904 lines
43 KiB
Plaintext
904 lines
43 KiB
Plaintext
Ethylene !Short name
|
||
74-85-1 !CAS number
|
||
Ethene !Full name
|
||
CH2=CH2 !Chemical formula {C2H4}
|
||
R-1150 !Synonym
|
||
28.05376 !Molar mass [g/mol]
|
||
103.986 !Triple point temperature [K]
|
||
169.379 !Normal boiling point [K]
|
||
282.35 !Critical temperature [K]
|
||
5041.8 !Critical pressure [kPa]
|
||
7.637 !Critical density [mol/L]
|
||
0.0866 !Acentric factor
|
||
0.0 !Dipole moment [Debye]; (exactly zero due to symmetry)
|
||
NBP !Default reference state
|
||
10.0 !Version number
|
||
1962 !UN Number :UN:
|
||
n-alkene !Family :Family:
|
||
1411.18 !Heating value (upper) [kJ/mol] :Heat:
|
||
3.7 !GWP (IPCC 2007) :GWP:
|
||
A3 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
|
||
1S/C2H4/c1-2/h1-2H2 !Standard InChI String :InChi:
|
||
VGGSQFUCUMXWEO-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
|
||
434e2a40 (ethane) !Alternative fluid for mixing rules :AltID:
|
||
9c1062b0 !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
|
||
! 02-13-96 MM, Original version.
|
||
! 06-24-98 EWL, Add Younglove BWR equation.
|
||
! 10-06-99 EWL, Add Smukala equation.
|
||
! 10-14-99 EWL, Add L-J parameters.
|
||
! 11-01-99 EWL, Add Span 12 term short equation of state.
|
||
! 03-07-00 EWL, Add DDMIX transport properties.
|
||
! 03-07-00 EWL, Add Holland transport properties.
|
||
! 04-26-04 EWL, Change pmax and dmax to match Smukala equation.
|
||
! 08-05-04 EWL, Add Harvey and Lemmon dielectric correlation.
|
||
! 10-14-04 MLH, Add family.
|
||
! 01-03-08 EWL, Add Cp0 equation of Smukala et al. Previous fluid files used the one from Jacobsen (although labeled as from Smukala). However, the maximum difference between the two is about 0.003%.
|
||
! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
|
||
! 08-28-15 MLH, Change TK3 to be consistent with Perkins et al. (2013), added TK1 dummy block, deactivated tco block.
|
||
! 03-29-16 MLH, Add new thermal conductivity model of Koutian et al. (2016).
|
||
! 08-09-16 MLH, Update reference for k model.
|
||
! 05-15-17 EWL, Change the hard coded VS0 model to the VS7 reverse Polish notation.
|
||
! 08-06-17 EWL, Change melting point at Ttrp to match triple point pressure of Smukala et al.
|
||
! 02-28-18 IHB, Add sublimation line model.
|
||
|
||
|
||
|
||
|
||
________________________________________________________________________________
|
||
|
||
#EOS !---Equation of state---
|
||
FEQ !Helmholtz equation of state for ethylene of Smukala et al. (2000).
|
||
:TRUECRITICALPOINT: 282.35 7.63676598 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
|
||
:DOI: 10.1063/1.1329318
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Smukala, J., Span, R., and Wagner, W.,
|
||
? "A New Equation of State for Ethylene Covering the Fluid Region for
|
||
? Temperatures from the Melting Line to 450 K at Pressures up to 300 MPa,"
|
||
? J. Phys. Chem. Ref. Data, 29(5):1053-1122, 2000.
|
||
?
|
||
?The uncertainties in density of the equation of state range from 0.02% in
|
||
? the liquid and most of the vapor phase to 0.1% for supercritical states. At
|
||
? p>100 MPa, the uncertainty in density is 0.5%. The uncertainty in heat
|
||
? capacity is 3% in the liquid phase, 0.2% in the vapor phase, and as high as
|
||
? 5% in the supercritical region at higher pressures. For the speed of sound,
|
||
? the uncertainty is 0.05 to 0.1% in the vapor phase, rising to 3% in the
|
||
? liquid phase. The uncertainty in vapor pressure is less than 0.05%
|
||
? above 140 K.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
300000.0 !Upper pressure limit [kPa]
|
||
27.03 !Maximum density [mol/L]
|
||
CPP !Pointer to Cp0 model
|
||
28.05376 !Molar mass [g/mol]
|
||
103.986 !Triple point temperature [K]
|
||
0.12196 !Pressure at triple point [kPa]
|
||
23.334 !Density at triple point [mol/L]
|
||
169.38 !Normal boiling point temperature [K]
|
||
0.0866 !Acentric factor
|
||
282.35 5041.8 7.63676598 !Tc [K], pc [kPa], rhoc [mol/L]
|
||
282.35 7.63676598 !Reducing parameters [K, mol/L]
|
||
8.31451 !Gas constant [J/mol-K]
|
||
30 4 5 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
||
1.861742910067 0.5 1. 0. !a(i),t(i),d(i),l(i)
|
||
-3.0913708460844 1.0 1. 0.
|
||
-0.17384817095516 2.5 1. 0.
|
||
0.08037098569284 0.0 2. 0.
|
||
0.23682707317354 2.0 2. 0.
|
||
0.021922786610247 0.5 4. 0.
|
||
0.11827885813193 1.0 1. 1.
|
||
-0.021736384396776 4.0 1. 1.
|
||
0.044007990661139 1.25 3. 1.
|
||
0.12554058863881 2.75 4. 1.
|
||
-0.13167945577241 2.25 5. 1.
|
||
-0.0052116984575897 1.0 7. 1.
|
||
0.00015236081265419 0.75 10. 1.
|
||
-0.24505335342756e-4 0.5 11. 1.
|
||
0.28970524924022 2.5 1. 2.
|
||
-0.18075836674288 3.5 1. 2.
|
||
0.15057272878461 4.0 2. 2.
|
||
-0.14093151754458 6.0 2. 2.
|
||
0.022755109070253 1.5 4. 2.
|
||
0.014026070529061 5.0 4. 2.
|
||
0.0061697454296214 4.5 6. 2.
|
||
-0.00041286083451333 15.0 7. 3.
|
||
0.012885388714785 20.0 4. 4.
|
||
-0.069128692157093 23.0 5. 4.
|
||
0.10936225568483 22.0 6. 4.
|
||
-0.0081818875271794 29.0 6. 4.
|
||
-0.05641847211717 19.0 7. 4.
|
||
0.0016517867750633 15.0 8. 4.
|
||
0.0095904006517001 13.0 9. 4.
|
||
-0.0026236572984886 10.0 10. 4.
|
||
-50.242414011355 1.0 2. 2. 2. -25.0 -325.0 1.16 1.0 0. 0. 0.
|
||
7484.6420119299 0.0 2. 2. 2. -25.0 -300.0 1.19 1.0 0. 0. 0.
|
||
-6873.4299232625 1.0 2. 2. 2. -25.0 -300.0 1.19 1.0 0. 0. 0.
|
||
-935.77982814338 2.0 3. 2. 2. -25.0 -300.0 1.19 1.0 0. 0. 0.
|
||
941.33024786113 3.0 3. 2. 2. -25.0 -300.0 1.19 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 ethylene of Smukala et al. (2000).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Smukala, J., Span, R., and Wagner, W., 2000.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
1.0 8.31451 !Reducing parameters for T, Cp0
|
||
1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
||
4.0 0.0
|
||
2.49395851 1251.564081
|
||
3.0027152 1623.061161
|
||
2.5126584 2203.115639
|
||
3.99064217 4400.457333
|
||
|
||
|
||
#AUX !---Auxiliary function for PX0
|
||
PX0 !Helmholtz energy ideal-gas function for ethylene of Smukala et al. (2000).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Smukala, J., Span, R., and Wagner, W., 2000.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
|
||
3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
||
-3.5344235665634898 0.0 !aj, ti for [ai*tau**ti] terms
|
||
3.4196435292559424 1.0 !aj, ti for [ai*tau**ti] terms
|
||
2.49395851 1251.564081 !aj, ti for [ai*log(1-exp(-ti/T)] terms
|
||
3.0027152 1623.061161
|
||
2.5126584 2203.115639
|
||
3.99064217 4400.457333
|
||
|
||
|
||
|
||
|
||
--------------------------------------------------------------------------------
|
||
|
||
@EOS !---Equation of state---
|
||
FE1 !Helmholtz equation of state for ethylene of Jahangiri et al. (1986).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Jahangiri, M., Jacobsen, R.T, Stewart, R.B., and McCarty, R.D.,
|
||
? "Thermodynamic properties of ethylene from the freezing line to 450 K at
|
||
? pressures to 260 MPa,"
|
||
? J. Phys. Chem. Ref. Data, 15(2):593-734, 1986.
|
||
?
|
||
?also summarized in the following references:
|
||
?
|
||
?Jahangiri, M., Jacobsen, R.T, Stewart, R.B., and McCarty, R.D.,
|
||
? "A thermodynamic property formulation for ethylene from the freezing line to
|
||
? 450 K at pressures to 260 MPa,"
|
||
? Int. J. Thermophysics, 17:491-501, 1986.
|
||
?
|
||
?Jacobsen, R.T, Jahangiri, M., Stewart, R.B., McCarty, R.D.,
|
||
? Levelt Sengers, J.M.H., White, H.J.Jr., Sengers, J.V., Olchowy, G.A.,
|
||
? Wakeham, W.A., Angus, S., de Reuck, K.M., and Craven, R.,
|
||
? International Thermodynamic Tables of the Fluid State - Volume 10: Ethylene (Ethene),
|
||
? International Union of Pure and Applied Chemistry, Physical Chemistry
|
||
? Division, Commission on Thermodynamics, Thermodynamic Tables Project, 1988.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450. !Upper temperature limit [K]
|
||
260000.0 !Upper pressure limit [kPa]
|
||
26.67 !Maximum density [mol/L]
|
||
CP1 !Pointer to Cp0 model
|
||
28.054 !Molar mass [g/mol]
|
||
103.986 !Triple point temperature [K]
|
||
0.1225 !Pressure at triple point [kPa]
|
||
23.348 !Density at triple point [mol/L]
|
||
169.350 !Normal boiling point temperature [K]
|
||
0.086 !Acentric factor
|
||
282.3452 5040.1 7.634 !Tc [K], pc [kPa], rhoc [mol/L]
|
||
282.3452 7.634 !Reducing parameters [K, mol/L]
|
||
8.31434 !Gas constant [J/mol-K]
|
||
41 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
||
3.24893703388 0.5 1. 0. !a(i),t(i),d(i),l(i)
|
||
-10.1727886161 1.0 1. 0.
|
||
7.38660405252 1.25 1. 0.
|
||
-1.56891635862 1.75 1. 0.
|
||
-0.0888451428662 4.0 1. 0.
|
||
0.0602106814262 2.0 2. 0.
|
||
0.107832458846 4.0 2. 0.
|
||
-0.0200402521069 5.0 2. 0.
|
||
0.00195049141244 6.0 2. 0.
|
||
0.0671800640346 0.25 3. 0.
|
||
-0.0420045146918 3.0 3. 0.
|
||
-0.00162050762577 0.25 4. 0.
|
||
0.000555515679497 0.5 6. 0.
|
||
0.00075836711463 2.5 6. 0.
|
||
-0.000287854402074 3.0 6. 0.
|
||
0.06258987063 0.5 1. 3.
|
||
-0.0641843116 1.0 1. 3.
|
||
-0.1368693752 0.5 2. 2.
|
||
0.517920766 2.0 2. 2.
|
||
-0.3026331319 4.0 2. 2.
|
||
0.7757213872 3.0 2. 4.
|
||
-2.639890864 4.0 2. 4.
|
||
2.927563554 5.0 2. 4.
|
||
-1.066267599 6.0 2. 4.
|
||
-0.0538047154 2.0 2. 6.
|
||
0.127792108 3.0 2. 6.
|
||
-0.0745015231 4.0 2. 6.
|
||
-0.01624304356 1.5 3. 3.
|
||
0.1476032429 0.5 4. 2.
|
||
-0.2003910489 1.5 4. 2.
|
||
0.2926905618 4.0 4. 2.
|
||
-0.1389040901 5.0 4. 2.
|
||
5.913513541 1.0 4. 4.
|
||
-38.0037013 2.0 4. 4.
|
||
96.9194057 3.0 4. 4.
|
||
-122.6256839 4.0 4. 4.
|
||
77.02379476 5.0 4. 4.
|
||
-19.22684672 6.0 4. 4.
|
||
-0.003800045701 0.5 8. 2.
|
||
0.01118003813 1.0 8. 2.
|
||
0.002945841426 5.0 8. 2.
|
||
|
||
|
||
@AUX !---Auxiliary function for Cp0
|
||
CP1 !Ideal gas heat capacity function for ethylene of Jahangiri et al.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Jahangiri, M., Jacobsen, R.T, Stewart, R.B., and McCarty, R.D.,
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
1.0 8.31434 !Reducing parameters for T, Cp0
|
||
1 12 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
||
4.0 0.0
|
||
1.0 4353.9071 ! omega_1 * hc/k = omega_1 * 1.4388325
|
||
1.0 2335.2251 ! omega_2 * hc/k
|
||
1.0 1930.9132 ! omega_3 * hc/k
|
||
1.0 1471.9256 ! omega_4 * hc/k
|
||
1.0 4464.6972 ! omega_5 * hc/k
|
||
1.0 1778.397 ! omega_6 * hc/k
|
||
1.0 1365.452 ! omega_7 * hc/k
|
||
1.0 1356.819 ! omega_8 * hc/k
|
||
1.0 4469.0137 ! omega_9 * hc/k
|
||
1.0 1188.4756 ! omega_1 * hc/k
|
||
1.0 4300.6703 ! omega_11 * hc/k
|
||
1.0 2077.6741 ! omega_12 * hc/k
|
||
|
||
|
||
@EOS !---Equation of state---
|
||
FES !Helmholtz equation of state for ethylene 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.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
600.0 !Upper temperature limit [K]
|
||
100000.0 !Upper pressure limit [kPa]
|
||
27.03 !Maximum density [mol/L]
|
||
CPP !Pointer to Cp0 model
|
||
28.054 !Molar mass [g/mol]
|
||
103.986 !Triple point temperature [K]
|
||
0.12123 !Pressure at triple point [kPa]
|
||
23.34 !Density at triple point [mol/L]
|
||
169.37 !Normal boiling point temperature [K]
|
||
0.087 !Acentric factor
|
||
282.35 5042.0 7.6367006 !Tc [K], pc [kPa], rhoc [mol/L]
|
||
282.35 7.6367006 !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
|
||
0.9096223 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
||
-2.4641015 1.125 1. 0.
|
||
0.56175311 1.5 1. 0.
|
||
-0.019688013 1.375 2. 0.
|
||
0.078831145 0.25 3. 0.
|
||
0.00021478776 0.875 7. 0.
|
||
0.23151337 0.625 2. 1.
|
||
-0.037804454 1.75 5. 1.
|
||
-0.20122739 3.625 1. 2.
|
||
-0.044960157 3.625 4. 2.
|
||
-0.02834296 14.5 3. 3.
|
||
0.012652824 12.0 4. 3.
|
||
|
||
|
||
@EOS !---Equation of state---
|
||
BWR !MBWR equation of state for ethylene of McCarty and Jacobsen (1981).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?McCarty, R.D., Jacobsen, R.T,
|
||
? "An Equation of State for Fluid Ethylene,"
|
||
? Natl. Bur. Stand., Tech. Note 1045, 1981.
|
||
?
|
||
?see also:
|
||
?Younglove, B.A.,
|
||
? "Thermophysical Properties of Fluids. I. Argon, Ethylene,
|
||
? Parahydrogen, Nitrogen, Nitrogen Trifluoride, and Oxygen,"
|
||
? J. Phys. Chem. Ref. Data, Vol. 11, Suppl. 1, pp. 1-11, 1982.
|
||
? All temperatures on IPTS-68
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
400.0 !Upper temperature limit [K]
|
||
40000.0 !Upper pressure limit [kPa]
|
||
23.343 !Maximum density [mol/L]
|
||
CP1 !Pointer to Cp0 model
|
||
28.054 !Molar mass [g/mol]
|
||
103.986 !Triple point temperature [K]
|
||
0.1213 !Pressure at triple point [kPa]
|
||
23.343 !Density at triple point [mol/L]
|
||
169.350 !Normal boiling point temperature [K]
|
||
0.086 !Acentric factor
|
||
282.3428 5040.4 7.65 !Tc [K], pc [kPa], rhoc [mol/L]
|
||
282.3428 7.65 !Reducing parameters [K, mol/L]
|
||
7.62492852 !gamma
|
||
0.0831434 !Gas constant [L-bar/mol-K]
|
||
32 1 !Nterm, Ncoeff per term
|
||
-0.02146684366683 1.791433722534 -36.7531560393
|
||
3707.178934669 -319828.2566709 0.0005809379774732
|
||
-0.7895570824899 114.8620375835 271377.4629193
|
||
-0.8647124319107e-4 0.1617727266385 -27.31527496271
|
||
-0.002672283641459 -0.0475238133199 -62.55637346217
|
||
0.004576234964434 -0.753483926932e-4 0.1638171982209
|
||
-0.00356309074074 -183300.078317 -18050742.09985
|
||
-4794.587918874 35319482.74957 -25.62571039155
|
||
1044.308253292 -0.1695303363659 -1710.334224958
|
||
-0.0002054114462372 0.06727558766661 -0.1557168403328e-5
|
||
-0.0001229814736077 0.0004234325938573
|
||
|
||
|
||
@AUX !---Auxiliary function for Cp0
|
||
CP1 !Ideal gas heat capacity function for ethylene of McCarty and Jacobsen (1981).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?McCarty, R.D., Jacobsen, R.T,
|
||
? "An Equation of State for Fluid Ethylene,"
|
||
? Natl. Bur. Stand., Tech. Note 1045, 1981.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
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
|
||
560361.5762 -3.0
|
||
-21410.69802 -2.0
|
||
253.2008897 -1.0
|
||
3.554495281 0.0
|
||
-0.009951927478 1.0
|
||
0.0000510893107 2.0
|
||
-0.1928667482e-7 3.0
|
||
-20.61703241 3000.0
|
||
|
||
|
||
|
||
|
||
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
||
|
||
#ETA !---Viscosity---
|
||
VS7 !Pure fluid viscosity model for ethylene of Holland et al. (1983).
|
||
:DOI: 10.1063/1.555701
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Holland, P.M., Eaton, B.E., and Hanley, H.J.M.,
|
||
? "A Correlation of the Viscosity and Thermal Conductivity Data of
|
||
? Gaseous and Liquid Ethylene,"
|
||
? J. Phys. Chem. Ref. Data, 12(4):917-932, 1983.
|
||
?
|
||
?The uncertainty in viscosity is 5%, increasing to 10% in the dense liquid phase.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
300000.0 !Upper pressure limit [kPa]
|
||
27.03 !Maximum density [mol/L]
|
||
NUL !Pointer to collision integral model
|
||
!
|
||
!Dilute gas function
|
||
$DG RED SUMTTHRD:9
|
||
!
|
||
!Residual function
|
||
$RF RED SUMEX:2 SUM:2 SUM:1 * SUM:2 SUM:1 * SUM:3 * + EXP CNST + *
|
||
!
|
||
!Coefficients
|
||
$CF
|
||
0.1 1. 1. 0. 0 !Reducing parameters for eta, T, rho
|
||
-3509822.5018 -3. 0. 0. 0
|
||
2500840.6184 -2. 0. 0. 0
|
||
-583655.40744 -1. 0. 0. 0
|
||
4554.9146583 0. 0. 0. 0
|
||
22881.683403 1. 0. 0. 0
|
||
-4731.8682077 2. 0. 0. 0
|
||
450.22249258 3. 0. 0. 0
|
||
-21.490688088 4. 0. 0. 0
|
||
0.41649263233 5. 0. 0. 0
|
||
0.1 1.0 35.64584569 0. 0 !Reducing parameters for eta, T, rho
|
||
-4.8544486732 0. 0. 0. 0 ! EXP(v1+v4/T)
|
||
-1824.1971308 -1. 0. 0. 0
|
||
13.033585236 0. 0. 0. 0 ! (v2+v3/T^1.5)
|
||
27808.928908 -1.5 0. 0. 0
|
||
1.0 0. 0.1 0. 0 ! dd^0.1
|
||
4.524886877828 0. 1. 0. 0 ! (dd/0.221-1)*SQRT(dd)
|
||
-1.0 0. 0. 0. 0
|
||
1.0 0. 0.5 0. 0
|
||
1.5913024509 0. 0. 0. 0 ! *(v5+v6/T+v7/T^2)
|
||
-205.13573927 -1. 0. 0. 0
|
||
-39478.454708 -2. 0. 0. 0
|
||
-1. 0. 0. 0. 0
|
||
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
||
|
||
|
||
|
||
|
||
================================================================================
|
||
|
||
#TCX !---Thermal conductivity---
|
||
TC1 !Pure fluid thermal conductivity model for ethylene of Assael et al. (2016).
|
||
:DOI: 10.1063/1.4958984
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Assael, M.J., Koutian, A., Huber, M.L., and Perkins, R.A.,
|
||
? "Reference Correlations of the Thermal Conductivity of Ethylene and Propylene,"
|
||
? J. Phys. Chem. Ref. Data, 45(3), 033104, 2016.
|
||
? doi: 10.1063/1.4958984
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
300000.0 !Upper pressure limit [kPa]
|
||
27.03 !Maximum density [mol/L]
|
||
7 5 !# terms for dilute gas function: numerator, denominator
|
||
282.35 0.001 !Reducing parameters for T, tcx
|
||
-54.1761 0.
|
||
541.904 1.
|
||
-656.108 2.
|
||
667.048 3.
|
||
-109.992 4.
|
||
60.6511 5.
|
||
-1.01377 6.
|
||
26.5363 0.
|
||
-20.1401 1.
|
||
19.4152 2.
|
||
-2.9269 3.
|
||
1.0 4.
|
||
10 0 !# terms for background gas function: numerator, denominator
|
||
282.35 7.637 1. !Reducing parameters for T, rho, tcx
|
||
0.0261453 0. 1. 0.
|
||
-0.0218619 0. 2. 0.
|
||
0.0362068 0. 3. 0.
|
||
-0.0136642 0. 4. 0.
|
||
0.00184752 0. 5. 0.
|
||
-0.0113225 1. 1. 0.
|
||
0.0269282 1. 2. 0.
|
||
-0.0223164 1. 3. 0.
|
||
0.00390241 1. 4. 0.
|
||
0.000668286 1. 5. 0.
|
||
TK3 !Pointer to critical enhancement auxiliary function
|
||
|
||
|
||
#AUX !---Auxiliary function for the thermal conductivity critical enhancement
|
||
TK3 !Simplified thermal conductivity critical enhancement for ethylene of Perkins et al. (2013).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Perkins, R.A., Sengers, J.V., Abdulagatov, I.M., and Huber, M.L.,
|
||
? "Simplified Model for the Critical Thermal-Conductivity Enhancement in Molecular Fluids,"
|
||
? Int. J. Thermophys., 34(2):191-212, 2013. doi: 10.1007/s10765-013-1409-z
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
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)
|
||
1.239 !Gamma (universal exponent)
|
||
1.02 !R0 (universal amplitude)
|
||
0.063 !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)
|
||
0.181e-9 !Xi0 (amplitude) [m]
|
||
0.058 !Gam0 (amplitude) [-]
|
||
0.49e-9 !Qd_inverse (modified effective cutoff parameter) [m]
|
||
423.53 !Tref (reference temperature) [K]
|
||
|
||
|
||
|
||
|
||
********************************************************************************
|
||
|
||
@TCX !---Thermal conductivity---
|
||
TC7 !Pure fluid thermal conductivity model for ethylene of Holland et al. (1983).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Holland, P.M., Eaton, B.E., and Hanley, H.J.M.,
|
||
? "A Correlation of the Viscosity and Thermal Conductivity Data of
|
||
? Gaseous and Liquid Ethylene,"
|
||
? J. Phys. Chem. Ref. Data, 12(4):917-932, 1983.
|
||
?
|
||
?The uncertainty in thermal conductivity is 5%, increasing to 10% in the dense
|
||
? liquid.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
300000.0 !Upper pressure limit [kPa]
|
||
27.03 !Maximum density [mol/L]
|
||
$DG RED SUMTTHRD:9
|
||
$RF RED SUMEX:2 SUM:2 DR CNST / 1 - DR SQRT * SUM:3 * + EXP 1 - *
|
||
$CF
|
||
0.001 1. 35.64584569 0. 0
|
||
-290342.35280 -3. 0. 0. 0
|
||
468062.49520 -2. 0. 0. 0
|
||
-189547.83215 -1. 0. 0. 0
|
||
-4826.2235392 0. 0. 0. 0
|
||
22434.093720 1. 0. 0. 0
|
||
-6620.6354818 2. 0. 0. 0
|
||
899.37717078 3. 0. 0. 0
|
||
-60.559143718 4. 0. 0. 0
|
||
1.6370306422 5. 0. 0. 0
|
||
0.001 1. 35.64584569 0. 0
|
||
-13.045033230 0. 0. 0. 0
|
||
742.05216310 -1. 0. 0. 0
|
||
18.214616599 0. 0.1 0. 0
|
||
-9903.0224960 -1.5 0.1 0. 0
|
||
0.221 0. 0. 0. 0
|
||
-0.30083271933 0. 0. 0. 0
|
||
96.456068829 -1. 0. 0. 0
|
||
13502.569620 -2. 0. 0. 0
|
||
TK3 !Pointer to critical enhancement auxiliary function
|
||
|
||
|
||
@ETA !---Viscosity---
|
||
VS2 !Pure fluid viscosity model from NIST14 for ethylene.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Coefficients are taken from NIST14, Version 9.08
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
300000.0 !Upper pressure limit [kPa]
|
||
27.03 !Maximum density [mol/L]
|
||
CI0 !Pointer to collision integral model
|
||
0.4163 !Lennard-Jones coefficient sigma [nm]
|
||
224.7 !Lennard-Jones coefficient epsilon/kappa [K]
|
||
0.141374566253583 !Const
|
||
0.5 !Exponent for T
|
||
0.0 !Coefficient for initial density dependence of viscosity
|
||
0.0
|
||
0.0
|
||
100.0
|
||
-8.03553028329404 !Coefficients for residual viscosity
|
||
-439.8962514
|
||
8.69536237617
|
||
5773.08496161
|
||
0.267589139152
|
||
-34.39391627
|
||
66.4795135739
|
||
7.63299886259
|
||
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
||
|
||
|
||
|
||
|
||
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
||
|
||
@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (Nitrogen reference); predictive mode for ethylene.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
128. !Lower temperature limit [K] based on Tc ratio with ref fluid
|
||
400.0 !Upper temperature limit [K]
|
||
40000.0 !Upper pressure limit [kPa]
|
||
27.03 !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)
|
||
0.4163 !Lennard-Jones coefficient sigma [nm] for ECS method
|
||
224.7 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
|
||
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 ethylene of Mulero et al. (2012).
|
||
:DOI: 10.1063/1.4768782
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Mulero, A., Cachadi<64>a, 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. !
|
||
1 !Number of terms in surface tension model
|
||
282.35 !Critical temperature used in fit (dummy)
|
||
0.0477 1.17 !Sigma0 and n
|
||
|
||
|
||
#DE !---Dielectric constant---
|
||
DE3 !Dielectric constant model for ethylene 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 1 4 0 0 0 !Number of terms in dielectric constant model
|
||
10.725 0. 1. 0. !Coefficient, T exp, D exp
|
||
55.19 0. 2. 0.
|
||
49.5 1. 2. 0.
|
||
-2045.0 0. 2.9 0.
|
||
-1154.0 1. 2.9 0.
|
||
|
||
|
||
#MLT !---Melting line---
|
||
ML1 !Melting line model for ethylene of Jahangiri et al. (1986).
|
||
:DOI: 10.1063/1.555753
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Jahangiri, M., Jacobsen, R.T, Stewart, R.B., and McCarty, R.D., 2005.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450. !Upper temperature limit [K]
|
||
0. !
|
||
0. !
|
||
103.986 1000. !Reducing temperature and pressure
|
||
3 0 0 0 0 0 !Number of terms in melting line equation
|
||
0.00012196 0.0 !Coefficients and exponents
|
||
357.924 2.0645
|
||
-357.924 0.0
|
||
|
||
|
||
#SBL !---Sublimation line---
|
||
SB2 !Sublimation line model for ethylene 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]
|
||
103.986 !Upper temperature limit [K]
|
||
0. !
|
||
0. !
|
||
1.0 1000.0 !Reducing temperature and pressure
|
||
5 0 0 0 0 0 !Number of terms in sublimation line equation
|
||
13.0909 0.0 !Coefficients and exponents
|
||
-2.20575e3 -1.0
|
||
-1.2163e4 -2.0
|
||
2.8429e5 -3.0
|
||
-2.2033e6 -4.0
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for ethylene of Smukala et al. (2000).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Smukala, J., Span, R., and Wagner, W., 2000.
|
||
?
|
||
?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. !
|
||
282.35 5041.8 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-6.3905741 1.0
|
||
1.4060338 1.5
|
||
-1.6589923 2.5
|
||
1.0278028 3.0
|
||
-2.5071716 4.5
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL4 !Saturated liquid density equation for ethylene of Smukala et al. (2000).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Smukala, J., Span, R., and Wagner, W., 2000.
|
||
?
|
||
?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. !
|
||
282.35 7.63676598 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
1.8673079 1.029
|
||
-0.61533892 1.5
|
||
-0.058973772 4.0
|
||
0.10744720 6.0
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV4 !Saturated vapor density equation for ethylene of Smukala et al. (2000).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Smukala, J., Span, R., and Wagner, W., 2000.
|
||
?
|
||
?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. !
|
||
282.35 7.63676598 !Reducing parameters
|
||
6 0 0 0 0 0 !Number of terms in equation
|
||
-1.9034556 1.047
|
||
-0.75837929 2.0
|
||
-3.7717969 3.0
|
||
-8.7478586 7.0
|
||
-23.885296 14.5
|
||
-54.197979 28.0
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
||
|
||
|
||
@TCX !Thermal conductivity model specification
|
||
TC1 pure fluid thermal conductivity model
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Coefficients are taken from NIST14, Version 9.08
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
300000.0 !Upper pressure limit [kPa]
|
||
27.03 !Maximum density [mol/L]
|
||
3 0 !# terms for dilute gas function: numerator, denominator
|
||
224.7 0.001 !Reducing parameters for T, tcx
|
||
1.35558587 0. !Coefficient, power in T
|
||
-0.14207565869509 -1.0 !Coefficient, power in T
|
||
1. -96. !Coefficient, power in T
|
||
6 0 !# terms for background gas function: numerator, denominator
|
||
282.350007277 7.63299886259 0.001 !Reducing parameters for T, rho, tcx
|
||
15.3064493136 0. 1. 0. !Coefficient, powers of T, rho, exp(rho)
|
||
25.0280721432 0. 3. 0.
|
||
-15.4526955192 0. 4. 0.
|
||
0.8590418672 -1. 4. 0.
|
||
3.32700049633 0. 5. 0.
|
||
-0.333048907849 -1. 5. 0.
|
||
TK3 !Pointer to critical enhancement auxiliary function
|
||
|
||
|
||
@AUX !---Thermal conductivity critical enhancement model
|
||
TK3 simplified thermal conductivity critical enhancement
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
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)
|
||
1.2415 !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)
|
||
0.0834e-9 !xi0 (amplitude) [m]
|
||
0.0532 !gam0 (amplitude) [-]
|
||
0.418e-9 !qd_inverse (modified effective cutoff parameter) [m]
|
||
564.7 !Tref (reference temperature) [K]
|
||
|
||
|
||
@ETA !Viscosity model specification
|
||
VS0 pure fluid viscosity model of Holland et al. (1983).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Holland, P.M., Eaton, B.E., and Hanley, H.J.M.,
|
||
? "A Correlation of the Viscosity and Thermal Conductivity Data of
|
||
? Gaseous and Liquid Ethylene,"
|
||
? J. Phys. Chem. Ref. Data, 12(4):917-932, 1983.
|
||
?
|
||
?The uncertainty in viscosity is 5%, increasing to 10% in the dense liquid.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
300000.0 !Upper pressure limit [kPa]
|
||
27.03 !Maximum density [mol/L]
|
||
ETY !Pointer to hardcoded thermal conductivity model
|
||
0 0 0 0 0 0 0 0 !Number of terms for various pieces
|
||
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
||
|
||
|
||
@TCX !Thermal conductivity model specification
|
||
TC0 pure fluid thermal conductivity model of Holland et al. (1983).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Holland, P.M., Eaton, B.E., and Hanley, H.J.M.,
|
||
? "A Correlation of the Viscosity and Thermal Conductivity Data of
|
||
? Gaseous and Liquid Ethylene,"
|
||
? J. Phys. Chem. Ref. Data, 12(4):917-932, 1983.
|
||
?
|
||
?The uncertainty in thermal conductivity is 5%, increasing to 10% in the dense
|
||
? liquid.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
103.986 !Lower temperature limit [K]
|
||
450.0 !Upper temperature limit [K]
|
||
300000.0 !Upper pressure limit [kPa]
|
||
27.03 !Maximum density [mol/L]
|
||
ETY !Pointer to hardcoded thermal conductivity model
|
||
0 0 0 0 0 0 0 0 !Number of terms for various pieces
|
||
TK3 !Pointer to critical enhancement auxiliary function
|
||
|
||
|