NBS TECHNICAL NOTE 1039

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

A Computer Program for the Prediction

of Viscosity and Thermal Conductivity

in Hydrocarbon Mixtures
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A Computer Program for the Prediction

of Viscosity and Thermal Conductivity in

Hydrocarbon Mixtures

James F. Ely

H.J.M. Hanley

.tAttoPAL. BURKAC

Of STANDASM

L1BBABY

JUL 2 1981

not. i' u^,

CiUoo

no- ioz<\

int

Thermophysical Properties Division

National Engineering Laboratory

National Bureau of Standards

Boulder, Colorado 80303

** OF

° Jrf. 7

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

NATIONAL BUREAU OF STANDARDS, Ernest Ambler, Director

Issued April 1981
NATIONAL BUREAU OF STANDARDS TECHNICAL NOTE 1039

Nat. Bur. Stand. (U.S.), Tech. Note 1039, 80 pages (April 1981)

CODEN: NBTNAE

U.S. GOVERNMENT PRINTING OFFICE

WASHINGTON: 1981 For sale by the Superintendent of Documents, U.S. Government Printing Office, Washington, D.C. 20402

Price $4.00 (Add 25 percent for other than U.S. mailing)
CONTENTS

Page

1. INTRODUCTION 1

2. THE ONE-FLUID MODEL AND EQUATIONS 2 2.1 Extended Corresponding States 4

2.2 Mixing Rules and Assumptions 5

3. SUMMARY OF THE CALCULATION PROCEDURE 7

4. THE REFERENCE FLUID: EXTENDED EQUATIONS FOR METHANE 7

5. RESULTS FOR PURE FLUIDS 14

6. RESULTS FOR MIXTURES 14

7. CONCLUSIONS 25

8. COMPUTER PROGRAM 25

9. ACKNOWLEDGMENTS 31

10. REFERENCES 32

APPENDIX A. TRAPP USER'S GUIDE 33

APPENDIX B. LISTING OF COMPUTER PROGRAM TRAPP 42

in
LIST OF FIGURES

Page

Figure 1. (a) Comparison of reduced density of methane and n-decane

as a function of reduced temperature, (b) Comparison of

scaled viscosity of methane and n-decane as a function of

reduced density 9 Figure 2. Comparison of calculated and experimental viscosity of

methane, pentane, decane and hexadecane as a function of

reduced density 20

Figure 3. Comparison of calculated and experimental viscosity for

toluene, carbon dioxide, ethylene and isobutane 21

Figure 4. Comparison of calculated and experimental thermal

conductivity for propane, decane, hexadecane, eicosane

and methyl cyclohexane 22

Figure 5. Comparison of calculated and experimental thermal

conductivity for ethylene, 1-hexene, benzene, toulene,

p-xylene and carbon dioxide 23

Figure 6. Comparison of calculated and experimental viscosity of

selected paraffin binary mixtures as a function of

reduced density 28

Figure 7. Comparison of calculated and experimental viscosity of

selected aromatic/paraffin mixtures 29

Figure 8. Comparison of calculated and experimental thermal

conductivity of selected binary mixtures 30

Figure Al. Block diagram of computer program TRAPP 35

Figure A2. Flow diagram of I/O portion of TRAPP 38

LIST OF TABLES

Table 1. Reference Fluid Equation of State 10

Table 2. Coefficients for Shape Factor Correlations 12

Table 3. Reference Fluid Viscosity Correlation 13

Table 4. Reference Fluid Translational Thermal Conductivity

Correlation 15

Table 5. Summary of Calculated Results for Pure Fluid Viscosity . . 16

Table 6. Summary of Calculated Results for Pure Fluid Thermal

Conductivity 18

IV
LIST OF TABLES (Continued)

Page

Table 7. Summary of Results for Binary Mixture Viscosity 26

Table 8. Summary of Results for Binary Mixture Thermal Conductivity . 27

Table Al. Listing of Components and TRAPP Data Base 34

Table A2 . Sample Input and Output 39

Table A3. Sample Input and Output 40

Table A4. Sample Input and Output 41

A COMPUTER PROGRAM FOR THE PREDICTION OF VISCOSITY AND

THERMAL CONDUCTIVITY IN HYDROCARBON MIXTURES

by

James F. Ely and H. J. M. Hartley

Thermophysical Properties Division

National Engineering Laboratory

National Bureau of Standards

Boulder, Colorado 80303

A model for the prediction of the density, viscosity and thermal

conductivity of non-polar fluid mixtures over the entire range of pVT

states is presented. The model is based on the extended corresponding

states model and covers molecular weight ranges including C20 Only

pure component equilibrium data such as the critical constants are required as input to the calculation procedure —no transport data are required. Extensive comparisons with experimental data for pure fluids

and binary mixtures are presented. The average percentage deviation

for both the viscosity and thermal conductivity was observed to be less

than 8 percent. A computer program (TRAPP) which performs the

calculations reported in this manuscript is described and listed in the

Appendices.

Key words: Computer Droaram; density; extended corresDonding states;

fluid mixtures; thermal conductivity; viscosity.

1. INTRODUCTION

Engineering design requires transport properties for heat exchangers,

compressors, pumps and for example, pipelines. Owing to the complexity of

transport phenomena in general, accurate methods for the prediction of these

properties have not advanced to a level comparable to equilibrium properties. In fact, most engineering calculations of transport properties are based on empirical correlations which are generally limited to narrow ranges of pressure

and temperature and very frequently to pure fluids. These methods have been

reviewed by Reid, et al . [1].

The purpose of this manuscript is to present a reliable, self-consistent

method for predicting the density, viscosity and thermal conductivity of pure

non-polar fluids and their mixtures. The method is applicable to a wide variety

of chemical types, to thermodynamic states ranging from the dilute gas to

compressed liquid and, in principle, the number of mixture components is

unrestricted.
The procedure is an extension of a method [2,3] which was proposed to

estimate the transport properties of natural gas and similar mixtures and is

based on the corresponding states principle and the conf ormal , one-fluid concept.

It is predictive and requires only the critical parameters, Pitzer's acentric

factor and the component ideal gas heat capacity as input. No mixture properties

or transport data are required. The basic idea is relatively straightforward.

It is assumed that the configurational properties of a single phase mixture can

be equated to those of a hypothetical pure fluid. The properties of this

hypothetical pure fluid are then evaluated via corresponding states with respect

to a given reference fluid.

The theoretical foundation of the approach is well defined for a conformal

system in equilibrium [4]. It is less well understood for a nonconformal system

(i.e., a system in which the mixture components do not interact with the same intermolecular potential, e.g., polyatomic molecules) and for a system in

nonequil ibrium. The assumptions involved in the latter example have, however,

been a topic of recent discussion [5,6], Nevertheless, we have found by

experience that the method gave very good agreement -- typically less than ten

percent uncertainty -- for the transport properties of liquefied natural gas

(LNG) like fluids (i.e., polyatomic nonpolar species). Further, even though the

procedure in our earlier work was optimized for the C, to Cr hydrocarbons and common inorganics, it gave acceptable results -- typically ten to forty percent

uncertainty -- for a diverse number of more complex pure components and their

mixtures. These results for fluids which were well beyond the intended scope of

the original model, encouraged us to explore a systematic extension of the method

to more complex systems.

In this manuscript we briefly report the details of the model and results of

the method for the viscosity and thermal conductivity of pure paraffins, alkenes,

aromatics and cycloalkanes in the C, to C

?f) molecular weight range and their

mixtures. Carbon dioxide is included in the comparisons as an example of a common inorganic.

2. THE ONE-FLUID MODEL AND EQUATIONS

In our procedure, the viscosity (n) of a mixture at density, p, and

temperature, T, and composition jxf is equated to the viscosity of a hypothetical

pure fluid, i.e., n. (P,T) = n (P,T). Then, via the corresponding states

' II I A A argument
nx (P,T) n (P J ) F n

(i)

where

= T^/T^ and h V

C /V

C a,o a o a,o a o

F n

=

where the subscript x referes to the fluid of interest, pure fluid or mixture,

and o refers to the reference fluid. M is the molecular weight and T ooand p are defined by the ratios

T = T/f and p = p h (3)

o x,o o x,o v;

where f and h are, in general, functions of the critical parameters and

x,o x,o ' 3

' K acentric factor. In the special case of two parameter corresponding states

between two pure fluids a and o, they reduce to the well known ratios of critical

constants:

P

C /P

C (4)

o a

v '

where V is the volume and the superscript c indicates a critical value.

Note for the special case of two parameter corresponding states for which

c c Z^ = Z . the factor F can be written in terms of the common viscosity

a o n

J reducing parameter c , viz

{ . T

c 1/6 1/2 c 2/3

( } a a a

KaK

'

so

where p is the pressure.

The thermal conductivity (A) of a mixture or pure fluid must be divided into

two contributions -- one arising from the transfer of energy from purely

collisional or translational effects, A', and the other from the transfer of

energy through the internal degrees of freedom, A". In our model, the

translational contribution to the thermal conductivity is equated to that of a hypothetical pure fluid, i.e., A'. (p,T) = A'(p,T), then, via the corresponding

[MIX A states argument
V(P,T) \Up«.tj f X

(7)

where

1/2

:l/2

h -2/3

X,0 X,0

The internal contribution is calculated via the mixing rule

Amix (p,T) = E E xa

x

B a; (p.T)

(8)

(9)

where

Xa3 (p ' T) = 2X

a(°' T ) A "(0,T)/[^(0,T) + A£(0,T)] (10)

Generally speaking, the density dependence of the internal contribution is not

known on sound theoretical grounds. We assume, therefore, that the contribution

for each component is the same as it would be in the dilute gas state | hence the

designation (0,T)} which we calculate from a Bromley [1] type formula, viz

5R" V'(0,T) = f. . or ' ' int

C pV T ) - 2 n (T)/M

'a

v

' a

(11)

where C is the ideal gas heat capacity of component a, n is the dilute gas

viscosity which is evaluated via eqM (1) v ' using3 T = T/f where f is the

o a,o a,o

reducing ratio for the component in the mixture, R is the gas constant and

f- . = 1.32. We have then our working equation for the thermal conductivity

of a mixture or pure fluid

WP'T

> " \^o'V F

A + Wp - T > (12)

2.1 Extended Corresponding States

The range of applicability of corresponding states in general can be

broadened considerably by introducing the extended corresponding states model

[7,8]. In this model, the two parameter corresponding states formalism is

maintained except that the equivalent substance reducing ratios become, using the

special case of the pure fluid as an example

f

a,o " < Ta

/T

S>

6a,o <V V M

a>

(13)
and

h = (V

C/VC

) $ (T , V , (D ) (14) a,o a o' a,o v a ' a ' or v

'

where 9 n and 4 n are the so-called shape factors [9,10] which are functions

a,o a,o * * of the acentric factor co and of the reduced variables T and V where the a a superscript "*" indicates reduction by the critical point value.

In principle, the shape factors can be determined exactly for any pure fluid

with respect to a reference fluid by simultaneous solution of the conformal

solution equations [8]. By performing this solution one could ensure that the

pure fluid a maps exactly with the reference fluid on a pVT surface via the shape

factors. However, it is much more convenient to have some generalized analytical

relationship for e and <t>. Leach and Leland [9,10] have obtained such relationships for the pure normal paraffins C-, - C-,,- with essentially a methane

reference fluid. Their results are generalized as follows

9 (T , V , a) ) = 1 + (u) - a) ) F(T

+

, V +

) (15)

a,o v a' a' or v a o' a* or

x '

*a,o(

Ta> V ^ = CI + K - »o>G(T

a>

Va) ] Z o /Za ^

F < Ta> V = a

l + bl l K + < cl + d

l /Ta>

(Va " °' 5 ) < 17 >

G(T , VJ = a^V* + b ) + c 9 (V +

v + d ) £nT* (18) a' or 2 a 2 2a 2 a

T+ = min |2, max {T

a

, 0.5J}

(19)

V+ = min

J2, max|V

a

, 0.5}} (20)

2.2 Mixing Rules and Assumptions

There are two basic assumptions of the theory: (1) A pure fluid and a reference fluid obey the two parameter classical corresponding states formalism

and, for a mixture, that all interactions in the mixture follow this principle;

(2) The mixture can be represented by a hypothetical pure fluid which implies

mixing rules exist to evaluate the reducing ratios. Clearly, it has been assumed
that^the introduction of extended corresponding states allows these assumptions

to be upheld.

As we pointed out in the introduction, the assumptions have been discussed

for a system in equilibrium but have received less attention for a system in

nonequil ibrium, expecially for polyatomic molecules. It is at once apparent that

the one-fluid concept is formally weak for transport since the transport

properties can contain contributions unique to the mixture -- the diffusion

coefficient, for example. There is also the difficulty in formulating a consistent mass mixing rule which is unnecessary for the equilibrium properties

but is required for eqs (2) and (8). These problems have been recently discussed

and the interested reader is referred to references [6] and [11] for details.

The mixing rules which are used in the model may be summarized as follows:

f

x,o

= h

x!o E E x xB f

aj?;0

hoB;0 (21)

h x,o -£ E Vfe hae

(22)

(? ?

X«X

E

( E E x xR

h 4 ' 3f

1 '2

M

1 ' 2

)

2

r

1 h"8/3

(23) ' 3 a3,o a3,o a3 / x,o x,o

v '

and

Ak iZE x «„

«-'«

f '« h*'

3 V

2

f h8/3

(24)

x \~ „ a 3 a3 a3,o a3,o/ x,o x,o

*-)

The combining rules are needed finally and these were selected to be

W < f

a,o

f

B,0>

1/2

(' "

kaB»

(25)

haB,o " ItC^^o'

3

'

1 " V (26)

and

Ma3

= 2 W(Ma +M

3) (27)

where ka

„ and I „ are correction factors or binary interaction parameters with

values close to zero. Although it is well known that thermodynamic calculations

(especially phase equilibria) can be sensitive to their numerical value, this
does not appear to be true for the viscosity or thermal conductivity, hence they were set equal to zero for the results reported here.

3. SUMMARY OF THE CALCULATION PROCEDURE

A summary of the calculation procedure to evaluate a viscosity or thermal

conductivity is as follows. Input parameters are the critical temperature,

volume, and pressure, the acentric factor and the ideal gas heat capacity and

molecular weight of each component of the mixture of interest. These parameters

for the reference fluid are required with an equation of state and some functional form for the viscosity and thermal conductivity for this reference

fluid.

Typical experimental input would be the pressure, temperature and mixture

composition. The density of the fluid or mixture is obtained by finding the

equivalent pressure of the reference substance via the ratio p

= p h /f

\) A A j U a jU

from the corresponding pressure in the mixture, p . Initially, the shape

factors in eqs (13) and (14) are set to unity. Given p

= p(p ,T ), the

density p follows. Thus, a first guess of the density is that obtained using

eqs (3)and (4). Repeated iterations using eqs (13) and (14) give the final

density.J Having,3 therefore, final values of p, f and h , one can

' X,0 X,0

evaluate F and F, of eqs (2) and (11), p„ and T and hence n (p„,T,J,

T| A

A' (p T ) and A"(p,T), thereby obtaining values for n (P,T) and A (p,T).

U U \j A A

4. THE REFERENCE FLUID: EXTENDED EQUATIONS FOR METHANE

The procedure outlined in the previous section does not in principle place

restrictions on the choice of the reference fluid and, especially, the reference

fluid does not have to be a component of the mixture. Nonetheless, common sense suggests that the reference fluid should be similar to the systems of interest.

Methane was chosen for the earlier work because we were concerned mainly with the

properties of LNG and the light hydrocarbons. Since the object of this work is

to study the heavy and aromatic hydrocarbons in particular, it would seem appropriate to select a fluid such as hexane or decane, or say benzene.

Unfortunately, at this time, methane is the only fluid which has sufficient

reliable data correlated over a wide range of experimental conditions for the

equation of state, the viscosity and the thermal conductivity. Methane was,

therefore, selected as the reference for this work. One can anticipate

problems — for example, lack of conformality between methane and the mixtures,

effects of internal degrees of freedom, of hindered rotation, and so on.
In practice, a more obvious difficultly occurs: methane freezes at a reduced

temperature of 0.48 which is well above the reduced temperatures commonly

encountered for the liquid states of fluids as simple as propane. This is

demonstrated in fig. (la) where we plot the saturated liquid density for methane

and n-decane in terms of T and p . One sees that the range of states of

n-decane is simply not covered by those of methane. Similarly, for the viscosity

as is shown in fig. (lb) in which n(P,T)£ is plotted versus p , where ? was defined by eq (5). Again the data for liquid methane terminate due to freezing

well before the freezing point of decane is reached. Similar problems are encountered for the thermal conductivity.

In order to overcome these problems, the methane pVT, shape factor,

viscosity and thermal conductivity correlations (surfaces) were extended to 40 K. The details of the methods used in performing these extensions may be found in

references [13] and [14]. Summarizing the results, the pVT surface is given by a 32 term BWR type equation [12] whose functional form and coefficients are given

in table 1. Table 2 lists the shape factor correlation parameters with the

functional form being given by eqs (15-20) except that the restriction given in

eq (19) is removed. The reference fluid viscosity is given by the equation

n (P ,T ) = n 0) (T ) + n (2)( T ) + A (p T )x

f| (28)

where X is a correction factor for non-correspondence in the viscosity given by

3f.

x,o

3T

• c-i

ft

1/2

(29)

where for a mixture Z

c

= 7 x Z c and i|> = 1.5. This expression has a basis

in the Enskog theory in that the density dependence of the viscosity is strongly

dependent on the derivative (dp/dT) . The detailed functional forms and

coefficients for eq (28) are given in table 3. Finally, the translational

reference fluid thermal conductivity is given by

V(P ,TJ = [a1 1} '(T ) + x! 2)

(T )p„ + AX fa.T )] X o

v 0'

where

A

(30)
LU

<

DC

LU

Q.

s

LU

hO

HI

O

Q

LU

450p

400- o n-Decane

/ —'Methane

200

P* 150

100

50

1.0 o n-Decane —Methane

0.8 —

0.6

O

O

o

0.4

n 9

(1a)

i

%o

I

1 2 /»3

REDUCED DENSITY, p

Figure l. (a) Comparison of reduced density of methane and n-decane as a

function of reduced temperature, (b) Comparison of scaled viscosity

of methane and n-decane as a function of reduced density.

9
Table 1. Reference Fluid Equation of State

(p, atm; p, mol/L; T, kelvin)

9

E

n=l

a

n (T) p' 15

n=10

a

n (T) p 2n " 17 e^p

= RT

'10

'11

'12

'13

'14

'15

I^T + N

2 Tl/2 + N

3 + N 4

/T + N

5/T2

N g T + N

? + N 8

/T + N

g/T

2

N 1QT + N n

+ N,,/T 12' = N 13

- N 14 /i + N 15 /r

= N 16

/T

= N,,/T + N 10 /T

J '17 n 19

/t;

n 2o/t

: n 22 /tJ

n 26 /t

: n 28 /t

: N 30

/T

'

+N21 /T

4 + N 23

/T

, + N 25

/T

+ N 27

/T

, + N 29

/T

J

+ N

31

/T

3 + N 32

/T

/

10
Table 1. Reference Fluid Equation of State (Continued)

i/N. i/N.

1 - 1.184347314485E-2 17

2 7.540377272657E-1 18

3 - 1.225769717554E+1 19

4 6.260681393432E+2 20

5 - 3.4906544091 21E+4 21

6 5.301046385532E-4 22

7 - 2.875764479978E-1 23

8 5.011947936427E+1 24

9 - 2.821562800903E+4 25

10 - 2.064957753744E+5 26

11 1.285951844828E-2 27

12 - 1.106266656726E+0 28

13 + 3.060813353408E-4 29

14 - 3.174982181302E-3 30

15 5.191608004779E+0 31 16 - 3.074944210271E-4 32

1.071143181503E-5

- 9.290851745353E-3

1.610140169312E-4

3.469830970789E+4

- 1.370878559048E+6

1.790105676252E+2

1.615880743238E+6

6.265306650288E-1

1.820173769533E+1

1. 44988850581 1E-3

- 3.159999123798E+1

- 5.290335668451E-6

1. 6943502441 52E-3

8.612049038886E-9

- 2.598235689063E-6

3.153374374912E-5

Y = 0.0096 0.08205616

1 atm = 0.101325 MPa

11
Table 2. Coefficients for Shape Factor Correlations

Coefficients [eg 16] Coefficients [eg 17]

l l 0.090569

b

1 -0.862762

c. = 0.316636

= -0.465684

a 2

= 0.394901

b

2 = -1 .023545

c 2

= -0.932813

d = -0.754639

12
where

Table 3. Reference Fluid Viscosity Correlation

n(p,T) = n

(1)

(T) + n

(2) (T)p + An (p,T)

,(D

9

n=l

c

nT (n-4)/3

n (2)

= b

1 + b 2 [b

3

- £n(T/b

4

)] 2

An = exp a-, + a 2 /T exp [(a^ + a A /T

0/ ^) p 3/2v 0.1

+ (p/p

c

- l)p

- 5 (a

5 + a 6

/T + a

y /T

2

)] - 1 .0

J

i a

i b.

l

1 -1.0239160427E+1 1.6969859271E+0

2 1. 7422822961 E+2 -1.3337234608E-1

3 1.7460545674E+1 1.4

4 -2.8476328289E+3 1.68E+2

5 1.3368502192E-1

6 1.4207239767E+2

7 5.0020669720E+3

8

9

2.907741307E+6

-3.312874033E+6

1.608101838E+6

-4.331904871E+5

7.062481330E+4

-7.116620750E+3

4.325174400E+2

-1.445911210E+1

2.037119479E-1

(T, kelvin; p, g/cm3

, p r = 0.1628)

13
h

r 3/2

3f \ ) Z Cn

X,0\ l f V3T / 7 c x,o \ x A. ; z x

X

(31)

The detailed functional forms and coefficients for eq (30) are listed in

table 4.

5. RESULTS FOR PURE FLUIDS

Having the reference fluid correlations for methane, it was straightforward

to calculate the transport properties of any pure species via eqs (1) and (12).

A considerable data base was assembled to provide a thorough test of the

procedure. The data and references used in this comparison are available upon

request. The data were evaluated as far as possible for accuracy and internal

consistency. One should point out that in general the data situation is not too

satisfactory for transport properties in that the more recent experimental

techniques have not been applied to many organic liquids other than methane, and

recently to ethane and propane. A realistic guess as to the accuracy of the data

is 5-15 percent and probably much worse for the very heavy species.

The results are summarized in tables 5 and 6 and in figs. (2-5). The tables

show the average absolute percent deviation, AAD, and the average percentage

error, BIAS. The overall deviations between experiment and the calculations are very satisfactory. The viscosity results become somewhat worse, and negative, as the freezing point of the fluid is approached. It is not clear why this should

be the case, but one can say that there is a good chance that the viscosity

becomes non-Newtonian in this region and that pre-freezing nucleation effects are important. One also observes that the viscosity results are markedly worse for

highly branched alkanes and for the cycloalkanes. We attribute this to a failure

of the corresponding states model to represent adequately the effect of the

molecular structure on the transport coefficient. In spite of these limitations,

the overall results are excellent, especially considering the limited input

(T

c

, p

c

, V" c, M, a), and C°) needed to make the predictions. In fact, the

thermal conductivity results are in better agreement with experiment than the

estimated error for this property.

6. RESULTS FOR MIXTURES

The main objective of this work was to develop a procedure to predict the

transport properties of mixtures: there is a real need for such a procedure, yet

14
Table 4. Reference Fluid Translational Thermal Conductivity

Correlation

A'(P,T) = X (1) '(T) + X (2) (T)p + AX(pJ)

A (1) '(T) - |^n (1) (T)

A (2) (T) = b

1 + b[b

3

- £n(T/b

4

)]

2

AX = exp a-, + a„, 3/2v 0.1

/T jexp [(a

3 + a 4 /T 3/2

) p

+ (p/p

c

- 1) p

- 5 (a

5 + a 6 /T + a ? /T

2 )] - 1.0

-7.1977082270E+0

8.5678222640E+1

1.2471834689E+1

-9.8462522975E+2

3.5946850007E-1

6.9798412538E+1

-8.7288332851E+2

-0.252762920E+0

0.334328590E+0

1.12

0.1680E+3

(T, kelvin; p, g/cm3

; p c

= 0.1628)

15
Table 5. Summary of Calculated Results for Pure Fluid Viscosity

(AAD = Average Absolute Percent Deviation;

BIAS = Percentage Bias)

Fluid N AAD BIAS

Methane 76 3.03 - 2.89

Ethane 48 12.31 9.99

Propane 146 6.56 - 5.10

n-Butane 200 3.39 - 2.80

i -Butane 68 11.49 -11.39

n-Pentane 195 4.15 - 1.49

neo-Pentane 75 32.83 -32.83

n-Hexane 66 3.30 2.16

i-Hexane 12 3.09 - 3.09

n-Heptane 78 6.31 3.45

n-Octane 52 6.22 4.30

n-Nonane 46 2.89 1.54

n-Decane 107 3.25 - 1.56

n-Undecane 19 3.47 1.29

n-Dodecane 41 5.12 1.19

n-Tridecane 58 4.69 - 1.12

n-Tetradecane 53 5.04 - 2.97

n-Pentadecane 18 5.37 - 2.23

n-Hexadecane 39 5.33 2.08

n-Heptadecane 15 6.11 3.56

n-Octadecane 28 9.66 5.89

n-Eicosane 16 6.37 3.89

Ethylene 10 2.02 - 0.61

Propylene 13 9.72 3.18

3-Methyl-l-butene 8 5.53 - 5.53

1 -Hexene 27 17.19 17.19

Cyclohexane 48 49.25 -49.25

Methylcyclohexane 14 30.69 -30.69

Ethyl cyclohexane 17 30.81 -30.81

Cyclopentane 10 29.20 -29.20

Benzene 82 8.39 - 8.33

16
Table 5. (Continued)

Fluid N AAD BIAS

Toluene 47 4.13 3.17

m- Xylene 16 20.35 20.35

Propyl benzene 5 8.16 8.16

Butylbenzene 5 12.12 12.12

Carbon Dioxide 111 4.75 - 4.53

Overall 1869 8.42 - 4.10

17
Table 6. Summary of Calculated Results for Pure Fluid Thermal

Conductivity

(AAD = Average Absolute Percent Deviation;

BIAS = Percentage Bias)

Fluid N

15

AAD

5.44

BIAS

Ethane 5.06

Propane 188 5.12 4.99

n-Butane 32 6.41 6.41

Isobutane 4 12.49 -12.49

n-Pentane 35 5.24 5.24

n-Hexane 10 1.88 -1.31

Isohexane 3 .91 -.91

3-Methylpentane 3 2.56 -2.56

2, 2 -Dimethyl butane 3 1.03 -1.03

2,3-Dimethylbutane 4 1.42 .95

n-Heptane 84 8.15 -8.13

2,4-Dimethyl pentane 3 1.69 1.69

2 , 2, 3-Tri methyl butane 1 4.40 4.40

n-Octane 15 5.37 -5.37

3-Methyl heptane 1 1.71 1.71

2,2,4-Trimethyl pentane 5 2.30 2.23

n-Nonane 15 6.13 -6.13

2,2,5-Trimethylhexane 4 3.68 .31

n-Decane 44 3.41 -1.54

n-Undecane 8 12.19 -12.19

n-Dodecane 3 6.67 -6.67

n-Tridecane 9 6.90 -6.90

n-Tetradecane 50 1.78 -1.76

n-Pentadecane 51 1.62 -.92

n-Hexadecane 49 .96 .40

n-Heptadecane 38 2.79 -2.19

n-Octadecane 34 3.44 -2.52

n-Nonadecane 8 7.12 -4.42

n-Eicosane 33 1.87 1.75

Cyclopentane 4 1.57 -1.57

18
Table 6. (Continued)

Fluid N

3

AAD

.16

BIAS

Methyl cycl open tane .13

Cyclohexane 4 1.80 -.58

Methyl cycl ohexane 10 5.39 5.39

Ethylene 75 8.53 -8.51

Propylene 42 9.96 -9.96

2-Methylpropene 3 5.27 5.27

1-Hexene 64 4.67 -2.43

1-Heptene 67 9.55 -9.55

Benzene 18 2.88 -1.71

Toluene 67 6.81 6.42

Ethylbenzene 8 4.67 4.67

ortho-Xylene 9 10.64 10.64

meta-Xylene 7 8.69 8.69

para-Xylene 66 6.24 5.72

Propyl benzene 5 2.32 1.04

Cumene 8 3.58 3.58

Butylbenzene 7 3.15 3.15

Bi phenyl 14 14.76 -14.76

Carbon Dioxide 22 6.67 6.67

Overall Results 1255 5.06 - 0.67

19
10

10

a 10

a> £

°

x-10

a>

I 2 10

o

5

O

O -10

10

10

1.

Methane

n-Decane

n-Hexadecane oo o

~© o

On °# eg

-tf1.5 2.0 2.5 3.0 3.5

REDUCED DENSITY, p

Figure 2. Comparison of calculated and experimental viscosity of methane,

pentane, decane and hexadecane as a function of reduced density.

20
a

x

a>

a

x

COo

O

O

10

-10

10

-10

10

-10h

10

-10

-20

-30

-

I TolueneI I I -

«*b°

Carbon Dioxide

o ?ra -

o

o

3 c'^qI!-

-

- Ethylene

o O

-

- isobutane

O

o

-

-

o

o

o

O °°^ 0<3|£

^°o9§>oo

-

I

00 °Oo o

1.0 1.5 2.0 2.5 3.0

REDUCED DENSITY, p

3.5

Figure 3. Comparison of calculated and experimental viscosity for toluene,

carbon dioxide, ethylene and isobutane.

21
Q.

X

a

x

I O

10

10

10

N-Decane

T

oo( a0 oO° y

--10-

C0o

O

O

N-Hexadecane

10

-10

10

- N-Eicosane

o

-10-

Methyicyclohexane

o<to&

1.0 2.0 3.0

Figure 4.

REDUCED DENSITY,/)

Comparison of calculated and experimental thermal conductivity for

propane, decane, hexadecane, eicosane and methylcyclohexane.

22
o.x

a

x

I O

COa

o

o

10-

-10

mUU ° ° ° o

2 °oo °o(5^gRtb

CD

1.0 2.0 3.0

REDUCED DENSITY,/)

Figure 5. Comparison jof calculated and experimental thermal conductivity for

ethylene, 1-hexene, benzene, toluene, p-xylene and carbon dioxide.
none exists which does not require in some way transport data of the pure

components. Our method, however, avoids this and the mixture evaluations are no more complicated than those for the pures, given the mixing and combining rules,

eqs (21-27). It is also worth remarking that the procedure also gives the

mixture density automatically.

One further refinement was considered for the mixture viscosity. We

introduced a X factor in eq (29) to account for the lack of correspondence

between the reference fluid and a pure fluid of interest. For mixtures, however,

X will act as a correction not only for lack of correspondence between the

reference fluid and hypothetical pure fluid, but should also account for the

basic lack of conformality in the mixture. It turns out that although most of

the mixtures studied cannot be conf ormal , the procedure works reasonably well

with X -x- 1.0. Our results for the mixture viscosity (but not thermal

conductivity) did show, however, a systematic disagreement with experiment in one special case, namely when the components of the mixture differed substantially in

effective size, e.g., in the values of the critical volume. In particular,

initial calculations for the methane/decane mixture viscosity showed large

deviations at high densities as the mole fraction of methane increased. In effect, the contribution of methane to the mixture viscosity was negligible until

its mole fraction approached 0.9 and the procedure tended to overestimate it.

For this system the critical volume ratio is approximately 6.

Since a methane/decane type mixture is relatively common, we attempted to

account for the size effect empirically in the present model. The correction

factor X was modified to become

n

n

where

-1

'1 - *

T /3f \

x I x,o \

f I 9T ) X,0 \ X A

z

c 1/2

X

Z o,

a + bR

1 + cR

(32)

R _1 = ]T x (V c /V

c

. *—d ) a

K a' mm'

1/3

(33)

and a =0.16129, b -4.51613, and c = -5.35484. V . is the critical mm

volume of the smallest component in the mixture.

24
It should be noted that for most mixtures, results from eq (32) are very

close to those from eq (29) and in fact X is often very close to unity. No

further corrections were made for the mixture thermal conductivity.

Tables 7 and 8 list the mixtures, number of points considered and the AAD

and BIAS between experiment and our procedure. Figures (6-8) are typical of the

deviations observed. In general the results are excellent with an average

absolute deviation of approximately seven percent for both transport properties.

An assessment of the method should, however, bear in mind that the data situation

for mixtures is very poor and that an assignment of 5-20 percent on the accuracy

of the mixture data is reasonable.

7. CONCLUSIONS

We have presented a predictive procedure to estimate the viscosity and

thermal conductivity of nonpol ar pure fluids and mixtures over the entire range

of fluid states, from the dilute gas to the dense liquid. Extensive comparisons

with data have shown that the transport properties of a wide variety of pure

fluids and mixtures are predicted to within an absolute percent deviation of

about seven percent. Not shown in this paper are comparisons for the density,

which is also predicted and for the dilute gas properties. In general the

density is predicted to better than one percent and the dilute gas transport

properties are predicted to within five to ten percent.

The basis of the method is the one fluid corresponding states concept with

the extended corresponding states approach included. The method is predictive

and requires only the common characterization parameters of the pures as input.

The number of components of a mixture which can be considered is, in principle,

unrestricted.

The application of the methodology described herein to polar fluids and to

molecules with structures which could cause hindered rotation and stearic effects

is under current investigation.

8. COMPUTER PROGRAM

A computer program for predicting the transport properties and the density

of pure fluids and their mixtures has been developed. The program is essentially

identical to that used to generate the results reported here. A detailed user's

manual has been prepared which describes the program input, output and overall

structure and is given in Appendix A. Appendix B lists the program.

25
T

fible 7. Summary of Results for Binary Mixture Viscosity

Component 1 Component 2 N

134

AAD

3.86

BIAS

Methane Propane - 2.85

n-Nonane 32 9.56 8.12

n-Decane 71 10.62 - 5.80

2,3-Dimethylbutane n-Octane 2 5.04 - 5.04

n-Hexane 2,3-Dimethyl butane 2 5.19 5.19

n-Tetradecane 10 1.23 0.99

n-Hexadecane 26 1.84 - 0.58

n-Heptane n-Dodecane 3 4.32 4.32

n-Tetradecane 3 2.47 2.47

n-Hexadecane 3 1.96 - 0.24

n-Octadecane 2 1.73 0.27

Methyl cyclohexane 24 17.31 -16.51

2, 2, 3-Tri methyl butane 2,3,3-Trimethyl pentane 2 29.93 -29.93

n-Octane n-Decane 2 3.83 3.83

n-Tetradecane n-Hexadecane 11 2.73 2.53

Benzene n-Hexane 15 6.02 - 1.58

n-Heptane 3 1.58 6.56

2, 2, 4-Tri methyl pentane 26 11.21 -11.21

n-Decane 3 5.68 4.00

n-Dodecane 3 7.04 7.04

n-Tetradecane 3 3.41 3.27

n-Hexadecane 3 3.57 2.46

n-Octadecane 3 2.79 2.79

Toluene n-Heptane 21 6.09 6.09

n-Octane 20 10.14 10.14

2,2,4-Trimethyl pentane 28 5.87 - 3.40

Overall Results 455 6.95 - 2.07

26
Table 8. Summary of Results for Binary Mixt lire Therma 1 Condu ctivity

Component 1 Component 2 N

15

AAD

11.69

BIAS

Methane n-Butane 11.49

2,3-Dimethylbutane 2,2,4-Trimethylpentane 6 5.15 5.15

n-Heptane 2,2,4-Trimethyl pentane 6 1.94 1.71

n-Heptane 1 -Hexene 8 7.18 - 7.18

n-Octane n-Hexane 5 2.09 - 2.09

n-Octane n-Heptane 6 2.77 - 2.77

n-Octane 2,2,4-Trimethyl pentane 9 3.96 - 3.96

n-Octane 1 -Hexene 9 7.19 - 7.19

2,2,5-Trimethylhexane 2,2,4-Trimethylpentane 6 4.35 4.35

n-Tetradecane 2,2,4-Trimethyl pentane 6 4.43 - 4.43

n-Hexadecane n-Heptane 2 2.81 - 2.81

n-Heptadecane n-Octane 6 4.16 - 4.16

Cyclopentane n-Heptane 6 1.72 1.29

Cyclopentane Methylcyclohexane 6 5.90 5.90

Methyl cyclohexane 2,2 ,4-Trimethyl pentane 6 11.42 -11.42

Benzene Cyclohexane 4 5.54 5.54

Benzene Toluene 12 6.79 6.79

Toluene n-Heptane 5 6.37 6.37

Toluene 2,2 ,4-Trimethyl pentane 6 11.05 11.05

Toluene Cyclohexane 4 5.26 5.26

Tol uene o-Xylene 6 13.97 13.97

o-Xylene 2 ,2 ,4-Trimethyl pentane 6 10.65 10.65

n-Heptane n-Decane 6 8.89 - 8.89

Benzene n-Heptane 8 2.80 - 1.71

Overall Results 159 6.58 1.73

27
10

-10

-20

10

X

\ -10

a

x

a) -20

'a "30k

15

o

P* 10

O

O

-10

1.0

o o Q> <y o

Methane/Propane

Methane/Decane

0D00

o

ctP

^°a%o

°° o G

°

° °o o o

Hexane/Tetradecane

^ooco^

-10-

Hexane Hexadecane

o o

1.5 2.0 2.5 3.0 3.5

REDUCED DENSITY, p

Figure 6. Comparison of calculated and experimental viscosity of selected

paraffin binary mixtures as a function of reduced density.

28
10

-10

a

X -20

0) ^

\ 20

a

X 10

P1 o

(0u -10

O

O 10

i"

-10

-20

I I Toluene/lsooctane

l I

-

c?

<3> —

—

Toluene/Octane

DOb® O

c9oo <£o

—

-

Benzene/Hexane

o

o

<2Ti

-

—

I I

o8

I o I

-

1.0 1.5 2.0 2.5 3.0 3.5

REDUCED DENSITY, p

Figure 7. Comparison of calculated and experimental viscosity of selected

aromatic/paraffin mixtures.

29
20

10-

-10

T

o o o

o

Methane/N-Butane

Q.

X

a

<D

COO

20 h

10

-10

j£_ _ Benzene/N-Heptane

<9 o oo

o

O

10

-10

10

-10

20

10

N-Heptane/N-Decane oool_

Cyclopentane/N-Heptane

-10- N-Octane/1-Hexene

o °o°o°

Figure 8,

1.0 2.0 3.0

REDUCED DENSITY, p

Comparison of calculated and experimental thermal conductivity of

selected binary mixtures.
9. ACKNOWLEDGMENTS

This work was supported by the Office of Standard Reference Data and, in

part, by the Gas Research Institute. We are grateful to Professor R. P. Danner

of Pennsylvania State University for making his viscosity and thermal

conductivity data bases available to us. Mrs. Karen Bowie helped substantially

in the preparation of this manuscript.

31
10. REFERENCES

[1 ] Reid, R. C, Prausnifz, J. M. and Sherwood, T. S., "The Properties of Gases

and Liquids," 3rd ed., McGraw-Hill, New York, 1978.

[2] Hanley, H. J. M. , "Prediction of the Viscosity and Thermal Conductivity of

Mixtures," Cryogenics ]_6, 643-51 (1976).

[3] Mo, K. C. and Gubbins, K. E., "Molecular Principle of Corresponding States

for Viscosity and Thermal Conductivity of Fluid Mixtures," Chem. Eng.

Commun. 2, 281-90 (1974).

[4] Henderson, D. L. and Leonard, P. J., in "Treatise on Physical Chemistry,"

D. Henderson, ed., Vol VI I IB, Ch. 7, Academic Press, New York, 1971.

[5] Mo, K. C. and Gubbins, K. E., "Conformal Solution Theory for Viscosity and

Thermal Conductivity of Mixtures," Mol . Phys. 3J_, 825-47 (1976).

[6] Evans, D. J. and Hanley, H. J. M. , "Viscosity of a Mixture of Soft Spheres,"

Phys. Rev. A20, 1648-54 (1979).

[7] Leland, T. W. , Rowlinson, J. S. and Sather, G. A., "Statistical

Thermodynamics of Mixtures of Molecules of Different Sizes," Trans. Farad.

Soc. 64, 1447-59 (1968).

[8] Rowlinson, J. S. and Watson, I. D., "The Prediction of the Thermodynamic

Properties of Fluids and Fluid Mixtures - I. The Principle of Corresponding

States and its Extension," Chem. Eng. Sci. 24, 1565-74 (1969).

p] Leach, J. W., "Molecular Structure Corrections for Application of the theory

of Corresponding States to Non-Spherical Pure Fluids and Mixtures," Ph. D. Thesis, Rice University, 1967.

[10] Leach, J. W. , Chappelear,P. S. and Leland, T. W. , "Use of Molecular Shape

Factors in Vapor-Liquid Equilibrium Calculations with the Corresponding

States Principle," A.I.Ch.E. J. T4, 568-76 (1968).

[11] Hanley, H. J. M. and Evans, D. J., "Behavior of a Nonconformal Mixture via

Computer Simulation," submitted for publication, Int. J. Thermophys., 1981.

[12] Jacobsen, R. T. and Stewart, R. B., "Thermodynamic Properties of Nitrogen

Including Liquid and Vapor Phases from 63 K to 2000 K with Pressures to

10,000 bar," J. Phys. Chem. Ref. Data 2, 757-922 (1973).

[13] Ely, J. F. and Hanley, H. J. M. , "Prediction of Transport Properties.

I. Viscosity of Fluids and Mixtures," submitted for publication, Ind. Eng.

Chem. Fundam. , 1981

.

P4] Ely, J. F. and Hanley, H. J. M. , "Prediction of Transport Properties.

II. Thermal Conductivity of Fluids and Mixtures," in preparation.

32
APPENDIX A. TRAPP USER'S GUIDE

The method is applicable to the full range of densities and temperatures,

from the dilute gas to dense liquid. The required material constants for each

mixture component are the critical parameters, T , p , V and Pitzer's

acentric factor. The thermal conductivity calculation also requires the ideal

gas heat capacity. No transport data for the mixture or components are required.

The computer program currently has a built in database for the 61 components.

These components and their synonyms are listed in table Al

.

Program Description

The program is modular in construction consisting of a sample driver or main

program and a collection of subroutines. Most of the communication between the

routines is accomplished via block common with a few parameters being passed in

the subroutine calling lists. Figure Al shows a block diagram of the program

communication links. The purpose of these routines are as follows:

TRAPP is the main program which inputs the components, temperature, pressure

and compositions. It then makes the appropriate subroutine calls and prints out

the calculated density, viscosity and thermal conductivity.

LIB takes the component names from TRAPP and tries to identify them in the

component library. After a successful identification, it loads the various

material constants in the common block/COMPRP/, initializes the binary

interaction constants to zero and returns. If the component is not identified as being in the database, it aborts with an error message. LIB utilizes the block

data subroutine LIBSET which loads the common block /LIBDAT/.

DCST takes the input pressure, temperature and composition and calculates

the mixture density via the extended. corresponding states model. It uses several

subroutines to accomplish this calculation which are described below. After the

density is calculated it calls the subroutine ECSTX to evaluate the derivatives

needed in the viscosity calculation.

RHOF is called by DCST and makes an initial guess at the reference fluid

density given the equivalent temperature and pressure.

DO is called by RHOF and performs a Newton-Raphson iteration to calculate

the reference fluid density given the temperature and pressure.

PVTO is called by DO and calculates the reference fluid pressure and its

derivative w.r.t. density given the density and temperature.

33
Table Al

.

Listing of Components and TRAPP Data Base

Component Name ( Synonym Component Name Synonym

Methane CI 2-Methyl-2-Butene 2M2C4-

Ethane C2 2-Methyl-l-Butene 2M1C4-

Propane C3 3-Methyl-l-Butene 3M1C4-

Isobutane IC4 Cis-2-Pentene C2C5-

n-Butane C4 Trans-2-Pentene T2C5-

2, 2-Dimethyl propane 22DMPR 1-Pentene C5-

Isopentane IC5 1-Hexene C6-

n-Pentane C5 1-Heptene C7-

2, 2-Dimethyl butane 22DMB Propadiene 12C5=

2 ,3-Dimethyl butane 23DMB 1 ,3-Butadiene 13C4=

3-Methylpentane 3MP 1 ,2-Butadiene 12C4=

Isohexane IC6 Cyclopentane CC5

n-Hexane C6 Methyl cycl opentane MCC5

n-Heptane C7 Ethyl cyclopentane ECC5

n-Octane C8 Cyclohexane CC6

n-Nonane C9 Methyl cycl ohexane MCC6

n-Decane CIO Ethyl cyclohexane ECC6

n-Undecane Cll Benzene BNZ

n-Dodecane CI 2 Toluene TOL

n-Tridecane CI 3 Ethyl benzene EB

n-Tetradecane CI 4 Ortho-xylene OXYL

n-Pentadecane CI 5 Meta-Xylene MXYL

n-Hexadecane C16 Para-Xylene PXYL

n-Heptadecane CI 7 Hydrogen H2

Ethene C2- Nitrogen N2

Propene C3- Oxygen 02

2-Methylpropene IC3- Water H20

Cis-2-Butene C-2C4- Carbon Monoxide CO

Trans-2-Butene T-2C4- Carbon Dioxide C02

1-Butene C4- Sulphur Dioxide S02

Hydrogen Sulphide H2S

34
Li_

CD CD

CD

I—>

Q-

<c

a:

scr. o

s-o.

s- +J

Q.eoo

4-OE

<T3 S-O)oo

S-en

35
ECSTX is called by DCST after the density has been calculated. It calculates the appropriate molecular weights for the transport calculations, part

of the transport correction factors and the derivatives of the equivalent

substance reducing ratios with respect to temperature.

THERMC is called by TRAPP after the density is calculated and evaluates the

mixture thermal conductivity. It calculates the contribution to the thermal

conductivity from the internal degrees of freedom using the routine VSCTY and

ideal gas heat capacity in the text. The routine then calculates the

translational contributions to the thermal conductivity using the routine TCOND

and combines all the results according to eq (12).

TCOND takes the equivalent temperature and density of the mixture and/or

components and calculates the translational contribution to the thermal

conductivity via a corresponding states principle. The procedure used is

described in the text.

VSCTY is called by TRAPP to evaluate the mixture viscosity via a corresponding states principle. The procedure used is described in the text.

Program Input and Output

The program expects input in a specified order and is set up to run in an interactive mode. When the program begins execution it prints a banner and then

inquires if the user desires a list of the library components. If the user answers yes as indicated by a "1" followed by a carriage return, the list is

displayed. A

"0" response indicates a no and the list is skipped. Next the

program asks if engineering units are desired. A "0" response indicates that

3 scientific units are desired (K, bar, Kg/m , Pa»s, and W/m-K) and a "1"

3

response means that engineering units are desired (F, psia, lb/ft , lb/ft-hr,

and BTU/ft-hr- F).

Next, (Step A) the program requests the number of components, the response

to which can be 0-20. If is entered, the program stops.

(Step B) A nonzero response causes the program to ask for the component

names (7A4 Format), one at a time. If a component name is incorrectly spelled or

not in the database, the program aborts with an error message. The synonym may

be entered in lieu of the full name. (Step C) If there is more than one component in the system the program then

requests the composition of each component, one component at a time. The

compositions may be entered in moles or mole percent. The program automatically

36
normalizes the compositions to sum to unity, i.e., they are internally converted

to mole fraction. If the composition of any component is entered as less than

zero, the program assumes that you want to change the mixture components and

reverts to step A. (Step D) The program next requests the temperature and pressure in the units

specified previously on one line separated by a comma. If "0,0" is entered the

program reverts to step C. For any other response the program then calculates

the density, viscosity and thermal conductivity and prints the results of the

calculations. The program then reverts to step D. The logical flow of the

input/output phases is shown in fig. A2.

Sample Input and Output

Tables A2-A4 give typical input/output examples.

Cautions

The program assumes that the mixture is single phased. If it is not, the

results of the calculations will be meaningless. In addition, if the mixture is

single phased but very close to the two-phase boundary it may converge to a liquid solution when the mixture is actually a vapor and vice-versa. If this

happens, raise or lower the pressure slightly until you get into the desired

phase. Appendix B lists the computer program.

37
Figure A2. Flow diagram of I/O portion of TRAPP,

38
Table A2 . Sample Input and Output

* %

* T R A P P #

* * * TRANSPORT PROPERTIES PREDICTION PROGRAM *

* *

* BY *

* *

* J. F. ELY AND H . J. M. HANLEY *

* U.S. NATIONAL BUREAU OF STANDARDS *

* NATIONAL ENGINEERING LABORATORY *

* THERMOPHYSICAL PROPERTIES DIVISION *

* BOULDER , COLORADO 80303 *

* *

* (PARTIALLY SPONSORED BY THE OFFICE OF *

* STANDARD REFERENCE DATA) *

* *

DO YOU WANT A LIST OF LIBRARY COMPONENTS ( 0-NO i 1-YES ) ?

DO YOU WANT ENGINEERING UNITS ( 0-NO r 1-YES )?

ENTER NUMBER OF COMPONENTS ? 1 ENTER NAME OF COMPONENT 1 ? METHANE

ENTER T(K) AND PCBAR ) ? 100 ,1

D= 439.219 KG/M**3 ETA = 1482. 3E-7 PA-S TC = .21842 W/M-K

ENTER T(K> AND P(BAR ) ? 120.1

D= 1.654 KG/M**3 ETA = 48.2E-7 PA-S TC = .01471 W/M-K

ENTER T(K) AND P(BAR ) ? 120 »

D= 410.533 KG/M**3 ETA = 971.3E-7 PA-S TC - .17804 W/M-K

ENTER T(K) AND P<BAR ) ? 140.10

D= 377.755 KG/M**3 ETA = 673.5E-7 PA-S TC = .14425 W/M-K

ENTER T(K) AND P(BAR ) ? 190r50

D= 239.837 KG/M**3 ETA = 239.7E-7 PA-S TC = .07190 W/M-K

ENTER T(K) AND P(BAR ) ? OrO

ENTER NUMBER OF COMPONENTS ?

.035 CP SECONDS EXECUTION TIME.

39
Tat|le A3. Sample Input and Output

T R A P P TRANSPORT PROPERTIES PREDICTION PROGRAM

BY

J. F. ELY AND H. J, M* HANLEY

U.S. NATIONAL BUREAU OF STANDARDS

NATIONAL ENGINEERING LABORATORY

T

I -I ER M P N Y S I C A L P R P E R T I E S DIVISION

B U L D E R y COL R A D 8 3 3

(PARTIALLY SPONSORED BY THE OFFICE OF

S T A N D A R D R E F E R E N C E D ATA)

DO YOU WANT A LIST OF LIBRARY COMPONENTS ( 0--NO ii 1 -YES ) ?

DO YOU WANT ENGINEERING UNITS ( O-NOr 1-YES ) ? 1 ENTER NUMBER OF COMPONENTS ? 3

ENTER NAME OF COMPONENT 1 ? METHANE

ENTER NAME OF COMPONENT 2 ? PROPANE

ENTER NAME OF COMPONENT 3 ? NITROGEN

ENTER NUMBER OF MOLES OF METHANE

ENTER NUMBER OF MOLES OF PROPANE

ENTER NUMBER OF MOLES OF NITROGEN

? 3

? 1 ? 6

ENTER T(F) AND P(PSIA) ? 400 » 1000

D» 2*8122 LB/FT**3 ETA = 053292 .B/FT-HR TC = ,02700 BTU/FT-HR-F

E N T E R T ( F > AND P ( P S I A ) ? - 1 t 1 D» 12.4563 LB/FT#*3 ETA = ,040324 LB/FT-HR ,02040 BTU/FT-HR-F

ENTER T(F) AND P(PSIA) ? -300 » 1430

D= 44,8939 LB/FT**3 ETA = 53S57 LB/FT-HR TC 11163 BTU/FT-HR-F

ENTER T(F) AND P(PSIA) ? 0»0

ENTER NUMBER OF MOLES OF METHANE

ENTER NUMBER OF MOLES OF PROPANE

ENTER NUMBER OF MOLES OF NITROGEN

ENTER T(F) AND P(PS1A) ? 77 » 14.7

D= .0523 LB/FT**3 ETA = ,030090 LB/FT-HR TC

ENTER T(F) AND P(PSIA) ? 77 » 3000

D= 12,4219 LB/FT**3 ETA = ,051985

ENTER T(F) AND P(PSIA) ? y ENTER NUMBER OF MOLES OF METHANE

ENTER NUMBER OF COMPONENTS ?

,155 CP SECONDS EXECUTION TIME,

.B/FT-HR TC

? -1

01912 BTU/FT-HR-F

,03323 BTU/FT-HR-F

40
Table A4 . Sample Input and Output **********************************

T R A P P

TRANSPORT PROPERTIES PREDICTION PROGRAM

BY

J. F. ELY AND H. J. M. HANLEY

U.S. NATIONAL BUREAU OF STANDARDS

NATIONAL ENGINEERING LABORATORY

THERMOPHYSICAL PROPERTIES DIVISION

BOULDER? COLORADO 80303

(PARTIALLY SPONSORED BY THE OFFICE OF

S T A N D A R D R E F E R E N C E DATA)

'j^

rf. ^^ ^^ ")t ^ ^\'it 'if ^ W^ /j\ ^V Sit ^ ^" "J^ ^ "^/ ^ ^ ^ ^ SU "^f "J^ ^ 4* ^ ^ "iV ^ "J/ SLf "J^ ^ ^* '^ SJ^ ^ ^ ^ W "4/ '& Sk "^f ^ "^ ^ ^ "iV ^ ^ ^. Jf. tf. /|S. ^ ^ ^ ^ ^ /^ ^ ^\ ^ ^ ^\ ^S, Jfi ^ ^ ^ ^ ^ fl^ ^ ^ ^i. ^ ^ ^i .Jp. ^i ^v ^ ^ ^ ^ ^ ^ ^

DO YOU WANT A LIST OF LIBRARY COMPONENTS < 0-NO J 1-YES ) ?

DO YOU WANT ENGINEERING UNITS ( 0-NO ? 1-YES)?

ENTER NUMBER OF COMPONEN'IS ? 6

ENTER NAME OF COMPONENT :l. ? N2

ENTER NAME OF COMPONENT- 2 ? CO2

ENTER NAME OF COMPONENT 3 ? C3

ENTER NAME OF COMPONENT 4 ? BNZ

ENTER NAME OF COMPONENT 5 ? H2S

ENTER NAME OF COMPONENT 6 ? ETHENE

ENTER NUMBER OF MOLES OF N2 '? 3

ENTER NUMBER OF MOLES OF C02 ? 4

ENTER NUMBER OF MOLES OF C3 ? 8

ENTER NUMBER OF MOLES OF BNZ '? 1 ENTER NUMBER OF MOLES OF H2S 'i> 0.

ENTER NUMBER OF MOLES OF ETHENE ? 50

ENTER T(K) AND PC BAR ) ? 400*0.0:1.

D= .010 KG/M**3 ETA * 138.6E-7 PA-S TC

ENTER T ( K ) AND P ( BAR ) ? 200 t 100

D= 594.880 KG/M**3 ETA » 1515. 8E-7 PA-S TC

ENTER TCK) AND P(BAR ) ? Os>0

ENTER NUMBER OF MOLES OF N2 •1

ENTER NUMBER OF COMPONENTS ? 2

ENTER NAME OF COMPONENT 1 ? CARBON DIOXIDE

ENTER NAME OF COMPONENT 2 ? CIO

ENTER NUMBER OF MOLES OF CARBON DIOXIDE ? 95

ENTER NUMBER OF MOLES OF CIO ? 5

ENTER TCK) AND P(BAR ) ? 273*250

D-1059.534 KG/M**3 ETA = 2158. 5E-7 •A-< TC

ENTER TCK) AND PC BAR ) ? 0*0

ENTER NUMBER OF MOLES OF CARBON DIOXIDE ?

ENTER NUMBER OF COMPONENTS ?

.082 CP SECONDS EXECUTION TIME.

41

03563 W/M-K

15493 W/M-K

16524 W/M-K
APPENDIX B. LISTING OF COMPUTER PROGRAM TRAPP

42
C PROGRAM TRAPP( INPUT, OUTPUT)

Cc***********************************

c

C PURPOSE — DEMONSTRATION DRIVER FOR EXTENDED CORRESPONDING

C STATES ESTIMATION OF VISCOSITY AND THERMAL

C CONDUCTIVITY OF HYDROCARBON MIXTURES.

C

C VERSION G2.3 8/11/80

C

C CODED BY: J. F. ELY

C NATIONAL BUREAU OF STANDARDS

C

* NATIONAL ENGINEERING LABORATORY

C THERMOPHYSICAL PROPERTIES DIVISION

C BOULDER, COLORADO 80303

Cr***********************************

DIMENSION X(20), TA(2), TD(2), PD(2), DM(2), VM(2), TM(2)

INTEGER TUNIT(2) , PUNIT(2)

COMMON /COMPRP/ NC, ND, NAME(20,7), DPR0PS(20,14) , DINC(380)

COMMON /MIXDAT/ FX, DFXDT, F(20), HX, DHXDT, H(20), CMX, CMXV,

1 CMXT, ZCX, CORV, CORT

COMMON /LIBDAT/ NLIB, NDUM, PR0PS(22,61)

LOGICAL MIX

DATA TA, TD, PD, DM, VM, TM / O.ODO, 459.67D0, l.ODO, 1.8D0,

1 1.01325D0, 14.69595D0, l.ODO, 0.06242795D0 , l.ODO, 2.419D-4,

2 l.OD-3, 5.777675D-4 /

DATA TUNIT, PUNIT / "K", "F", "BAR", "PSIA" /

PRINT 260

PRINT 280

READ *, INOT

IF(INOT.EQ.O) GO TO 015

NC = NLIB / 2 PRINT 270

DO 010 K=1,NC

010 PRINT 290, (PR0PS(J,K),J = 1,9), (PROPS(J ,K+NC) ,J = 1,9)

PRINT 290, (PR0PS(J,NLIB),J=1,9)

C

C SEE IF ENGINEERING UNITS ARE DESIRED

015 IU = 1 PRINT 300

READ *, INOT

IF(INOT.EQ.O) GO TO 020

IU = 2 C

C INITIALIZE PROGRAM PARAMETERS

43
020 X(l) = 1.0

MIX = .FALSE.

C INPUT THE NUMBER OF COMPONENTS

C IF IT IS ZERO OR LESS, STOP.

PRINT 200

READ *, NC

IF (NC.LE.O) STOP

IF(NC.GT.l) MIX = .TRUE.

DO 040 K=1,NC

PRINT 210, K READ 230, (NAME(K,J) ,J=1,7)

CALL LIB(K)

040 CONTINUE

IF ( .NOT. MIX) GO TO 080

C

C IF A MIXTURE, GET THE COMPOSITION

050 XSUM =0.0

DO 060 K=1,NC

PRINT 220, (NAME(K,J),J = 1,4)

READ * X(K)

IF (X(K).LT.O.O) GO TO 020

XSUM = XSUM + X(K)

060 CONTINUE

DO 070 K=l, NC

X(K) = X(K) / XSUM

070 CONTINUE

C INPUT THE TEMPERATURE AND PRESSURE

C 080 PRINT 240, TUNIT(IU), PUNIT(IU)

READ *, TIN, PIN

IF (TIN. NE. 0.0 .AND. PIN. NE. 0.0) GO TO 100

090 IF(.NOT.MIX) GO TO 020

GO TO 050

C CONVERT TO K AND ATM FOR CALCULATIONS

C 100 TK = (TIN + TA(IU)) / TD(IU)

PATM = PIN / PD(IU)

CALL DCST(PATM,DX,TK,X)

ETAX = VM(IU) * VSCTY(DX,TK)

TCX = TM(IU) * THERMC(DX,TK,X)

DX = DX * CMX * DM(IU)

IF (IU.EQ.2) GO TO 110

PRINT 250, DX, ETAX, TCX

GO TO 080

110 PRINT 255, DX, ETAX, TCX

GO TO 080

C 200 FORMAT(/" ENTER NUMBER OF COMPONENTS :K")

210 FORMATC ENTER NAME OF COMPONENT", 13," :K")

220 FORMATC ENTER NUMBER OF MOLES OF " ,4A4," :K")

230 F0RMAT(7A4)

240 FORMAT(/" ENTER T(",A1,") AND P(",A4,") :K")

250 FORMATC D=",F8. 3," KG/M**3 ETA =" ,F9.1 ,"E-7 PA-S TC=",

44
1 F7.5," W/M-K")

255 FORMATC D=",F8.4," LB/FT**3 ETA =",F9.6," LB/FT-HR TC =",

1 F7.5," BTU/FT-HR-F")

260 F0RMAT(/6X,48(1H*)/6X,1H*,46X,1H*/6X,1H*,18X,"T R A",

1" P P",19X,1H*/6X,1H*,46X,1H*/6X, "* TRANSPORT P",

2"R0PERTIES PREDICTION PROGRAM *"/6X,lH*,46X,lH*/

36X,1H*,22X,"BY",22X,1H*/6X,1H*,46X,1H*/6X,1H*,8X,"J. F. ELY AND

4H. J. M. HANLEY",7X,1H*/6X,1H*,8X, "U.S. NATIONAL BUREAU OF STA

5NDARDS",5X,1H*/6X,1H*,8X, "NATIONAL ENGINEERING LABORATORY" ,7X,1H*

6/ 6X,1H*,8X,"THERM0PHYSICAL PROPERTIES DIVISION" ,4X,1H*/ 6X,1H*

7, 8X, "BOULDER, COLORADO 80303" ,14X,1H*/ 6X,1H*,46X ,1H*/

8 6X,1H*,5X,"(PARTIALLY SPONSORED BY THE OFFICE 0F",4X,1H*

9 / 6X,1H*,11X, "STANDARD REFERENCE DATA)", 11X.1H* /

A 6X,1H*,46X,1H*/ 6X,48(1H*) //)

270 FORMAT(/" COMPONENT NAME", 11X, "SYNONYM" ,7X, "COMPONENT NAME",

1 13X, "SYNONYM")

280 FORMATC DO YOU WANT A LIST OF LIBRARY C0MP0NENTS(0-N0;1-YES) :K")

290 FORMAT ( IX, 9A4,3X,9A4)

300 FORMAT(/" DO YOU WANT ENGINEERING UNITS(0-N0,1-YES) :K")

END

45
SUBROUTINE DCST(PX ,DX,TX,X)

C

r ***********************************

C

C PURPOSE --- THIS ROUTINE CALCULATES A HYDROCARBON MIXTURE

C DENSITY USING THE SHAPE FACTOR APPROACH TO

C CORRESPONDING STATES.

C

C CODED BY : J. F. ELY

C NATIONAL BUREAU OF STANDARDS

C NATIONAL ENGINEERING LABORATORY

C THERMOPHYSICAL PROPERTIES DIVISION

C BOULDER, COLORADO 80303

CC VERSION G2.1 - - 1/15/80

Q

***********************************

c COMMON /REFDAT/ R, PCO, DCO, TCO, ZCO, WO, CMWO, GAMMA, A(32),

* CT(4), CPU), COO), CD(4), CE(8), C0T(9),

* CDTU), CET(8)

COMMON /COMPRP/ NC, ND, NAME(20,7), PC(20), DC(20), TC(20),

* ZC(20), W(20), CMW(20), TB(20), CPC(20,7),

* 0MK(190), 0ML(190)

COMMON /MIXDAT/ FX, DFXDT, F(20), HX, DHXDT, H(20), CMX, CMXV,

1 CMXT, ZCX, CORV, CORT

DIMENSION X(l)

LOGICAL MASK(20)

C DATA TOLERS / l.OE-5 /

THETAF(TR,VR,WN) = 1. + (WN - WO) * (CT(1) + CT(2) * ALOG(TR)

* + (CT(3) + CT(4) / TR) * (VR - 0.5))

PHIF(TR,VR,WN) = (1.0 + (WN - WO) * (CP(1) * (VR + CP(2))

* + CP(3) * (VR + CPU)) * ALOG(TR)))

C

C INITIALIZE THE SHAPE FACTORS AND CST PARAMETERS

C 020 FX = 1.0

HX = 1.0

DO 040 N = 1, NC

MASK(N) = .FALSE.

IF(X(N).LE.O.O) MASK(N) = .TRUE.

F(N) = TC(N) / TCO

H(N) = DCO / DC(N)

040 CONTINUE

C SHAPE FACTOR ITERATION LOOP

DO 200 LOOP = 1, 15

C SAVE RESULTS FROM PREVIOUS ITERATION

FXS = FX

HXS = HX

HX = 0.0

FX = 0.0

C

C CALCULATE CST PARAMETERS FOR MIXTURE

46
DO 100 N = 1, NC

IF(MASK(N)) GO TO 100

K = N * (N - 1) / 2 GN = CBRT(H(N))

52 = 0.0

53 = 0.0

DO 080 M = 1, N IF(MASK(M)) GO TO 080

TMP2 = 0.125 * X(M) * (GN + CBRT(H(M) ) )**3 * OML(K+M)

TMP3 = SQRT(F(N) * F(M)) * TMP2 * OMK(K + M)

52 = S2 + TMP2

53 = S3 + TMP3

080 CONTINUE

HX = HX + X(N) * (2.0 * S2 - TMP2)

FX = FX + X(N) * (2.0 * S3 - TMP3)

100 CONTINUE

FX = FX / HX

C CALCULATE THE EQUIVALENT METHANE DENSITY.

TO = TX / FX

PO = PX * HX / FX

DO = RHOF(PO,TO)

C RECALCULATE SHAPE FACTORS AND CHECK FOR

C CONVERGENCE IN FX AND HX

140 DO 160 N = 1, NC

IF(MASK(N)) GO TO 160

TR = AMIN1(2.0,F(N) * TO / TC(N))

VR = AMIN1(2.0,AMAX1(0.5,H(N)*DC(N)/D0))

WN = W(N)

F(N) = TC(N) * THETAF(TR,VR,WN) / TCO

H(N) = DCO * PHIF(TR,VR,WN) * ZCO / (ZC(N) * DC(N))

160 CONTINUE

C TEST FOR CONVERGENCE

C IF(ABS(FX / FXS - 1.0) .GT.TOLERS) GO TO 200

IF(ABS(HX / HXS - 1.0) .GT.TOLERS) GO TO 200

GO TO 220

C NO CONVERGENCE YET - - TRY AGAIN

200 CONTINUE

C FAILURE—ISSUE MESSAGE & RETURN

C 210 PRINT 300, TX, PX

C

C CONVERGENCE!!!

220 DX = DO / HX

CALL ECSTX(PX,DX,TX,X)

RETURN

300 FORMAT(/" /DCST/ FAILED TO CONVERGE AT T=",F8.3," AND P=",G14.7)

END

47
SUBROUTINE ECSTX(PX „DX,TX,X)

C

c

C PURPOSE — THIS ROUTINE EVALUATES VARIOUS SUMS WHICH ARE USED

C TO EVALUATE THE DERIVATIVES OF FX AND HX W.R.T.

C T. IT ASSUMES THAT ECSTD HAS BEEN CALLED TO EVALUATE

C DENSITY, FX AND HX.

C

C CODED BY: J. F. ELY

C NATIONAL BUREAU OF STANDARDS

C NATIONAL ENGINEERING LABORATORY

C THERMOPHYSICAL PROPERTIES DIVISION

C BOULDER, COLORADO 80303

CC VERSION G2.0 — 5/20/80

CQ**********************************

c REAL MIJ

COMMON /REFDAT/ R, PCO, DCO, TCO, ZCO, WO, CMWO, GAMMA, A(32),

* CT(4), CPU), COO), CD(4), CEO), COTO),

* CDT(4), CET(8)

COMMON /COMPRP/ NC, ND, NAME(20,7), PC(20), DC(20), TC(20),

* ZC(20), WOO), CMWOO), TBOO), CPC(20,7),

* 0MK(190), 0MLU90)

COMMON /MIXDAT/ FX, DFXDT, F(20), HX, DHXDT, H(20), CMX, CMXV,

1 CMXT, ZCX, CORV, CORT

DIMENSION SO,3), SJ(5), Z(5), X(l)

EQUIVALENCE (Z(1),FIJ), (Z(2),GIJ), (Z(3),MIJ)

DATA Z / 5*0.0 / C

C

C INITIALIZE

ZCX = 0.0

CMX = 0.0

CMXV = 0.0

CMXT =0.0

RBAR = 0.0

DCMAX =0.0

DO 015 I = 1, NC

IF(DC(I).GT. DCMAX) DCMAX = DC(I)

015 CONTINUE

DO 020 M=l,3

DO 020 N=l,5

020 S(N,M) = 0.0

C DO 120 I = 1,NC

IF (X(I).LE.O.O) GO TO 120

K = I * (1-1) / 2 GI = CBRT(H(I))

DO 040 M = 1, 5 040 SJ(M) = 0.0

DO 080 J = 1, NC

48
IF (X(J).LE.O.O) GO TO 080

L = K + J IF (J.GT.I) L = I + J * (J-l) / 2 GIJ = 0.5 * (GI+CBRT(H(J)))

HIJ = GIJ**3 * OML(L)

FIJ = SQRT(F(I)*F(J)) * OMK(L)

RMIJ = CMW(I)*CMW(J)/(CMW(I)+CMW(J))

Z(4) = 1.0 / RMIJ

MIJ = CBRT(HIJ) * SQRT(RMIJ/FIJ)

GIJ = GIJ / GI

TERM = X(J) * HIJ / GIJ

DO 060 M = 1, 5 SJ(M) = SJ(M) + TERM

060 TERM = TERM * Z(M)

080 CONTINUE

THETA = F(I) * TCO / TC(I)

PHI = H(I) * DC(I) / DCO

TR = AMIN1(2.0,F(I) * TX / (FX * TC(I)))

VR = AMIN1(2.0,AMAX1(0.5,H(I)*DC(I)/(HX*DX)))

TEMP = (W(I) - WO) / THETA

Z(l) = 1.0 - TEMP * (CT(2) - CT(4) * (VR-0.5) / TR)

1(2) = TEMP * (CT(3) + CT(4) / TR) * VR

TEMP = (W(I)-WO) * ZCO / (PHI * ZC ( I )

Z(3) = 1.0 - TEMP * (CP(l) + CP(3) * ALOG(TR)) * VR

Z(4) = TEMP * CP(3) * (VR + CP(4))

IF(TR.LT.2.0) GO TO 085

Z(l) = 1.0

Z(4) = 0.0

085 IF (VR.GT.0.5 .AND. VR.LT.2.0) GO TO 090

Z(2) = 0.0

Z(3) = 1.0

090 Z(5) = Z(l) * Z(3) - Z(2) * Z(4)

TERM = HX

DO 100 M = 1, 3 SJ(M) = X(I) * SJ(M) / (Z(5) * TERM)

TERM = FX * HX

DO 100 N = 1, 5 100 S(N,M) = S(N,M) + Z(N) * SJ(M)

CMX = CMX + X(I) * CMW(I)

CMXV = CMXV + X(I) * SJ(4)

CMXT = CMXT + X(I) * SJ(5)

ZCX = ZCX + X(I) * ZC(I)

RBAR = RBAR + X(I) * CBRT(DCMAX/DC( I)

120 CONTINUE

TERM = 1.0 + S(l,l) - S(5,l)

TEMP = S(3,3) + S(4,2)

TRM2 = 1.0 + S(2,3) + S(l,2) - S(5,2)

DFXDT = 1.0 - TERM / (TERM * TEMP - S(4,l) * TRM2)

DHXDT = S(4,l) * (1.0 - DFXDT) / TERM

TERM = FX * HX**(8. 0/3.0)

CMXV = 2.0 * CMXV * CMXV / TERM

CMXT = 2.0 * TERM / (CMXT * CMXT)

DFXDT = FX * DFXDT / TX

DHXDT = HX * DHXDT / TX

49
RBAR = 1.0/RBAR /

CORV = (0. 161290-4. 516129*RBAR)/(1. 0-5. 354839*RBAR)

RETURN

END

50
FUNCTION RHOF(P,T)

C

c

C PURPOSE --- THIS ROUTINE CALCULATES THE DENSITY IN MOL/L OF A

C FLUID FROM AN EQUATION OF STATE GIVEN THE TEMPERATURE

C T IN KELVIN AND THE PRESSURE P IN ATMOSPHERES.

CC CODED BY : J. F. ELY

C NATIONAL BUREAU OF STANDARDS

C NATIONAL ENGINEERING LABORATORY

C THERMOPHYSICAL PROPERTIES DIVISION

C BOULDER, COLORADO 80303

C

C VERSION G2.2 — 1/9/80

CQ***********************************

c COMMON /REFDAT/ R, PCO, DCO , TCO, ZCO, WO, CMWO, GAMMA, A(32),

* CT(4), CPU), C0(9), CDU), CE(8), C0T(9),

* CDTU), CET(8)

DIMENSION AP(4), BP(3)

DATA AP / 6.3240720088E+00,-6.7447661253E+00,-2.5239605832E+00,

* 0.4188447111E+00/

DATA BP / 1.5213153011E+01, 9 .2665399400E+00, 1 .3551718205E+01/

C

C

C FIND THE INITIAL DENSITY GUESS. FIRST SEE

C IF THE SYSTEM IS SOLIDLY IN A ONE PHASE REGION

C PS = PCO

FOP = P / (R * T) IF (T.GT.TCO) GO TO 080

CC SUB-CRITICAL TEMPERATURE.

C CALCULATE THE VAPOR PRESSURE. IF T > 170 K,

C USE THE CRITICAL REGION FUNCTION. OTHERWISE

C THE FROST-KALKWARF TYPE EQUATION.

C

TR = T / TCO

TAU = 1.0 - TR

IF (T.GT. 170.0) GO TO 040

TMP1 = AP(1) + AP(2) / TR + AP(3)*AL0G(TR)

TMP2 = AP(4)/(TR*TR)

PRR = 0.100

DO 020 K = 1, 50

PR = EXP(TMP1 + TMP2 * PRR)

IF (ABS(PR/PRR-1.0).LE.1.0E-6) GO TO 060

020 PRR = PR

C 040 PR = EXP(BP(1)*(1.0-1.0/TR) + BP(2)*TAU + BP(3)*TAU*TAU)

51
060 PS = PR * PCO

C tF P % PS, USE A LIQUID DENSITY. OTHERWISE, USE

C IDEAL GAS DENSITY CALCULATED ABOVE.

C 080 IF (P.GT.PS) FOP = 3.0 * DCO

100 RHOF = DO(P,T,FOP)

RETURN

END

52
FUNCTION DO (PO, TO, FOP)

LOGICAL LIQUID

C

cC PURPOSE -- THIS ROUTINE CALCULATES THE DENSITY OF A FLUID AT

C T AND P GIVEN AN INITIAL GUESS IN FOP. ON EXIT,

C IT RETURNS THE FUGACITY COEFFICIENT IN FOP. IT

C REQUIRES A ROUTINE "PVTO" WHICH CALCULATES P,

C DPDD, AND F/P, GIVEN T AND D.

CC CODED BY : J. F. ELY

C NATIONAL BUREAU OF STANDARDS

C NATIONAL ENGINEERING LABORATORY

C THERMOPHYSICAL PROPERTIES DIVISION

C BOULDER, COLORADO 80303

CC VERSION G2.2 — 1/9/80

C

COMMON /REFDAT/ R, PCO, DCO, TCO, ZCO, WO, CMWO, GAMMA, A(32),

*. CT(4), CP(4), C0(9), CD(4), CE(8), C0T(9),

* CDTU), CET(8)

DATA TOLERD, TOLERP / 1.0E-8, 1.0E-8/

CC INITIALIZE PARAMETERS

D1=F0P

NTRY=0

DMAX=3.2E0*DC0

C ESTABLISH BOUNDS AND START NEWTON RAPHSON

020 DLO=0.0

DHI=DMAX

D=D1

DO 100 LAP=1,20

CALL PVTO(PX,D,TO,DPDD,FOP)

C

C IF DPDD IS ZERO OR NEGATIVE, TRY BISECTION

C IF(DPDD.LE.1.0E-2) GO TO 120

DP=PO-PX

DD=DP/DPDD

C SAVE DENSITY FOR POSSIBLE BISECTION

C IF (DP) 040,300,060

040 DHI=D

GO TO 080

060 DLO=D

080 DN=D+DD

C KEEP D WITHIN BOUNDS OR GO TO BISECTION

C IF (DN.LT.0.0 .OR. DN.GT.DMAX) GO TO 120

D=DN

IF(LAP.EQ.l) GO TO 100

IF(A8S(DP/P0).LE. TOLERP) GO TO 300

53
\ IF(ABS(DD/D).LE.TOLERD) GO TO 300

100 CONTINUE /

C NEWTON-RAPHSON FAILURE. TRY BISECTION

120 NTRY=NTRY+1

IF(NTRY.LT.3) GO TO 130

PRINT 400, TO, PO

400 FORMATC'/DO/ FAILED TO CONVERGE AT T0=" ,F8.3," AND P0=",G14.7)

STOP

130 IF(TO.GT.TCO) GO TO 160

C SUB-CRITICAL. MAKE SURE THAT WE HAVE THE

C PROPER BOUNDS ON THE DENSITY.

C IF(Dl.LT.DCO) GO TO 140

LIQUID=.TRUE.

IF(DLO.LE.DCO) DLO=DCO

IF(DHI.LE.DCO) DHI=DMAX

GO TO 160

C 140 LIQUID=. FALSE.

IF(DLO.GE.DCO) DLO=0.0

IF(DHI.GE.DCO) DHI=DCO

C

C START THE BISECTION

160 D=0.50E0*(DL0+DHI)

CALL PVTO(PX,D,TO,DPDD,FOP)

DP=PX-PO

IF(DPDD.LT.O.O) GO TO 180

IF(DP) 200,300,220

180 IF(. NOT. LIQUID) DPDD=-DPDD

IF(DPDD) 200,240,220

200 DLO=D

GO TO 240

220 DHI=D

240 IF(ABS(DPDD).LE.TOLERP .AND. ABS(DP) .GT.TOLERP) GO TO 260

IF(ABS(DP/PO) .LE. TOLERP) GO TO 300

IF(ABS(DL0/DHI-1.0).GT.T0LERD) GO TO 160

C

C BISECTION FAILED. WE ARE PROBABLY TRYING ON

C THE WRONG SIDE OF THE DOME.

260 D1=3.0*DC0

IF(LIQUID) Dl=0.01

GO TO 020

C CONVERGENCE ! ! ! 300 DO=D

RETURN

END

54
SUBROUTINE PVTO(PO,DO,TO ,DPDDO,FOPO)

***********************************

PURPOSE — THIS ROUTINE CALCULATES THE EQUIVALENT PRESSURE AND

DERIVATIVE OF PRESSURE WRT DENSITY OF METHANE. THE

EQUATION USED IS THAT OF STEWART AND JACOBSEN. THE

DENSITY IS IN G-MOL/LIT AND TEMPERATURE IN KELVIN. IT YIELDS THE PRESSURE IN ATMOSPHERES AND RATIO OF THE

FUGACITY TO THE PRESSURE.

CODED BY : J. F. ELY

NATIONAL BUREAU OF STANDARDS

NATIONAL ENGINEERING LABORATORY

THERMOPHYSICAL PROPERTIES DIVISION

BOULDER, COLORADO 80303

VERSION G2.1 1/15/80

**********************************

DIMENSION G(15), B(9), F(6), S(6)

COMMON /REFDAT/ R, PCO, DCO, TCO, ZCO, WO, CMWO, GAMMA, A(32),

* CT(4), CPU), C0(9), CD(4), CE(8), C0T(9),

* CDTU), CET(8)

DATA TLAST, B/ -1.00, 9*0.0/

DATA F / 1.0, 1.0, 2.0, 6.0, 24.0, 120.0 /

T=TO

D=DO

IF(T.EQ. TLAST) GO TO 040

TLAST=T

TS=SQRT(T)

Tl=1.0/T

T2=T1*T1

G(l) = G(2) = G(3)

G(4) = G(5) = G(6) = G(7) = G(8) = G(9) = G(10)

G(ll)

G(12)

G(13)

R*T

A(l)

A(6)

A(10

A(13

A(14

A(16

A(17

A(19

=T2*

=T2*

=T2*

=T2*

*T+A(2)*TS+A(3)+A(4)*T1+A(5)*T2

*T+A(7)+A(8)*T1+A(9)*T2

)*T+A(11)+A(12)*T1

))*T1+A(15)*T2

)*T1

)*T1+A(18)*T2

)*T2

(A(20)+A(21)*T1)

(A(22)+A(23)*T2)

(A(24)+A(25)*T1)

(A(26)+A(27)*T2)

55
G(14)=T2*(A(28)+A(29/)*T1)

G(15)=T2*(A(30)+T1*(A(31)+T1*A(32)))

C DO 010 J=2,9

010 B(J)=G(J)/(G(1)*FL0AT(J-D)

DO 030 K=l,6

S(K)=0.0

TERM=1.0

DO 020 J=K,6

S(K)=S(K)+F(J)*G(J+9)*TERM

020 TERM=TERM/GAMMA

030 S(K)=S(K)/(G(1)*F(K))

C 040 P1=0.0

D1=0.0

F1=0.0

DO 050 J=l,9

P1=P1*D+G(10-J)

D1=D1*D+P1

050 F1=F1*D+B(10-J)

C DSQ=D*D

P2=0.0

D2=0.0

F2=0.0

DO 060 J=10,15

P2=(P2+G(25-J))*DSQ

D2=D2*DSQ+P2

060 F2=F2*DSQ+S(16-J)

TERM=EXP(-GAMMA*DSQ)

P0=D*(P1+P2*TERM)

IF (PO.EQ.0.0) PO = 1.0E-20

ZO=PO/(D*G(D)

DPDD0=(D1+TERM*(P2+2.0*(D2-DSQ*GAMMA*P2)))

F0P=F1-(F2*TERM-S(1))/(2.0*GAMMA)+Z0-1.0-AL0G(Z0/P0)

FOPO=EXP(FOP)/PO

RETURN

END

56
FUNCTION VSCTY(DX,TX)

***********************************

PURPOSE - - THIS ROUTINE CALCULATES THE VISCOSITY OF METHANE

USING HANLEV'S CORRELATION

CODED BY : J. F. ELY

NATIONAL BUREAU OF STANDARDS

NATIONAL ENGINEERING LABORATORY

THERMOPHYSICAL PROPERTIES DIVISION

BOULDER, COLORADO 80303

VERSION G2.0 3/12/80

***********************************

COMMON /MIXDAT/ FX, DFXDT, F(20), HX, DHXDT, H(20), CMX, CMXV,

1 CMXT, ZCX, CORV, CORT

COMMON /REFDAT/ R, PCO, DCO, TCO, ZCO, WO, CMWO, GAMMA, A(32),

* CT(4), CP(4), COO), CD(4), CE(8), C0T(9),

* CDT(4), CET(8)

DATA TLAST, PSI / -1.00, 1.5 /

CALCULATE THE EQUIVALENT DENSITY

DO = 0.001 * DX * HX * CMWO

TO = TX / FX

CALCULATE THE TEMPERATURE DEPENDENT PART OF THE

VISCOSITY CORRELATION IF T ISN"T THE SAME AS

THE LAST CALL TO THIS ROUTINE (USUAL CASE)

IF(TO.EQ. TLAST) GO TO 040

TLAST = TO

TI = 1.0 / TO

ETA1 = CD(1) + CD(2) * (CD(3) - ALOG(TO / CD(4))) ** 2 TRMO = CE(1) + CE(2) * TI TRM1 = CEO) + CE(4) * TI / SQRT(TO)

TRM2 = CEO) + TI * (CEO) + CE(7) * TI)

TRMX = EXP (TRMO)

TI = CBRT(TO)

ETAO = 0.0

DO 020 J = 1,9

ETAO = ETAO + COO) * TI

020 TI = TI * TI DENSITY DEPENDENCE IS CALCULATED HERE.

040 Rl = DO ** 0.10

R2 = SQRT(DO) * (DO / CEO) - 1.0)

ETAX = EXP (TRMO + TRM1 * Rl + TRM2 * R2) - TRMX

FETA = SQRT(FX * CMXV / CMWO) / CBRT(HX * HX)

CORV = SQRT((1.0 - T0*PSI*AMIN1(0.0,DFXDT))*ZCX/ZC0)*C0RV

VSCTY = (ETAO + ETA1 * DO + ETAX * CORV) * FETA

RETURN

END

57
FUNCTION TCOND(DX,TX)

Q***********************************

C PURPOSE - - THIS ROUTINE CALCULATES THE TRANSLATIONAL PORTION

C OF THE METHANE THERMAL CONDUCTIVITY USING HANLEY"S

C CORRELATIONS

C

C CODED BY : J. F. ELY

C NATIONAL BUREAU OF STANDARDS

C NATIONAL ENGINEERING LABORATORY

C THERMOPHYSICAL PROPERTIES DIVISION

C BOULDER, COLORADO 80303

C

C VERSION G2.1 7/12/80

CC***********************************

c REAL LAMO, LAM1 , LAMX

C COMMON /MIXDAT/ FX, DFXDT, F(20), HX, DHXDT, H(20), CMX, CMXV,

1 CMXT, ZCX, CORV, CORT

C COMMON /REFDAT/ R, PCO, DCO, TCO, ZCO, WO, CMWO, GAMMA, A(32),

* CT(4), CPU), C0(9), CD(4), CE(8), C0T(9),

* CDT(4), CET(8)

C DATA TLAST, CON, PSI / -1.00, 0.19434504, 1.00 /

C

C CALCULATE THE EQUIVALENT DENSITY

DO = 0.001 * DX * HX * CMWO

TO = TX / FX

C CALCULATE THE TEMPERATURE DEPENDENT PART OF THE

C THERMAL CONDUCTIVITY CORRELATION IF T ISN"T THE

C SAME AS THE LAST CALL TO THIS ROUTINE (USUAL

C CASE)

C

IF( TO. EQ. TLAST) GO TO 040

TLAST = TO

TI = 1.0 / TO

LAM1 = CDT(l) + CDT(2) * (CDT(3) - ALOG(TO / CDT(4))) ** 2 TRMO = CET(l) + CET(2) * TI TRM1 = CET(3) + CET(4) * TI / SQRT(TO)

TRM2 = CET(5) + TI * (CET(6) + CET(7) * TI)

TRMX = EXP (TRMO)

TI = CBRT(TO)

C CALCULATE THE IDEAL GAS TRANSLATIONAL THERMAL

C CONDUCTIVITY FROM THE EUCKEN FORMULA

C K = 15 * R * ETAO / (4 * M)

LAMO = 0.0

DO 020 J = 1,9

LAMO = LAMO + CO(J) * TI 020 TI = TI * TI

LAMO = CON * LAMO

C DENSITY DEPENDENCE IS CALCULATED HERE.

58
040 Rl = DO ** 0.10

R2 = SQRT(DO) * (DO / CET(8) - 1.0)

LAMX = EXP(TRMO + TRM1 * Rl + TRM2 * R2) - TRMX

FLAM = SQRT(FX * CMWO / CMXT) / CBRT(HX * HX)

CORT = ((1.0 - TO * AMIN1(0.0,PSI*DFXDT)) * ZCO / ZCX) ** 1.5

TCOND = (LAMO + LAM1 * DO + LAMX) * FLAM * CORT

RETURN

END

59
FUNCTION THERMC(DX,TX,X)

C {

c

C PURPOSE —- THIS ROUTINE CALCULATES THE THERMAL CONDUCTIVITY OF

C A MIXTURE FROM THE EXTENDED CORRESPONDING STATES

C MODEL

C

C CODED BY : J. F. ELY

C NATIONAL BUREAU OF STANDARDS

C NATIONAL ENGINEERING LABORATORY

C THERMOPHYSICAL PROPERTIES DIVISION

C BOULDER, COLORADO 80303

CC VERSION G2.1 1/21/81

CQ***********************************

c COMMON /COMPRP/ NC, ND, NAME(20,7), PC (20), DC (20), TC(20),

* ZC(20), W(20), CMW(20), TB(20), CPC(20,7),

* 0MK(190), 0MLU90)

C COMMON /MIXDAT/ FX, DFXDT, F(20), HX, DHXDT, H(20), CMX, CMXV,

1 CMXT, ZCX, CORV, CORT

C DIMENSION TCINT(20), X(20)

C FINT = 1.32 * 4.184 / 10.0

C CALCULATE THE TRANSLATIONAL THERMAL

C CONDUCTIVITY OF THE MIXTURE

TCTMIX = TCOND(DX,TX)

C SAVE THE CST RESULTS

C FXS = FX

HXS = HX

CMS = CMXV

C CALCULCATE THE INTERNAL CONTRIBUTION

TCIMIX = 0.0

DO 100 J = 1, NC

FX=F(J)

HX=H(J)

CMXV=CMW(J)

CPO = CPC(J,1)

TRM = TX

DO 040 K = 2, 7 CPO = CPO + TRM * CPC(J,K)

040 TRM = TRM * TX

TCINT(J) = FINT * (CPO - 4.968) * VSCTY(O.O.TX) / CMW(J)

100 CONTINUE

DO 120 1=1, NC

TRM = 0.0

DO 110 J=1,I

TIJ = X(J) * TCINT(J) / (TCINT(I)+TCINT(J))

TRM = TRM + TIJ

60
110 CONTINUE

TCIMIX = TCIMIX + X(I) * TCINT(I) * (2.0 * TRM - TIJ)

120 CONTINUE

FX = FXS

HX = HXS

CMXV = CMS

THERMC = TCTMIX + 2.0 * TCIMIX

RETURN

END

61
FUNCTION CBRT(X) r***********************************

C

C PURPOSE --- THIS ROUTINE CALCULATES THE CUBE ROOT OF A NUMBER

CQ***********************************

SIGN = 1.0

IF (X.LT.O.O) SIGN = -1.0

CBRT = SIGN * ABS(X)**(1. 0/3.0)

RETURN

END

62
SUBROUTINE LIB(N)

c PURPOSE — THIS ROUTINE TAKES THE COMPONENT NUMBER "N"

WHOSE NAME RESIDES IN NOM(N,l-7) AND COMPARES

IT WITH NAMES IN THE DATABASE CONTAINED IN /LIBDAT/

IF A MATCH IS OBTAINED, THE APPROPRIATE LOCATIONS

OF THE COMMON BLOCK /COMPRP/ ARE LOADED WITH THE

DATA FROM THE CORRESPONDING COMPONENT IN /LIBDAT/

CODED BY

C

C

C

C

C

C

C

C

C

C

c

c

cc

c

c REAL NOM, CPROPS

C

C

c

cc

c

VERSION G2.1

J. F. ELY

NATIONAL BUREAU OF STANDARDS

NATIONAL ENGINEERING LABORATORY

THERMOPHYSICAL PROPERTIES DIVISION

BOULDER, COLORADO 80303

- 8/15/80

COMMON /COMPRP/ NC, ND, N0M(20,7), P(20,14), 0MK(190), 0ML(190)

COMMON /LIBDAT/ NLIB, NDUM, CPR0PS(22,61)

READ THROUGH THE LIBRARY TO IDENTIFY

THE COMPONENT BY NAME OR SYNONYM.

DO 040 L = 1, NLIB

IF ( N0M(N,1).EQ.CPR0PS(8,L) .AND. N0M(N,2) .EQ.CPR0PS(9,L) ) * GO TO 030

DO 020 K = 1, 7 IF (NOM(N,K).NE.CPROPS(K,L)) GO TO 040

020 CONTINUE

030 K = L GO TO 120

040 CONTINUE

PRINT 200

STOP

COMPONENT COULDN'T BE IDENTIFIED.

N0M(N,K),K=1,7)

COPY DATA FROM LIBRARY TO WORKING

COMMON AREA AND CALCULATE ZC

120 L = 9

DO 130 M = 1, 14

IF(M.EQ.4) GO TO 130

L = L + 1 P(N,M) = CPROPS(L,K)

130 CONTINUE

P(N,2) = 1000.0 / P(N,2)

P(N,4) = P(N,1)/(0.08205616*P(N,2)*P(N,3))

63

m
C DUMMY IN THE INTERACTION CONSTANTS

C DO 140 L=1,N

I=L*(L-l)/2

DO 140 J=1,L

K=I+J

0MK(K)=1.0

0ML(K)=1.0

140 CONTINUE

RETURN

C 200 FORMAT(/" /LIB/ FAILED TO IDENTIFY THE COMPONENT ",7A4)

END

64
BLOCK DATA LIBSET

***********************************

PURPOSE — THIS ROUTINES LOADS VARIOUS COMMON BLOCKS WITH

DATA WHICH DOES NOT CHANGE DURING THE CALCULATIONS

THE ORDER OF THE LIBRARY DATA IS AS FOLLOWS:

XPRPXX(K)

1-7

8-9

10

11

12

13

14

15

16-22

QUANTITY

COMPONENT NAME

SYNONYM

PC (ATM)

VC (CM**3/M0L)

TC (KELVIN)

ACENTRIC FACTOR

MOLECULAR WEIGHT

T(NBP) (KELVIN)

IDEAL HEAT CAPACITY COEFFICIENTS

WHERE CP0=SUM(C(J)*T**(J-1)) J=l,7

CODED BY : J. F. ELY

NATIONAL BUREAU OF STANDARDS

NATIONAL ENGINEERING LABORATORY

THERMOPHYSICAL PROPERTIES DIVISION

BOULDER, COLORADO 80303

VERSION G2.1 - - 8/12/80

************************************

COMMON /REFDAT/ R, PCO, DCO, TCO, ZCO, WO, CMWO, GAMMA, A(32),

* CT(4), CPU), C0(9), CD(4), CE(8), C0T(9),

* CDTU), CET(8)

COMMON /LIBDAT/

1 XPRP04(22)

1 XPRP09(22)

2 XPRP14(22)

3 XPRP19(22)

4 XPRP24(22)

5 XPRP29(22)

6 XPRP34(22)

7 XPRP39(22)

8 XPRP44(22)

9 XPRP49(22)

A XPRP54(22)

B XPRP59(22)

NLIB, NDUM

XPRP05(22)

XPRP10(22)

XPRP15(22)

XPRP20(22)

XPRP25(22)

XPRP30(22)

XPRP35(22)

XPRP40(22)

XPRP45(22)

XPRP50(22)

XPRP55(22)

XPRP60(22)

XPRP0K22)

XPRP06(22)

XPRP1K22)

XPRP16(22)

XPRP2K22)

XPRP26(22)

XPRP3K22)

XPRP36(22)

XPRP4K22)

XPRP46(22)

XPRP5K22)

XPRP56(22)

XPRP6K22)

XPRP02(22)

XPRP07(22)

XPRP12(22)

XPRP17(22)

XPRP22(22)

XPRP27(22)

XPRP32(22)

XPRP37(22)

XPRP42(22)

XPRP47(22)

XPRP52(22)

XPRP57(22)

REFERENCE FLUID FIXED POINT DATA

AND EQUATION OF STATE CONSTANTS

XPRP03(22)

XPRP08(22)

XPRP13(22)

XPRP18(22)

XPRP23(22)

XPRP28(22)

XPRP33(22)

XPRP38(22)

XPRP43(22)

XPRP48(22)

XPRP53(22)

XPRP58(22)

65
DATA R, TCO, PCO, DCO, ZCO, WO, CMWO/ 0.08205616, 190.555

1 45.387, 10.23, 0.283742, 0.01131, 16.043 /

DATA GAMMA / 0.0096 /

DATA A/-1.184347314485E-02,

6.260681393432E+02,-

-2.875764479978E-01,

-2.064957753744E-05,

3.060813353408E-04,

-3.074944210271E-04,

1.610140169312E-04,

1.790105676252E+02,

1.820173769533E+01,

-5.290335668451E-06,

-2.598235689063E-06,

7.540377272657E-01,-

3.490654409121E+04,

5.011947936427E+01,-

1.285951844828E-02,-

•3.174982181302E-03,

1.071143181503E-05,-

3.469830970789E+04,-

1.615880743238E+06,

1.449888505811E-03,-

1.694350244152E-03,

3.153374374912E-05/

1.225769717554E+01

5.301046385532E-04

2.821562800903E+04

1.106266656726E+00

5.191608004779E+00

9.290851745353E-03

1.370878559048E+06

6.265306650288E-01

3.159999123798E+01

8.612049038886E-09

SHAPE FACTOR CORRELATION CONSTANTS

DATA CT / 0.090569,-0.862762, 0.316636,-0.46568 /

DATA CP / 0.394901,-1.023545,-0.932813,-0.754639 /

VISCOSITY CORRELATION CONSTANTS

DATA CO / 0.2907741307E+07,-0.3312874033E+07, 0.1608101838E+07,

1 -0.4331904871E+06, 0.7062481330E+05,-0.7116620750E+04,

2 0.4325174400E+03,-0.1445911210E+02, 0.2037119479E+00/

DATA CD / 1.6969859271E+00,-1.3337234608E-01, 1 .4000000000E+00,

1 1.6800000000E+02/

DATA CE /-1.0239160427E+01,

1 -2.8476328289E+03

2 5.0020669720E+03.

1 .7422822961E+02 , 1 .7460545674E+01

,

1.3368502192E-01, 1.4207239767E+02,

1.62800000000E-01/

THERMAL CONDUCTIVITY CORRELATION

CONSTANTS

DATA C0T/-0.214762100E+06, 0.219046100E+06,-0.861809700E+05,

1 . 149609900E+05 ,-0 .473066000E+03,-0 .233117800E+03

,

2 0.377843900E+02,-0.232048100E+01, 0.531176400E-01/

DATA CDT/-0.252762920E+00, 0.334328590E+00, 1 .120000000E+00,

1 0.168000000E+03/

DATA CET/-7.1977082270E+00,

1 -9.8462522975E+02

2 -8.7288332851E+02

8 .5678222640E+01 , 1 .2471834689E+01

3.5946850007E-01 , 6.9798412538E+01

0.1628000000E+00/

LIBRARY COMPONENT DATA

DATA NLIB / 61 /

66
DATA XPRP01

i

ii ii n H

2 190.555E0

3 .76692963E+01

4 -.19759199E-10

DATA XPRP02

i H ii n ii

2 305.330E0

3 .77063866E+01

4 .13183583E-10

DATA XPRP03

i n ii n ii

2 369.820E0

3 .54902525E+01

4 -.71806497E-11

DATA XPRP04

i

ii n ii ii

2 408.150E0

3 .83448658E+01

4 .57571458E-09

DATA XPRP05

i

ii ii ii ii

2 425.160E0

3 .86549559E+01

4 -.35770071E-11

DATA XPRP06

i

ii H H ii

2 433.780E0

3 .51988869E+01

4 .49657490E-11

1 DATA XPRP07

ii H ii ii

2 460.430E0

3 .61029072E+01

4 .17894175E-10

DATA XPRP08

i n H H ii

2 469.750E0

3 .10821614E+02

4 .20500044E-09

DATA XPRP09

i H ii H H

2 488.780E0

3 .52148046E+01

4 -.34860062E-11

/ "METH"

"CI ", " " .011314E0

.33677582E-14

-.12233376E-21

/ "ETHA"

II PO II ii ' .'10038E0

•44587991E-05

.21689626E-13

/ "PROP"

"C3 ", " .15418E0

.40763758E-01

.42920084E-18

/ "ISOB"

II T f

A II II II !l8300E0

.40337532E-02

-.27078809E-12

/ "N-BU"

np/i > H ii .'20038E0

.34204803E-01

.46492802E-13

/ "2,2-"

"22DM", "PR

" .19700E0

.68223744E-01

.61782974E-13

/ "I SOP"

"IC5 \

" .22700E0

.78716077E-01

-.30123834E-13

/ "N-PE"

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.20021084E-14

"OGEN", " 33.457E0,

28.010E0,

.58071192E-06,

-.23281314E-26/

II rU H II II tN , , 49.771E0,

32.000E0,

.24461570E-05,

.12183202E-19/

ii p H ii ii 217.617E0!

18.020E0,

.38989103E-05,

.44003939E-20/

"ON M", "ONOX",

34.532E0,

28.010E0,

.72321240E-06,

-.25343692E-20/

"ON D", "IOXI",

72.860E0,

44.010E0,

-.99279448E-05,

-.45337256E-20/

"HUR ", "DIOX",

77.809E0,

64.060E0,

.19711439E-04,

.10072061E-17/

"OGEN", " SUL",

88.231E0,

34.080E0,

•48952396E-05,

-.31539707E-18/

H ii H n 89.000E0

77.350E0

.11181148E-08

H ii ii H 73.000E0

90.180E0

-.25044950E-08

ii n n ii 56.000E0

373.150E0

-.24559562E-08

"IDE ",

" 93.000E0

81.650E0

-.37141838E-09

n p>r ii H 94.430E0

194.600E0

.38773364E-08

"IDE \

" 122.000E0

263.200E0

-.35434399E-07

"PHID", "E " 98.000E0

213.500E0

.37981427E-09

73
U.S. DEPT. OF COMM.

BIBLIOGRAPHIC DATA

SHEET (See instructions)

1. PUBLICATION OR

REPORT N/O. NBS TN-1039

2. Performing Organ. Report No 3. Publication Date

April 1981

4. TITLE AND SUBTITLE

A A COMPUTER PROGRAM FOR THE /PREDICTION OF VISCOSITY

AND THERMAL CONDUCTIVITY IN HYDROCARBON MIXTURES

5. AUTHOR(S)

James F. Ely and H. J. M. Hanley

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 Cover

9. SPONSORING ORGANIZATION NAME AND COMPLETE ADDRESS (Street, City. State, ZIP)

10. SUPPLEMENTARY NOTES

]] Document describes a computer program; SF-185, FlPS Software Summary, is attached.

11. ABSTRACT (A 200-word or less factual summary of most significant information. If document includes a significant

bibliography or literature survey, mention it here) A model for the prediction of the density, viscosity and thermal conductivity of

non-polar fluid mixtures over the entire range of pVT states is presented. The mode

is based on the extended corresponding states model and covers molecular weight

ranges including C2o» Only Pure component equilibrium data such as the critical

constants are required as input to the calculation procedure—no transport data are required. Extensive comparisons with experimental data for pure fluids and binary

mixtures are presented. The average percentage deviation for both the viscosity and

thermal conductivity was observed to be less than 8 percent. A computer program

(TRAPP) which performs the calculations reported in this manuscript is described and

listed in the Appendices.

12. KEY WORDS (Six to twelve entries; alphabetical order; capitalize only proper names; and separate key words by semicolons)

Computer program; density; extended corresponding states; fluid mixtures;

thermal conductivity; viscosity.

13. AVAILABILITY

[X~l Unlimited

| | For Official Distribution. Do Not Release to NTIS

^\ Order From Superintendent of Documents, U.S. Government Printing Office, Washington, D.C. 20402.

I I Order From National Technical Information Service (NTIS), Springfield, VA. 22161

14. NO. OF

PRINTED PAGE

80

15. Price

$4.00
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