970 lines
46 KiB
Plaintext
970 lines
46 KiB
Plaintext
Ethane !Short name
|
|
74-84-0 !CAS number
|
|
Ethane !Full name
|
|
CH3CH3 !Chemical formula {C2H6}
|
|
R-170 !Synonym
|
|
30.06904 !Molar mass [g/mol]
|
|
90.368 !Triple point temperature [K]
|
|
184.569 !Normal boiling point [K]
|
|
305.322 !Critical temperature [K]
|
|
4872.2 !Critical pressure [kPa]
|
|
6.856886685 !Critical density [mol/L] (206.18 kg/m^3)
|
|
0.0995 !Acentric factor
|
|
0.0 !Dipole moment [Debye]; (exactly zero due to symmetry)
|
|
NBP !Default reference state
|
|
10.0 !Version number
|
|
1035 !UN Number :UN:
|
|
n-alkane !Family :Family:
|
|
1560.69 !Heating value (upper) [kJ/mol] :Heat:
|
|
5.5 !GWP (IPCC 2007) :GWP:
|
|
7000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
|
|
A3 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
|
|
1S/C2H6/c1-2/h1-2H3 !Standard InChI String :InChi:
|
|
OTMSDBZUPAUEDD-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
|
|
???? !Alternative fluid for mixing rules :AltID:
|
|
434e2a40 !Hash number from InChI Key :Hash:
|
|
|
|
|
|
|
|
|
|
!The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the
|
|
! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended
|
|
! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to
|
|
! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary
|
|
! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and
|
|
! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the
|
|
! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the
|
|
! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations,
|
|
! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and
|
|
! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface
|
|
! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a
|
|
! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The
|
|
! end of the fluid file is marked with @END. Anything below that is ignored.
|
|
|
|
|
|
! compiled by M. McLinden, NIST Physical and Chemical Properties Division, Boulder, Colorado
|
|
! 03-28-96 MM, Original version.
|
|
! 11-01-99 EWL, Add Span 12 term short equation of state.
|
|
! 11-19-99 EWL, Add transport equations of Friend.
|
|
! 03-26-03 EWL, Add Buecker equation.
|
|
! 08-05-04 EWL, Add Harvey and Lemmon dielectric correlation.
|
|
! 10-13-04 MLH, Add family.
|
|
! 08-08-05 EWL, Change Ptrp in melting line equation slightly to match EOS at Ttrp.
|
|
! 12-02-06 MLH, Update LJ in ECS.
|
|
! 03-05-07 MLH, Add VS4 model.
|
|
! 04-11-12 MLH, Add extra blank FT coeff for consistent formatting.
|
|
! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
|
|
! 11-22-16 EWL, Add Vogel viscosity correlation (2015).
|
|
! 02-16-17 KG, Add ancillary equations.
|
|
! 05-08-17 EWL, Update VS7 to the new reverse Polish notation.
|
|
! 02-28-18 IHB, Add sublimation line model.
|
|
|
|
|
|
|
|
|
|
________________________________________________________________________________
|
|
|
|
#EOS !---Equation of state---
|
|
FEQ !Helmholtz equation of state for ethane of Buecker and Wagner (2006).
|
|
:TRUECRITICALPOINT: 305.322 6.856886685 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
|
|
:DOI: 10.1063/1.1859286
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Bücker, D. and Wagner, W.,
|
|
? "A Reference Equation of State for the Thermodynamic Properties of Ethane
|
|
? for Temperatures from the Melting Line to 675 K and Pressures up to 900 MPa,"
|
|
? J. Phys. Chem. Ref. Data, 35(1):205-266, 2006.
|
|
?
|
|
?The uncertainties in the equation of state are 0.02% to 0.04% in density
|
|
? from the melting line up to temperatures of 520 K and pressures of 30 MPa.
|
|
? The uncertainties increase to 0.3% at higher temperatures and to 1% at
|
|
? higher pressures. The uncertainty in speed of sound ranges from 0.02% in
|
|
? the gaseous phase to 0.15% in the liquid phase. Above 450 K, the
|
|
? uncertainties increase to 0.3% at lower pressures and to 1% at higher
|
|
? pressures. At pressures above 40 MPa at all temperatures, the
|
|
? uncertainties are 1% up to 100 MPa, and 5% at higher pressures. The
|
|
? uncertainties in heat capacities range from 2% in the vapor and liquid
|
|
? regions below 450 K and 30 MPa to 5% at high pressures. The uncertainties
|
|
? in vapor pressure are 0.01% above 170 K and 10 Pa below 170 K.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.368 !Lower temperature limit [K]
|
|
675.0 !Upper temperature limit [K]
|
|
900000.0 !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
CPP !Pointer to Cp0 model
|
|
30.06904 !Molar mass [g/mol]
|
|
90.368 !Triple point temperature [K]
|
|
0.001142 !Pressure at triple point [kPa]
|
|
21.668 !Density at triple point [mol/L]
|
|
184.569 !Normal boiling point temperature [K]
|
|
0.0995 !Acentric factor
|
|
305.322 4872.2 6.856886685 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
305.322 6.856886685 !Reducing parameters [K, mol/L]
|
|
8.314472 !Gas constant [J/mol-K]
|
|
39 4 5 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
0.83440745735241 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
|
-1.4287360607171 1.0 1. 0.
|
|
0.34430242210927 0.25 2. 0.
|
|
-0.42096677920265 0.75 2. 0.
|
|
0.012094500886549 0.75 4. 0.
|
|
-0.57976201597341 2.0 1. 1.
|
|
-0.033127037870838 4.25 1. 1.
|
|
-0.11751654894130 0.75 2. 1.
|
|
-0.11160957833067 2.25 2. 1.
|
|
0.062181592654406 3.0 3. 1.
|
|
0.098481795434443 1.0 6. 1.
|
|
-0.098268582682358 1.25 6. 1.
|
|
-0.00023977831007049 2.75 7. 1.
|
|
0.00069885663328821 1.0 9. 1.
|
|
0.19665987803305e-4 2.0 10. 1.
|
|
-0.014586152207928 2.5 2. 2.
|
|
0.046354100536781 5.5 4. 2.
|
|
0.0060764622180645 7.0 4. 2.
|
|
-0.0026447330147828 0.5 5. 2.
|
|
-0.042931872689904 5.5 5. 2.
|
|
0.0029987786517263 2.5 6. 2.
|
|
0.005291933517501 4.0 8. 2.
|
|
-0.0010383897798198 2.0 9. 2.
|
|
-0.054260348214694 10.0 2. 3.
|
|
-0.21959362918493 16.0 3. 3.
|
|
0.35362456650354 18.0 3. 3.
|
|
-0.12477390173714 20.0 3. 3.
|
|
0.18425693591517 14.0 4. 3.
|
|
-0.16192256436754 18.0 4. 3.
|
|
-0.082770876149064 12.0 5. 3.
|
|
0.050160758096437 19.0 5. 3.
|
|
0.0093614326336655 7.0 6. 3.
|
|
-0.00027839186242864 15.0 11. 3.
|
|
0.23560274071481e-4 9.0 14. 3.
|
|
0.0039238329738527 26.0 3. 4.
|
|
-0.00076488325813618 28.0 3. 4.
|
|
-0.004994430444073 28.0 4. 4.
|
|
0.0018593386407186 22.0 8. 4.
|
|
-0.00061404353331199 13.0 10. 4.
|
|
-0.0023312179367924 0.0 1. 2. 2. -15.0 -150.0 1.05 1.0 0. 0. 0.
|
|
0.002930104790876 3.0 1. 2. 2. -15.0 -150.0 1.05 1.0 0. 0. 0.
|
|
-0.00026912472842883 3.0 3. 2. 2. -15.0 -150.0 1.05 1.0 0. 0. 0.
|
|
184.13834111814 0.0 3. 2. 2. -20.0 -275.0 1.22 1.0 0. 0. 0.
|
|
-10.397127984854 3.0 2. 2. 2. -20.0 -400.0 1.16 1.0 0. 0. 0.
|
|
eta beta gamma epsilon
|
|
EXP[eta*(delta-epsilon)^2+beta*(tau-gamma)^2]
|
|
|
|
|
|
#AUX !---Auxiliary function for Cp0
|
|
CPP !Ideal gas heat capacity function for ethane of Buecker and Wagner (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Bücker, D. and Wagner, W., 2006.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 8.314472 !Reducing parameters for T, Cp0
|
|
1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
4.003039265 0.0
|
|
1.117433359 430.23083
|
|
3.467773215 1224.3159
|
|
6.94194464 2014.12064
|
|
5.970850948 4268.34363
|
|
|
|
|
|
#AUX !---Auxiliary function for PX0
|
|
PX0 !Helmholtz energy ideal-gas function for ethane of Buecker and Wagner (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Bücker, D. and Wagner, W., 2006.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
|
|
3.003039265 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
|
-3.0938209725939316 0.0 !aj, ti for [ai*tau**ti] terms
|
|
3.2503021100636769 1.0 !aj, ti for [ai*tau**ti] terms
|
|
1.117433359 430.23083 !aj, ti for [ai*log(1-exp(-ti/T)] terms
|
|
3.467773215 1224.3159
|
|
6.94194464 2014.12064
|
|
5.970850948 4268.34363
|
|
|
|
|
|
#AUX !---Auxiliary function for PH0
|
|
PH0 !Ideal gas Helmholtz form for ethane of Buecker and Wagner (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Bücker, D. and Wagner, W., 2006.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
|
|
3.003039265 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
|
9.212802589 0.0 !aj, ti for [ai*tau**ti] terms
|
|
-4.68224855 1.0
|
|
1.117433359 -1.4091052332 !aj, ti for [ai*log(1-exp(ti*tau)] terms
|
|
3.467773215 -4.0099170712
|
|
6.94194464 -6.5967098342
|
|
5.970850948 -13.9798102659
|
|
|
|
|
|
|
|
|
|
--------------------------------------------------------------------------------
|
|
|
|
@EOS !---Equation of state---
|
|
FEK !Helmholtz equation of state for ethane of Kunz and Wagner (2004).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Kunz, O., Klimeck, R., Wagner, W., Jaeschke, M.
|
|
? "The GERG-2004 Wide-Range Equation of State for Natural Gases
|
|
? and Other Mixtures," GERG Technical Monograph 15,
|
|
? Fortschritt-Berichte VDI, VDI-Verlag, Düsseldorf, 2007.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.368 !Lower temperature limit [K]
|
|
675.0 !Upper temperature limit [K]
|
|
900000.0 !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
PHK !Pointer to Cp0 model
|
|
30.06904 !Molar mass [g/mol]
|
|
90.368 !Triple point temperature [K]
|
|
0.001113 !Pressure at triple point [kPa]
|
|
21.66 !Density at triple point [mol/L]
|
|
184.56 !Normal boiling point temperature [K]
|
|
0.0995 !Acentric factor
|
|
305.322 4871.8 6.87085454 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
305.322 6.87085454 !Reducing parameters [K, mol/L]
|
|
8.314472 !Gas constant [J/mol-K]
|
|
24 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
0.63596780450714 0.125 1. 0.
|
|
-1.7377981785459 1.125 1. 0.
|
|
0.28914060926272 0.375 2. 0.
|
|
-0.33714276845694 1.125 2. 0.
|
|
0.022405964699561 0.625 4. 0.
|
|
0.015715424886913 1.5 4. 0.
|
|
0.11450634253745 0.625 1. 1.
|
|
1.0612049379745 2.625 1. 1.
|
|
-1.2855224439423 2.75 1. 1.
|
|
0.39414630777652 2.125 2. 1.
|
|
0.31390924682041 2.0 3. 1.
|
|
-0.021592277117247 1.75 6. 1.
|
|
-0.21723666564905 4.5 2. 2.
|
|
-0.28999574439489 4.75 3. 2.
|
|
0.42321173025732 5.0 3. 2.
|
|
0.04643410025926 4.0 4. 2.
|
|
-0.13138398329741 4.5 4. 2.
|
|
0.011492850364368 7.5 2. 3.
|
|
-0.033387688429909 14.0 3. 3.
|
|
0.015183171583644 11.5 4. 3.
|
|
-0.0047610805647657 26.0 5. 6.
|
|
0.046917166277885 28.0 6. 6.
|
|
-0.039401755804649 30.0 6. 6.
|
|
-0.0032569956247611 16.0 7. 6.
|
|
|
|
|
|
@AUX !---Auxiliary function for PH0
|
|
PHK !Ideal gas Helmholtz form for ethane of Kunz and Wagner (2004).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Kunz, O., Klimeck, R., Wagner, W., Jaeschke, M.
|
|
? "The GERG-2004 Wide-Range Equation of State for Natural Gases
|
|
? and Other Mixtures," GERG Technical Monograph 15,
|
|
? Fortschritt-Berichte VDI, VDI-Verlag, Düsseldorf, 2007.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1 2 0 2 2 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
|
|
3.00263 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
|
24.675437527 0.0 !aj, ti for [ai*tau**ti] terms
|
|
-77.42531376 1.0
|
|
-1.23722 0.731306621 !aj, ti for cosh and sinh terms
|
|
6.01989 3.508721939
|
|
4.33939 1.831882406
|
|
13.1974 3.378007481
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
FE1 !Helmholtz equation of state for ethane of Friend et al. (1991).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Friend, D.G., Ingham, H., and Ely, J.F.,
|
|
? "Thermophysical Properties of Ethane,"
|
|
? J. Phys. Chem. Ref. Data, 20(2):275-347, 1991.
|
|
?
|
|
?The uncertainties of the equation of state are 0.2% in density, 2.5% in
|
|
? isobaric heat capacity above 150 K, and 1.5% in isochoric heat capacity above
|
|
? 150 K. The uncertainty in speed of sound ranges from 0.6% in the liquid and
|
|
? vapor below the critical temperature to less than 2% elsewhere, except in the
|
|
? critical region.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.352 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
70000. !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
CP1 !Pointer to Cp0 model
|
|
30.070 !Molar mass [g/mol]
|
|
90.352 !Triple point temperature [K]
|
|
0.00113 !Pressure at triple point [kPa]
|
|
21.665 !Density at triple point [mol/L]
|
|
184.552 !Normal boiling point temperature [K]
|
|
0.0993 !Acentric factor
|
|
305.33 4871.8 6.87 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
305.33 6.87 !Reducing parameters [K, mol/L]
|
|
8.31451 !Gas constant [J/mol-K]
|
|
32 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
0.46215430560 0.0 1. 0. !a(i),t(i),d(i),l(i)
|
|
-1.9236936387 1.5 1. 0.
|
|
0.39878604003 2.5 1. 0.
|
|
0.016054532372 -0.5 2. 0.
|
|
0.12895242219 1.5 2. 0.
|
|
0.035458320491 2.0 2. 0.
|
|
0.03492784454 0.0 3. 0.
|
|
-0.01130618338 1.0 3. 0.
|
|
-0.039809032779 2.5 3. 0.
|
|
0.00083031936834 0.0 6. 0.
|
|
0.00045921575183 2.0 7. 0.
|
|
0.17530287917e-6 5.0 7. 0.
|
|
-0.70919516126e-4 2.0 8. 0.
|
|
-0.23436162249 5.0 1. 2.
|
|
0.084574697645 6.0 1. 2.
|
|
0.14861052010 3.5 2. 2.
|
|
-0.10016857867 5.5 2. 2.
|
|
-0.059264824388 3.0 3. 2.
|
|
-0.041263514217 7.0 3. 2.
|
|
0.021855161869 6.0 5. 2.
|
|
-0.74552720958e-4 8.5 6. 2.
|
|
-0.0098859085572 4.0 7. 2.
|
|
0.0010208416499 6.5 8. 2.
|
|
-0.00052189655847 5.5 10. 2.
|
|
0.9859216203e-4 22.0 2. 4.
|
|
0.046865140856 11.0 3. 4.
|
|
-0.019558011646 18.0 3. 4.
|
|
-0.046557161651 11.0 4. 4.
|
|
0.0032877905376 23.0 4. 4.
|
|
0.13572090185 17.0 5. 4.
|
|
-0.10846471455 18.0 5. 4.
|
|
-0.0067502836903 23.0 5. 4.
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CP1 !Ideal gas heat capacity function for ethane of Friend et al.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Friend, D.G., Ingham, H., and Ely, J.F.,
|
|
? "Thermophysical Properties of Ethane,"
|
|
? J. Phys. Chem. Ref. Data, 20(2):275-347, 1991.
|
|
?
|
|
?Note: Friend et al. give a Helmholtz form for the ideal gas term; it
|
|
? has been converted to a Cp0 form, by the transform:
|
|
?
|
|
?Cp0/R = (1 + Q_2) - 4/9*Q_3*Tr**(1/3) - 10/9*Q_4*Tr**(2/3)
|
|
? - 2*Q_5*Tr + Q_6*U*U*exp(U)/[1 - exp(U)]**2
|
|
? where: Tr = T/Tcrit,
|
|
? U = Q_7*Tcrit/T,
|
|
? and the Q_i are the original coefficients given by Friend.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
305.33 8.31451 !Reducing parameters for T, Cp0
|
|
4 1 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
4.8159476 0.0 ! = 1 + Q_2; power in T
|
|
-3.8231688 0.33333333333333 ! = -4/9*Q_3
|
|
3.6750817 0.66666666666667 ! = -10/9*Q_4
|
|
1.1191336 1.0 ! = -2*Q_5
|
|
5.0722267 -1681.601128 ! = -Q_6; Q_7*Tcrit
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
FES !Helmholtz equation of state for ethane of Span and Wagner (2003).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Span, R. and Wagner, W.
|
|
? "Equations of State for Technical Applications. II. Results for Nonpolar Fluids,"
|
|
? Int. J. Thermophys., 24(1):41-109, 2003. doi: 10.1023/A:1022310214958
|
|
?
|
|
?The uncertainties of the equation of state are approximately 0.2% (to
|
|
? 0.5% at high pressures) in density, 1% (in the vapor phase) to 2% in
|
|
? heat capacity, 1% (in the vapor phase) to 2% in the speed of sound, and
|
|
? 0.2% in vapor pressure, except in the critical region.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.352 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
CPS !Pointer to Cp0 model
|
|
30.07 !Molar mass [g/mol]
|
|
90.352 !Triple point temperature [K]
|
|
0.0010902 !Pressure at triple point [kPa]
|
|
21.721 !Density at triple point [mol/L]
|
|
184.53 !Normal boiling point temperature [K]
|
|
0.099 !Acentric factor
|
|
305.322 4872.0 6.8706352 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
305.322 6.8706352 !Reducing parameters [K, mol/L]
|
|
8.31451 !Gas constant [J/mol-K]
|
|
12 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
0.97628068 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
|
-2.6905251 1.125 1. 0.
|
|
0.73498222 1.5 1. 0.
|
|
-0.035366206 1.375 2. 0.
|
|
0.084692031 0.25 3. 0.
|
|
0.00024154594 0.875 7. 0.
|
|
0.23964954 0.625 2. 1.
|
|
-0.042780093 1.75 5. 1.
|
|
-0.22308832 3.625 1. 2.
|
|
-0.051799954 3.625 4. 2.
|
|
-0.027178426 14.5 3. 3.
|
|
0.011246305 12.0 4. 3.
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CPS !Ideal gas heat capacity function for ethane of Jaeschke and Schley (1995).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Jaeschke, M. and Schley, P.
|
|
? "Ideal-Gas Thermodynamic Properties for Natural-Gas Applications,"
|
|
? Int. J. Thermophys., 16(6):1381-1392, 1995. doi: 10.1007/BF02083547
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 8.31451 !Reducing parameters for T, Cp0
|
|
1 0 2 2 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
4.00263 0.0
|
|
61682.52 -2.0 223.284 -1.0 -2.0
|
|
-6908801.0 -2.0 1071.29 -1.0 -2.0
|
|
1357501.0 -2.0 559.314 -1.0 -2.0
|
|
14038660.0 -2.0 1031.38 -1.0 -2.0
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
BWR !MBWR equation of state for ethane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.,
|
|
? "Thermophysical properties of fluids. II. Methane, ethane, propane,
|
|
? isobutane and normal butane,"
|
|
? J. Phys. Chem. Ref. Data, 16:577-798, 1987.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.348 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
70000.0 !Upper pressure limit [kPa]
|
|
21.68 !Maximum density [mol/L]
|
|
CP2 !Pointer to Cp0 model
|
|
30.070 !Molar mass [g/mol]
|
|
90.348 !Triple point temperature [K]
|
|
0.0011308 !Pressure at triple point [kPa]
|
|
21.680 !Density at triple point [mol/L]
|
|
184.548 !Normal boiling point temperature [K]
|
|
0.0993 !Acentric factor
|
|
305.34 4871.43 6.875 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
305.34 6.875 !Reducing parameters [K, mol/L]
|
|
6.875 !gamma
|
|
0.0831434 !Gas constant [L-bar/mol-K]
|
|
32 1 !Nterm, Ncoeff per term
|
|
-0.003204748852 0.6529792241 -16.69704591
|
|
1147.983381 -185472.1998 0.0004994149431
|
|
-0.4858871291 122.5345776 86226.15988
|
|
-0.1081290283e-4 0.06279096996 -17.16912675
|
|
-0.0001640779401 -0.04356516111 -19.66649699
|
|
0.004026724698 -0.6498241861e-4 0.05111594139
|
|
-0.001113010349 -7157.747547 -18485710.24
|
|
-2137.365569 62750799.86 -9.974911056
|
|
1129.115014 -0.1026469558 -5660.525915
|
|
-0.000420984643 0.2374523553 -0.1289637823e-5
|
|
-0.0005423801068 0.0223971723
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CP2 !Ideal gas heat capacity function for ethane of Younglove and Ely.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.,
|
|
? "Thermophysical properties of fluids. II. Methane, ethane, propane,
|
|
? isobutane and normal butane,"
|
|
? J. Phys. Chem. Ref. Data, 16:577-798, 1987.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 8.31434 !Reducing parameters for T, Cp0
|
|
7 1 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
-693414.06909 -3.0
|
|
31534.834135 -2.0
|
|
-610.3375287 -1.0
|
|
9.9507922459 0.0
|
|
-0.028657877948 1.0
|
|
0.000090922897821 2.0
|
|
-5.2750109915e-8 3.0
|
|
-14.243593411 3000.0
|
|
|
|
|
|
|
|
|
|
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
|
|
|
#ETA !---Viscosity---
|
|
VS7 !Pure fluid viscosity model for ethane of Vogel et al. (2015).
|
|
:DOI: 10.1063/1.4930838
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Vogel, E., Span, R., and Herrmann, S.,
|
|
? "Reference Correlation for the Viscosity of Ethane,"
|
|
? J. Phys. Chem. Ref. Data, 44, 043101, 2015.
|
|
? doi: 10.1063/1.4930838
|
|
?
|
|
?The viscosity in the limit of zero density has an expanded uncertainty (at 95% confidence)
|
|
? of 0.5% for 290 <T <625 K, increasing to 1% at temperatures down to 212 K.
|
|
? The uncertainty is 1.5% for 290 <T <430 K at pressures to 30 MPa. For additional
|
|
? information on uncertainty consult the referenced manuscript.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.352 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
70000.0 !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
NUL !Omega model
|
|
!
|
|
!Dilute gas function
|
|
$DG RED SUM:2
|
|
!
|
|
!Residual function
|
|
$RF RED SUM:10 CMPLX:2 +
|
|
!
|
|
!Coefficients
|
|
$CF
|
|
1.0 305.322 1. 0. 0 !Reducing parameters for eta, T, rho
|
|
9.6634694892149 1. 0. 0. 0 !Dilute gas terms
|
|
-0.22985582151676 3. 0. 0. 0
|
|
!Simple polynomial/exponential terms
|
|
1.0 305.322 6.856886685 0. 0 !Reducing parameters for eta, T, rho
|
|
6.6687966976352 -0. 1. 0. 0
|
|
-4.6983342709702 -1. 1. 0. 0
|
|
19.688847427047 -0. 2. 0. 0
|
|
-9.5399537393789 -1. 2. 0. 0
|
|
0.063640646131666 -0. 7. 0. 0
|
|
0.0079981217444542 -1. 8. 0. 0
|
|
7.0489675750657e-8 -3. 17. 0. 0
|
|
-22.734655865556 -0. 3. 0. 1
|
|
22.124096051632 -2. 3. 0. 1
|
|
-0.30986358885564 -5. 3. 0. 1
|
|
^12TERMS !Complex polynomial/exponential terms
|
|
0.64034200732045 1. 1. 2. 1. -90. -100. 1. 1. 0. 0. 0.
|
|
0.70437620805249 1. 1. 2. 1. -50. -250. 1. 1. 0. 0. 0.
|
|
^END12TERMS
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
|
|
|
|
================================================================================
|
|
|
|
#TCX !---Thermal conductivity---
|
|
TC1 !Pure fluid thermal conductivity model for ethane of Friend et al. (1991).
|
|
:DOI: 10.1063/1.555881
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Friend, D.G., Ingham, H., and Ely, J.F.,
|
|
? "Thermophysical Properties of Ethane,"
|
|
? J. Phys. Chem. Ref. Data, 20(2):275-347, 1991.
|
|
?
|
|
?The uncertainty in thermal conductivity is 2%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.352 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
70000. !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
3 0 !# terms for dilute gas function: numerator, denominator
|
|
245.0 0.001 !Reducing parameters for T, tcx
|
|
1.7104147 0. !Coefficient, power in T
|
|
-0.6936482 -1.
|
|
0. -96.
|
|
7 0 !# terms for background gas function: numerator, denominator
|
|
305.33 6.87 0.00441786 !Reducing parameters for T, rho, tcx
|
|
0.96084322 0. 1. 0. !Coefficient, powers of t, rho, exp(rho)
|
|
2.7500235 0. 2. 0.
|
|
-0.026609289 0. 3. 0.
|
|
-0.078146729 0. 4. 0.
|
|
0.21881339 0. 5. 0.
|
|
2.3849563 -1.5 1. 0.
|
|
-0.75113971 -1. 3. 0.
|
|
TK3 !Pointer to critical enhancement auxiliary function
|
|
|
|
|
|
#AUX !---Auxiliary function for the thermal conductivity critical enhancement
|
|
TK3 !Simplified thermal conductivity critical enhancement for ethane of Friend et al. (1991).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Friend, D.G., Ingham, H., and Ely, J.F., 1991.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
9 0 0 0 !# terms: terms, spare, spare, spare
|
|
1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
|
|
0.63 !Nu (universal exponent)
|
|
1.242 !Gamma (universal exponent)
|
|
1.01 !R0 (universal amplitude)
|
|
0.065 !Z (universal exponent--not used for t.c., only viscosity)
|
|
1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
|
|
0.19e-9 !Xi0 (amplitude) [m]
|
|
0.0563 !Gam0 (amplitude) [-]
|
|
0.545e-9 !Qd_inverse (modified effective cutoff parameter) [m]
|
|
610.66 !Tref (reference temperature) [K]
|
|
|
|
|
|
|
|
|
|
********************************************************************************
|
|
|
|
@ETA !---Viscosity---
|
|
VS1 !Pure fluid viscosity model for ethane of Friend et al. (1991).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Friend, D.G., Ingham, H., and Ely, J.F.,
|
|
? "Thermophysical Properties of Ethane,"
|
|
? J. Phys. Chem. Ref. Data, 20(2):275-347, 1991.
|
|
?
|
|
?The uncertainty in viscosity is 2%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.352 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
70000.0 !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
1 !Number of terms associated with dilute-gas function
|
|
CI2 !Pointer to reduced effective collision cross-section model
|
|
0.43682 !Lennard-Jones coefficient sigma [nm]
|
|
245.0 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
1.0 1.0 !Reducing parameters for T, eta
|
|
0.1463897 0.5 !Chapman-Enskog term
|
|
0 !Number of terms for initial density dependence
|
|
0 0 9 3 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
|
|
305.33 6.87 15.977 !Reducing parameters for T, rho, eta
|
|
0.47177003 0.0 1. 0. 0 !Simple polynomial terms
|
|
-0.23950311 -1.0 1. 0. 0
|
|
0.39808301 0.0 2. 0. 0
|
|
-0.27343335 -1.0 2. 0. 0
|
|
0.3519226 -1.5 2. 0. 0
|
|
-0.21101308 0.0 3. 0. 0
|
|
-0.00478579 -2.0 3. 0. 0
|
|
0.07378129 0.0 4. 0. 0
|
|
-0.030425255 -1.0 4. 0. 0
|
|
1.0 0.0 0. 0. 0
|
|
-0.30435286 0.0 1. 0. 0
|
|
0.001215675 -1.0 1. 0. 0
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS2 !Pure fluid viscosity model for ethane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.,
|
|
? "Thermophysical properties of fluids. II. Methane, ethane, propane,
|
|
? isobutane and normal butane,"
|
|
? J. Phys. Chem. Ref. Data, 16:577-798, 1987.
|
|
?
|
|
?The uncertainty in viscosity is 2%, except in the critical region which is 5%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.348 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
70000.0 !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
CI2 !Pointer to collision integral model
|
|
0.440110 !Lennard-Jones coefficient sigma [nm]
|
|
240.0 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
0.146388493 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12
|
|
0.5 !Exponent in Eq 19 for T
|
|
2.102436247 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1)
|
|
-1.065920192 !Fv(2)
|
|
1.4 !Fv(3)
|
|
305.33 !Fv(4)
|
|
-19.03481042 !Coefficients for residual viscosity, eqs (22 - 25)
|
|
1799.260494 !Ev(2)
|
|
15.61316986 !Ev(3)
|
|
-14972.21136 !Ev(4)
|
|
0.1130374601 !Ev(5)
|
|
-21.86440756 !Ev(6)
|
|
8235.954037 !Ev(7)
|
|
6.875 !Ev(8)
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
@AUX !---Auxiliary function for the collision integral
|
|
CI2 !Collision integral model for ethane of Klein et al (1974).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Klein, M., Hanley, H.J.M., Smith, F.J., and Holland, P.,
|
|
? Natl. Bur. Stand. (U.S.), Monograph 47, 1974.
|
|
?
|
|
?also repeated in:
|
|
? Friend, D.G., Ingham, H., and Ely, J.F., 1991.
|
|
?
|
|
?Younglove, B.A. and Ely, J.F., 1987.
|
|
? (but note that there is an error in the Younglove and Ely paper)
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
9 !Number of terms
|
|
-3.0328138281 0 !Omega: coeffs of {(e/kT)**((i-1)/3 - 1)}
|
|
16.918880086 0
|
|
-37.189364917 0
|
|
41.288861858 0
|
|
-24.61592114 0
|
|
8.948843096 0
|
|
-1.8739245042 0
|
|
0.209661014 0 !Wrong sign in Younglove and Ely, Table 2
|
|
-0.009657044 0
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS4 !Pure fluid generalized friction theory viscosity model for ethane of Quinones-Cisneros and Deiters (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Quinones-Cisneros, S.E. and Deiters, U.K.,
|
|
? "Generalization of the Friction Theory for Viscosity Modeling,"
|
|
? J. Phys. Chem. B, 110(25):12820-12834, 2006. doi: 10.1021/jp0618577
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.348 !Lower temperature limit [K]
|
|
500.0 !Upper temperature limit [K]
|
|
55000.0 !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
4 0 0 0 0 0 !Number of terms associated with dilute-gas function
|
|
NUL !Pointer to reduced effective collision cross-section model; not used
|
|
0.440110 !Lennard-Jones coefficient sigma [nm] (not used)
|
|
240.0 !Lennard-Jones coefficient epsilon/kappa [K] (not used)
|
|
305.322 1.0 !Reducing parameters for T, eta
|
|
0.0 0.5 !Chapman-Enskog term; not used here
|
|
15.9252 0.0 !Empirical terms for eta0
|
|
-49.7734 0.25
|
|
43.4368 0.50
|
|
0 !Number of terms for initial density dependence
|
|
-7.50685764546476e-6 -1.50327318940575e-6 5.58090793793288e-15 0. 0. ! a(0),a(1),a(2)
|
|
6.72861662009487e-5 -4.36450942982638e-5 -7.97441663817752e-14 0. 0. ! b(0),b(1),b(2)
|
|
3.8803950324223e-5 -1.38523739665972e-5 -2.64094611051755e-15 0. 0. ! c(0),c(1),c(2)
|
|
7.68043111364307e-10 -1.32047872761278e-10 0.0 0. 0. ! A(0),A(1),A(2)
|
|
9.15406537766279e-9 4.13028199950288e-10 0.0 0. 0. ! B(0),B(1),B(2)
|
|
-1.45842039761136e-7 2.39764228120527e-7 0.0 0. 0. ! C(0),C(1),C(2)
|
|
0.0 0.0 0.0 0. 0. ! D(0),D(1),D(2)
|
|
0.0 0.0 0.0 0. 0. ! E(0),E(1),E(2)
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
|
|
|
|
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
|
|
|
@TRN !---ECS Transport---
|
|
ECS !Extended Corresponding States model (Nitrogen reference); predictive mode for ethane.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Klein, S.A., McLinden, M.O., and Laesecke, A., "An Improved Extended Corresponding States Method for Estimation of Viscosity of Pure Refrigerants and Mixtures," Int. J. Refrigeration, 20(3):208-217, 1997. doi: 10.1016/S0140-7007(96)00073-4.
|
|
?McLinden, M.O., Klein, S.A., and Perkins, R.A., "An Extended Corresponding States Model for the Thermal Conductivity of Refrigerants and Refrigerant Mixtures," Int. J. Refrigeration, 23(1):43-63, 2000. doi: 10.1016/S0140-7007(99)00024-9
|
|
?
|
|
?The Lennard-Jones parameters were taken from Reid, R.C., Prausnitz, J.M., and Poling, B.E., "The Properties of Gases and Liquids," 4th edition, New York, McGraw-Hill Book Company, 1987.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.348 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
70000.0 !Upper pressure limit [kPa]
|
|
22.419 !Maximum density [mol/L]
|
|
FEQ NITROGEN.FLD
|
|
VS1 !Model for reference fluid viscosity
|
|
TC1 !Model for reference fluid thermal conductivity
|
|
NUL !Large molecule identifier
|
|
1 !Lennard-Jones flag (0 or 1) (0 => use estimates)
|
|
0.43682 !Lennard-Jones coefficient sigma [nm]
|
|
245.0 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
|
|
0.00132 0. 0. 0. !Coefficient, power of T, spare1, spare2
|
|
1 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
|
|
1.0 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
|
1 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
|
1.0 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
|
TK3 !Pointer to critical enhancement auxiliary function
|
|
|
|
|
|
|
|
|
|
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
|
|
|
|
#STN !---Surface tension---
|
|
ST1 !Surface tension model for ethane of Mulero et al. (2012).
|
|
:DOI: 10.1063/1.4768782
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Mulero, A., Cachadiña, I., and Parra, M.I.,
|
|
? "Recommended Correlations for the Surface Tension of Common Fluids,"
|
|
? J. Phys. Chem. Ref. Data, 41(4), 043105, 2012. doi: 10.1063/1.4768782
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
2 !Number of terms in surface tension model
|
|
305.322 !Critical temperature used in fit (dummy)
|
|
0.07602 1.32 !Sigma0 and n
|
|
-0.02912 1.676
|
|
|
|
|
|
#DE !---Dielectric constant---
|
|
DE3 !Dielectric constant model for ethane of Harvey and Lemmon (2005).
|
|
:DOI: 10.1007/s10765-005-2351-5
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Harvey, A.H. and Lemmon, E.W.,
|
|
? "Method for Estimating the Dielectric Constant of Natural Gas Mixtures,"
|
|
? Int. J. Thermophys., 26(1):31-46, 2005. doi: 10.1007/s10765-005-2351-5
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
273.16 1000.0 1.0 !Reducing parameters for T and D
|
|
0 2 4 0 0 0 !Number of terms in dielectric constant model
|
|
11.1552 0. 1. 0. !Coefficient, T exp, D exp
|
|
0.0112 1. 1. 0.
|
|
36.759 0. 2. 0.
|
|
23.639 1. 2. 0.
|
|
-808.03 0. 2.75 0.
|
|
-378.84 1. 2.75 0.
|
|
|
|
|
|
#MLT !---Melting line---
|
|
ML1 !Melting line model for ethane of Buecker and Wagner (2006).
|
|
:DOI: 10.1063/1.1859286
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Bücker, D. and Wagner, W., 2006.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.368 !Lower temperature limit [K]
|
|
2000.0 !Upper temperature limit [K]
|
|
0. !
|
|
0. !
|
|
90.368 0.0011421 !Reducing temperature and pressure
|
|
3 1 0 0 0 0 !Number of terms in melting line equation
|
|
1.0 0.0 !Coefficients and exponents
|
|
105262374. 2.55
|
|
-105262374. 0.0
|
|
223626315. 1.0
|
|
|
|
|
|
#SBL !---Sublimation line---
|
|
SB2 !Sublimation line model for ethane of Brown and Zeigler (2009).
|
|
:DOI: 10.1007/978-1-4613-9856-1_76
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
? Based on G.N. Brown and W.T. Ziegler, Adv. Cryo. Eng., 25:662-670, 1979.
|
|
? Modified to match the triple point of the equation of state.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
20.0 !Lower temperature limit [K]
|
|
90.368 !Upper temperature limit [K]
|
|
0. !
|
|
0. !
|
|
1.0 1000.0 !Reducing temperature and pressure
|
|
6 0 0 0 0 0 !Number of terms in sublimation line equation
|
|
12.8111 0.0 !Coefficients and exponents
|
|
-2.20746e3 -1.0
|
|
-2.4113e4 -2.0
|
|
7.7444e5 -3.0
|
|
-1.1615e7 -4.0
|
|
6.7633e7 -5.0
|
|
|
|
|
|
#PS !---Vapor pressure---
|
|
PS5 !Vapor pressure equation for ethane of Gao (2017).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Gao, K., 2017.
|
|
?
|
|
?Functional Form: P=Pc*EXP[SUM(Ni*Theta^ti)*Tc/T] where Theta=1-T/Tc, Tc and Pc
|
|
? are the reducing parameters below, which are followed by rows containing Ni and ti.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
305.322 4872.2 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
-6.4725 1.0
|
|
1.5079 1.5
|
|
-0.70589 2.0
|
|
-2.1566 4.15
|
|
|
|
|
|
#DL !---Saturated liquid density---
|
|
DL4 !Saturated liquid density equation for ethane of Buecker and Wagner (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Bücker, D. and Wagner, W., 2006.
|
|
?
|
|
?Functional Form: D=Dc*EXP[SUM(Ni*Theta^(ti/3))] where Theta=1-T/Tc, Tc and Dc are
|
|
? the reducing parameters below, which are followed by rows containing Ni and ti.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
305.322 6.856886685 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
1.56138026 0.987
|
|
-0.381552776 2.0
|
|
0.0785372040 4.0
|
|
0.0370315089 9.5
|
|
|
|
#DV !---Saturated vapor density---
|
|
DV3 !Saturated vapor density equation for ethane of Gao (2017).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Gao, K., 2017.
|
|
?
|
|
?Functional Form: D=Dc*EXP[SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are
|
|
? the reducing parameters below, which are followed by rows containing Ni and ti.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
305.322 6.856886685 !Reducing parameters
|
|
5 0 0 0 0 0 !Number of terms in equation
|
|
-2.3513 0.371
|
|
-5.3497 1.09
|
|
-14.875 3.0
|
|
-45.711 6.9
|
|
-117.44 16.5
|
|
|
|
|
|
@END
|
|
c 1 2 3 4 5 6 7 8
|
|
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|