irence

NATL INST. OF STAND & TECH

NBS

Publications

AlllDb 3MD07b

^^'fffAU O? "^ NBS TECHNICAL NOTE 1048

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

1l)46

1962
NATIONAL BUREAU OF STANDARDS

The National Bureau of Standards' was established by an act of Congress on March 3, 1901. The Bureau's overall goal is to strengthen and advance the Nation's science and technology

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the Institute for Computer Sciences and Technology.

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' Headquarters and Laboratories at Gaithersburg, M D, unless otherwise noted; mailing address Washington, DC 20234. 'Some divisions within the center are located at Boulder, CO 80303.
Interactive Fortran Program to Calculate

Thermophysical Properties of Six Fluids

Ben A. Younglove

Thermophysical Properties Division

National Engineering Laboratory

National Bureau of Standards

Boulder, Colorado 80303

e.

^^MZSO^^'/

Aatiooal Bureau of Standaras SEP 3 1982

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

NATIONAL BUREAU OF STANDARDS, Ernest Ambler, Director

Issued July 1982
i^<^^t ia iiS-Sii^ i^^iyesft

National Bureau of Standards Technical Note 1048

Nat. Bur: Stand. (U.S.), Tech. Note 1048, 56 pages (July 1982)

CODEN: NBTNAE

U.S. GOVERNMENT PRINTING OFFICE

WASHINGTON: 1982

For sale by the Superintendent of Docunnents, U.S. Government Printing Office, Washington, DC 20402

Price $4.75

(Add 25 percent for other than U.S. mailing)
Contents

Page

1. Introduction 1

2. Computer Routines 1

3. Thermophysical and Related Properties 2 3.1 The Equation of State 2 3.2 Two Phase Boundaries 2 3.2.1 Vapor Pressure 2 3.2.2 Vapor Densities at Coexistence 3 3.2.3 Liquid Densities as Coexistence 3 3.2.4 The Melting Line 3 3.3 Derived Thermodynamic Properties 3 3.3.1 Entropy 3 3.3.2 Ideal Gas Specific Heat 4 3.3.3 Reference State 4 3.3.4 Enthalpy 4 3.3.5 Internal Energy 4 3.3.6 Specific Heat at Constant Volume 4 3.3.7 Specific Heat at Constant Pressure 4 3.3.8 Sound Velocity 5

4. Transport Properties: Viscosity and Thermal Conductivity 5

5. Dielectric Constant 6

6. Sample Calculations 6 7. Acknowledgments 6

8. References 7 Appendix A. List of Symbols and Units 8 Appendix B. Sample Interactive Session ... 9 Appendix C. Properties for Computer Program Verification 10 Appendix D. Program Listing for Program Fluids . 12 Appendix E. Data Subroutines 17 Appendix F. Properties Subroutines 32

m

Interactive Fortran Program to Calculate Thermophysical

Properties of Six Fluids

Ben A. Younglove

Thermophysical Properties Division

National Engineering Laboratory

National Bureau of Standards

Boulder, Colorado 80303

An interactive FORTRAN IV computer program is given for computing thermophysical

properties of argon, ethylene, parahydrogen, nitrogen, nitrogen trifluoride, and oxygen.

The program is designed for use with a computer terminal accessing a large computer in an interactive mode. The program provides prompting for selection of several options

including: I) choice of fluid, 2) choice of SI or engineering units, 3) choice of the

single phase or liquid-vapor phase, and 4) a table of properties or a single value.

Properties are computed for the single phase region from input of two of the

variables, temperature, pressure, and density. Values on the liquid-vapor boundary are computed from an entry of temperature or pressure. The program returns values for

pressure, temperature, density, internal energy, enthalpy, entropy, specific heats at constant volume and pressure, and sound velocity. Viscosity, thermal conductivity, and

dielectric constant are given for some of the fluids. Copies of the programs may be

obtained from Office of Standard Reference Data, Attention: Reference Center, National

Bureau of Standards, Washington, D.C. 20234.

Key words: argon; computer programs; density; enthalpy; equation of state; ethylene;

hydrogen; nitrogen; nitrogen trifluoride; oxygen; specific heat at constant pressure;

specific heat at constant volume.

1. Introduction

This report presents an interactive FORTRAN IV program for computing thermophysical properties

of argon, ethylene, parahydrogen, nitrogen, nitrogen trifluoride, and oxygen. It is a companion

publication to reference [1]. The properties found in this reference are computed from a standard

set of equations and are presented in tables. References to the original works from which these

correlations were abstracted are given in [1],

This is an interactive program which allows selection of several options including: 1) a choice

of fluids, 2) SI or engineering units, 3) properties for the single phase or for the liquid-vapor

boundary, and 4) a table of values or a single value. Properties of the homogeneous phase are computed at a single point from entry of any two of the three variables, temperature, pressure, and

density. Properties on an isobar may be specified as well. Properties on the liquid-vapor boundary

are computed from an entry of temperature or pressure.

2. Computer Routines

This program is a modification of program "Fluids Pack" by R. D. McCarty [2]. An early version

of this type of program, which represents the thermophysical properties of several fluids, is program

"GASP" (gas properties) by R. C. Hendricks, et al . [3]. The improvements in the experimental data

used in the correlations, that have occurred since the publication of [3], have been incorporated in this report. Also, by retaining the same form of the equations for all fluids, the computer

programming is much simplified and easier to use. Only the numerical constants, which are found in Appendix E, are changed from one fluid to the next.

A complete listing of the computer program is in Appendices D, E and F. The thermophysical

properties produced by this system are the values given in reference [1]. The program is designed to be run interactively and provides instructions for its use and detects certain types of errors such
as entry of variables outside of the range of validity for the equation of state. The temperature

and pressure range allowed for each fluid is automatically displayed v^hen the fluid is first called.

Since the basic equation of state for the fluids is semi-empirical in nature, the program should not

be used outside the temperature and pressure range displayed for each fluid. Large errors in

calculatea properties can be expected outside the allowed ranges. An example of the program in use

is presented in appendix B. Properties for computer program verification are given for each of the

fluids in appendix C.

3. Thermodynamic and Related Properties

3.1 The Equation of State

The relation for computing pressure as a function of temperature and density is a 32-term

modified Benedict-Webb-Rubin (MBWR) equation of state. Its versatility and adaptability to efficient

computer technique make it appropriate for use with multi property fitting techniques, v/here deviations from the PVT surface and heat capacity or sound velocity data are minimized simultaneously,

resulting in a more accurate model than would be the case if the PVT data alone were used. This

technique has been described by R. D. McCarty [2,4]. Other advantages of ttie MBWR are: (1) accurate

representation of the thennodynamic surface over wide ranges of temperature and pressure,

(2) adaptability to least squares fitting methods using many different kinds of experimental data,

and (3) convenience in correlating data from different sources.

The mathematical form of the MBWR is,

P = pRT + p^(G(l)T + G(2)T^/^ + G(3) + G(4)/T + G(5)/T^)

+ p^(G(6)T + G(7) + G(8)/T + G(9)/T^)

+ p^(G(10)T + G(ll) + G(12)/T) + p^(G(13))

+ p^(G(14)/T + G(15)/t2) + p^(G(16)/T)

+ p^(G(17)/T + G(18)t2) + p^(G(19)/t2)

+ p^(G(20)/t2 + G(21)/t2) exp{Yp2) (1)

+ p^(G(22)/T^ + G(23)/T^) exp(YP^)

+ p^G(24)/t2 + G(25)/T^) exp(YP^)

+ p^G(26)/T^ + G(27)/T^) explyp^)

+ p^^G(28)/T^ + b(29)/T-^) exp(Yp^)

+ p^^(G(30)/T^ + G(31)/T-^ + G(32)/T^) exp(Yp^)

2 The nonlinear coefficient, y, is defined generally as y = -1/p , and is held constant during tne fitting process to determine the linear coefficients G(i).

Coefficients for each of the fluids are given in appendix E.

3.2 Two Phase Boundaries

3.2.1 Vapor Pressure

The temperature of the liquid-vapor boundary for each isobar in the tables is computed from a vapor pressure equation.
? 3 4 ^(^)

ix\? = £n P^ + Vp(l)x + Vp(2)x'^ + Vp(3)x-^ + Vp(4)x^ + Vp(5)x(l-x) P (2)

where

X = (1 - T^/T)/(i - yr^) (3)

The coefficients shov/n here as V ?i.rQ. given in appendices U, E and F as VP since these appendices

?iTQ. listings of Fortran programs and subroutines. The same applies for other subscripted

coefficients.

3.2.2 Vapor Densities at Coexistence

Densities of the vapor in coexistence with liquid, which are used to generate all the saturated

densities given in the tables, are given by

P = py (Ptv " Pc^ ^^P ^^^^ ^^^

and

f(T) - A(l) Jin X +

4 -13

E A(i)(l - x^^"^)/^) + X) A(i)(l - x)^^"^^/^ (5)

i=2 i=5

where

x = (T - TJ/(T^ - T^) . (6)

3.2.3 Liquid Densities at Coexistence

The liquid density at coexistence is calculated from.

Pc " ^Pt£ " Pc^ ^^^ ^^^^ ^^^

and

f(T) = A(14) £n x + Y. A(i)(l - x^^"^^)/^) + D A( i

) (1 - x^^'"^^^/-^) (8)

i=15 i=18

where x is defined in eq 6. 3.2.4 The Melting Line

The pressures at melting are given by,

P (3)

P = P^(l) + P^(2)T ^ (9)

3.3 Derived Thermodynamic Properties

The properties derived from the equation of state and ideal heat capacity ^vo. entropy, enthalpy,

internal energy, specific heat at constant volume and at constant pressure, and sound velocity.

3.3.1 Entropy

The entropy is computed from

S(T,p) = S^(T^) + J

{c°/T}dT - R £n(RTp/P^) + J|r/p - (l/p2)^|^^

I dp . (10)

° P T
3.3.2 Ideal Gas Specific Heat

The ideal gas specific heat, C is computed from the following,

C°/R = G.(l)/T^ + G.(2)/T^ + G.(3)/T + G.(4) + G.(5)T + G.(6)t2

+ G,{7)t2 + G,(8)u^e^(e' - 1)^

:ii)

where.

3.3.3 Reference State

u = G.(9)/T . (12)

The reference states S and H at T = 298.15 K (given below in table 1) are from Wagman,

et al . [5], except for parahydrogen whicti is taken from Woolley, Scott, and Brickwedde [5], since

reference [5] gives only the norinal hydrogen values.

Table 1. Reference Values for Temperature, Entropy and Enthalpy.

The reference value for temperature is T = 298.15 K for all fluids. Values of S° and H° are from NBS

TN 270-3 [5], except hydrogen [6].

S° J/mol K H° J/mol

argon 154.7335 6169.5

ethylene 219.451 10564.6

parahydrogen 130.407 8409.8

nitrogen 191.502 8669.0

nitrogen trifluoride 260.621 ' 11828.0

oxygen 2U5.029 8680.1

3.3.4 Enthalpy

Tlie enthalpy is computed from

H(T,p) - H° + (P - pRT)/p +/ j^ - I^ fe) { dp + / C° dT . 13'

( p p

^ /p'-j- T^

3.3.5 Internal Energy

The internal energy is,

E(T,p) = H(T,p) - P/p . (14)

3.3.6 Specific Heat at Constant Volume

The specific heat at constant volume is,

^0 „

P U /a^P

C (T,p) = r - R - f \^ {^] } dp . (15)

^ Jq I p \3T

3.3.7 Specific Heat at Constant Pressure

The specific heat as constant pressure is.

T /3P\^,/3P

Cp(T,p) = C^(T,p) . j^ [A) \J^)^\ • (16)
3.3.8 Sound Velocity

The sound velocity can be computed as,

W(T.P) '\/{^)\ . (17)

4. Transport Properties: Viscosity and Thermal Conductivity

Viscosity and thermal conductivity are given for argon, methane, nitrogen, and oxygen. The

theory and discussion of the relations used here are from the work of Hanley, McCarty and Haynes [7].

The functional forins for viscosity and thermal conductivity are,

n - n^lT) + n^{T)p + n^lp.T) (18)

and

^ = Aq(T) + X^(T)p + X2(p,T) + A^(p,T) . (19)

The first terms of eqs (18) and (19) are the contributions of the dilute gas,

n<,(T) = i G^(i)T<^-^)/5 ,

and (20)

X„(T) = E G.dJTC-')/^ .

i = l

The second terms in eqs (18) and (19) represent the contribution to the transport coefficients of the

moderately dense gas.

n^d) = F^(l) + F^(2) F^(3) - £n (T/F^(4)) ^

,

and (21)

A^d) = F^(l) + F^(2) FJ3) - £n (T/F^(4)) ^ .

The third terms in these equations are the contribution of the dense gas,

n2(p,T) = exp F(p,T) - exp G(T) :22:

F(p,T) = Ey(l) + E^(2)H(p) + Ey(3)p"-^ + £,(4)H(p)/t2

+ Ey(5)p°-VT^-^ + E^(6)/T + E^(7)H(p)/T

:23;

where

G(T) = E^(l) + E^(2)/T (24)

H(p) = p°-5 (p - E^(8))/E^(8) . (25;

The functional forms of eqs (22), (23), (24) and (25) are used for the corresponding tiiermal

conductivity equations with the coefficients E. substituted for the E 's.
The last term of eq (19) is the critical enhancement term. Critical effects can be very larye,

especially in the range (p-p )/p < 0.25 and (T-T )/T < 0.025 and in fact, as the critical point is approached, this term may be larger than the sum of the other terms by several orders of magnitude.

We include A to give the proper behavior in the critical region and to produce a smooth transition

from outside the critical region to witnin it.

5. Dielectric Constant

The dielectric constant defines the well known Clausius Mossotti relation,

C^ = ^

1/p . (26) m e+2 '

The C[n is represented by the empirical relation,

C^ = B^(l) + B^(2)p + B^(3)p2 + B^(4)p^ + B^(5)T + B^(6)P . (27)

Coefficients are given for parahydrogen, nitrogen, and oxygen, but not for argon, ethylene, or nitrogen trifluoride. The coefficients of Stewart [8] for parahydrogen were modified to conform to eq (27). The data of Ely and Straty for nitrogen [9] ^^ere used in a fit of eq (27). The oxygen

coefficients are from Younglove [10].

Although tne range of the Clausius-Mossotti function for most liquids is small, the very high

precision of the data require the terms of eq (27). The temperature and pressure terms are useful in

fitting t\\e compressed liquid states. The pressure term allows the flexibility which is useful in fluids with low compressibilities, usually found at low temperatures and high pressures [9].

6. Sample Calculations

In appendix C we have provided numerical values computed from the program (as given in appendices D, E and F). Values for the various properties are given for the saturated vapor and

liquid at a pressure of 0.101325 MPa (1 atmosphere), and for the single phase at 35 MPa and 300 K. Failure to reproduce these numbers usually arises from using too few significant figures. This work

was done using a 60 bit word. Use of double precision calculations may be necessary on computers

with smaller word length.

7. Acknowledgments

We are indebted to the Office of Standard Reference Data of the National Bureau of Standards for

its generous support, and to Robert D. McCarty on whose work this report is based.
8. References

[1] Younylove, B. A., Thermophysical properties of fluids, Vol. I: Argon, ethylene, paraliydrogen,

nitrogen, nitrogen trifluoride, and oxygen, J. Chein. Phys. Ref. Data jj^ (1982), Suppl . 2. [2] McCarty, R. D. , Interactive FORTRAN IV computer programs for the thermodynamic and transport

properties of selected cryogens [Fluids Pack], Nat. Bur. Stand. (U.S.), Technical Note 1025

(1980).

[3] Hendricks, R. D. , Baron, A. K. and Paller, I. C. , GASP - A computer code for calculating the

thermodynamic and transport properties for ten fluids: Parahydrogen, helium, neon, methane,

nitrogen, carbon monoxide, oxygen, fluorine, argon, and carbon dioxide, NASA Teclinical Note

D-7808 (1975).

[4] McCarty, R. D., Determination of thermodynamic properties from the experimental P-V-T

relationships, Vol.11, Experimental Thermodynamics of Non-Reacting Fluids, B. LeNeindre and B. Vodar, Editors, Butterworth and Co., Ltd., London, England (1975).

[5] Wagman, D. D., Evans, W. H., Parker, V. B., Halow, I., Baily, S. M. and Schumm, R. H., Selected

values of chemical thermodynamic properties, Nat. Bur. Stand. (U.S.), Technical Note 270-3

(1968).

[6] Woolley H. W, Scott, R. B. and Brickwedde, F. G. , Compilation of thermal properties of hydrogen

in its various isotopic and ortho-para modifications, Nat. Bur. Stand. (U.S.), Research Paper

RP1932 (1948).

[7] Hanley, H. J. M. , McCarty, R. D. and Haynes, W. M. , The viscosity and thermal conductivity

coefficients for dense gaseous and liquid argon, krypton, xenon, nitrogen, and oxygen. J. Phys.

Chem. Ref. Data ^, 979-1017 (1979).

[8] Stewart, J. W. , Dielectric polarizabi 1 ity of fluid para-hydrogen, J. Chem. Phys. 4_0, 3297-3306

(1964).

[9] Ely, J. F. and Straty, G. C. , Dielectric constants and molar polarizabil ities of saturated and

compressed fluid nitrogen, J. Chem. Phys. 6],, 1480-1485 (1974).

[10] Younglove, B. A., Dielectric constant of compressed gaseous and liquid oxygen, J. Res. Nat. Bur. Stand. (U.S.), 76A, 37-40 (1972).
Appendix A. List of Symbols and Units.

Primary Thermophysical Quantities . P,P^,P^ pressure, P at critical point, P at triple point, MPa

p ,p density, p at critical point, mol/dm'^

Pt£'Ptv P °^ liquid at triple point, p of gas at triple point

T,T_,T^ temperature, T at critical point, T at triple point, K Cp,Cp specific heat at constant pressure, C of ideal gas, J/mol K Cy,C^ specific heat at constant volume, C for ideal gas, J/mol K

E internal energy, J/mol

H,H° enthalpy, reference value of H, J/mol

S,S° entropy, reference value of S, J/mol K W sound velocity, m/s

n viscosity, yPa s

A thermal conductivity, W/m K

e dielectric constant

Other Variables and Constants .

R the gas constant, 8.31434 J/mol K

K4. isothermal bulk modulus, (MPa)"-'-

M|„ molecular weight, g/mol

Ng Avagodro's number, per mol

C^ CI ausius-Mossotti function

T reference temperature, 298.15 K

Critical Point Values .

P(, (MPa) p^ (mol/dm^) T^ (K)

Ar 4.9058 13.41 • 150.86

C2H4 5.0404 7.650 282.34

H2 1.28377 15.556 32.938

N2 3.39908 11.21 126.26

Nf3 4.4607 7.92 234.0

O2 5.043 13.630 154.581
Appendix B. Sample Interactive Session

CALL, FLUIDS

FOR INFORMATION ON HOW TO USE THIS PROGRAM, ENTER "0" OTHERWISE, ENTER "1'

?

WHEN THE PROGRAM ASKS FOR A FLUID SELECTION, ENTER THE APPROPRIATE

NUMBER. AN INAPPROPRIATE NUMBER WILL TERMINATE THE PROGRAM. WHEN

IT ASKS FOR A PRESSURE, DENSITY, AND TEMPERATURE, ENTER ANY TWO OF OF THE THREE AND A ZERO FOR THE THIRD.

THE ORDER MUST BE P,D,T, AND ONE OF THE THREE MUST BE ZERO.

IF ALL THREE ARE ZERO THE PROGRAM ASKS FOR A NEW FLUID.

SELECT A FLUID BY ENTERING THE CORRESPONDING NUMBER

1=ARG0N, 2=ETHYLENE, 3=PARA HYDROGEN,

4=NITR0GEN, 5=NITR0GEN TRIFLUORIDE, 6=0XYGEN 7=ST0P

? 1

THE TEMPERATURE RANGE FOR ARGON IS 83.8 TO 400 K WITH PRESSURES TO 100 MPA

FOR ENGINEERING UNITS ENTER "0", FOR METRIC ENTER "1"

? 1

FOR SATURATION PROPERTIES ENTER "0", FOR FLUID ENTER "1"

? 1

FOR A SINGLE POINT ENTER "0", FOR A TABLE ENTER "1"

? 1

ENTER A PRESSURE(MPA), A STARTING TEMPERATURE(K) , A FINAL TEMPERATURE

AND A TEMPERATURE INCREMENT AND IN THAT ORDER.

? 10 100 150 10

P T DEN E H S CV CP SOUND VISC COND MPA K MOL/L === J/MOL/ == ==== J/MOL-K -== M/S PA-S MW/M-K

E+6

10.000 100.000 33.744 -4271. -3974. 59.6 20.4 44.0 800. 205.0 115.1

10.000 110.000 32.191 -3839. -3529. 63.8 19.5 45.2 739. 162.7 102.9

10.000 120.000 30.525 -3396. -3069. 67.8 18.8 46.9 672. 131.2 92.1

10.000 130.000 28.695 -2936. -2587. 71.7 18.2 49.5 602. 106.4 81.8

10.000 140.000 26.609 -2447. -2072. 75.5 17.6 54.1 526. 85.9 71.7

10.000 150.000 24.096 -1909. -1494. 79.5 17.3 62.3 444. 67.9 61.7

ENTER A PRESSURE(MPA), A STARTING TEMPERATURE(K) , A FINAL TEMPERATURE

AND A TEMPERATURE INCREMENT AND IN THAT ORDER

?

SELECT A FLUID BY ENTERING THE CORRESPONDING NUMBER

1=ARG0N, 2=ETHYLENE, 3=PARA HYDROGEN,

4=NITR0GEN, 5=NITR0GEN TRIFLUORIDE, 6=0XYGEN 7=ST0P

? 8

EXIT.
Appendix C. Properties for Computer Program Verification

ARGON PROPERTIES.

T DEN E H S CV CP SOUND VI SC COND

K MOL/L === J/MOL ==- ==== J/MOL-K =--= M/S PA-S MW/M-K

E+6

SATURATED VAPOR AT 0.101325 MPA. 87.2815 .1446 1038.7 1739.4 128.63 13.22 22.76 170.7 7.3 5.9

SATURATED LIQUID AT 0.101325 MPA. 87.2815 34.8946 -4708.7 -4705.8 54.82 22.27 44.73 814.4 260.3 128.3

SINGLE PHASE AT 35 MPA AND 300 K. 300.0000 13.6426 1830.3 4395.8 100.94 14.07 32.82 445.8 39.5 36.9

ETHYLENE PROPERTIES

T DEN E H S CV CP SOUND VISC COND

K MOL/L === J/MOL = = = ==== J/MOL-K ==== M./S PA-S MW/M-K

E+6

SATURATED VAPOR AT 0.101325 MPA. 169.4093 .0744 4180.6 5541.6 197.66 27.13 36.89 252.3

SATURATED LIQUID AT 0.101325 MPA. 169.4093 20.2449 -8001.8 -7996.8 117.73 38.22 67.92 1310.1

SINGLE PHASE AT 35 MPA AND 300 K. 300.0000 15.8136 -504.6 1708.7 151.74 41.68 70.79 868.6

HYDROGEN PROPERTIES

T DEN E H S CV CP SOUND VISC COND DIEL

K MOL/L === J/MOL === --== J/MOL-K -=== M/S PA-S MW/M-K ==

E+6

SATURATED VAPOR AT 0.101325 MPA. 20.27 .564 22^.5 382.0 60.40 13.31 24.68 354. 1.00404

SATURATED LIQUID AT 0.101325 MPA. 20.27 35.118 -518.9 -516.0 16.11 11.43 19.49 1100. 1.22981

SINGLE PHASE AT 35 MPA AND 300 K. 300.00 11.517 5837.0 8875.8 81.58 22.23 31.12 1609. 1.07174

NITROGEN PROPERTIES,

T DEN E H S CV CP SOUND VISC COND DIEL

K MOL/L === J/MOL === ==== J/MOL-K ==== M/S PA-S MW/M-K == E+6

SATURATED VAPOR AT 0.101325 MPA. 77.36 .154 1548.0 2163.5 151.54 21.59 31.45 175. 5.3 7.5 1.00217

SATURATED LIQUID AT 0.101325 MPA. 77.36 28.863 -3404.3 -3400.8 79.54 27.82 57.80 939. 151.6 133.7 1.43356

SINGLE PHASE AT 35 MPA AND 300 K. 300.00 11.756 4623. q 7601.1 138.73 22.29 38.11 514. 28.7 48.0 1.16337

10
NITROGEN TRIFLUORIDE PROPERTIES.

T DEN E H S CV CP SOUND VISC COND

K MOL/L === J/MOL === ==== J/MOL-K ==== M/S PA-S MW/M-K

E+6

SATURATED VAPOR AT 0.10132S MPA. 144.1082 .0879 3575.7 4728.5 227.83 29.65 39.49 144.1

SATURATED LIQUID AT 0.101325 MPA. 144.1082 21.6563 -6832.5 -6827.8 147.66 40.30 72.20 757.5

SINGLE PHASE AT 35 MPA AND 300 K. 300.0000 14.3859 3299.9 5732.9 197.40 50.03 80.58 412.4

OXYGEN PROPERTIES.

T DEN E H S CV CP SOUND VISC COND DIEL

K MOL/L === J/MOL === ==== J/MOL-K ==== M/S PA-S MW/M-K == E+6

SATURATED VAPOR AT 0.101325 MPA. 90.19 .140 1811.5 2535.6 169.58 21.72 31.34 178. 6.7 8.5 1.00166

SATURATED LIQUID AT 0.101325 MPA. 90.19 35.658 -4265.5 -4262.7 94.19 29.54 54.22 905. 194.7 151.8 1.48704

SINGLE PHASE AT 35 MPA AND 300 K. 300.00 13.742 4233.0 6780.0 150.97 22.62 41.95 442. 34.7 46.4 1.17222

11
Appendix D. Program Listing for Program Fluids

PROGRAM FLUIDS! INPUT, OUTPUT)

DIMENSION G(32),VP(9)

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

COMMON/CONT/IF

COMMON/CRIT/EM,EOK,RM,TC,DC,X,PC,SIG

C0MM0N/DIEL/BX(6),PX(6)

1000 FORMAT(* FOR INFORMATION ON HOW TO USE THIS PROGRAM, ENTER "0" *

A * OTHERWISE, ENTER "1"*)

PRINT 1000

IP = 3 PRINT 1210 READ 1010,1

IF{I.EQ.O)CALL INFO

PRINT 1210

1010 FORMAT(Il)

110 PRINT 1020

PRINT 1030

1020 FORMAT(* SELECT A FLUID BY ENTERING THE CORRESPONDING NUMBER*)

1030 FORMAT(* 1=ARG0N, 2=ETHYLENE, 3=PARA HYDROGEN,

A *,/,* 4=NITR0GEN, 5=NITR0GEN TRIFLUORIDE, 6-OXYGEN*

B ,* 7=ST0P*)

READ *,IF

PRINT 1210

GO T0(1,2,3,4,5,6,999),IF

1 CALL DATA AR GO TO 120

2 CALL DATA C3 GO TO 120

3 CALL DATA PH2

GO TO 120

4 CALL DATA N2 GO TO 120

5 CALL DATA NF3

GO TO 120

6 CALL DATA 02 GO TO 120

120 PRINT 1040

1040 FORMAT(* FOR ENGINEERING UNITS ENTER "0", FOR METRIC ENTER "1"*) READ 1010, lU PRINT 1210

PRINT 1050

1050 FORMAT(* FOR SATURATION PROPERTIES ENTER "0", FOR FLUID ENTER * A *"1"*)

READ 1010, IC PRINT 1210

PRINT 1060

1060 FORMAT(* FOR A SINGLE POINT ENTER "0", FOR A TABLE ENTER "1"*) READ 1010, IV PRINT 1210

160 IF(IC.EQ.0)G0 TO 240

IFdV.EQ.DGO TO 330

170 IF(IU.EQ.O)GO TO 180

PRINT 1080 READ *,P,D,T

PRINT 1210

GO TO 190

180 PRINT 1070

1070 FORMAT!* ENTER PRESSURE! PSI A) , DENSITY! LB/CU FT), AND TEMPERATURE*

A *!F)*)

READ *,P,D,T

PRINT 1210

P=!P/14. 695949)*. 101325

12
D=D*16.01846371/EM

IF(T.E0.0.0)G0 TO 190

T=(T-32.)/l. 8+273. 15

190 IF{P.LE.O.O)GO TO 220

1080 FORMAT(* ENTER PRESSURE(MPA) , DENSITY(MOL/L) , AND TEMPERATURE(K)^

IF(D.LE.O.O)GO TO 210

IF(T.LE.0.0)G0 TO 200

GO TO 170

200 IF(P.LE.0.0R.D.LE.0.0)G0 TO 110

T=FIND T(P,D)

CALL LIMITS(P,T,IL)

IF(IL.LE.O)GO TO 170

GO TO 230

210 IF(T.LE.n.0R.P.LE.0)G0 TO 110

CALL LIMITS(P,T,IL)

IF(IL.LE.0)G0 TO 170

D=FIND D(P,T)

GO TO 230

220 IF(D.LE.O.0.OR.T.LE.O)G0 TO 110

P=FIND P(D,T)

CALL LIMITS(P,T,IL)

IF(IL.LE.O)GO TO 170

230 CALL REPRO(P,D,T,IU,IV,IC,IP,TF,DELT)

GO TO 170

240 PRINT 1090

1090 FORMAT(* FOR SATURATED LIQUID ENTER "0", FOR VAPOR ENTER "1"*) READ 1010, IP PRINT 1210

IFdV.EQ.DGO TO 330

PRINT 1095

1095 FORMAT(* TO ENTER WITH TEMPERATURE ENTER "0", FOR PRESSURE "1"*) READ 1010,11

PRINT 1210

IFdI.EQ.DGO TO 290

250 IFdU.EO.DGO TO 260

1100 FORMAT(* ENTER A TEMPERATURE IN DEGREES F*)

PRINT 1100 READ *,TI

PRINT 1210

T=(TI-32.)/l. 8+273. 15

IF(T.LE.O.O)GO TO 110

GO TO 270

260 PRINT 1110

1110 FORMAT (* ENTER A TEMPERATURE(K)*)

READ *,T

PRINT 1210

270 IF(T.LT..000001)G0 TO 110

IF(T.GT.TCC.OR.T.LT.TTP)GO TO 280

P=VPN(T)

IF{IP.EO.O)P=P+. 00001

D=FIND D(P,T)

CALL RE PRO(P,D,T,IU,IV,IC,IP,TF,DELT)

GO TO 250

280 PRINT 1120, TTP,TCC,(TTP-273.15)*1. 8+32., (TCC-273.15)*1. 8+32.

1120 FORMAT(* FOR SATURATION < *,F6.2,* K*,/, * ,F6 .2,* < TEMP

A * OR *,F7.2,* < TEMP < *

,F7 .2,* F*) GO TO 250

290 IFdU.EQ.DGO TO PRINT 1130

300

1130 FORMAT(* ENTER A READ *,PI

PRINT 1210

IF(PI.LE.O.O)GO

P=(PI/14. 695949)-

GO TO 310

PRESSURE

TO 110

M01325

IN LB/SQ IN*)

13
300 PRINT 1140

1140 FORMAK* ENTER A PRESSURE(MPA)*)

READ *,PI

PRINT 1210

IF(PI.LE.0.0)G0 TO 110 P=PI 310 IF{P.GT.PCC.OR.P.LT.PTP)GO TO 320

T=FIND TV(P)

P=VPN(T)

IF(IP.E0.0)P=P+. 00001

D=FIND D(P,T)

CALL RE PRO(P,D,T,IU,IV,IC,IP,TF,DELT)

GO TO 290

320 PRINT 1150, PTP,PCC

1150 F0RMAT(* YOUR INPUT PRESSURE IS OUTSIDE THE RANGE OF SATURATION*

A * PRESSURES*/* FOR THIS FLUID. TRIPLE P0INT=*,F6.5 ,* MPA,*

B * CRITICAL P0INT=*,F6.3,* MPA*/* TRY AGAIN*)

GO TO 290

330 IFdC.EQ.DGO TO 370

IFdU.EO.DGO TO 340

PRINT 1160

1160 F0RMAT(* ENTER A STARTING TEMPERATURE, A FINAL TEMPERATURE*

A /* AND A TEMPERATURE INCREMENT, IN DEGREES F AND IN THAT ORDER*)

READ *,TS,TF,DELT

PRINT 1210

IF(DELT.LE.0.0)G0 TO 110

TS=(TS-32.)/l. 8+273. 15 TF=(TF-32.)/l. 8+273. 15 .

• DELT=DELT/1.8

IF(TS.LT.TTP.OR.TS.GT.TCC)GO TO 360

IF(TF.LT.TTP.0R.TF.GT.TCC)G0 TO 360

GO TO 350

340 PRINT 1170

1170 FORMAT!* ENTER A STARTING TEMPERATURE, A FINAL TEMPERATURE*

1/* AND A TEMPERATURE INCREMENT IN KELVINS AND IN THAT ORDER*)

READ *,TS,TF,DELT

PRINT 1210

IF(DELT.LE.0.0)G0 TO 110

IF{TS.LT.TTP.OR.TS.GT.TCC)GO TO 360

IF(TF.LT.TTP.OR.TF.GT.TCC)Gn TO 360

350 T=TS

P=VPN(T)

IF(IP.EQ.0.0)P=P+. 00001

D=FIND D(P,T)

CALL RE PRO(P,D,T,IU,IV,IC,IP,TF,DELT)

GO TO 330

360 PRINT 1180, TTP,TCC,(TTP-273.15)*1. 8+32. ,(TCC-273.15)*1. 8+32

1180 F0RMAT(* FOR SATURATION, *,F6.2,* < TEMP < *,F6.2,* K*,/,

A ,13X,*0R, *,F7.1,* < TEMP < *,F7.1,* F. TRY AGAIN.*)

GO TO 330

370 IFdU.EO.DGO TO 380

PRINT 1190

1190 FORMATf* ENTER PRESSURE(PSIA) , STARTING TEMPERATURE(F) , FINAL * A *TEMPERATURE(F)*/* AND A TEMPERATURE INCREMENT, IN THAT ORDER*)

READ *,PI,TS,TF,DELT

PRINT 1210

IF(DELT.LE.O.O)GO TO 110

P=(PI/14. 695949)*. 101325

T=(TS-32.)/l. 8+273. 15

TF=(TF-32.)/l. 8+273. 15 DELT=DELT/1.8

CALL LIMITS(P,T,IL)

IF(IL.LE.O)GO TO 370

CALL LIMITS(P,TF,IL)

IF(IL.LE.O)GO TO 370

14
GO TO 390

380 PRINT 1200

1200 FORMAT(* ENTER A PRESSURE(MPA) , A STARTING TEMPERATURE(K) , A 1*FINAL TEMPERATURE AND A*/* TEMPERATURE INCREMENT*

2* AND IN THAT ORDER, TO RESTART PROGRAM ENTER "0,0,0,0"*)

READ *,PI,TS,TF,DELT

PRINT 1210

IF(DELT.LE.0.0)G0 TO 110

T=TS

P=PI CALL LIMITS(P,T,IL)

IF(IL.LE.O)GO TO 370

CALL LIMITS(P,TF,IL)

IF(IL.LE.O)GO TO 370

390 D=FIMD D(P,T)

CALL RE PRO(P,D,T,IU,IV,IC,IP,TF,DELT)

GO TO 370

999 CONTINUE

1210 FORMAT(* *) END

SUBROUTINE REPRO(P,D ,T, lU, IV, IC, IP ,TF ,DELT)

DIMENSION G(32) ,VP(q)

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

COMMON/CONT/IF

COMMON/CRIT/EM,EOK,RM,TC,DC,X,PC,SIG

C0MM0N/CPID/GI(11),GH(11),GL(11)

COMMON/HAN/CR,TCI

N=500

IF(IV.EO.O)TF=T-1.

IF(IU.E0.O)GO TO 100

PRINT 1000

PRINT 1010

PRINT 1020

GO TO 110

100 PRINT 1000

PRINT 1030

PRINT 1040

110 CONTINUE

DO 210 1=1,

N

IFd.EO.DGO TO 120

D^FIND D(P,T)

120 H=ENTHAL{P,D,T)

E=H-1000.*P/D

S=ENTROP(D,T)

W=SOUND(D,T)

CPP=CPfD,T)

CVV=CV(D,T)

IF(IU.EQ.O)GO TO 160

IF(IF.EQ.4.0R.IF.E0.6) GO TO 150

C IF-4 FOR N2, IF=6 FOR 02.

IF(IF.En.l) GO TO 140

C IF=1 FOR AR IF(IF.E0.3) GO TO 130

C IF=3 FOR H2

C IF=2 FOR C2H4, IF-5 FOR NF3

PRINT 2000, P,T,D,E,H,S,CVV,CPP,W

GO TO 200

130 EPS=DIEL(P,D,T)

PRINT 2010, P,T,D,E,H,S,CVV,CPP,W,EPS

GO TO 200

140 TH=THERM(D,T)*1000.

V=VISC(D,T)

PRINT 2020, P,T,D,E,H,S,CVV,CPP,W,V,TH

15
GO TO 200

150 V=VISC(D,T)

TH=THERM(D,T)*1000.

EPS=DIEL(P,D,T)

PRINT 2030, P,T,D,E,H,S,CVV,CPP,W,V,TH,EPS

GO TO 200

160 H=H/(2.324445*EM)

E=E/(2.324445*EM)

S-S/(4.184001*EM)

CPP=CPP/{4.184001*EM)

CVV=CVV/(4.184001*EM)

W=W*3. 280840

P0=(P/.101325)*14. 695949

D0=D*EM/16. 01846371

T0=T*1. 8-459. 67

IF{IF.EQ.4.0R.IF.EQ.6) GO TO 190

IF(IF.EO.l) GO TO 180

IF(IF.E0.3) GO TO 170

PRINT 3000, PO,TO,DO,E,H,S,CVV,CPP,W

GO TO 200

170 EPS=DIEL(P,D,T)

PRINT 3010, PO,TO,DO,E,H,S,CVV,CPP,W,EPS

GO TO 200

180 V=VISC(D,T)*. 067196897

TH=THERM(D,T)*. 578176

PRINT 3020, P0,T0,D0,E,H,S,CVV,CPP,W,V,TH

GO TO 200

190 V=VISC(D,T)*. 067196897

TH-THERM(D,T)*. 578176

EPS=DIEL(P,D,T)

PRINT 3030, P0,TO,D0,E,H,S,CVV,CPP,W,V,TH,EPS

200 T=T+DELT

IF(T.GT.TF+.01)G0 TO 220

IF(IC.EQ.O)P-VPN(T)

IF(IP.EQ.O)P=P+. 00001

210 CONTINUE

220 CONTINUE

PRINT 1000

1000 FORMAT(* *)

RETURN

1010 FORMAT (3X,*P*,5X,*T*,6X,*DEN*,5X,*E*,6X,*H*,6X,*S*,4X,*CV*,4X,

A *CP* ,3X ,*SOUND* ,2X ,*VISC* ,2X ,*C0ND* ,2X ,*DIEL*)

1020 F0RMAT(3X,*MPA*,3X,*K*,6X,*M0L/L*,2X,*=== J/HOL ==*,2X,"==== ", A "J/MOL-K -==" ,2X ,*M/S* ,3X ,"PA-S" ,1X

, "MW/M-K" ,2X ,*==*,/ ,61X ,*E+6*)

1030 F0RMAT(3X,*P*,5X,*T*,7X,*DENS*,3X,*E*,8X,*H*,5X,*S*,5X,*CV*,

A 4X,*CP*,2X,*S0UND*,1X,*VISC*,2X,*C0ND*,2X,*DIEL*)

1040 F0RMAT(3X,*PSIA*,2X,*F*,7X,*LB/*,3X,*-=== BTU/ ===*, IX ,*======*,

A * BTU/ ====-*, 2X,*F/S*,3X,*LB/*,2X,*BTU/*,2X,*=-*,/,17X,*CU FT*,

B 6X,*LB*,14X,"LB-F",13X,"FT-S",lX,"FT-HR-F",/,62X,"E+7")

2000 F0RMAT(F7.3,F8.3,F7.3,2F7.0,F6.1,F5.1,F6.1,F6.0)

2010 F0RMAT(F7.3,F8.3,F7.3,2F7.0,F6.1,F5.1,F6,1,F6.0,13X,F8.5)

2020 F0RMAT(F7.3,F8.3,F7.3,2F7.0,F6.1,F5.1,F6.1,F6.0,F6.1,F6.1)

2030 F0RMAT(F7.3,F8.3,F7.3,2F7.0,F6.1,F5.1,F6.1,F6.0,F6.1,F6.1,F8.5)

3000 F0RMAT(F7.1,F8.3,F7.3,2F7.1,3F6.3,F6.0)

3010 F0RMAT(F7.1,F8.3,F7.3,2F7.1,3F6.3,F6.0,11X,F8.5)

3020 F0RMAT(F7.1,F8.3,F7.3,2F7.1,3F6.3,F6.0,F5.2,F6.4)

3030 F0RMAT(F7.1,F8.3,F7.3,2F7.1,3F6.3,F6.0,F5.2,F6.4,F8.5)

END

16
Appendix E. Data Subroutines

SUBROUTINE DATA AR DIMENSION G(32),VP(9)

DIMENSION GV(9) ,GT(9) ,FV(4) ,FT(4) ,EV(8) ,ET{8)

DIMENSION A(20)

COMMON/SEN/BETA, XO, DELTA, El, E2, AGAM

COMMON/SATC/A,DTPV

COMMON/CRIT/ EM, EOK, RM, TC, DC, X , PC, SIG

COMMON/DATA/G,R , GAMMA, VP , DTP ,PCC ,PTP ,TCC ,TTP ,TUL ,TLL ,PUL ,DCC

C0MM0N/DATA1/GV,GT,FV,FT,EV,ET

COMMON/CPID/GKll) ,GH(11) ,GL(11)

COMMON/ISP/N,NW,NWW

COMMON/FIXPT/TO,SO,HO

C0MM0N/DIEL/BX(6),PX(6)

NWW=0

PRINT 100

100 FORMAT(* THE TEMPERATURE RANGE FOR ARGON IS 83.8 TO 400 K* 1/* WITH PRESSURES TO 100 MPA*)

N=0 $ NW-1

EM=39.948 $ E0K=152.8 $ RM=3.669E-08 $ TC=150.725

DC-0.533 $ X=1.7124 $ PC=4.8619 $ SIG=3.297

X0=0.183 $ BETA=0.355 $ DELTA=4.352 $ El=2.27 $ E2=0.287

AGAM=1.190

C ARGON COEFFICIENTS FOR MBWR EON

G [ 1) G 2) G 3)

G 4)

G 5)

G 6)

G 7)

G 8)

G 9) G 10)

G 11)

G 12)

G 13)

G 14)

G 15)

G 16)

G 17)

G 18)

G 19)

G 20)

G( 21)

G 22)

G 23)

G 2^)

G 25)

G 26)

G 27)

G 28)

G 29)

G 30)

G 31)

G 32)

GAMMA=

-.65697312940E-04

.18229578010E-01

-.36494701410E+00

.12320121070E+02

-.86135782740E+03

.79785796910E-05

-.29114891100E-02

.75818217580E+00

.87804881690E+03

.14231459890E-07

.16741461310E-03

-.32004479090E-01

.25617663720E-05

-.54759349410E-04

-.45050320580E-01

.20132546530E-05

-.16789412730E-07

.42073292710E-04

-.54442129960E-06

-.80048550110E+03

-.13193042010E+05

-.49549239300E+01

.80921321770E+04

-.98701040510E-02

.20204415620E+00

-.16374172050E-04

-.70389441360E-01

-.11543245390E-07

.15559901170E-05

-.14921785360E-10

-.10013560710E-08

.29339632160E-07

.0055542372

C **** ARGON COEFFICIENTS FOR VAPOR PRESSURE

C VP(1)= 3.4151115519 $ VP(2)= 1.1910812519

17
VP(3)= -.3407632334

VP(6)= 1.5

VP(7)= 83.80

VP(4)= 0.0

S VP(5)= .89555855251

$ VP(9)= .06890606625

$ VP(8)= 150.86

ARGON COEFFICIENTS FOR SATURATED LIQUID AND VAPOR DENSITIES,

1) = Z) = 3) = 4) =

5) = 6)-

7) =

A(A(

A(

A(

A(

A(

A(

A( 8) = A( 9) = A(10)=

A(ll)=

A(12)=

A(13)=

A(14)=

A(15)=

A(16)=

A(17)=

A(18)=

A(19)=

A(20)=

-.270262923777E+02

.131040241866E+00

-.267486438128E+01

.300176804406E+02

-.875899149326E+02

-.408267436456E+02

.104268066451E+03

-.671278555379E+02

.151002935701E+02

-.331243536637E+02

.633146212581E+02

-.427149706899E+02

.100599900030E+02

.137682084900E+02

-.664630363191E-01

.133368782730E+01

-.144371463244E+02

.501938472000E+02

-.230888463887E+02

.465318358887E+01   ARGON COEFFICIENTS FOR IDEAL GAS CP.

GI(1)=GI(2)-GI(3)=0

GI(4)=GI(9)-2.5

GI(5)=GI(6)=GI(7)=0

GI(8)=0

GI(10)=GI(11)=0.0

** ** ARGON COEFFICIENTS FOR FIRST TERM OF VISCOSITY EQN. **** VISCOSITY IN MICRO-PA*S, DENSITY IN G/CC.

GV(1)= .61145472787E+04 S GV(2)= -.10394390312E+05

GV(3)= .67594614619E+04 S GV(4)= - .22536509380E+04

6V(5)- .42593950138E+03 S GV(6)- -.47252671093E+02

GV(7)= .31795275425E+01 S GV(8)= - .11629083780E+00

GV(9)- .18043010592E-02 **** ARGON COEFFICIENTS FOR FIRST TERM OF THERMAL CONDUCTIVITY EQN. **** THERMAL CONDUCTIVITY IN WATT/(M*K), DENSITY IN G/CC.

GT(1)- .62777703742E+01 S GT(2)= -.96096376637E+01

GT(3)- .58887549191E+01 S GT(4)= - .18920926320E+01

GT(5)= .34886571437E+00 S GT(6)= -.38016786193E-01

GT(7)= .25207283167E-02 $ GT(8)= -.91098744478E-04

GT(9)= .13990842942E-05 **** ARGON COEFFICIENTS FOR SECOND TERM OF VISCOSITY EQN.

FV(1)= .14653652433E+00 S FV(2)= -.77487424965E-01

FV(3)= .14000000000E+01 S FV(4)= .15280000000E+03   ARGON COEFFICIENTS FOR SECOND TERM OF THERMAL CONDUCTIVITY EQN,

FT(1)- .24142103270E-01 S FT(2)= .75696234255E-02

FT(3)= .lOOOOOOOOOOE+01 $ FT(4)- .15280000000E+03 ** ** ARGON COEFFICIENTS FOR THIRD TERM OF VISCOSITY EQN.

18
EV(1)= -.12313579086E+02 $ EV(2)= .20694685712E+00

EV(3)= .16029145122E+02 $ EV(4)= .11717461351E+04

EV(5)= -.56995898780E+03 $ EV(6)= .40136071933E+02

EV(7)= .39870122403E+02 $ EV(8)= .53700000000E+00

C

C   ARGON COEFFICIENTS FOR THIRD TERM OF THERMAL CONDUCTIVITY EQN.

C ET(1)= -.33327027332E+02 $ ET(2)= 0.0

ET(3)= .30694859971E+02 $ ET(4)= 0.0

ET(5)= .22956551674E+04 $ ET(6)= -.35559415848E+03

ET(7)= 0.0 $ ET(8)= 1.0

CC ** ** ARGON COEFFICIENTS FOR MELTING EQUATION.

C PX(1)= -.210562165E+03

PX(2)= .177760527E+00

PX(3)= .159817868E+01

C THE FOLLOWING ARE CONSTANTS USED IN THE COMPUTATION OF PROPERTIES FOR

C ARGON

R=. 08205616*. 101325

T0=298.15 $ S0=154.7335 $ H0=6196.5

GI(10)-H0-HI(T0)

GI(11)=S0-SI(T0)

DTP=.3540027619188E+02

DTPV=. 1029227022329

TCC=VP(8)

PCC=VPN(TCC)

PTP=VP(9)

TTP=VP(7)

TUL=400.

TLL=TTP

PUL=100.

DCC=13.41

RETURN

END

C

C SUBROUTINE DATA C3

C COEFFICIENTS FOR ETHYLENE

DIMENSION A(20)

DIMENSION G(32),VP(9)

DIMENSION GV(9),GT(9),FV(4),FT(4),EV(8),ET(4)

C0MM0N/CPID/GI(11),GH(11),GL(11)

COMMON/CRIT/ EM, EOK, RM, TC, DC, X , PC, SIG

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

C0MM0N/DATA1/GV,GT,FV,FT,EV,ET

COMMON/ISP/N,NW,NWW

COMMON/SATC/A,DTPV

C0MM0N/DIEL/BX(5),PX(6)

N=0

PRINT 100

100 FORMAT(* THE TEMPERATURE RANGE FOR ETHYLENE IS 104 TO 400K*

1/* WITH PRESSURES TO 40 MPA*)

C

C **** ETHYLENE COEFFICIENTS FOR MBWR EQN

C

G( 1)= -.2146684366683E-02

G( 2)= .1791433722534E+00

G( 3)= -.3675315603930E+01

G( 4)= .3707178934669E+03

G( 5)= -.3198282566709E+05

G( 6)= .5809379774732E-04

G( 7)= -.7895570824899E-01

19
8)= .1148620375835E+02

9)= .2713774629iq3E+05

10)= -.8647124319107E-05

11)= .1617727266385E-01

12)= -.2731527496271E+01

13)= -.2672283641459E-03

14)= -.4752381331990E-02

15)= -.6255637346217E+01

16)= .4576234964434E-03

17)= -.7534839269320E-05

18)= .1638171982209E-01

19)= -.3563090740740E-03

20)= -.1833000783170E+05

21)= -.1805074209985E+07

22)= -.4794587918874E+03

23)= .3531948274957E+07

24)= -.2562571039155E+01

25)= .1044308253292E+03

26)= -.1695303363659E-01

27)= -.1710334224958E+03

28)= -.2054114462372E-04

29)= .6727558766661E-02

30)= -.1557168403328E-06

31)= -.1229814736077E-04

32)= .4234325938573E-04

GAMMA=-.0172

  ETHYLENE COEFFICIENTS FOR VAPOR PRESSURE

VP(1)= 8.2095798

VP(3)= -1.692585975

VP(6)= 1.5

VP(7)= 103.986

VP(4)= -.1976495575

VP(2)=

VP(5)=

VP(9)=

4.315424145

3.446501098

.00012129514

$ VP(8)= 282.3428

ETHYLENE COEFFICIENTS FOR SATURATED LIQUID AND VAPOR DENSITIES.

1)= -.609621515594E+02

2)= .203185312702E-01

3)= -.925441265813E+00

4)= .243630795888E+02

5)= -.854745622888E+03

6)= .123927868183E+04

7)= -.142710711789E+04

8)= .837358670405E+03

9)= .432203696552E+03

10)= -.137917541161E+04

11)= .126858600124E+04

12)= -.571552321713E+03

13)= .106012234360E+03

14)= -.479047060183E+01

15)= .151381345283E-01

16)= -.403456079445E+00

17)= .508683920225E+01

18)= -.246711997987E+02

19)= .980030915247E+01

20)= -.216846516122E+01

** ** ETHYLENE COEFFICIENTS FOR IDEAL GAS HEAT CP

GI(l)=.5603615762E+6

GI(2)=-.2141069802E+5

GI(3)=.2532008897E+3

GI(4)=.3554495281E+1

GI(5)=-.9951927478E-2

20
GI(6)=.5108931070E-4

GI(7)=-.1928667482E-7

GI(8)=-.2061703241E+2

GI(9)=.3E+4

GI(10)=GI(11)=0

T0=298.15 $ 50=219.451 $ H0=10564.6

GI(10)=H0-HI(T0)

GI(11)=S0-SI(T0)

C

C **** ETHYLENE COEFFICIENTS FOR MELTING EQUATION.

C PX(1)= -.357923875E+03

PX(2)= .245332143E-01

PX(3)= .206450000E+01

C THE FOLLOWING CONSTANTS USED IN THE COMPUTATION OF PROPERTIES FOR

C ETHYLENE

GAMMA=-.0172

R=. 08205616*. 101325

DTP=23. 34296694034

DTPV=.1425455127094E-03

EM=28.054

TCC=VP(8)

PCC=VPN(TCC)

PTP=VP(9)

TTP=VP(7)

TUL=400.

TLL=TTP

PUL=40.

DCC=7.650

RETURN

END

SUBROUTINE DATA P H2 DIMENSION G(32),VP(9),GI(11),GH(11),GL(11)

DIMENSION GV(9),GT(9),FV(4),FT(4),EV(8),ET(8)

DIMENSION A(20)

COMMON/SATC/A,DTPV

COMMON/CPID/GI,GH,GL

COMMON/CRIT/ EM, EOK, RM, TC, DC, X , PC, SIG

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

C0MM0N/DATA1/GV,GT,FV,FT,EV,ET

C0MM0N/DIEL/BX(6),PX(6)

COMMON/ISP/N,NW,NWW

N=l

PRINT 100

100 FORMAT(* THE TEMPERATURE RANGE FOR HYDROGEN IS 13.8 TO 400 K* 1/* WITH PRESSURES TO 120 MPA*)

C

C **** PARAHYDROGEN COEFFICIENTS FOR MBWR EQUATION.

C G( 1)= .4675528393416E-04

G( 2)= .4289274251454E-02

G( 3)= -.5164085596504E-01

G( 4)= .2961790279801E+00

G( 5)= -.3027194968412E+01

G( 6)= .1908100320379E-05

G( 7)= -.1339776859288E-03

G( 8)= .3056473115421E-01

G( 9)- .5161197159532E+01

G(10)= .1999981550224E-07

G(ll)= .2896367059356E-04

G(12)= -.2257803939041E-02

G(13)= -.2287392761826E-06

G(14)= .2446261478645E-05

21
G(15)= -.1718181601119E-03

G(16)= -.5465142603459E-07

G(17)= .4051941401315E-09

G(18)= .1157595123961E-06

G(19)= -.1269152728389E-08

G(20)= -.4983023605519E+01

6(21)= -.1606676092098E+02

G(22)= -.1926799185310E-01

G(23)= .9319894638928E+00

G(24)= -.3222596554434E-04

G(25)= .1206839307669E-03

G(26)= -.3841588197470E-07

G(27)= -.4036157453608E-05

G(28)= -.1250868123513E-10

G(29)= .1976107321888E-09

G(30)= -.2411883474011E-13

G(31)= -.4127551498251E-13

G(32)= .8917972883610E-12

GAMMA=-.0041

' PARAHYDROGEN COEFFICIENTS FOR VAPOR PRESSURE

VP(1)= 3.05300134164 $ VP(2)=

VP(3)= -0.655461216567 $ VP(5)=

VP(6)= 1.5814454428 $ VP(9)=

VP(7)= 13.8 $ VP(8)=

VP(4)= 0.0

2.80810925813

1.59514439374

0.0070420875

32.938

PARAHYDROGEN COEFFICIENTS. SATURATED LIQUID AND VAPOR DENSITIES,

1)= .916617720187E+02

2)= -.1794Q2524446E+00

3)= .454671158395E+01

4)= -.658499589788E+02

5)= .734466804535E+03

-6)= -.682501045175E+03

7)= .631783674710E+03

8)= -.539408873282E+03

9)= .430923811783E+03

10)= -.300295738811E+03

11)= .156567165346E+03

12)= -.504103608225E+02

13)= .720706926514E+01

14)= -.123944440318E+03

15)= .140334800142E+01

16)= -.211023804313E+02

17)= .173254622817E+03

18)= -.444294580871E+03

19)= .138699365355E+03

20)= -.235774161015E+02

  PARAHYDROGEN COEFFICIENTS FOR IDEAL GAS CP. FOR TEMPERATURES > 140 K.

GH( 1)= .5262185164597E+08

GH( 2)= -.1487906248823E+07

GH( 3)= .1601391392264E+05

GH( 4)= -.8031235938946E+02

GH( 5)= .2307407941873E+00

GH( 6)= -.3176386248370E-03

GH( 7)= .1643857271214E-06

GH( 8)= .9230816464058E+01

GH( 9)= .3E+4

GH(10)= 0.0

GH(11)= 0.0

22
cC ** ** PARAHYDROGEN COEFFICIENTS FOR IDEAL GAS CP.

C FOR TEMPERATURES 40 < T < 140 K.

C GL( 1)= .2905965792270E+06

GL( 2)= -.2831103639248E+05

GL( 3)= .1050424877391E+04

GL( 4)= -.1535751501769E+02

GL( 5)= .1218941696566E+00

GL( 6)= -.2599406479908E-04

GL( 7)= -.1288757333406E-05

GL( 8)= .1717441975231E+06

GL( 9)= .3E+4

GL(10)= 0.0

GL(11)= 0.0

T0=298.15 $ S0=130.407 $ H0=8409.8

C HO AND SO TAKEN FROM WOOLLEY, SCOTT, AND BRICKWEDDE

C NBS RP 1932, PAGE 387. VALUES FOR PARAHYDROGEN.

GH(10)=H0-HI(T0)

GL(10)=GH(10)

GH(11)=S0-SI(T0)

GL(11)=GH(11)

C

CC   PARAHYDROGEN COEFFICIENTS FOR MELTING PRESSURE.

C FOR TEMPERATURES < 22 K : C PX(1)= -21.281484395

PX(2)- .125746643

PX(3)= 1.955

C

C ** ** PARAHYDROGEN COEFFICIENTS FOR MELTING PRESSURE.

C FOR TEMPERATURES > 22 K : C PX(4)= -26.5289115

PX(5)= .248578596

PX(6)= 1.764739

C

C **** PARAHYDROGEN COEFFICIENTS FOR DIELECTRIC CONSTANT.

C BX(1)= .20245443E-02

BX(2)= .37171832E-06

BX(3)= -.92085013E-08

BX(4)= -.34065328E-11

BX(5)= .0 BX(6)= .0

C THE FOLLOWING ARE CONSTANTS USED IN THE COMPUTATION OF PROPERTIES FOR

C PARAHYDROGEN

R=. 08205616*. 101325

DTP=.3821428945438E+02

DTPV=.6322296353698E-01

EM=2. 01594

TCC=VP(8)

PCC=VPN(TCC)

PTP=VP(9)

TTP=VP(7)

TUL=400.

TLL=TTP

PUL=120.

DCC=15.556

RETURN

END

23
SUBROUTINE DATA N2 DIMENSION G(32),VP(9)

DIMENSION GV(9),GT(9),FV(4),FT(4),EV(8),ET(8)

DIMENSION A(20)

COMMON/CRIT/ EM, EOK, RM, TC, DC, X , PC, SIG

COMMON/SATC/A,DTPV

C0MM0N/DATA1/GV,GT,FV,FT,EV,ET

COMMON/SEN/BETA, XO, DELTA, El, E2, AGAM

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

C0MM0N/CPID/GI(11),GH(11),GL(11)

COMMON/ISP/N,NW,NWW

C0MM0N/DIEL/BX(6),PX(6)

NWW=0

PRINT 100

100 FORMAT(* THE RANGE OF TEMPERATURE FOR NITROGEN IS 63.15 TO 1900K*

1/* WITH PRESSURES TO 1000 MPA*)

N=0 $ NW=1

E0K=118. $ RM=3.933E-08 $ TC=126.24

X=l. 67108 l; PC=3.443 $ SIG=3.54

BETA=0.355 $ DELTA=4.352 $ El=2.17 S E2=0.287

EM=28.016 : DC=0.3139 3 X0=0.164 ; AGAM=1.190

NITROGEN COEFF FOR MBWR EQUATION

1)= .138029747465691E-03

2)= .108450650134880E-01

3)= -.247132406436209E+00

4)= .345525798080709E+01

5)= -.427970769066595E+03

6)= .106491156699760E-04

7)= -.114086707973499E-02

8)= .144490249728747E-04

9)= .187145756755327E+04

10)= .821887688683079E-08

11)= .236099049334759E-03

12)= -.514480308120135E-01

13)= .491454501366803E-05

14)= -.115162716239893E-03

15)= -.716803724664983E-01

16)= .761666761949981E-05

17)= -.113093006621295E-06

18)= .373683116683089E-04

19)= -.203985150758086E-06

20)= -.171966200898966E+04

21)= -.121305519974777E+05

22)= -.988139914142789E+01

23)= .561988689351085E+04

24)= -.182304396411845E-01

25)= -.259982649847705E+00

26)= -.419189342315742E-04

27)= -.259640667053023E-01

28)= -.125868320192119E-07

29)= .104928659940046E-05

30)= -.545836930515201E-10

31)= -.767451167059717E-09

32)= .593123287099439E-08

GAMMA=-.0056

**** NITROGEN COEFF FOR VAPOR PRESS.

VP(1)= 5.1113192094

VP(3)= -.15108730916

VP(6)= 1.5

VP(7)= 63.15

VP(2)=. 6482667539

VP(5)=. 74028493342

VP(9)=. 012462975

VP(8)= 126.26

24
VP(4)= 0.0

' HZ COEF FOR SAT LIQUID AND VAPOR DENS.

A( 1)= -.158453465507E+02

A( 2)= .419136911423E-01

A( 3)= -.101965371660E+01

A( 4)= .134763743799E+02

A( 5)= -.109930399087E+03

A( 6)= .925518835497E+02

A( 7)= -.956233831320E+02

A( 8)= .100104366710E+03

A( 9)= -.701857937398E+02

A(10)= .900076998647E+01

A(ll)= .286981120347E+02

A(12)= -.216767601780E+02

A(13)= .496558226471E+01

A(14)= .218307928477E+02

A(15)= -.126493309807E+00

A(16)= .241544188633E+01

A(17)= -.245256871794E+02

A(18)= .935925207124E+02

A(19)= -.36Q938251632E+02

A(20)= .757453271989E+01

  N2 COEF FOR IDEAL GAS CP.

GI(1)= -0.735210401157252E 03

GI(2)= 0.342239980411978E 02

6I(3)= -0.557648284567620E 00

GI(4)= 0.350404228308756E 01 GI(5)= -0.173390185081005E-04

GI(6)= 0.174650849766463E-07

GI(7)= -0.356892033544348E-11

GI(8)= 0.100538722808834E 01 GI(9)= 0.335340610000000E 04

GI(10)=GI(11)=0.0

-** * N2 COEF FOR 1ST TERM OF VISC

Vise IN MICRO PA*S, DENSITY IN G/CC

GV(1)= -.18224240000E+05 $ GV(2)=

GV(3)= -.91542324494E+04 $ GV(4)=

GV(5)= -.36307214228E+03 $ GV(6)=

GV(7)= -.22261880817E+01 $ GV(8)=

GV(9)= -.11894029104E-02

.19915327374E+05

.23255484059E+04

.36457506811E+02

.78053904895E-01

**** N2 COEF FOR 1ST TERM THERM. COND.

THERM. COND. IN WATT/(M*K), DENS. IN G/CC,

GT(1)= -.20029573972E+02 $

GT(3)= .80188959378E+01 $

GT(5)= .15363738965E+01 $

GT(7)= .19360547346E-01 $

GT(9)= .15564670935E-04

**** N2 COEF FOR 2ND TERM VISC.

GT(2)=

GT(4)=

GT(6)=

GT(8)=

FV(1)= -.11217739623E+00 $ FV(2)=

FV(3)= .14000000000E+01 $ FV(4)=   N2 COEF FOR 2ND TERM THERM. COND.

FT(1)= .53875666637E-01 $ FT(2)=

FT(3)= .12000000000E+01 $ FT(4)=

.49765746684E+01

-.55022716888E+01

-.22974737257E+00

-.85677385768E-03

.32912317244E-01

.11800000000E+03

.61027911104E-02

.11800000000E+03

25
** ** N2 COEF FOR 3RD. TERM VISC.

EV(1)= -.12128154129E+02 $ EV{2)=

EV(3)= .16094611148E+02 $ EV(4)=

EV(5)= -.80889801180E+03 $ EV(6)=

EV(7)= -.21241135912E+01 $ EV(8)=

.57156092139E+00

.36954086158E+04

.68464435640E+02

.31500000000E+00

N2 COEF FOR 3RD TERM OF THERM. COND.

ET(1)= -.38613291627E+02 : ET(3)= .37201743333E+02 : ET(5)= -.39013509079E+02 : ET(7)= .0 ;

  N2 COEF FOR MELTING.

PX(1)= -.160000281E+03

PX(2)= .938575502E-01

PX(3)= .179500000E+01

** ** N2 COEF FOR DIEL. CONST.

ET(2)= .0 ET(4)= .0 ET(6)= -.31826109485E+02

ET(8)= 1.0

BX(1)^

BX(2)^

BX(3)- 0. BX(4)=

BX(5) = BX(6) =

.43993836E-02

.18932096E-05

.31450178E-08

.28592703E-06

.44566034E-07

THE FOLLOWING ARE CONSTANTS USED IN THE COMPUTATION OF PROPERTIES FOR

NITROGEN

R=(8.20539E-2)*. 101325

T0=298.15 $ S0=191.502

GI(10)=H0-HI(T0)

GI(11)=S0-SI(T0)

DTP=.3097717741477E+2

DTPV=.242822085710E-1

TCC-VP(8)

PCC=VPN(TCC)

PTP=VP(9)

TTP=VP(7)

TUL=1900.

TLL=TTP

PUL=1000.

DCC=11.21

RETURN

END

$ H0=8669.0

SUBROUTINE DATA NF3

DIMENSION G(32),VP(9),A(20)

COMMON/CRIT/ EM, EOK, RM, TC , DC, X , PC, SIG

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

COMMON/SATC/A,DTPV

C0MM0N/CPID/GI(11),GH(11),GL(11)

C0MM0N/DIEL/BX(6),PX(6)

PRINT 100

100 F0RMAT(* THE RANGE OF TEMPERATURE FOR NITROGEN TRIFLUORIDE IS*

A ,/,* 66.36 K TO 500 K, WITH PRESSURES TO 50 MPA.*)

CC **** NITROGEN TRIFLUORIDE COEFFICIENTS FOR MBWR EQUATION.

C

G( 1)= .1774353868E-02

G( 2)= -.5409379418E-01

G( 3)= .3976634466E+00

G( 4)= -.5209476694E+02

G( 5)= -.3285322888E+04

26
6)= -.5990517411E-04

7)= .9217525601E-01

8)= -.4848977075E+02

9)= -.4235892691E+06

10)= -.9824248063E-06

11)= .5432235989E-02

12)= -.1462388500E+01

13)= -.3366180440E-03

14)= .2801374599E-01

15)= .8435288597E+00

16)= -.1324421452E-02

17)= .1875604377E-04

18)= .2959643991E-01

19)= -.7009976870E-03

20)= .4365820912E+06

21)= -.1111397536E+07

22)= .2411866612E+04

23)= .3179136276E+06

24)= .6166849090E+01

25)= .4260854720E+01

26)= .1090598789E-01

27)= -.3340951059E+01

28)= .8597429644E-05

29)= .1240544214E-03

30)= .1286224248E-07

31)= -.8941104276E-07

32)= .3353054595E-05

GAMMA=-.0056

' NITROGEN TRIFLUORIDE COEFFICIENTS FOR VAPOR PRESSURE,

VP(1)=

VP(3)=

VP(6)=

VP(7)=

VP(4)=

11.593879492

-2.8727732815

1.5

66.36

-1.37977007

$ VP(2)= 9.6548502312

$ VP(5)= 7.3112441673

$ VP(9)= .18537827E-6

$ VP(8)= 234.0

NITROGEN TRIFLUORIDE COEFF. FOR SATURATED LIQUID AND VAPOR DENSITIES

1) = .131285181636E+03

2) = -.226998555536E+01

3) = .384708389498E+02

4) = -.309827268239E+03

5) = -.635348526635E+03

6) = .926979028357E+03

7) = .371498011259E+03

8) = -.182291654470E+04

9) = .105592403853E+04

10) = .121673895344E+04

11) = -.207208928323E+04

12) = .113463394710E+04

13) = -.226642137140E+03

14) = .105087295173E+01

15) = -.131686474246E-02

16) = .390141331900E-01

17) = -.587796597975E+00

18) = .400900521017E+01

19) = -.203385386977E+01

20) = .400434364424E+00

  NITROGEN TRIFLUORIDE COEFF CIENTS FOR IDEAL GAS CP

GI(1)= .7427518245951E+06

GI(2)= -.4389825372134E+05

GI(3)= .1012629224351E+04'

27
GI(4)= -.7140693612211E+01

GI(5)= .5481339146452E-01

GI(6)= -.7677196006769E-04

GI(7)= .4203630864340E-07

GI(8)= -.6328752997967E+00

GI(9)= .3E+4

GI(10)=GI(11)=0.0

C

C ** ** NITROGEN TRIFLUORIDE COEFFICIENTS FOR MELTING.

C PX(1)= -.190939971E+03

PX(2)= .813750194E-01

PX(3)= .185000000E+01

C THE FOLLOWING ARE CONSTANTS USED IN THE COMPUTATION OF PROPERTIES FOR

C NITROGEN TRIFLUORIDE

C**- THE TO, HO, SO IDEAL GAS REFERENCE VALUES ARE FROM

C TO, HO, SO ARE FROM NBS TN 270-3('68), "SELECTED VALUES OF CHEMICAL

C THERMODYNAMIC PROPERTIES" WAGMAN ET AL., PP 70 T0=298.15 $ S0=260.621 $ HO-11828.

GI(10)=H0-HI(T0)

GI(11)=S0-SI(T0)

EM=71.019

R=. 0820568*. 101325

PTP-.185425E-06

DTP=26.32

DTPV-.33612E-08

TTP=66.36

PCC=4.4607

DCC=7.92

TCC=234.0

TC=234.0

VP(8)=TC

DC=7.92

PUL= 50.

TUL=500.

TLL=TTP

RETURN

END

SUBROUTINE DATA 02 DIMENSION G(32),VP(9),GI(11),GH(11),GL(11)

DIMENSION GV(9),GT(9),FV(4),FT(4),EV(8),ET(8)

DIMENSION A(20)

COMMON/SATC/A,DTPV

COMMON/DATAl /GV ,GT , FV , FT , EV , ET COMMON/SEN/BETA, XO, DELTA, El, E2, AGAM

COMMON/CRIT/ EM, EOK, RM, TC, DC, X , PC, SIG

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

COMMON/ISP/N,NW,NWW

COMMON/CPID/GI,GH,GL

C0MM0N/DIEL/BX(6),PX(6)

N=0 $ NW=1 $ NWW=0

PRINT 100

100 FORMAT!* THE TEMPERATURE RANGE FOR OXYGEN IS 54.359 TO 400 K* 1/* WITH PRESSURES TO 120 MPA*)

X0=0.183 $ BETA=0.355 $ DELTA=4.352 $ El=2.21 $ E2=0.287

EM=31.9988 $ E0K=113.0 $ RM=3.8896E-08$ TC=154.575

DC=0.4362 $ X=2. 210636 $ PC=5.0429 $ SIG-3.437

AGAM = 1.190

C

C **** OXYGEN COEFFICIENTS FOR MBWR EQUATION.

C

G( 1)= -.4365859650E-04

G( 2)= .2005820677E-01

G( 3)= -.4197909916E+00

G( 4)= .1878215317E+02

28
G( 5)= -.1287473398E+04

G( 6)= .1556745888E-05

G( 7)= .1343639359E-03

G( 8)= -.2228415518E+00

G( 9)= .4767792275E+03

G(10)= .4790846641E-07

G(ll)= .2462611107E-03

G(12)= -.1921891680E-01

G(13)= -.6978320847E-06

G(14)= -.6214145909E-04

G(15)= -.1860852567E-01

G(16)= .2609791417E-05

G(17)= -.2447611408E-07

G(18)= .1457743352E-04

G{19)= -.1726492873E-06

G(20)= -.2384892520E+03

G(21)= -.2301807796E+05

G(22)- -.2790303526E+01

G(23)= .9400577575E+04

G(24)= -.4169449637E-02

G(25)= .20n8497853E+00

G(26)= -.1256076520E-04

G(27)= -.6406362964E-01

G(28)= -.2475580168E-08

G(29)= .1346309703E-05

G(30)= -.116150247nE-10

G(31)= -.1034699798E-08

G(32)- .2365936964E-07

GAMMA=-.0056

' OXYGEN COEFFICIENTS FOR VAPOR PRESSURE,

VP(1)=

VP(3)=

VP(6)=

VP(7)-

VP(4)=

7.568956

-2.13746

1.514

54.359

0.0

VP(2)= 5.004836

VP(5)= 3.454481

VP(9)= .0001479953

VP(8)= 154.581

OXYGEN COEFFICIENTS FOR SATURATED LIOUID AND VAPOR DENSITIES.

1)= .581394753076E+02

2)= -.490241196133E-01

3)= .168328893252E+01

4)= -.325161223398E+02

5)= .550300989872E+03

6)= -.510968506115E+03

7)= .315091559049E+03

8)= -.232566659258E+02

9)= -.488425479359E+02

10)= -.150624217523E+03

11)= .280441603851E+03

12)= -.176693896861E+03

13)= .403247747449E+02

14)= .252198688365E+01

15)= -.136098316472E-01

16)= .282316159403E+00

17)= -.286645905341E+01

18)= .617024212284E+01

19)= -.810220795462E+00

20)= -.279601068969E+00

  OXYGEN COEFFICIENTS FOR IDEAL GAS CP.

GI(1)= -0.498199853711943E 04

GI(2)= 0.230247779995218E 03

29
GI(3)= -0.345565323510732E 01 GI(4)= 0.352187677367116E 01 GI(5)= -0.435420216024420E-04

GI(6)= 0.134635345013162E-07

GI(7)= 0.162059825959105E-10

GI(8)= 0.103146851572565E 01 GI(9)= 0.223918105000000E 04

GI(10)=GI(11)=0.0

** ** OXYGEN COEFFICIENTS FOR FIRST TERM OF VISCOSITY EQN,

VISCOSITY IN MICRO-PA*S, DENSITY IN G/CC.

GV(1)= -.97076378593E+04

GV(3)= -.24668758803E+04

GV(5)= .37851049522E+02

GV(7)= .11134441304E+01

GV(9)= .10279379641E-02

$ GV(2)= .82801254201E+04

$ GV(4)= .21324360243E+03

$ GV(6)= -.10487216090E+02

$ GV(8)= -.53676093757E-01

**** OXYGEN COEFFICIENTS FOR FIRST TERM OF THERMAL CONDUCTIVITY EQN,

THERMAL CONDUCTIVITY IN WATTS/(M*K), DENSITY IN G/CC.

GT(1)= -.20395052193E+03 $ GT(2)= .24088141709E+03

GT(3)= -.12014175183E+03 $ GT(4)= .32954949190E+02

GT(5)= -.54244239598E+01 $ GT(6)= .54734865540E+00

GT(7)= -.32854821539E-01 $ GT(8)= .10753572103E-02

GT(9)- -.14610986820E-04 **** OXYGEN COEFFICIENTS FOR SECOND TERM OF VISCOSITY EQN.

FV(1)= .43526515153E+00 $ FV(2)= -.20361263878E+00

FV(3)= .14000000000E+01 $ FV(4)= .lOOOOOOOOOOE+03   OXYGEN COEFFICIENTS FOR SECOND TERM OF THERMAL CONDUCITIVY EQN,

FT(1)= .30600000000E-01 $ FT(2)= .27850000000E-01

FT(3)- .11200000000E+01 $ FT(4)= .lOOOOOOOOOOE+03 ** ** OXYGEN COEFFICIENTS FOR THIRD TERM OF VISCOSITY EQN.

EV(1)= -.14454972110E+02 $ EV(2)= -.31421728994E+00

EV(3)= .18201161468E+02 $ EV(4)= .27390429525E+03

EV(5)= -.27498956948E+04 $ EV(6)= .24340689667E+03

EV(7)= .11911504104E+03 $ EV(8)= .43500000000E+00

**** OXYGEN COEFFICIENTS FOR THIRD TERM OF THERMAL CONDUCTIVITY EQN.

.0

.0.47350508788E+03

ET(1)= -.21520741137E+02 $ ET(2)=

ET(3)= .16799504261E+02 $ ET(4)=

ET(5)= -.29944878721E+04 $ ET(6)=

ET(7)= .0 $ ET(8)= 1.0

' OXYGEN COEFFICIENTS FOR MELTING

PX(1)= -.267226854E+03

PX(2)= .227606348E+00

PX(3)= .176900000E+01

OXYGEN COEFFICIENTS FOR DIELECTRIC CONSTANT.

BX(1)=

BX(2)=

BX(3)=

.39608100E-02

.29700000E-06

.41300000E-07

BX(4)= 0.0

BX(5)= 0.0

BX(6)= -.21400000E-07

30
C THE FOLLOWING ARE CONSTANTS USED IN THE COMPUTATION OF PROPERTIES FOR

C OXYGEN

C TO, HO, SO ARE FROM NBS TN270 (SELECTED VALUES OF CHEM THERMO PROPS)

C PAGE 11. COMPUTED IDEAL GAS PROPS CONFORM TO JANAF( NSRDS-NBS37(71)

)

T0=298.15 $ S0=205.029 $ H0=8680.1

GI(10)= HO-HI(TO)

GI(11)= SO-SI(TO)

R=8.20539E-2*. 101325

DTP=.4081997364372E+02

DTPV=.3318894767078E-03

TCC=VP(8)

PCC=VPN(TCC)

PTP=VP(9)

TTP=VP(7)

TUL=400.

TLL=TTP

PUL=120.

DCC=13.63

RETURN

END

31
Appendix F. Properties Subroutines

SUBROUTINE PROPS(PP,DD,TT)

C THE 32 TERM EQUATION OF STATE, INPUT IS DENSITY(MOLES/L)

,

C TEMPERATURE(K), OUTPUT (PP) IS PRESSURE(MPA) ,0R DP/DD IN

C LITER-MP A/MOLE OR DP/DT MPA/K OR S,H,OR CV AT ONE LIMIT OF

C INTEGRATION

DIMENSION X(33)

DIMENSION B(33),G(32),VP(9)

EQUIVALENCE (B,X)

C0MM0N/DATA/G,R,GAMMA3VP,DTP,PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

COMMON/1/B

DATA{ID=1)

DATA(IZ=1)

1 CONTINUE

IF(IZ.LE.O)GO TO 2 IZ=0

2 CONTINUE

D=DD

P=PP

T=TT

GM=GAMMA

02=0*0

D3=D2*D

D4=D3*D

D5=D4*D

D6=D5*D

D7=D6*D

D8=D7*D

D9=D8*D

D10=D9*D

D11=D10*D

D12=D11*D

D13=D12*D

TS=SQRT (T)

T2=T*T

T3-T2*T

T4=T3*T

T5-T4*T

F=EXP (GM*D2)

GO TO (100, 200, 300, 400, 500, 600, 700),

K

ENTRY PRESS

C ENTRY FOR PRESSURE, INPUT IS DENSITY

C AND TEMP. IN MOL/L AND K, OUTPUT IS IN MPA.

K=l

GO TO 1 00 CONTI

B( 1)

B( 2)

B( 3)

B( 4)

B( 5)

B( 6)

B( 7)

B( 8)

B( 9)

B( 10)

B( 11)

B( 12)

B( 13)

B( 14)

R( 15)

B( 16)

B( 17)

NUE =D2*T

=D2*TS

=D2

=D2/T

=D2/T2

=D3*T

=D3

=D3/T

=D3/T2

=D4*T

=D4

=D4/T

=D5

=D6/T

=D6/T2

=D7/T

-D8/T

32
B(18)=D8/T2

B(19)=D9/T2

B(20)=D3*F/T2

B{21)=D3*F/T3

B(22)=D5*F/T2

B(23)-D5*F/T4

B(24)=D7*F/T2

B(25)=D7*F/T3

B(26)=D9*F/T2

B(27)=D9*F/T4

B(28)=D11*F/T2

B(29)=D11*F/T3

B(30)=D13*F/T2

B(31)=D13*F/T3

B(32)=D13*F/T4

IF(ID.GT.O)GO TO 102

B(33)=P-R*D*T

RETURN

102 P=0

M=32

DO 101 1=1,

M

101 P=P+B(I)*G(I)

P=P+R*D*T

PP=P RETURN

ENTRY DPDD

C PARTIAL OF PRESSURE WITH RESPECT TO

C DENSITY - SEE PRESSURE

C ENTRY FOR UNITS

K=2

GO TO 1 200 CONTINUE

F1=2.00*F*GM*D

F21=3.000*F*D2

F22=5.000*F*D4

F23=7.000*F*D6 +F1*D7

F24=9.000*F*D8 +F1*D9

+F1*D3

+F1*D5

F25 = F26=

12

34

56

78

910

111213

14

15

16

17

1819

20

2122

23

24

25

26

1.00*F*D10+F1*D11

3.00*F*D12+F1*D13

=2.00*D*T

=2.00*D*TS

00*D

00*D/T

00*D/T2

00*D2*T

00*D2

=3.00*D2/T

=3.00*D2/T2

=4.00*D3*T

=4.Q0*D3

=4.00*D3/T

=5,00*n4

=6.00*D5/T

=6.00*D5/T2

=7.00*D6/T

=8.00*D7/T

=8.00*D7/T2

=9.00*D8/T2

=F21/T2

=F21/T3

=F22/T2

=F22/T4

=F23/T2

=F23/T3

=F24/T2

33
B(27)=F24/T4

B(28)=F25/T2

P(29)=F25/T3

B(30)=F26/T2

B(31)-F26/T3

B(32)=F26/T4

M=32

IF(ID.GT.O)GO TO 202

B(33)=P-R*T

RETURN

202 P=0

DO 201 1=1,

M

201 P=P+B(I)*G(I)

P=P+R*T

PP=P RETURN

ENTRY DPDT

C PARTIAL OF PRESSURE WITH RESPECT

C TO TEMPERATURE - SEE PRESSURE

C ENTRY FOR UNITS

K = 3 GO TO 1 300 CONTINUE

X( 1)=D2

X( 2)=D2/(2.00*TS)

X( 3)=0

X( 4)=-D2/T2

X( 5)=-2.00*D2/T3

X( 6)=D3

X( 7)=0

X( 8)=-D3/T2

X( 9)=-2.00*D3/T3

X(10)=D4

X(11)=0

X(12)=-D4/T2

X(13)=0

X(14)=-D6/T2

X(15)=-2.00*D6/T3

X(16)=-n7/T2

X(17)=-D8/T2

X(18)=-2.00*D8/T3

X(19)=-2.00*D9/T3

X(20)=-2.00*n3*F/T3

X(21)=-3.00*D3*F/T4

X(22)=-2.00*D5*F/T3

X(23)=-4.00*D5*F/T5

X(24)=-2.00*D7*F/T3

X(25)=-3.00*D7*F/T4

X(26)=-2.00*D9*F/T3

X(27)=-4.00*D9*F/T5

X(28)=-2.00*D11*F/T3

X(29)=-3.00*D11*F/T4

X(30)=-2.00*D13*F/T3

X(31)=-3.00*D13*F/T4

X(32)=-4.00*D13*F/T5

IF(ID.GT.0)G0 TO 302

X(33)=PP-R*D

RETURN

302 P=0 no 301 1=1,32

301 P=P+G(I)*X(I)

PP=P+R*D

RETURN

ENTRY DSDN

C PARTIAL OF ENTROPY WITH

34
+CPOS(T)

RESPECT TO THE G COEFFICIENTS

K=4

GO TO 1 400 CONTINUE

S=S0-R*L0GF(D*R*T/P0)+(DSDN(D)-DSDN(O))*1000,

G1=F/(2.00*GM)

G2=( F*D2-2 .00*G1 ) /( 2 .00*GM)

G3=(F*D4-4.00*G2)/(2.00*GM)

G4=(F*D6-6.00*G3)/(2.00*GM)

G5= ( F*D8-S .00*G4 ) / ( 2 . 0O*GM)

G6= ( F*D10-10 .00*G5 )/( 2 .00*GM)

=-D =-D/(2.00*TS)

=0.D0

=+D/T2

=2.00*D/T3

=-D2/2.00

-O.DO

=D2/(2.00*T2)

=D2/T3

I--D3/3.00

=0.D0

l=D3/(3.00*T2)

=0.D0

l=D5/(5.00*T2)

= 2.00*D5/(S.00*T3)

=D6/(6.00*T2)

=D7/(7.00*T2)

=2.00*D7/(7.00*T3)

i=D8/(4.0n*T3)

=2.00*G1/T3

I=3.00*G1/T4

=2.00*G2/T3

=4.00*G2/T5

=2.00*G3/T3

l=3.00*G3/T4

=2.nO*G4/T3

=4.no*G4/T5

=2.00*G5/T3

=3.00*G5/T4

-2.00*G6/T3

=3.00*G6/T4

=4.00*G6/T5

IF(ID.GT.0)G0 TO 402

RETURN

402 P=0

DO 401 1-1,32

401 P-P+G(I)*X(I)

PP-P RETURN

ENTRY DUDN

C TERMS NEEDED FOR ENTHALPY CALCULATION

K=F GO TO 1 500 CONTINUE

C H=H0+(T*DSDN(D)-DSDN(0))*1000.+(DUDN(D-DUDN(0))*1000.+CP0H(T)

C +(P/D-P*T)*1000.

G1-F/(2.00*GM)

G2=(F*D2-2.00*G1)/(2.00*GM)

G3=(F*D4-4.00*G2)/(2.00*GM)

G4=(F*D6-6.00*G3)/(2.00*GM)

G5=(F*D8-8.00*G4)/(2.00*GM)

G6=(F*D10-10.00*G5)/(2.00*GM)

X( 1)=D*T

X( 2)=D*TS

X [ 1)

X [ 2)

X [ 3)

X [ 4)

X [ 5) X 6)

X 7)

X 8)

X 9)

X 10)

X 11)

X 12)

X 13)

X 14)

X 15)

X( 16)

X 17)

X 18)

X 19)

X 20)

X 21)

X 22)

X 23)

X 24)

X 25)

x( 26)

X 27)

X( 28)

X 29)

X 30)

X 31)

X 32)

35
X( 3 =D

Xf 4 =D/T

X( 5 -D/T2

X{ 6 )=D2*T/2.00

X( 7 )=D2/2.00

X( 8 )=D2/(2.00*T)

X( 9 )=D2/(2.00*T2)

X(10 )=D3*T/3.00

X(ll =D3/3.00

X(12 =D3/(3.00*T)

X(13 )=D4/4.00

X(14 =D5/(5.00*T)

X(15 =D5/(5.00*T2)

X(16 )=D6/(6.00*T)

X(17 =D7/(7.00*T)

X(18 )=D7/(7.00*T2)

X(19 )=D8/(8.00*T2)

X(20 =G1/T2

X(21 =G1/T3

X(22 =G2/T2

X(23 =G2/T4

X(24 =G3/T2

X(25 -G3/T3

X(26 =G4/T2

X(27 =G4/T4

X(28 =G5/T2

X(29 )=G5/T3

X(30 =G6/T2

X(31 =G6/T3

X(32

IF(I[

=G6/T4

).GT.0)G0 TO 502

RETU?m

502 P=0

DO 5(n 1=1,32

501 P=P+Cun*x(i)

PP = P RETUfni EMTR^( TDSDT

C TEMP TIMES THE PARTIAL OF

C EMTR()PY WITH RESPECT TO TEMP. K=6

GO T() 1 600 COMT [HUE

c cv=c\/0+(TDSDN(/)-TDSDM(D))*1000

G1=F/a2.00*GM)

G2=(F*D2-2.00*Gl)/(2 00-^GM)

G3 = (F-*D4-4.00*G2)/(2 00^^GM)

G4=(F-*D6-6.00*G3)/(2 00^^GM)

G5-(F*D8-8.00*G4)/(2 00*GM)

G6=(F-*Din-10.00*G5)/(2.(30*GM)

X(l) ==0 X( 2 =-D/(4.00*TS)

X(3)^=0 X( 4 =2.00*D/T2

X( 5 =6.00*D/T3

X(6) ==0 X(7)=0

X( 8)=D2/T2

X( 9)=3.00*D2/T3

X(10)=0

X(11)=0

X(12)=(2.00*D3)/(3.00*T2)

X(13)=0

X(14)=(2.0n*D5)/(5.00*T2)

X(15)=(6.00*D5)/(5.00*T3)

36
X(16)=D6/(3.00*T2)

X(17)-(2.00*D7)/(7.00*T2)

X(18)=(6.00*D7)/(7.00*T3)

X(19)-(3. 00*08)7(4. 00*T3)

X(20)=6.000*G1/T3

X(21)=12.00*G1/T4

X(22)=6.000*G2/T3

X(23)=20.00*G2/T5

X(24)=6.000*G3/T3

X(25)=12.00*G3/T4

X(26)-6.00n*G4/T3

X(27)=20.00*G4/T5

X(28)-6.000*G5/T3

X(29)=12.00*G5/T4

X(30)=6.00n*G6/T3

X(31)=12.00*G6/T4

X(32)=2n.00*G6/T5

IF(ID.GT.0)G0 TO 602

RETURN

602 P=0

DO 601 1=1,32

601 P=P+G(I)*X(I)

PP=P RETURN

ENTRY DP2D2

SECOND PARTIAL OF PRESSURE WITH

RESPECT TO DENSITY SQUARED

K=7

GO TO 1 700 CONTINUE

F1=2.*F*GM*D

F12=2.*F1*GM*D+2.*F*GM

F212=3.*F1*D2+3.*2.*D*F+F12*D3+F1*3.*

F222=5 .*F1*D4 +5 .*4 .*D3*F+5 .*D4*F1+F1

F232=7 .*Fl*D6+7 .*6 .*D5*F+7 .*D6*F1+F12

F242=9 .*F1*D8+P .*8 .*D7*F+9 .*D8*F1+F12

F252=11.*F1*D10+10.*11.*D9*F+11.*D10*

F262=13.*F1*D12+13.*12.*D11*F+13.*D12

B(1)=2.*T $B(2)=2.*TS $ B(3)=2.

B(4)=2./T $ B(5)=2./T2 $ B(6)=6.*

B(7)=6.*D $ B(8)=6.*D/T S B(9)=6

B(10)=12.*D2*T $ B(11)=12.*D2 $ B B(14)=30.*D4/T S P

S B(17)=56.*D6/T $

% B(20)=F212/T2 S

702

701

B(13)=20.*D3 $

B(16)=42.*D5/T

B(19)=72.*D7/T2

B(22)=F222/T2

B(23)=F222/T4 $

R(26)=F242/T2 $

B(29)=F252/T3 $

B(32)=F262/T4

M=32

IF(ID.GT.O)GO TO 702

B(33)=PP

RETURN

P=0

DO 701 1=1,

M

P=P+B(I)*G(I)

PP=P RETURN

END

B(24)=F232/T2

B(27)=F242/T4

B(30)=F262/T2

D2

2*05

*07

*D9

F1+F12*D11

*F1+F12*D13

0*T

*D/T2

(12)=12.*02/T

(15)=30.*D4/T2

B(18)=56.*D6/T2

B(21)=F212/T3

$ B(25)=F232/T3

$ B(28)=F252/T2

$ B(31)=F262/T3

FUNCTION VPN(TT)

CALCULATES VAPOR PRESSURE(MPA] INPUT IS TEMP(K)

37
DIMENSION G(32),VP(9)

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

T=TT

X=(1.-VP(7)/T)/(1.-VP(7)/VP(8))

VPN=VP(9)*EXP (VP(1)*X+VP{2)*X*X+VP(3)*X**3+VP(4)*X**4+VP(5)*X1(1.-X)**VP(6))

RETURN

END

FUNCTION FINDTV(POBS)

C ITERATES VAPOR PRESS EON TO FIND TEMP(K), FOR INPUT OF PRESS(MPA).

C GIVEN AN INPUT PRESSURE( MPA)

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

DIMENSION G(32),VP(9)

T=VP{8)

DO 7 1=1,10

P=VPN(T)

IF(ABS (P-P0BS)-.000001*P0BS)8,8,6

6 CONTINUE

CORR=(PnBS-P)/DPDTVP(T)

7 T=T+CORR

8 CONTINUE

FINDTV=T

RETURN

END

FUNCTION CV(D,T)

CALCULATES CV( J/( MOL*K) ) . INPUT DENS{MOL/L) AND TEMP(K).

DATA(R=8. 31434)

DD=D

TT=T

CALL. TDSDT(CD,DD,TT)

DD=0

CALL TDSDT(C0,DD,TT)

CV=CPI(TT)+(C0-CD)*1000.

CV=CV-R

RETURN

END

FUNCTION FIND D(P,T)

C ITERATES EOUATION OF STATE FOR DENSITY( MOL/L) , FOR GIVEN PRESSURE(MPA) AND

C TEMPERATllRE(K) . IF ITERATION FAILS TRY USING FUNCTION FIND m, DIMENSION G(32),VP{9)

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

TT=T

IF(TT.GT.VP(8)*.99999)G0 TO 100

IF( P.GT.VPN(TT))G0 TO 101

DD=SATV(TT)

GO TO 102

100 PC=PCC

X=(1.1/(9.*PC))

DD=P/(R*T*X)

*P+ .7/9.

IF(P/PC.GT.20.. AND .T/VP(8).LT .2 5)DD==DTP GO TO 102

101 DD=SATL(TT)

102 CONTINUE

DO 10 1=1,50

IF(DD.LE.0.0.0R .DD .GT.50.)G0 TO 11 CALL PRESS(PP,DD,TT)

38
IF(PP.LE.O.O)GO TO 11 P2=PP

IF(ABS (P-P2)-1.E-7*P)20,20,1

1 CALL DPDD(PP,DD,TT)

DP-PP

C0RR=(P2-P)/DP

IF(ABS (C0RR)-1.E-7*DD)20,20,10

10 DD=DD-CORR

11 CALL REGULA(P,DD,T)

20 FIND D=DD RETURN

END

SUBROUTINE REGULA( PI ,DD ,TT)

ITERATES EON OF STATE FOR DENSITY WHEN SUBPROG FINDD FAILS.

DIMENSION G(32) ,VP(9)

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

T=TT

P=PI D2-0

IF(T.LT.TCC)GO TO 10 DO=DCC*TCC/T

GO TO 20 10 PP=VPN(T)

IF(P.GT.PP)GO TO 15 DO-SATV(T)

DO 11 1-1,150

CALL PRESS(P0,D0,T)

IF(P0.GE.P)G0 TO 12 11 D0-D0+.0001*DO

GO TO 42

12 D1=D0

13 CALL PRESS(P1,D1,T)

IF(P1.LT.P)G0 TO 14 IF(D1.LE..1*PTP)G0 TO 42 D0=D1

Z=(P1-P)/P

IF(Z.LT..l)Z=.l

IF(Z.GT..9)Z=.9

D1=D1-Z*D1

GO TO 13 14 CALL PRESS(PO,DO,T)

DO 140 1=1,50

D=D1

P3=P1

IF(ARS(P-P1) .LT..00001*P)G0 TO 40

P2-P-P1

D1=D1+(D1-D0)*P2/(P1-P0)

IF(ABS(D-Dl).LE..nn001*D)G0 TO 40

IF(ABS(P-P1).LT..005*P)D2=FIND M(P,T,D1)

IF(D2.GT.O.O.AND.02.LT.50.)D1=D2

D2=0

CALL PRESS(P1,D1,T)

IF{P0.GT.P.AND.P1.GT.P)G0 TO 120

IF(P0.LT.P.AND.P1.LT.P)G0 TO 120

GO TO 140

120 P0=P3

DO=D

140 CONTINUE

GO TO 41 15 DO=SATL(T)

DO 16 1=1,10

CALL PRESS(PO,DO,T)

39
IF(PO.LE.P)GO TO 17 16 D0=D0-.0001*D0

GO TO 42

17 Dl-DO

18 CALL PRESS(P1,D1,T)

IF(D1.GE.50.)G0 TO 42 IF(P1.GT.P)G0 TO 14 D0=D1

Z=(P-P1)/P

Z=Z*10

IF(T/TCC.LT. .6)7=1.

IF(Z.LT.1.)Z=1.

IF(Z.GT.9.)Z=9.

D1=D1+.01*D1*Z

GO TO 18 20 CALL PRESS(Pn,DO,T)

IF(P.LE.PO)GO TO 30 D1=D0

21 CALL PRESS(P1,D1,T)

IF(P1.GE.P)G0 TO 14 IF(D1.GE.50.)G0 TO 42 D0=D1

Z=(P-P1)/P

Z=Z*10

IF(Z.LT.1)Z=1

IF(Z.GT.9)Z=9

Dl=ni+.1*D1*Z

GO TO 21 30 D1=D0

31 CALL PRESS(P1,D1,T)

IF(P1.LE.P)G0 TO 14 IF(D1.LE..1*PTP)G0 TO 42 D0=D1

Z=(P1-P)/P

Z=Z*10

IF{Z.LT.1)Z=1

IF(Z.GT.9)Z=9

D1=D1-.1*D1*Z

GO TO 31 40 DD=D1

RETURN

41 PRINT 101,P,T,D

102 FORMAT{* REGULA FAILED AT P=*,F7.2,* AND T=*,F7.2)

101 F0RMAT(* DENSITY ITTERATION FAILED AT P=*,F7.2,* AND T=*,F7.2,

1/* DENSITY RETURNED IS*,E17.8)

RETURN

42 PRINT 102, P,T

RETURN

END

FUNCTION CP(D,T)

CALCULATES CP( J/( M0L*K ) ) . INPUT DENS(M0L/L), TEMP(K)

CVEE=CV(D,T)

CALL DPDT(DPT,D,T)

CALL DPDD(DPD,D,T)

CP=CVEE+(T/(D**2)*(DPT**2)/DPD)*1000.

RETURN

END

40
FUNCTION DPDTVP(TT)

C CALCULATES THE DERIVATIVE OF PRESSURE WITH RESPECT TO TEMPERATURE

C AT SATURATION. INPUT IS TEMP(K), OUTPUT IS DPDT(MPA/K).

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

DIMENSION G(32),VP(9)

T=TT

IF(TT.GT.VP(8))G0 TO 1 X=(1.-VP(7)/T)/(1.-VP(7)/VP(8))

DXDT=(VP(7)/T**2)/(1.-VP(7)/VP(8))

DPDT=VP(1)*DXDT+2.*VP(2)*X*DXDT+VP(3)*3.*X**2*DXDT+VP(5)*

1((1.-X)**VP(6))*DXDT+VP(5)*X*((1.-X)**(VP(6)-1.))*VP(6)*(-DXDT)

DPDT=DPDT*VPN(T)

DPDTVP=DPDT

RETURN

1 DPDTVP=0

RETURN

END

FUNCTION FIND M{P,T,DD)

C SOLVES FOR DENSITY(MOL/L) BY ITERATION. INPUT IS PRESSURE(MPA)

,

C TEMPERATURE(K), AND A STARTING VALUE OF DENSITY. THIS FCN IS AN

C ALTERNATIVE FOR FUNCTION FIND D. TT=T

DO 10 1=1,50

CALL PRESS(PP,DD,TT)

P2=PP

IF(ABS (P-P2)-1.E-7*P)20,20,1

1 CALL DPDD(PP,DD,TT)

DP=PP

C0RR=(P2-P)/DP

D=DD

IF(ABS (C0RR)-1.E-7*D)20,20,10

10 DD=DO-CORR

FIND M=0

RETURN

20 FIND M=DD RETURN

END

FUNCTION ENTHAL(P,D,T)

C RETURNS ENTHALPY(J/MOL) FOR AN INPUT OF PRESSURE(MPA) AND DENSITY(MOL/L]

C AND TEMPERATURE(K).

R= .00831434

DD=D

TT=T

CALL DSDN{SD,DD,TT)

CALL DUDN(UD,DD,TT)

DD=0

CALL DSDN(SO,DD,TT)

CALL DUDN(UO,DD,TT)

ENTHAL=T*(SD-S0)*1000.+(UD-U0)*1000.+HI{T)+(P/D-R*T)*1000.

RETURN

END

FUNCTION ENTROP(D,T)

CALCULATES ENTROPY(J/(MOL-K) , FROM INPUT OF DENSITY(MOL/L) AND TEMP(K)

R= .00831434

P0= .101325

DD=D

41
TT=T

CALL DSDN(SD,DD,TT)

DD=0

CALL DSDN(SO,DD,TT)

ENTROP=(SD-S0)*1000.-P,*ALOG(D*R*T/P0)*1000.+SI(T)

RETURN

END

FUNCTION SATL(TT)

CALCULATES DENSITY(MOL/L) OF SATURATED LIQUID. INPUT IS TEMP(K)

DIMENSION A(20)

DIMENSION G(32),VP(9)

C0MM0N/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

COMMON/SATC/A,DTPV

T=TT

K = 14

KK=7

GO TO 10 ENTRY SATV

K = l KK=13

T=TT

10 IF(T.GE.TCC*.995^5?)G0 TO 20

ITT=TCC

IF(ITT+1-T.LT.1.)T=ITT

X-(T-TCC)/(TTP-TCC)

D=A(K)*ALOG(X)

DO 11 1=2, KK K=K + 1 MM=I IF(MM.GE.5)MM=MM+1

11 D=D+A(K)*(l.-X**((MH-5)/3.))

IF(K.LT.14)G0 TO 12 D=DCC+EXP(D)*(DTP-DCC)

GO TO 13 12 D=DCC+EXP(D)*(DTPV-DCC)

13 SATL=D

IF(ITT+1-TT.LT.1.)SATL=D-(D-DCC)*(TT-T)

RETURN

20 DSATL=DCC

RETURN

END

FUNCTION SOUND(D,T)

CALCULATES SPEED OF SOUND(M/S). INPUT IS DENSITY(MOL/L) AND TEMP(K).

COMMON/CRIT/ W, EOK, RM, TC, DC, X , PC, SIG

CALL DPDD(DP,D,T)

S0UND=((CP(D,T)/CV(D,T))*DP*1000000./W)**.5

RETURN

END

FUNCTION VISC(DD,T)

CALCULATES VISCOSITYf MICRO PA*S) . INPUT IS DENSITY(MOL/L) AND TEMP(I<)

COMMON/CRIT/ EM, EOK, RM, TC, DC, X , PC, SIG

D=DD*EM/1000.

VISC=DILV(T)+FDCV(D,T)+EXCESV(D,T)

RETURN

END

42
FUNCTION THERM(DD,T)

RETURNS THERMAL CONDUCTIVITY( W/( M*K) ) . INPUT IS DENSITY(MOL/L) , TEMP(K)

COMMON/HAN/CR,TCI

COMMON/ I SP/N,NW,NWW

COMMON/CRIT/ EM, EOK, RM, TC, DC, X , PC, SIG D=DD*EM/1000.

CR=CRITC(n T)

THER=DILT(f)+FDCT(D,T)+EXCEST(D,T)+CR

TCI=THER-CR

THERM=THER

RETURN

END

C FUNCTION EXCESV(D,T)

C CALCULATES EXCESS VISCOSITY

COMMON/DATAl/GV ,GT ,FV , FT , EV , ET DIMENSION GV(9),GT(9),FV(4),FT(4),EV(8),ET(8)

R2=D**(.5)*((D-EV(8))/EV(8))

R=D**(.l)

X=EV(1)+EV(2)*R2+EV(3)*P+EV(4)*R2/(T*T)+EV(5)*R/T**(1.5)+EV(6)/T

1+EV(7)*P,2/T

X1=EV(1)+EV(6)/T

EXCESV= EXP(X)- EXP(Xl)

RETURN

ENTRY EXCEST

C CALCULATES EXCESS THERMAL CONDUCTIVITY

R2=D**(.5)*((D-ET(8))/ET(8))

R=D**( .1)

X-ET(1)+ET(2)*R2+ET(3)*R+ET(4)*R2/(T*T)+ET(5)*R/T**(1.5)+ET(6)/T

1+ET(7)*R2/T

X1=ET(1)+ET(6)/T

EXCESV= EXP(X)- EXP(Xl)

RETURN

END

FUNCTION FDCV(D,T)

FIRST DENSITY CORRECTION FOR VISC AND THERMAL COND. COMMON/DATAl/GV, GT,FV, FT, EV,ET

DIMENSION GV(9) ,GT(9) ,FV(4) ,FT(4) ,EV(8) ,ET(8)

FDCV=(FV(1)+FV(2)*(FV(3)-AL0G(T/FV(4)))**2)*D

RETURN

ENTRY FDCT

FDCV=(FT(1)+FT(2)*(FT(3)-AL0G(T/FT(4)))**2)*D

RETURN

END

FUNCTION CRITC(D,T)

C CALCULATES CRITICAL ENHANCEMENT FOR THERM. COND.

C INPUT UNITS ARE G/CC, K, OUTPUT IS W/(M*K).

COMMON/CRIT/ EM, EOK, RM, TC, DC, X , PC, SIG

COMMON/CHECK/DELD,DELT,DSTAR,TSTAR

COMMON/HJM/EPSI,CPCV,RRR,AKT

COMMON/ I SP/N,NW,NWW

AV=6.0225E+23 $ BK=1 .38054E-16

DELD=ABS (D-DC)/DC $ DELT=ABS (T-TC)/TC

C CALCULATE DISTANCE PARAMETER

R=(RM**2.5)*(D**O.5)*(AV/EM)**0.5

R=R*(E0K**0.'^)*X/(T**0.5)

43
RRR=R

C GENERAL EQUATION

DX=D*1000.0/EM

C DX IN MOL/L, D IN G/CM3.

CALL DPDT(DPT,DX,T)

C DPDT IN MPA/K.

DPT=DPT*1.0E+7

C DPDT NOW IN DYNES/{CM2*K)

CALL DPDD(DPD,DX,T)

C DPDD IN L*MPA/MOL.

DPD=DPD*1.0E+7*1000./EM

C DPDD NOW IN DYNE*CM/G.

IF( DPD.LT.0.0) DPD^l.O

94 VIS=VISC(DX,T)*(1.0E-05)

C VISCOSITY NOW IS G/{CM*S).

IF(DELD.E0.0.25. OR. DELD.LT. 0.25) 8,10

8 IFCDELT.EQ. 0.025. OR. DELT.LT. 0.025 ) 9, 10

9 COMPRES=SEMG{D,T)

GO TO 12 10 C0MPRES=1.0/(D*DPD)**0.5

12 EX=BK*T**2*(DPT**2)*C0MPRES

EXB=R*((BK*T)**0.5)*(D**0.5)*((AV/EM)**0.5)

CRIT=EX/(EXB*6.0*3.14159*VIS)

C THERMAL COND, CRIT, IS IN ERG/( CM*SEC*K)

C PUT IN DAMPING FACTOR

BDD=((D-DC)/DC)**4

BTT-((T-TC)/TC)**2

BXX- -18.66*PTT - 4.25*PDD

IF(BXX.LT.-l.E+2) BXX= -l.E+2

FACT= EXP( BXX ) C FACT=EXP (-18.66*BTT - 4.25*BDD)

DELC=CPIT*FACT

CRITC=DELC/100000.

C THERMAL COMD, CRITC, IS NOW IN W/(M*K)

AKT=COMPRES*COMPRES

EPSI = R*T^*BK*T*(AV*D/EM)*AKT

EPSI=EPSI**0.5

C CALC CP-CV

CPCV=T*(DPT**2)*AKT/D

RETURN

END

FUNCTION SENG(D,T)

SCALED EOUATION OF STATE FOR CRITICAL REGION

COMMON/CRIT/ EM, EOK, RM, TC, DC, X , PC, SIG

COMMON/SEN/BETA, XO, DELTA, El, E2, AGAM

COMMON/CHECK/DELD,DELT,DSTAR,TSTAR

DSTAR= D/DC $ TSTAR-T/TC

BET0=1./BETA

XX=DELT/DELD**RETO

AG=AGAM-1.0

BET2= 2.0*BETA

AGP=AG/BET2

DEL1=DELTA-1.0

AGBB=(AG-BET2)/BET2

XXO=(XX+ XO)/XO

XXB=XX0**BET2

BRAK=1.0 + E2*XXB

BRAK1=BRAK**AGB

H=E1*XX0*BRAK1

HPRIM=(E1/X0)*BRAK1 + ( AG/X0)*E1*E2*(XXB)*( BRAK**AGBB)

RC0M=(DELD**DEL1)*(DELTA*H - (XX/BETA)*HPRIM ) RCOMP= 1 . 0/ ( RC0M*DSTAR**2

)

44
c

RCM=RC0MP/(PC*1.0E+7)

RCM IN CM2/DYNIE, PC IN MPA RCM=RCM**0.5

.SENG=RCM RETURN

END

FUNCTION DILV(T)

DILUTE GAS VISCOSITY AND THERMAL CONDUCTIVITY.

C0MM0N/DATA1/GV,GT,FV,FT,EV,ET

DIMENSION GV(9),GT(9),FV(4),FT(4),EV(8),ET(8)

SUM=0

TF=T**(l./3.)

TFF-T**(-4./3.)

DO 10 1=1,9

TFF=TFF*TF

10 SUM=SUM+GV(I)*TFF

DILV=SUM

RETURN

ENTRY DILT TF=T**(l./3.)

TFF=T**(-4./3.)

SUM=0

DO 20 1=1,9

TFF=TFF*TF

20 SUM=SUM+CT(I)*TFF

DILV=SUM

RETURN

END

FUNCTION FIND P(D,T)

DIMENSION G(32) ,VP(9)

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

DD=D TT=T

IF(TT.LT.TCC)GO TO 10

1 CALL PRESS(PP,DD,TT)

FIND P=PP RETURN

10 P=VPN(TT)

DV=FIND D(P-.n001,TT)

DL=FIND D(P+.0001,TT)

IF(DD.LE.DV.OR.DD.GE.DL)G0 TO 1 PRINT 100,DV,DL,DD

CALL PRESS(PP,DV,TT)

FIND P=PP D=DV RETURN

100 FORMAT(* THE STATE POINT YOU HAVE SPECIFIED CORRESPONDS TO A

* 1/* DENSITY IN THE LIQUID VAPOR COEXISTENCE REGION*

2/* THE DENSITY OF THE SATURATED VAPOR IS *,F6.4,* MOLES/LITER*

3/* THE DENSITY OF THE SATURATED LIOUID IS *,F8.4,* MOLES/LITER*

4/* AND THE INPUT DENSITY IS *,F8.4,* MOLES/LITER*

5/* SATURATED VAPOR IS ASSUMED*)

END

FUNCTION FINDT(P,D)

RETURNS TEMPERATURE(K) , FROM THE 32-TERM MBWR EON OF STATE,

45
INPUT IS PRESSURE(MPA) AND DENSITY( MOL/L)

.

DIMEMSIOM G(32),VP(9)

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

PP=P DD=D

IF(P.GE.PCC)GO TO 1 TSAT=FINDTV(PP)

DV=FIMD D(PP-. 00001, TSAT)

DL=FIMD D(PP+. 0001, TSAT)

IF{nD.GT.DV.AND.DD.LT.DL)GO TO 30 TT=TSAT

GO TO 2

1 TT=TCC

2 DO 10 1=1,10

CALL PRESS(P2,DD,TT)

IF(ABS(PP-P2)-1.E-7*PP)20,20,11

11 CALL nPDT(DP,DD,TT)

C0RR=(P2-PP)/DP

IF(ARS(C0RR)-1.E-'^)20,20,10

10 TT=TT-CORR

20 FINDT=TT

RETURN

30 FINDT=TSAT

D=DV

PRINT 100,DV,DL,DD

100 F0RMAT(* THE STATE POINT YOU HAVE SPECIFIED CORRESPONDS TO*

1/* A DENSITY IN THE LIQUID VAPOR COEXISTENCE REGION*

2/* DENSITY OF THE SATURATED VAPOR IS*,F8.4,* MOLES/LITER*

3/* DENSITY OF THE SATURATED LIOUID IS*,F8.4,* MOLES/LITER*

4/* INPUT DENSITY IS*,F8.4,* MOLES/LITER*

5/* SATURATED VAPOR CONDITIONS ARE ASSUMED*)

RETURN

END

SUBROUTINE INFO

PRINT 100

100 F0RMAT(/* WHEN THE PROGRAM ASKS FOR A FLUID SELECTION, ENTER THE*

1*APPR0PRIATE NUMBER.*/* AN INAPPROPRIATE NUMBER WILL TERMINATE*

2* THE PROGRAM. WHEN THE PROGRAM ASKS*/* FOR A PRESSURE, DENSITY*

3*, AND TEMPERATURE, ENTER ANY TWO OF THE THREE*/* AND A ZERO FOR*

4* THE THIRD.*/* THE ORDER MUST BE P,D,T, AND ONE OF THE THREE*

5* MUST BE ZERO.*/* IF ALL THREE ARE ZERO THE PROGRAM ASKS FOR A*

6* NEW FLUID.*)

RETURN

END

FUNCTION DIEL(P,D,T)

DIELECTRIC CONSTANT. INPUT P(MPA), D(MOL/L) AND T(K).

C0MM0N/DIEL/BX(6) ,PX(6)

CM= BX(1)+ BX(2)*D+ BX(3)*D**2+ BX(4)*D**3+ BX(5)*P+ BX(6)*T

DIEL=(1.+2.*D*CM)/(1.-D*CM)

RETURN

END

FUNCTION CPI(T)

C CALCULATES SPECIFIC HEAT, ENTROPY, AND ENTHALPY FOR THE IDEAL GAS.

C OUTPUT IS IN J/(MOL*K), FOR CP AND S, AND J/MOL FOR H.

C HYDROGEN, (N=l), IS TREATED AS A SPECIAL CASE AS THE COEFF. FOR

C CP ARE IN THREE TEMPERATURE RANGES. T < 40 K , 40 < T < 140 K,

C AND T > 140 K.

46
COmON/CPID/G(ll) ,GH(11) ,GL(11)

COMMON/ISP/N,MW,NWW

K = l IF(H.EQ.l) 10,15

10 C=CPO(T)

15 U=G(9)/T

EU=EXP (U)

TS=1./T**4

GO TO (20,40,55),K

20 CPI-G(8)*U*U*EU/(EU-1.)**2

DO 25 1=1,7

TS=TS*T

25 CPI=CPI+G(I)*TS

CPI = CPI*8. 31434

RETURN

ENTRY SI K=2

IF(N.EO.l) 30,35

30 C=CPO(T)

35 GO TO 15 40 CPI=G(8)*(U/(EIJ-1.)-AL0G(1.-1./EU))

l-G(l)*TSn/3.-G(2)*TSn*T/2.-G(3)/T+G(4)*AL0G(T)+G(5)*T+G(6)*Tn/2

2.+G(7)*T**3/3.

CPI=CPI*8.31434+G(11)

RETURN

ENTRY HI K=3

IF(N.EQ.l) 45,50

45 C=CPO(T)

50 GO TO 15 55 CPI=G(8)*Un/(EU-l.)-G(l)/(2.*T*T)-G(2)/T+G(3)*AL0G(T)+G(4)*T

l+G(5)*T*T/2.+G(6)*T**3/3.+G(7)*T**4/4.

CPI = CPI*8. 31434+0(10)

RETURN

END

FUNCTION CPO(T)

C SELECTS PROPER COEFF FOR G(I), AND COMPUTES G(10) AND G(ll)

C FOR HYDROGEN ONLY.

C0MM0N/CPID/G(11) ,GH(11) ,GL(11)

TX1=140.

TX2=40.

DO 10 J=l,ll

10 G(J)=GH(J)

IF(T.LT.140.) 30,20

20 CP0=1.0

RETURN

30 G(10)=G(10)+GHI(TX1)

G(11)=G(11)+GSI(TX1)

DO 40 J=l,8

40 G{J)=GL(J)

G(10)=G(10)-GHI(TX1)

G(11)=G(11)-GSI(TX1)

IF(T.LT.40.) 60,50

50 CP0=1.0

RETURN

60 G(10)=G(10)+GHI(TX2)

G(11)=G(11)+GSI(TX2)

DO 70 J=l,8

70 G(J)=0.0

G(4)=2. 5000315

G(10)=G(10)-GHI(TX2)

47
G(11)-G(11)-GSI(TX?)

CP0=1.0

RETURN

END

FUNCTION GHI(T)

COMMON/CPID/Gdl) ,GH(11) ,GL(11)

1 U=G(9)/T

EU=EXP(U)

GHI=G(R)*U*T/(EU-1.)-G(1)/(2.*T*T)-G(2)/T+G(3)*AL0G(T)+G(4)*T

A +G(5)*Tn/2.+G(6)*T**3/3.+G(7)n**4/4.

GHI=GHI*8. 31434

RETURN

ENTRY GSI U=G(9)/T

EU=EXP(U)

TS=1./T**4

GHI= G(8)*(U/(EU-1.)-AL0G(1.-1./EU))-

A G(l)*TS*T/3.-G(2)*TS*T*T/2.-G(3)/T+G(4)*AL0G(T)+G(5)*T+

B G(6)n*T/2.+G(7)*T**3/3.

GHI=GHI*8. 31434

RETURN

END

SUBROUTINE LIMITS(P,T,IL)

DIMENSION G(32),VP{9)

COMMON/DATA/G,R, GAMMA, VP, DTP, PCC,PTP,TCC,TTP,TUL,TLL,PUL,DCC

C0MM0N/DIEL/BX(6),PX(6)

IF(P.GT.PUL)GO TO 10 IF(T.GT.TUL.OR.T.LT.TLL)GO TO 12 PM=PMELT(T) ' IF(P.GT.PM) GO TO 20

IL=1 S RETURN

10 PRINT 11,PUL

11 FORMAT! * THE INPUT PRESSURE IS OUT OF THE RANGE OF THIS EQUATION * 1/* THE RANGE FOR THIS EQUATION IS FROM TO *,F6.0,* BAR*)

IL=0 S RETURN

12 TLLF= (TLL-273.15)*1.8+32.

TULF= (TnL-273.15)*1.8+32.

PRINT 13, TLL,TUL,TLLF,TULF

13 F0RMAT(* THE INPUT TEMPERATURE IS OUT OF RANGE*

A /* THE RANGE FOR THIS EQUATION IS *,F6.2,* K TO *,F6.0,* K*,/,

B 27X,* OR *,F8.2,* F TO *,F6.0,* F*)

IL=C $ RETURN

20 TM=TMELT(P)

TF=(TM-273.15)*1.8+32.

PRINT 22, TM,TF

22 FORMAT(* SOLID PHASE DETECTED.*,/,* FOR THIS PRESSURE, TEMP*

A * SHOULD EXCEED *,F8.3,* K, 0R*,F9.3,* F*)

IL=0 $ RETURN

END

FUNCTION PMELT(T)

COMPUTES MELTING PRESSURE(MPA) FOR INPUT TEMPERATURE(K)

C0MM0N/DIEL/BX(6),PX(6)

COMMON/ I SP/N,NW,NWW

IF(N.EO.l) 20,10

10 PMELT= PX(1)+ PX(2)*T**PX(3)

RETURN

20 IF(T.GT.22.) 30,10

30 PMELT= PX(4)+ PX( 5)*T**PX(6)

48
RETURN

END

FUNCTION TMELT(P)

COMPUTES MELTING TEMPERATURE(K) FOR INPUT PRESSURE(MPA)

COMM0N/DIEL/BX(6),PX(6)

COMMON/ I SP/N,NW,NWW

IF(N.EO.l) 20,10

10 TMELT=((P-PX(1))/PX(2))**(1./PX(3))

RETURN

20 IF(P.GT.31.64) 30,10

30 TMELT=((P-PX(4))/PX(5))**(1./PX(6))

RETURN

END

49
NBS-n4A 'REV. 2-8C)

_.S. OEPT. OF COMM.

BIBLIOGRAPHIC DATA

SHEET :See instructions;

1. PUBLICATION OR

REPORT NO.

NBS TN-1048

2. Performing Organ. Report No 3. Publ i cation Date June 19 82

4. TITLE AND SUBTITLE

INTERACTIVE FORTRAN PROGRAM TO CALCULATE THERMOPHYSICAL PROPERTIES OF SIX FLUIDS

5. AUTHOR(S)

Ben A. Younglove

6. PERFORMING ORGANIZATION i / f joint or other th on N BS. see instructions)

NATIONAL BUREAU OF STANDARDS

DEPARTMENT OF COMMERCE

WASHINGTON, D.C. 20234

7. Contract/Grant No.

8. Type cf Report & Period Covered

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 significc^

bi b!!OgraphY or liieraiure survey, mention it here)

If document includes a si gnificari

An interactive FORTRAN IV computer program is given for computing thermophysical

properties of argon, ethylene, parahydrogen, nitrogen, nitrogen trifluoride, and

oxygen. The program is designed for use with a computer terminal accessing a large

computer in an interactive mode. The program provides prompting for selection of

several options including: 1) choice of fluid, 2) choice of SI or engineering units,

3) choice of the single phase or liquid-vapor phase, and 4) a table of properties or

a single value.

Properties are computed for the single phase region from input of two of the

variables, temperature, pressure, and density. Values on the liquid-vapor boundary

are computed from an entry of temperature or pressure. The program returns values

for pressure, temperature, density, internal energy, enthalpy, entropy, specific

heats at constant volume and pressure, and sound velocity. Viscosity, thermal

conductivity, and dielectric constant are given for some of the fluids. Copies of

the programs may be obtained from Office of Standard Reference Data, Attention:

Reference Center, National Bureau of Standards, Washington^ D .C 20234.

12 KEY WORDS (S'x to tA^efv-e entries; ainhabetsca: orde-- caqi tci: ze or.', c 'jce- na.-jes- and sec-Jrci^ <£/ .-.z'CS b/je-^icojcrs.

rgon; computer programs; density; enthalpy; equation of state; ethylene; hydrogen,

nitrogen; nitrogen trifluoride; oxygen; specific heat at constant pressure; specific

heat at constant volume.

13. AVAILABILITY

I X| Unlimited

I

I For Official Distribution. Do Not Release to NTIS

["X, Order From Superintendent of Documents, U.S. Government Printing Office, Vvashington, D.C. 20402.

I

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

14. NO. OF

PRINTED PAGES

56

15. Price

S4.75

G PO 836 - 092 USCOWM-DC 6043-PO-''


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