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., Cachadiņa, 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