.24576

1.3944 5 1.55111

1.71597

1.88926

2.07122

2.26209

2.46211

.33300

.35361 .38710

.42230

.45928

.49810

.53880

.58145

.62610

.67280

.72162

.77260

.82581

.88130

.93911

,99932

1.06197

1.1271 1 1.19480

1.26510

.48152

.49219

.50908

.52631

.54388

.56181 .58010

.59876

.61780

.63723

.65705

.67728

.69791 .71895

.74042

.76231

.78464

.80740

.83060

.85426

.0001804

.0001994

.0002279

.0002556

.0002325

.0003088

.0003347

.0003604

.0003858

. 0004 1 1 1 .0004363

.0004516

.0004370

.0005124

.0005381

.0005640

.0005902

.0006167

.0006435

.0006708

Isobutane Isotherm at 340 K

5.00

10.00

15.00

20.00

25.00

26.28

492.00

495.00

500.00

505.00

510.00

515.00

520.00

525.00

530.00

535.00

540.00

545.00

550.00

555.00

560.00

565.00

570.00

575.00

580.00

585.00

590.00

595.00

600.00

.2318

.4455

.5415

.8186

.9763

1.0135

1.0135

1.7247

3.0085

4.4232

5.9760

7.6744

9.5264

11.5398

13.7233

16.0853

18.6347

21.3809

24.3331

27.5012

30.8951

34.5251

38.4018

42.5360

45.9388

51.5215

56.5958

61.8736

67.4671

.95338

.91614

.87925

.84154

.80293

.79291

.04236

.07164

.12372

.18009

.24093

.30640

.37667

.45194

.53238

.61818

.70953

.80663

.90966

1.01883

1.13434

1.25641 1.38522

1.52101

1.66397

1.81433

1.97231

2.13812

2.31 198

.04449

.04099

.03733

.03350

.02957

.02854

.22954

.24417

.26962

.29650

.32487

.35477

.38627

.41941

.45425

.49085

.52925

.56952

.61170

.65585

.70205

.75032

.80072

.85332

.90816

.96531

1.02481

1.08672

1.15110

,00074 -.0000 02 ,00156 -.0000010

,00246 -.0000030

,00347 -.0000069

,00461 -.0000145

,00493 -.0000174

,38865 .0000091

,39719 -.0000109

,41163 -.0000423

,42636 -.0000717

.44140 -.0000997

,45676 -.0001264

47244 -.0001523

,48846 -.0001774

50482 -.0002021

52153 -.0002262

53859 -.0002501

,55602 -.0002738

57382 -.0002973

59199 -.0003207

51054 -.0003441

62948 -.0003675

64882 -.0003909

66855 -.0004145

68869 -.0004383

70924 -.0004522

73021 -.0004864

75160 -.0005108

77341 -.0005356

118
Table 18 (Continued).

Isobutane Isotherm at 360 K

Isotherm Isochore Isochore

Density Pressure Z Der i vat i ve Der i vat i ve Curvature

kg/m3 MPa MPa .m3/kg MPa/K MPa/K^

5.00 .2467 .95805 .04758 .00074 -.0000001

10.00 .4766 .92544 .04437 .00154 -.0000007

15.00 .6902 .89352 .04105 .00241 -.0000020

20.00 .8869 .86111 .03761 .00337 -.0000041

25.00 1.0662 .82818 .03412 .00440 -.0000076

30.00 1.2282 .79498 .03066 .00554 -.0000129

35.00 1.3729 .76173 .02726 .00678 -.0000210

40.00 1 . 5009 .72861 .02392 .00814 -.0000342

41.72 1.5410 .71727 .02278 .00864 -.0000407

457.14 1.5410 .06546 .14072 .30093 .0001891

460.00 1.9568 .08260 . 1 5040 .30763 .0001659

465.00 2.7528 .11496 .16819 .31954 .0001292

470.00 3.6405 .15041 .18710 .33170 .0000963

475.00 4.6258 .18911 .20718 .34413 .0000661

480.00 5.7144 .23118 .22848 .35683 .0000381

485.00 6.9127 .27677 .25105 .36982 .0000117

490.00 8.2271 .32604 .27494 .38310 -.0000135

495.00 9.6644 .37913 .30019 .39669 -.0000376

500.00 11.2314 .43620 .32686 .41059 -.0000610

505.00 12.9354 .49740 .35499 .42481 -.0000837

510.00 14.7838 .56291 .38464 .43936 -.0001059

515.00 16.7844 .63288 .41586 .45423 -.0001278

520.00 18.9451 .70748 .44870 .46944 -.0001493

525.00 21.2742 .78689 .48321 .48500 -.0001706

530.00 23.7801 .87128 .51945 .50090 -.0001918

535.00 26.4717 .96083 .55747 .51715 -.0002129

540.00 29.3578 1.05572 .59731 .53377 -.0002339

545.00 32.4479 1.15614 .63905 .55075 -.0002550

550.00 35.7516 1.26227 .68273 .56810 -.0002760

555.00 39.2786 1.37430 .72840 .58583 -.0002972

560.00 43.0390 1.49243 .77613 .60393 -.0003184

565.00 47.0433 1.61685 .82595 .62243 -.0003398

570.00 51.3021 1.74775 .87794 .64131 -.0003613

575.00 55.8264 1.88535 .93214 .66059 -.0003831

580.00 60.6273 2.02983 .98861 .68028 -.0004050

585.00 65.7164 2.18141 1.04740 .70037 -.0004273

590.00 71.1053 2.34029 1.10857 .72087 -.0004498

119
Table 18 (Continued).

Isobutane Isotherm at 380 K

Isotherm Isochore Isochore

Density Pressure Z Derivative Oer i vat i ve Curvature

kg/m3 MPa MPa.m3/kg MPaA MPaA2

5.00 .2615 .96201 .05064 .00074 -.0000001

10.00 .5073 .93322 .04769 .00153 -.0000005

15.00 .7381 .90529 .04464 .00238 -.0000014

20.00 .9535 .87705 .04149 .00330 -.0000028

25.00 1 . 1 530 .84846 .03832 .00428 -.0000049

30.00 1.3367 .81972 .03519 .00534 -.0000078

35.00 1.5050 .79107 .03214 .00646 -.0000118

40.00 1.6583 .76269 .02919 .00766 -.0000170

45.00 1.7971 .73469 .02635 .00894 -.0000238

50.00 1.9220 .70715 .02360 .01030 -.0000328

55.00 2.0333 .68011 .02095 .01174 -.0000450

60.00 2.1316 .65358 .01840 .01328 -.0000622

65.00 2.2174 .62758 .01592 .01493 -.0000882

67.11 2.2500 .61674 .01490 .01567 -.0001036

412.97 2.2500 .10023 .06754 .21595 .0004007

415.00 2.3909 .10599 .07153 .21959 .0003759

420.00 2.7741 .12151 .08189 .22872 .0003231

425.00 3.2111 .13899 .09302 .23804 .0002794

430.00 3.7057 .15854 .10498 .24757 .0002419

435.00 4.2623 .18026 .11780 .25734 .0002089

440.00 4.8852 .20425 .13152 .25735 .0001792

445.00 5.5791 .23064 .14619 .27761 .0001521

450.00 6.3488 .25955 .16185 .28814 .0001269

455.00 7.1993 .29108 .17853 .29893 .0001032

460.00 8.1359 .32538 .19629 .31000 .0000807

465.00 9.1640 .36255 .21516 .32135 .0000592

470.00 10.2894 .40275 .23519 .33300 .0000384

475.00 11.5179 .44609 .25642 .34493 .0000182

480.00 12.8557 .49271 .27390 .35717 -.0000015

485.00 14.3090 .54276 .30267 .36971 -.0000208

490.00 15.8846 .59637 .32779 .38256 -.0000398

495.00 17.5892 .65370 .35429 .39572 -.0000586

500.00 19.4299 .71489 .38224 .40921 -.0000772

505.00 21.4141 .78009 .41167 .42302 -.0000957

510.00 23.5492 .84946 .44265 .43716 -.0001141

515.00 25.8432 .92316 .47521 .45163 -.0001325

520.00 28.3040 1.00134 .50941 .46644 -.0001509

525.00 30.9401 1 . 084 1

8

.54531 .48160 -.0001693

530.00 33.7600 1.17183 .58295 .49711 -.0001878

535.00 36.7727 1.26447 .62240 .51297 -.0002063

540.00 39.9871 1.36227 .66369 .52919 -.0002250

545.00 43.4128 1.46541 .70690 .54577 -.0002438

550.00 47.0594 1.57406 .75206 .56272 -.0002627

555.00 50.9368 1.68840 .79925 .58005 -.0002818

560.00 55.0553 1.80863 .84850 .59775 -.0003011

565.00 59.4253 1.93491 .89987 .61583 -.0003206

570.00 64.0576 2.06745 .95343 .63431 -.0003404

575.00 68.9633 2.20642 1.00921 .65317 -.0003604

120
Table 18 (Continued).

1 sobutane Isotherm at 390 K

Isotherm 1 sochore 1 sochore

Dens ity Pressure Z Der i vati ve Der i vat i ve Curvature

kg/m3 MPa MPa'm3/kg MPa/K MPa/K^

5.00 .2688 .96378 .05217 .00074 -.0000001

10.00 .5226 .93667 .04932 .00152 -.0000005

15.00 .7619 .91046 .04640 .00237 -.0000012

20.00 .9863 .88401 .04337 .00327 -.0000024

25.00 1.1956 .85724 .04033 .00424 -.0000041

30.00 1.3898 .83037 .03734 .00527 -.0000064

35.00 1.5691 .80361 .03443 .00636 -.0000095

40.00 1.7342 .77713 .03162 .00751 -.0000133

45.00 1.8855 .75104 .02891 .00873 -.0000182

50.00 2.0235 .72541 .02631 .01002 -.0000241

55.00 2.1487 .70029 .02381 .01137 -.0000315

60.00 2.2618 .67570 .02142 .01278 -.0000408

65.00 2.3631 .65166 .01913 .01426 -.0000524

70.00 2.4532 .62819 .01694 .01581 -.0000673

75.00 2.5326 .60530 .01485 .01744 -.0000871

80.00 2.6019 .58298 .01286 .01915 -.0001148

85.00 2.6614 .56124 .01096 .02097 -.0001566

87.39 2.6865 .55106 .01008 .02188 -.0001854

383.70 2.6865 .12550 .03760 .17280 .0005647

385.00 2.7365 .12741 .03926 .17473 .0005405

390.00 2.9494 .13556 .04598 .18226 .0004636

395.00 3.1974 .14510 .05329 .18994 .0004041

400.00 3.4834 .15610 .06123 .19780 .0003560

405.00 3.8108 .16866 .06982 .20586 .0003156

410.00 4.1828 .18287 .07912 .21414 .0002807

415.00 4.6031 .19882 .08914 .22265 .0002499

420.00 5.0755 .21661 .09993 .23139 .0002222

425.00 5.6038 .23635 .11153 .24038 .0001968

430.00 6.1922 .25813 .12398 .24962 .0001733

435.00 6.8451 .28206 .13730 .25912 .0001512

440.00 7.5668 .30826 .15154 .26888 .0001302

445.00 8.3621 .33683 .16674 .27891 .0001101

450.00 9.2358 .36789 .18294 .28922 .0000908

455.00 10.1932 .40157 .20018 .29980 .0000721

460.00 11.2395 .43797 .21851 .31067 .0000538

465.00 12.3801 .47723 .23795 .32183 .0000359

470.00 13.6209 .51948 .25857 .33328 .0000183

475.00 14.9678 .56484 .28040 .34502 .0000009

480.00 16.4270 .61344 .30348 .35708 -.0000163

485.00 18.0048 .66543 .32787 .36943 -.0000333

490.00 19.7080 .72095 .35362 .38211 -.0000503

495.00 21.5434 .78013 .38076 .39509 -.0000673

500.00 23.5180 .84312 .40935 .40840 -.0000842

505.00 25.6394 .91007 .43944 .42203 -.0001011

510.00 27.9150 .98113 .47108 .43599 -.0001181

515.00 30.3528 1.05645 .50431 .45029 -.0001351

520,00 32.9609 1.13619 .53920 .46493 -.0001522

525.00 35.7477 1.22052 .57579 .47991 -.0001695

530.00 38.7218 1.30959 .61414 .49524 -.0001868

535.00 41.8921 1.40357 .65429 .51092 -.0002043

540.00 45.2678 1.50263 .69631 .52695 -.0002219

545.00 48.8584 1.60694 .74025 .54335 -.0002397

550.00 52.6735 1.71667 .78615 .56012 -.0002577

555.00 56.7233 1.83200 .83408 .57726 -.0002759

560.00 61.0178 1.95311 .88409 .59477 -.0002943

565.00 65.5678 2.08017 .93624 .61267 -.0003130

570.00 70.3838 2.21338 .99057 .63095 -.0003319

121
Tab I

I sobutane

8. (Continued),

sotherm at 400 K

Dens ity

kg/m3

10.00

20.00

30.00

40.00

50.00

50.00

70.00

80.00

90.00

100.00

110.00

120.00

120.37

341.92

350.00

360.00

370.00

380.00

390.00

400.00

410.00

420.00

430.00

440.00

450.00

460.00

470.00

430.00

490.00

500.00

510.00

520,00

530.00

540.00

550.00

560.00

Pressure

MPa

.5378

1.0190

1.4421 1.8087

2.1225

2.3877

2.6084

2.7887

2.9327

3.0446

3.1281

3.1868

3.1885

3.1885

3.3153

3.5363

3.8433

4.2547

4.7915

5.4759

6.3367

7.3994

8.6963

10.2614

12.1321

14.3485

16.9543

19.9967

23.5264

27.5977

32.2690

37.6025

43.6648

50.5263

58.2619

66.9509

.93986

.89040

.84011

.79026

.74191

.69550

.65124

.60922

.55950

.53209

.49699

.46412

.45294

.16298

.16555

.17167

. 1 8 1 53 .19568

.21472

.23930

.27011

.30790

.35345

.40758

.47118

.54514

.63044

.72808

.83911

.96454

1.10580

1.25379

1.43985

1.53525

1.85133

2.08944

Isotherm

Der i vat i ve MPa.m3/kg

.05095

.04523

.03943

.03395

.02888

.02422

.01998

.01615

.01273

.00971 .00706

.00473

.00465

.01318

.01835

.0261

.03559

.04704

.06070

.07681 .09563

. 1 1 743

.14251

.171 14 .20365

.24036

.28160

.32773

.37911

.43613

.49917

.56865

.64497

.72857

.31988

.91932

I sochore

Derivative

MPa/K

.00152

.00325

.00521

.00739

.00981

.01243

.01526

.01329

.02150

.02490

.02852

.03248

.03263

.12606

.13505

.14653

.15889

.17195

.18587

.20071 .21650

.23329

.25111

.27000

.28998

.31110

.33337

.35565

.33155

.40753

.43480

.46340

.49337

.52475

.55757

.59186

I sochore

Curvature

MPa/K^

-.0000004

-.0000021

-.0000054

-.0000109

-.0000189

-.0000301

-.0000455

-.0000668

-.0000972

-.0001438

-.0002259

-.0004235

-.0004367

.0009258

.0005796

.0005155

.0004140

.0003420

.0002850

.0002394

.0001988

.0001520

.0001277

.0000951

.0000635

.0000325

.0000019

-.0000287

-.0000594

-.0000904

-.0001217

-.0001536

-.0001851

-.0002194

-.0002534

-.0002884

122
Table 13. (Continued).

Isobutane Isotherm at 405 K

1 sotherm 1 sochore 1 sochore

Density Pressure Z Oer i vat i ve Der i vati ve Curvature

kg/m3 MPa MPaTn3/kg MPa/K MPa/l<2

10.00 .5454 .94136 .05176 .00152 -.0000004

20.00 1.0352 .89341 .04615 .00324 -.0000019

30.00 1.4681 .34468 .04046 .00518 -.0000050

40.00 1.84 55 .79640 .03510 .00734 -.0000099

50.00 2.1713 .74959 .03013 .00972 -.0000170

50.00 2.4495 .70469 .02557 .01229 -.0000256

70.00 2.6842 .66188 .02142 .01505 -.0000391

80.00 2.8793 .62126 .01768 .01798 -.0000554

90.00 3.0391 .58287 .01434 .02107 -.0000765

100.00 3.1675 .54674 .01140 .02429 -.0001041

1 10.00 3.2683 .51286 .00883 .02763 -.0001415

120.00 3.3453 .48119 .00662 .03109 -.0001951

130.00 3.4018 .45169 .00475 .03465 -.0002795

140.00 3.4412 .42423 .00318 .03835 -.0004385

150.00 3.4663 .39888 .00188 .04234 -.0008902

151.35 3.4687 .39560 .00172 .04292 -.0010297

305.86 3.4687 .19575 .00381 .09741 .0016199

310.00 3.4866 .19414 .00485 .10079 .0012557

320.00 3.5498 .19148 .00794 .10912 .0008360

330.00 3.6487 .19085 .01201 .11797 .0006367

340.00 3.7939 .19261 .01723 .12748 .0005162

350.00 3.9978 .19716 .02381 .13774 .0004328

360.00 4.2752 .20498 .03194 .14880 .0003697

370.00 4.6424 .21658 .04183 .16070 .0003188

380.00 5.1184 .23250 .05372 . 1 7348 .0002756

390.00 5.7242 .25335 .06783 .18717 .0002375

400.00 6.4833 .27977 .08441 .20181 .0002028

410.00 7.4216 .31245 .10373 .21742 .0001705

420.00 8. 5678 .35212 . 1 2604 .23405 .0001398

430.00 9.9534 .39955 .15164 .25171 .0001100

440.00 11.6126 .45556 .18082 .27044 .0000809

450.00 13.5827 .52100 .21389 .29027 .0000522

460.00 15.9043 .59679 .25117 .31124 .0000235

470.00 18.6212 .68587 .29300 .33337 -.0000052

480.00 21.7806 .78324 .33973 .35669 -.0000342

490.00 25.4334 .89593 .39174 .38125 -.0000635

500.00 29.6342 1.02303 .44939 .40707 -.0000932

510.00 34.4414 1.16568 .51310 .43418 -.0001234

520.00 39.9176 1.32504 .58325 .46263 -.0001543

530.00 46.1293 1.50234 .66027 .49244 -.0001859

540.00 53.1473 1.69885 .74458 .52365 -.0002182

550.00 61.0456 1.91587 .83561 .55630 -.0002514

560.00 69.9067 2.15475 .93579 .59042 -.0002856

123
Table 18. (Continued)

Isobutane ! sotherm at 407.85 K

Isotherm Isochore Isochore

Density Pressure Z Derivative Derivative Curvature

kg/m3 MPa MPa.m3/kg MPa/K MPa/K^

10.00 .5497 .94220 .05222 .00152 -.0000004

20.00 1.0444 .89508 .04567 .00323 -.0000018

30.00 1.4828 .84721 .04105 .00517 -.0000048

40.00 1.8664 .79979 .03574 .00731 -.0000094

50.00 2.1990 .75382 .03083 .00967 -.0000160

60.00 2.4845 .70975 .02633 .01222 -.0000248

70.00 2.7269 .66772 .02223 .01495 -.0000362

80.00 2.9304 .62785 .01853 .01783 -.0000505

90.00 3.0989 .59017 .01523 .02086 -.0000682

100.00 3.2363 .55471 .01232 .02402 -.0000902

110.00 3.3465 .52146 .00978 .02727 -.0001176

120.00 3.4331 .49038 .00760 .03060 -.0001521

130.00 3.4996 .46142 .00575 .03399 -.0001965

140.00 3.5491 .43452 .00420 .03742 -.0002550

150.00 3.5845 .40960 .00294 .04086 -.0003353

160.00 3.6087 .38659 .00194 .04430 -.0004508

170.00 3.6241 .36541 .001 18 .04771 -.0006283

180.00 3.6331 .34596 .00064 .05105 -.0009257

190.00 3.6376 .32816 .00029 .05430 -.0014906

200.00 3.6394 .31191 .00010 .05741 -.0027936

210.00 3.6399 .29710 .00002 .05028 -.0071451

220.00 3.6400 .28360 .00000 .05274 -.0539386

230.00 3.6400 .27127 .00000 .06458 .0383802

240.00 3.6401 .25997 .00003 .05725 .0076146

250.00 3.6408 .24962 .00013 .07059 .0035631

260.00 3.6433 .24018 .00038 .07451 .0021727

270.00 3.6492 .23166 .00085 .07900 .0015110

280.00 3.6614 .22414 .00164 .08410 .0011366

290.00 3.5834 .21771 .00285 .08982 .0009003

300.00 3.7202 .21255 .00460 .09519 .0007392

310.00 3.7778 .20888 .00704 .10324 .0006229

320.00 3.8637 .20696 .01031 .11100 .0005347

330.00 3.9872 .20710 .01457 .11951 .0004651

340.00 4.1591 .20967 .02001 .12879 .0004082

350.00 4.3921 .21509 .02582 .13887 .0003601

360.00 4.7007 .22381 .03519 .14978 .0003184

370.00 5.1017 .23634 .04533 .16156 .0002812

380.00 5.6139 .25322 .05747 .17423 .0002472

390.00 6.2586 .27506 .07185 .18782 .0002156

400.00 7.0592 .30249 .08871 .20236 .0001855

410.00 8.0419 .33620 .10831 .21789 .0001568

420.00 9.23 54 .37690 .13091 .23443 .0001287

430.00 10.6712 .42537 .15681 .25201 .0001011

440.00 12.3836 .48241 .18650 .27066 .0000735

450.00 14.4102 .54888 .21959 .29041 .0000462

460.00 16.7914 .62568 .25729 .31130 .0000187

470.00 19.5713 .71374 .29946 .33335 -.0000090

480.00 22.7970 .81406 .34654 .35659 -.0000371

490.00 26.5197 .92767 .39890 .38105 -.0000557

500.00 30.7939 1.05564 .45592 .40680 -.0000947

510.00 35.6784 1.19910 .52100 .43383 -.0001243

520.00 41.2355 1.35922 .59154 .45219 -.0001547

530.00 47.5320 1.53720 .66895 .49191 -.0001357

540.00 54.6388 1.73432 .75366 .52303 -.0002175

550.00 62.6311 1.95186 .8461

.55559 -.0002504

560.00 71.5882 2.19116 .94672 .58951 -.0002841

124
Table 18 (Continued).

i sobutane Isotherm at 410 K

Isotherm Isochore Isochore

Density Pressure Z Der i vat i ve Der ivati ve Curvature

kg/ni3 r^^a MPa.m3/kg MPa/K MPa/K^

10.00 .5530 .94282 .05256 .00152 -.0000004

20.00 1.0514 .89631 .04706 .00323 -.0000018

30.00 1.4939 .84907 .04149 .00516 -.0000046

40.00 1.8821 .80229 .03622 .00729 -.0000091

50.00 2.2197 .75695 .03136 .00963 -.0000154

60.00 2.5107 .71347 .02690 .01217 -.0000237

70.00 2.7590 .67203 .02283 .01487 -.0000342

80.00 2.9686 .63271 .01916 .01773 -.0000473

90.00 3.1436 .59555 .01589 .02072 -.0000631

100.00 3.2877 .56057 .01300 .02383 -.0000820

110.00 3.4049 .52777 .01049 .02703 -.0001045

120.00 3.4986 .49711 .00831 .03030 -.0001310

130.00 3.5722 .46853 .00647 .03361 -.0001619

140.00 3.6290 .44197 .00493 .03694 -.0001972

150.00 3.6717 .41736 .00366 .04026 -.0002361

160.00 3.7031 .39462 .00266 .04355 -.0002759

170.00 3.7256 .37367 .00188 .04678 -.0003100

180.00 3.7415 .35441 .00132 .04994 -.0003274

190.00 3.7526 .33676 .00094 .05301 -.0003139

200.00 3.7609 .32062 .00073 .05603 -.0002601

210.00 3.7676 .30590 .00063 .05905 -.0001694

220.00 3.7738 .29248 .00062 .06213 -.0000547

230.00 3.7802 .28023 .00065 .06534 .0000730

240.00 3.7870 .26905 .00073 .06872 .0002071

250.00 3.7952 .25884 .00092 .07235 .0003342

260.00 3.8059 .24959 .00127 .07633 .0004358

270.00 3.8213 .24132 .00186 .08075 .0004991

280.00 3.8442 .23409 .00277 .08570 .0005236

290.00 3.8782 .22802 .00412 .09126 .0005182

300.00 3.9285 .22327 .00602 .09748 .0004944

310.00 4.0010 .22006 .00861 .10439 .0004614

320.00 4.1035 .21865 .01204 .11203 .0004251

330.00 4.2452 .21934 .01647 .12042 .0003885

340.00 4.4369 .22250 .02208 .12960 .0003532

350.00 4.6914 .22855 .02906 .13959 .0003197

360.00 5.0234 .23792 .03762 .15043 .0002880

370.00 5.4497 .25113 .04795 .16213 .0002578

380.00 5.9891 .26873 .06029 .17474 .0002290

390.00 6.6629 .29130 .07487 .18827 .0002011

400.00 7.4947 .31947 .09193 .20275 .0001740

410.00 8.5107 .35393 .11175 .21822 .0001473

420.00 9.7397 .39540 .13457 .23470 .0001210

430.00 11.2132 .44463 .16070 .25222 .0000947

440.00 12.9657 .50244 .19042 .27081 .0000684

450.00 15.0347 .56966 .22405 .29051 .0000420

450.00 17.4608 .64721 .26190 .31133 .0000153

470.00 20.2879 .73600 .30432 .33332 -.0000118

480.00 23.5636 .83703 .35166 .35651 -.0000393

490.00 27.3388 .95131 .40429 .38092 -.0000673

500.00 31.6683 1.07992 .46259 .40659 -.0000958

510.00 36.6108 1.22399 .52695 .43356 -.0001250

520.00 42.2288 1.38466 .59777 .46186 -.0001549

530.00 48.5892 1.56315 .67548 .49151 -.0001856

540.00 55.7628 1.76071 .76050 .52257 -.0002171

550.00 63.8250 1.97864 .85326 .55505 -.0002496

125
Table 18. (Continued).

Isobutane Isotherm at 4 15 K

Isotherm Isochore Isochore

Density Pressure Z Derivative Der ivat ive Curvature

kg/m3 iVPa MPaTrv5/kg MPa/K MPa/K^

10.00 .5605 .94423 .05337 .00151 -.0000003

20.00 1.0675 .89910 .04797 .00322 -.0000017

30.00 1.5197 .85329 .04250 .00514 -.0000043

40.00 1.9185 .80793 .03734 .00725 -.0000083

50.00 2.2677 ,76400 .03257 .00956 -.0000140

60.00 2.5712 .72187 .02820 .01205 -.0000213

70.00 2.8329 .68172 .02421 .01471 -.0000303

80.00 3.0567 .64363 .02061 .01751 -.000041

1

90.00 3.2464 .60763 .01740 .02043 -.0000537

100.00 3.4059 .57373 .01456 .02346 -.0000678

110.00 5.5388 .54192 .01208 .02656 -.0000833

120.00 3.6486 .51217 .00993 .02973 -.0000997

130.00 3.7385 .48442 .00810 .03292 -.0001163

140.00 3.8115 .45861 .00656 .03614 -.0001318

150.00 3.3705 .43466 .00529 .03935 -.0001446

160.00 3.9131 .41250 .00426 .04255 -.0001524

170.00 3.9566 .39205 .00347 .04573 -.0001530

180.00 3.9882 .37323 .00289 .04889 -.0001444

190.00 4.0150 .35596 .00250 .05207 -.0001253

200.00 4.0388 .34017 .00230 .05528 -.0000976

210.00 4.0614 .32579 .00224 .05857 -.0000618

220.00 4.0840 .31271 .00229 .06198 -.0000202

230.00 4.1075 .30083 .00240 .06554 .0000254

240.00 4.1324 .29004 .00259 .06931 .0000741

250.00 4.1597 .28028 .00291 .07332 .0001239

260.00 4.1913 .27155 .00344 .07763 .0001719

270.00 4.2295 .26388 .00425 .08232 .0002148

280.00 4.2776 .25734 .00543 .08746 .0002495

290.00 4.3396 .25208 .00707 .09311 .0002743

300.00 4.4209 .24824 .00929 .09934 .0002388

310.00 4.5278 .24604 .01223 .10621 .0002938

320.00 4.6683 .24574 .01602 .11377 .0002911

330.00 4.8516 .24765 .02083 .12207 .0002823

340.00 5.0889 .25213 .02684 .13114 .0002691

350.00 5.3931 .25956 .03424 .14101 .0002529

360.00 5.7789 .27041 .04322 .15173 .0002346

370.00 6.2634 .28515 .05399 .16331 .0002148

380.00 6.3655 .30434 .06679 .17579 .0001941

390.00 7.6066 .32855 .08184 .18920 .0001726

400.00 8.5105 .35840 .09939 .20356 .0001505

410.00 9.6036 .39457 .1 1970 .21890 .0001279

420.00 10.9146 .43776 .14304 .23526 .0001049

430.00 12.4754 .48872 .16970 .25266 .0000814

440.00 14.3206 .54825 .19996 .27112 .0000574

450.00 16.4877 .61719 .23414 .29069 .0000329

460.00 19.0176 .69642 .27257 .31139 .0000078

470.00 21.9544 .78686 .31558 .33325 -.0000178

480.00 25.3456 .88948 .36353 .35630 -.0000439

490.00 29.2426 1.00529 .41678 .38058 -.0000708

500.00 33.7001 1.13536 .47571 .4061

1

-.0000983

510.00 38.7770 1.28079 .54072 .43293 -.0001265

520.00 44.5362 1.44272 .61222 .46108 -.0001555

530.00 51.0444 1.62236 .69062 .49058 -.0001854

540.00 58.3730 1.32092 .77634 .52148 -.0002161

550.00 66.5971 2.03970 .86982 .55381 -.0002478

126
Table 18. (Continued),

sobutane Isothenn at 420 K

Isotherm 1 sochore 1 sochore

Dens ity Pressure Z Der i vat ive Der i vat ive Curvature

kg/m3 MPa MPa.[n3/kg MPa/K MPa/K^

20.00 1.0836 .90179 .04887 .00321 -.0000016

40.00 1.9547 .81336 .03844 .00721 -.0000077

60.00 2.6312 .72993 .02947 .01195 -.0000193

80.00 3.1437 .65408 .02203 .01732 -.0000363

100.00 3.5224 .58629 .01608 .02315 -.0000577

120.00 3.7960 .526 53 .01150 .02928 -.0000808

140.00 3.9907 .47446 .00815 .03557 -.0001001

160.00 4.1291 .42955 .00585 .04191 -.0001079

180.00 4.2311 .39125 .00449 .04831 -.0000963

200.00 4.3142 .35904 .00395 .05489 -.0000633

220.00 4.3937 .33241 .00408 .06189 -.0000137

240.00 4.4797 .31068 .00458 .06960 .0000464

260.00 4.5813 .29328 .00574 .07832 .0001 105 280.00 4.7176 .28044 .00815 .08847 .0001677

300.00 4.9208 .27302 .01258 .10055 .0002064

320.00 5.2404 .27258 .01998 .1 1504 .0002218

340.00 5.7477 .23138 .03156 .13234 .0002165

360.00 6.5403 .30239 .04877 .15280 .0001964

380.00 7.7467 .33932 .07323 .17669 .0001667

400.00 9.5301 .39656 .10679 .204 26 .0001309

420.00 12.0922 .47921 .15145 .23575 .0000909

440.00 15.6769 .59303 .20944 .27139 .0000474

460.00 20.5746 .74447 .28318 .31141 .0000010

480.00 27.1266 .94065 .37532 .35607 -.0000483

500.00 35.7294 1.18940 .48876 .40561 -.0001006

520.00 46.8396 1.49928 .62659 .46030 -.0001561

540.00 60.9777 1.87953 .79211 .52040 -.0002151

Isobutane Isotherm at 430 K

20.00 1 . 1 1 56 .90688 .05066 .00320 -.0000014

40.00 2.0264 .82360 .04061 .00714 -.0000066

60.00 2.7498 .74509 .031^8 .01 178 -.0000161

80.00 3.3152 .67371 .02480 .01699 -.0000292

100.00 3.7512 .60985 .01903 .02264 -.0000443

120.00 4.0852 .55346 .01457 .02859 -.0000586

140.00 4.3420 .50421 .01129 .03474 -.0000682

160.00 4.5436 .46168 .00904 .04105 -.0000694

180.00 4.7101 .42542 .00777 .04756 -.0000596

200.00 4.8605 .39509 .00741 .05440 -.0000389

220.00 5.0120 .37038 .00785 .06178 -.0000095

240.00 5.1775 .35072 .00879 .06994 .0000258

260.00 5.3690 .33572 .01055 .07915 .0000643

280.00 5.6093 .32569 .01378 .08976 .0001011

300.00 5.9351 .32163 .01925 .10218 .0001306

320.00 6.4005 .32517 .02791 .11585 .0001483

340.00 7.0808 .33857 .04096 .13416 .0001527

360.00 8.0772 .36476 .05978 .15448 .0001445

380.00 9.5212 .40734 .08600 .17814 .0001262

400.00 11.5787 .47060 .12144 .20541 .0001000

420.00 14.4538 .55948 .16811 .23654 .0000677

440.00 18.3928 .67959 .22822 .27177 .0000304

460.00 23.6886 .83721 .30421 .31136 -.0000109

480.00 30.6847 1.03928 .39873 .35555 -.0000 560 500.00 39.7804 1.29346 .51466 .40458 -.0001047

520.00 51.4348 1.60808 .65513 .45873 -.0001571

540.00 66.1710 1.99217 .82341 .51826 -.0002133

127
Table 18. (Continued).

Isobutane Isotherm at 450 K

1 sotherm Isochore Isochore

Density Pressure Z Der i vat i ve Derivative Curvature

kg/m3 MPa MPa.m5/kg MPa/:< MPa/K^

20.00 1.1794 .91609 .05420 .00318 -.0000011

40.00 2.1680 .84199 .04485 .00702 -.0000051

60.00 2.9824 .77220 .03682 .01150 -.0000118

80.00 3.6493 .70874 .03013 .01650 -.0000205

100.00 4.1963 .65190 .02473 .02192 -.0000297

120.00 4.6471 .60160 .02054 .02766 -.0000373

140.00 5.0255 .55765 .01748 .03369 -.0000415

160.00 5.3532 .51976 .01548 .04000 -.0000409

180.00 5.6516 .48776 .01454 .04666 -.0000348

200.00 5.9421 .46155 .01469 .05381 -.0000234

220.00 6.2460 .44105 .01584 .06162 -.0000077

240.00 6.5802 .42593 .01772 .07029 .0000111

260.00 6.9621 .41598 .02071 .08005 .0000318

280.00 7.4206 .41171 .02551 .09121 .0000522

300.00 7.9998 .41426 .03293 .10409 .0000700

320.00 8.7617 .42535 .04394 .11906 .0000826

340.00 9.7893 .44728 .05972 .13648 .0000881

360.00 11.1912 .48293 .08162 .15672 .0000857

380.00 13.1054 .53577 .11123 .18011 .0000755

400.00 15.7037 .60989 .15034 .20695 .0000580

420.00 19.1956 .71000 .20094 .23753 .0000342

440.00 23.8325 .84144 .26523 .27211 .0000047

460.00 29.9122 1.01018 .34565 .31095 -.0000296

480.00 37.7836 1.22284 .44485 .35430 -.0000684

500.00 47.8507 1.48671 .56573 .40242 -.0001114

520.00 60.5779 1.80976 .71140 .45558 -.0001585

Isobutane Isotherm at 500 K

20.00 1.3370 .93465 .06285 .00313 -.0000007

40.00 2.5139 .87871 .05501 .00683 -.0000029

60.00 3.5453 .82615 .04832 .01106 -.0000065

80.00 4.4543 .77846 .04276 .01576 -.0000108

100.00 5.2631 .73586 .03831 .02087 -.0000150

120.00 5.9942 .69339 .03499 .02637 -.0000183

140.00 6.6701 .66612 .03280 .03227 -.0000200

160.00 7.3140 .63913 .03181 .03860 -.0000199

180.00 7.9511 .61760 .03214 .04545 -.0000177

200.00 8.6092 .60184 .03391 .05295 -.0000136

220.00 9.3173 .59213 .03712 .06123 -.0000079

240.00 10.1017 .58848 .04154 .07047 -.0000012

260.00 10.9903 .59100 .04766 .08087 .0000062

280.00 12.0249 .60045 .05628 .09265 .0000134

300.00 13.2641 .61817 .06829 .10608 .0000197

320.00 14.7857 .64602 .08471 .12143 .0000239

340.00 16.6897 .68631 .10673 .13902 .0000252

360.00 19.1011 .74184 .13570 .15916 .0000227

380.00 22.1744 .81587 .17318 .18216 .0000159

400.00 26.0965 .91217 .22090 .20832 .0000045

420.00 31.0917 1.03502 .28082 .23794 -.0000116

440.00 37.42 53 1.18923 .35513 .27130 -.0000323

460.00 45.4087 1.38017 .44622 .30868 -.0000575

480.00 55.4036 1.61380 .55675 .35035 -.0000870

500.00 67.8276 1.89665 .68962 .39658 -.0001207

128
Table 18 (Continued).

1 sobutane Isotherm at 550 K

Isotherm ISO chore Isochore

Density Pressure Z Der i vat i ve Der i vat i ve Curvature

kg/m3 MPa MPa.m3/kg MPa/< MPa/K^

20.00 1.4929 .94876 .07131 .00311 -.0000004

40.00 2.8523 .90636 .06478 .00671 -.0000019

60.00 4.0913 .86671 .05929 .01080 -.0000041

80.00 5.2306 .83104 .05481 .01533 -.0000068

100.00 6.2907 .79957 .05138 .02028 -.0000093

120.00 7.2934 .77252 .04908 .02565 -.00001 14 140.00 8.2621 .75011 .04800 .03147 -.0000127

160.00 9.2227 .73265 .04830 .03780 -.0000130

180.00 10.2045 .72057 .05016 .04472 -.0000124

200.00 11.2411 .71439 .05380 .05235 -.0000108

220.00 12.3687 .71459 .05924 .06082 -.0000086

240.00 13.6215 .72140 .06634 .07028 -.0000059

260.00 15.0369 .73510 .07563 .08092 -.0000031

280.00 16.6672 .75660 .08799 .09293 -.0000005

300.00 18.5833 .78734 .10438 .10654 .0000014

320.00 20.8763 .82920 .12587 .12201 .0000019

340.00 23.6601 .88450 .15368 .13959 .0000006

360.00 27.0748 .95592 .18920 .15957 -.0000032

380.00 31.2896 1.04659 .23396 .18224 -.0000098

400.00 36. 5063 1.16002 .28970 .20787 -.0000197

420.00 42.9637 1.30020 .35836 .23676 -.0000331

440.00 50.9413 1.47155 .442 10 .26919 -.0000500

460.00 60.7643 1.67899

Isobutane

.54332

Isotherm at 600 K

.30543 -.0000707

20.00 1.6477 .95986 .07965 .00309 -.0000003

40.00 3.1859 .92799 .07431 .00663 -.0000013

60.00 4.6267 .89845 .06994 .01063 -.0000029

80.00 5.9896 .87233 .066 52 .01505 -.0000047

100.00 7.2945 .84989 .06415 .01989 -.0000065

120.00 8.5634 .83145 .06296 .02518 -.0000080

140.00 9.8217 .81739 .06311 .03094 -.0000092

160.00 11.0981 .80817 .06481 .03724 -.0000098

180.00 12.4264 .80435 .06834 .04417 -.0000099

200.00 13.8456 .80659 .07394 .05184 -.0000096

220.00 15.3986 .81551 .08170 .06038 -.0000090

240.00 17.1271 .83146 .09151 .06992 -.0000082

260.00 19.0767 .85487 .10397 .08064 -.0000075

280.00 21.3098 .88673 .12001 .09272 -.0000072

300.00 23.9078 .92852 .14065 .10637 -.0000075

320.00 26.9738 .98212 .16700 .12181 -.0000088

340.00 30.6345 1.04979 .20034 .13929 -.0000115

360.00 35.0432 1.13415 .24205 .15906 -.0000160

380.00 40.3828 1.23818 .29370 .18139 -.0000227

400.00 46.8692 1.36521 .35704 .20655 -.0000319

420.00 54.7551 1.51896 .43399 .23481 -.0000438

440.00 64.3340 1.70356 .52672 .26645 -.0000585

129
Table 18. (Continued).

Isobutane Isotherm at 650 K

1 sotherm Isochore Isochore

Density Pressure Z Der ivative Der i vat i ve Curvature

kg/m3 MPa MPa.m3/kg MPa/l< MPaA^

20.00 1.8016 .96881 .08791 .00307 -.0000002

40.00 3.5161 .94538 .08367 .00658 -.0000010

60.00 5.1548 .92400 .08036 .01050 -.0000021

80.00 6.7367 .90567 .07799 .01485 -.0000035

100.00 8.2817 .89070 .07670 .01961 -.0000049

120.00 9.8131 .87949 .07666 .02483 -.0000061

140.00 11.3581 .87254 .07810 .03053 -.0000072

160.00 12.9488 .87040 .08129 .03680 -.0000080

180.00 14.6233 .87374 .08653 .04372 -.0000085

200.00 16.4260 .88330 .09415 .05138 -.0000089

220.00 18.4061 .89980 .10426 .05992 -.0000091

240.00 20.6122 .92368 .11679 .06948 -.0000094

260.00 23.0981 .95546 .13240 .08020 -.0000098

280.00 25.9350 .99618 .15206 .09226 -.0000107

300.00 29.2146 1.04734 .17684 .10587 -.0000121

320.00 33.0505 1.11080 .20791 .12121 -.0000144

340.00 37.5814 1.18878 .24655 .13854 -.0000178

360.00 42.9728 1.28381 .29421 .15807 -.0000228

380.00 49.4205 1.39872 .35247 .18007 -.0000294

400.00 57.1537 1.53671 .42306 .20478 -.0000380

420.00 66.4383 1.70129 .50795 .23248 -.0000489

Isobutane Isotherm at 700 K

20.00 1.9550 .97618 .09610 .00306 -.0000002

40.00 3.8438 .95966 .09291 .00653 -.0000008

60.00 5.6775 .94500 .09063 .01041 -.0000017

80.00 7.4750 .93314 .08929 .01469 -.0000027

100.00 9.2567 .92445 .08908 .01940 -.0000039

120.00 1 1.0473 .91939 .09022 .02455 -.0000049

140.00 12.8764 .91852 .09298 .03021 -.0000059

160.00 14.7795 .92249 .09768 .03643 -.0000068

180.00 16.7989 .93203 .10468 .04331 -.0000076

200.00 18.9842 .94795 .11433 .05095 -.0000083

220.00 21.3908 .97102 .12679 .05947 -.0000090

240.00 24.0740 1.00175 .14203 .06899 -.0000099

260.00 27.0951 1.04074 .16075 .07967 -.0000110

280.00 30.5340 1.08905 .18398 .09168 -.0000125

300.00 34.4915 1.14819 .21281 .10519 -.0000146

320.00 39.0918 1.22000 .24846 .12041 -.0000174

340.00 44.4842 1.30662 .29226 .13755 -.0000212

360.00 50.8461 1.41052 .34566 .15683 -.0000263

380.00 58.3854 1.53442 .41028 .17850 -.0000328

400.00 67.3436 1.68136 .48787 .20280 -.0000410

130
Table 19. The Joule-Thomson inversion locus for isobutane.

Temp. Density Pressure

K kg/m3 MPa

330 508.1 1.012

340 502.7 3.742

350 497.2 6.314

360 491.8 8.740

370 486.5 11.027

380 481.2 13.187

390 475.9 15.226

400 470.7 17.152

410 465.5 18.972

420 460.4 20.691

430 455.3 22.315

440 450.3 23.850

450 445.3 25.300

460 440.4 26.668

470 435.5 27.960

480 430.7 29.179

490 425.9 30.328

500 421.1 31.411

510 416.4 32.430

520 411.8 33.389

530 407.1 34.289

540 402.5 35.133

550 398.0 35.924

560 393.4 36.663

570 389.0 37.352

580 384.5 37.994

590 380.1 38.589

600 375.7 39.141

610 371.3 39.649

620 367.0 40.116

630 362.7 40.543

640 358.4 40.932

650 354.

l

41.283

660 349.9 41.598

670 345.6 41.879

680 341.4 42.127

690 337.3 42.342

700 333.1 42.526

710 329.0 42.680

720 324.9 42.805

730 320.8 42.901

740 316.7 42.972

750 312.6 43.015

760 308.6 43.035

770 304.5 43.031

780 300.5 43.003

790 296.6 42.956

800 292.6 42.886

810 288.7 42.798

820 284.7 42.691

830 280.8 42.566

840 277.0 42.425

131
Tab Ie 20. Thermophysical propert ies of ;jatuirated liqui d isobutane •

1 sochore 1 sotherm

Temp. Pa PJI kg/m3

Z)l Zg dPa/dT dpjj^/dT Derivative Derivative

H MPa kg/m3 MPa/K kg/(m3.K) MPa/K MPa,m3/kg

113,,550 .19481E-07 741,,38 .11994E-05 .00000 1.00000 .5101E-08 -.9717 2.3582 ,2427 E+01

120,,000 .95569E-07 735..12 .55675E-05 .00000 1.00000 .2219E--07 -.9687 2.2392 .2312E+01

130.,000 .80164E-06 725,,45 .43108E-04 .00000 1.00000 .1561E--06 -.9653 2.0713 ,2146E+01

140.,000 .48217E-05 715,.81 .24077E-03 .00000 .99998 .7967E--06 -.9634 1.9203 ,1993E+01

150.,000 .22265E-04 706,.18 .1037 7 E-02 .00000 .99994 .3152E--05 -.9631 1.7835 ,1852E+01

160.,000 .83070E-04 696,.54 .36302E-02 .00001 .99982 .1017E--04 -.9645 1.6586 ,1720E+01

170.,000 .26041E-03 686..88 .10714E-01 .00002 .99952 .2776E--04 -.9677 1.5441 ,1596E+01

180.,000 .70698E-03 677..18 .27488E-01 .00004 .99890 .6612E--04 -.9728 1 .4384 ,1478E+01

190,,000 .17026E-02 667,.42 .62785E-01 .00009 .99773 .1406E--03 -.9799 1.3405 ,1368E+01

200,,000 .37071E-02 657..57 .13012E+00 .00020 .99578 .2718E--03 -.9892 1.2493 ,1263E+01

205,,000 . 52933 E-02 652..61 .18 152 E+00 .00028 .99443 .3664E--03 -.9947 1 .2060 ,1212E+01

210,,000 .74113E-02 647..62 .24851 E+00 .00038 .99277 .4850E--03 -1.0008 1.1641 ,1163E+01

215,,000 .10190E-01 642..60 .33440E+00 .00052 .99079 .6313E--03 -1.0075 1.1236 ,in5E+01

220,,000 .13777E-01 637..55 .44289E+00 .00069 .98845 .8090E--03 -1.0149 1.0843 .1068E-K)1 225.,000 .18339E-01 632..45 .57802E+00 .00090 .98574 .1022E--02 -1.0230 1 .0462 ,1022E+01

230.,000 .24061E-01 627..32 .74424E+00 .00117 .98262 .1274E--02 -1.0318 1.0092 ,9768E-K)0 235.,000 .31147E-01 622..13 .94634 E+00 ,00149 .97909 .1568E--02 -1.0414 .9732 ,9330E+00

240.,000 .39820E-01 616..90 .11895E+01 .00188 .97514 .1909E--02 -1.0518 .9383 .8903E+00

245.,000 .50320E-01 611..61 . 14791 E+01 .00235 .97076 .2299E--02 -1.0631 ,9043 ,8485E+00

250.,000 .62903E-01 606..27 .18210E+01 .00290 .96595 .2743E--02 -1.0752 .8712 ,8077E+O0

255,,000 .77842E-01 600..86 .22213E+01 .00355 .96071 .3242E--02 -1.0884 .8390 ,7679E+00

260,.000 .95423E-01 595..38 ,26864E+01 .00431 .95505 .3800E--02 -1.1026 .8076 ,7290E+00

261..517 .10133E+00 593..71 .28414E+01 .00456 .95324 .3982E--02 -1.1071 .7982 ,7174E+00

270,,000 .13973E+00 584..20 .38386E+01 .00619 .94244 .5103E--02 -1.1344 ,7470 ,6540E+00

275,,000 .16708E+00 578..49 .45402E+01 .00734 .93550 .5852E--02 -1.1523 .7178 ,6179E+00

280,,000 .19836E+00 572..68 .53359E+01 .00865 .92813 .6669E--02 -1.1716 .6893 ,5826E+00

285,.000 . 23389 E+00 566..77 .62339E+01 .01012 .92031 .7556E--02 -1.1924 .6614 ,5483 E+00

290,,000 .27404E+00 560..75 .72432E+01 .01 178 .91203 .8515E--02 -1.2149 .6341 ,5149E+{)0

295,,000 .31917E+00 554..62 .83736E+01 .01364 .90324 .9547E-02 -1.2393 .6074 ,48 24 E+00

300,,000 .36964E+00 548.,35 .96355E+01 .01571 .89393 .1065E--01 -1.2658 .5812 .4507E+00

305,,000 .42 584 E+00 541..95 . 1 1 04 1 E+02 .01801 .88403 .1184E--01 -1.2947 .5556 ,42 00 E+00

310,,000 .48816E+00 535..40 .12603E+02 .02056 .87349 .1310E--01 -1.3261 .5304 ,3901 E+00

315..000 .55699E+00 528..69 .14336E+02 .02338 .86225 .1444E--01 -1.3606 .5057 ,3611 E+00

320..000 .63274E+00 521..79 .16258E+02 .02649 .85023 .1587E--01 -1.3983 ,4815 ,3330E+00

325,.000 .71 584 E+00 514..70 .18388E+02 .02992 .83737 .1738E--01 -1.4400 ,4577 ,3058E+00

330..000 .80670E+00 507..38 .20750E+02 .03368 .82357 .1898E--01 -1.4862 ,4343 ,2795E+00

335,.000 .90577E+00 499,.83 .23370E+02 .03782 .80878 .2067E--01 -1.5376 ,4113 .2541 E+00

340,.000 .10135E+01 492,.00 .26281 E+02 .04236 .79291 .2245E--01 -1.5954 .3887 .2295E+00

345,.000 .11304E+01 483,.86 .29521 E+02 .04734 .77589 .2432E--01 -1.6606 .3663 .2059 E+00

350,.000 .12569E+01 475,.38 .33135E+02 .05281 .75767 .2630E--01 -1.7350 .3443 ,1833E+00

355,.000 .13936E+01 466,.49 .37 178 E+02 .05883 .73815 .2839E--01 -1.8209 .3225 ,1615E+00

360,.000 .15410E+01 457,.14 .41719E+02 .06546 .71727 .3059E--01 -1.9212 .3009 ,1407E+00

365,.000 .16997E+01 447,.25 .46846E+02 .07279 .69490 .3291 E--01 -2.0403 .2796 ,1209 E+00

370,.000 .18703E+01 436,.70 .52673E+02 .08092 .67087 .3535E--01 -2.1846 .2583 ,1021 E+00

375,.000 .20535E+01 425,.34 .59355E+02 .09000 .64494 .3794E--01 -2.3640 .2372 .8427E-01

380,.000 .22500E+01 412,.97 .67114E+02 .10023 .61674 .4069E--01 -2.5947 .2159 ,6754E-01

385,.000 .24607E+01 399,.27 .76281 E+02 .11191 .58573 .4362E--01 -2.9052 .1946 ,5196E-01

390,.000 .26865E+01 383,.70 .87387E+02 .12550 .55106 .4675E--01 -3.3523 .1728 ,3760E-01

395,.000 .29286E+01 365,.30 .10139E+03 .14188 .51120 .5015E--01 -4.0691 .1502 ,2460E-01

400,.000 .31885E+01 341,.92 .12037E+03 .16298 .46294 .5391E--01 -5.4740 .1261 ,1318E-01

405,.000 .34687E+01 305,.86 .15135E+03 .19575 .39560 .5835E--01 -10.2449 .0974 ,38 12 E-02

407,.850 .36400E+01 224,.36 .22436E+03 .27808 .27808 .6351 E--01 — .0635 0,

132
Table 20. (Continued) Heat of Internal Fugacity/ Vel . of

Temp. Vap. Energy Enthal py Entropy Cv Ca Cp Pressure Sound Dielectr ic K J/mol J/mol J/mol J/(mol.K) J/(mol .K) J/(mol .K) J/(mol.K) Ratio m/s Constant

113.550 28117.1 .0 .0 108.800 69.14 96.65 96.65 1.00000 1841 2.10788

120.000 27825.2 625.9 625.9 114.179 69.99 97.99 97.99 1 .00000 1798 2.09370

130.000 27376.3 1614.4 1614.4 122.103 71.39 100.10 100.10 1 .00000 1734 2.07235

140.000 26930.9 2625.3 2625.3 129.598 72.88 102.26 102.26 1 .00000 1672 2.05162

150.000 26487.9 3659.0 3659.0 136.730 74.46 104.49 104.49 .99997 1612 2.03142

160.000 26046.0 4715.3 4715.4 143.547 76.10 106.77 106.77 .99985 1553 2.01166

170.000 25603.8 5794.8 5794.8 150.090 77.78 109.08 109.08 .99954 1495 1.99224

180.000 25160.0 6897.5 6897.5 156.390 79.48 111.40 111.41 .99889 1439 1.97310

190.000 24712.8 8023.6 8023.7 162.476 81.17 113.74 113.74 .99766 1384 1.95418

200.000 24260.9 9173.2 9173.5 168.368 82.86 116.08 116.09 .99562 1330 1.93540

205.000 24032.6 9756.8 9757.2 171.249 83.69 117.25 117.26 .99418 1303 1 .92605

210.000 23802.4 10346.2 10346.9 174.089 84.52 118.43 118.44 .99242 1276 1.91671

215.000 23570.0 10941.6 10942.5 176.889 85.35 119.61 119.63 .99037 1249 1.90738

220.000 23335.3 11542.8 11544.0 179.652 86.17 120.79 120.82 .98788 1223 1.89805

225.000 23098.0 12149.8 12151.5 182.380 87.00 121.99 122.02 .98497 1197 1.88871

230.000 22857.8 12762.7 12765.0 185.075 87.82 123.19 123.24 .98172 1170 1.87936

235.000 22614.4 13381.5 13384.4 187.737 88.64 124.41 124.47 .97795 1144 1.86998

240.000 22367.4 14006.3 14010.0 190.370 89.47 125.64 125.71 .97373 1118 1.86058

245.000 22116.6 14637.1 14641.9 192.973 90.29 126.89 126.98 .96913 1092 1.85114

250.000 21861.7 15273.9 15280.0 195.549 91.13 128.16 128.27 .96402 1066 1.84165

255.000 21602.2 15917.0 15924.5 198.100 91.96 129.45 129.59 .95846 1040 1.83211

260.000 21337.8 16566.4 16575.7 200.626 92.81 130.76 130.94 .95254 1014 1.82250

261.517 21256.5 16764.7 16774.7 201.388 93.06 131.17 131.36 .95065 1006 1.81957

270.000 20792.3 17884.8 17898.7 205.611 94.51 133.48 133.75 .93939 962 1 .80306

275.000 20510.4 18554.3 18571.1 208.073 95.37 134.88 135.20 .93230 935 1.79321

280.000 20221.7 19230.8 19250.9 210.516 96.24 136.31 136.70 .92484 909 1.78326

285.000 19925.6 19914.5 19938.5 212.942 97.11 137.77 138.24 .91706 883 1.77319

290.000 19621.4 20605.7 20634.1 215.351 97.98 139.27 139.84 .90898 857 1.76300

295.000 19308.6 21304.7 21338.2 217.745 98.85 140.81 141.48 .90067 830 1.75267

300.000 18986.3 22011.5 22050.7 220.125 99.72 142.38 143.18 .89207 804 1.74218

305.000 18653.7 22726.5 22772.1 222.492 100.58 144.00 144.94 .88323 777 1.73152

310.000 18309.8 23449.7 23502.7 224.847 101.44 145.66 146.78 .87416 751 1.72067

315.000 17953.7 24181.5 24242.8 227.192 102.29 147.37 148.69 .86490 724 1.70962

320.000 17584.1 24922.0 24992.5 229.527 103.14 149.13 150.70 .85539 697 1.69833

325.000 17199.6 25671.4 25752.2 231.853 103.97 150.97 152.82 .84567 670 1 .68679

330.000 16798.8 26430.0 26522.4 234.172 104.79 152.89 155.08 .83572 643 1 .67496

335.000 16379.8 27198.2 27303.6 236.486 105.61 154.90 157.51 .82555 615 1.66281

340.000 15940.5 27976.5 28096.2 238.796 106.43 157.05 160.16 .81516 587 1 .65030

345.000 15478.4 28765.6 28901.4 241.104 107.27 159.37 163.07 .80457 559 1.63738

350.000 14990.4 29566.2 29719.9 243.414 108.13 161.90 166.35 .79373 530 1.62399

355.000 14472.9 30379.8 30553.4 245.730 109.05 164.73 170.10 .78266 501 1.61008

360.000 13921.2 31207.9 31403.8 248.056 110.06 167.95 174.49 .77136 472 1.59553

365.000 13329.5 32052.8 32273.7 250.398 111.21 171.70 179.77 .75985 442 1.58025

370.000 12690.1 32917.4 33166.4 252.766 112.56 176.21 186.30 .74814 410 1.56409

375.000 11992.7 33805.7 34086.3 255.169 114.24 181.78 194.65 .73620 378 1.54683

380.000 11222.6 34723.3 35040.0 257.623 116.37 188.94 205.79 .72404 345 1.52820

385.000 10358.1 35678.9 36037.1 260.152 119.20 198.54 221.47 .71165 310 1.50776

390.000 9364.2 36686.8 37093.8 262.792 123.06 212.25 245.33 .69901 273 1.48479

395.000 8177.8 37773.7 38239.6 265.615 128.52 233.70 286.39 .68611 234 1.45801

400.000 6660.7 38999.6 39541.6 268.781 136.48 273.72 376.24 .67284 190 1.42448

405.000 4345.7 40572.7 41231.9 272.850 144.95 396.05 771.24 ,65905 142 1.37394

407.850 0.0 42487.2 43430.2 278.161 — — — .65069 1.26472

133
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190
NBS-n4A (REV. 2-ac) U.S. DEPT. OF COMM.

BIBLIOGRAPHIC DATA

SHEET (See instructions)

1. PUBLICATION OR

REPORT NO.

NBS TN-1051

2. Performing Organ. Report No, 3. Publ ication Date

January 1982

4. TITLE AND SUBTITLE

THERMOPHYSICAL PROPERTIES OF ISOBUTANE FROM 114 TO 700 K AT

PRESSURES TO 70 MPa

5. AUTHOR(S)

Robert D. Goodwin and William M. Haynes

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

9. SPONSORING ORGANIZATION NAME AND COMPLETE ADDRESS (Street. City, State. ZIP)

10. SUPPLEMENTARY NOTES

QJ Document describes a computer program; SF-185, FlPS Software Summary, is attached.

11. ABSTRACT (A 200-word or less (actual summary of most significant 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 isobutane are derived from physical properties data and are tabulated at

integral temperatures over the entire range of fluid states from 114 to 700 K along

isobars at pressures to 70 MPa. Results include dielectric constants, densities,

enthalpies, entropies, equation of state, internal energies, isobars, isochores,

isotherms, Joule-Thomson inversion, heats of vaporization, melting line, orthobaric

densities, specific heats, sound velocities, vapor pressures, and virial

coefficients. In addition to the equation of state, equations are given for vapor

pressures, orthobaric vapor and liquid densities, ideal gas properties, second virial

coefficients, dielectric constants, heats of vaporizatiofc, melting pressures, and

orthobaric liquid specific heats, enthalpies, and entropies. Several new sets of

data have been used in this correlation; comparisons between experimental and

calculated values are given.

12. KEY WORDS (Six to twelve entries; alphabetical order; capitalize only proper names; and separate key words by semicolons)

Densities; dielectric constants; enthalpies; entropies; equation of state;

fugacities; internal energies; isobars; isobutane; isochores; isotherms;

Joule-Thomson inversion; latent heats of vaporization; melting line; orthobaric —Hf^nciM-pg- gppfifir hpaf-s; gniind vplnrit ies; vapor pressures: virial coefficients.

13. AVAILABILITY

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I I For Official Distribution. Do Not Release to NTIS

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[X] Order From National Technical Information Service (NTIS), Springfield, VA. 22161

14. NO. OF

PRINTED PAGES

196

15. Price

$15.50

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