R1234ze(E) !Short name 29118-24-9 !CAS number trans-1,3,3,3-Tetrafluoropropene !Full name CHF=CHCF3 (trans) !Chemical formula {C3F4H2} HFO-1234ze(E) !Synonym 114.0416 !Molar mass [g/mol] 169.0 !Triple point temperature [K] 254.177 !Normal boiling point [K] 382.513 !Critical temperature [K] 3634.9 !Critical pressure [kPa] 4.29 !Critical density [mol/L] 0.313 !Acentric factor 1.27 !Dipole moment [Debye]; Cousins and Laesecke, J. Research NIST, 117:231-256, 2012 IIR !Default reference state 10.0 !Version number ???? !UN Number :UN: halocb !Family :Family: ???? !Heating value (upper) [kJ/mol] :Heat: 6.0 !GWP :GWP: A2L !Safety Group (ASHRAE Standard 34, 2010) :Safety: 1S/C3H2F4/c4-2-1-3(5,6)7/h1-2H/b2-1+ !Standard InChI String :InChi: CDOOAUSHHFGWSA-OWOJBTEDSA-N !Standard InChI Key :InChiKey: 40377b40 (R1234yf) !Alternative fluid for mixing rules :AltID: 9905ef70 !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. Thol, Thermodynamics, Ruhr-Universitaet Bochum, Germany ! 11-30-09 MT, Original version. ! 04-14-10 MT, Update with new equation of state fitted to McLinden data. ! 06-22-10 MT, Update with new equation fitted to Lago speed of sound data. ! 09-07-10 EWL, Finalize fit. ! 09-07-10 MLH, Add preliminary transport. ! 12-02-11 EWL, Change reference state from NBP to IIR. ! 02-10-11 EWL, Change CAS number to match the (E) isomer, not a mixture of (E) and (Z). ! 05-17-12 MLH, Add dipole moment from Cousins, D.S.& Laesecke, A., J. Res. NIST submitted 2012. ! 05-17-12 MLH, Update thermal conductivity to match 2011 publication. ! 03-19-13 EWL, Update equation of state fitted to sound speed data of McLinden and PVT data of Klomfar. ! 04-17-14 EWL, Add surface tension coefficients of Mulero et al. (2014). ! 11-11-14 EWL, Minor updates to comply with new publication of this equation. ! 03-01-16 MLH, Add new viscosity correlation. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for R-1234ze(E) of Thol and Lemmon (2016). :TRUECRITICALPOINT: 382.513 4.29 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: 10.1007/s10765-016-2040-6 ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M. and Lemmon, E.W., ? "Equation of State for the Thermodynamic Properties of ? trans-1,3,3,3-Tetrafluoropropene [R1234ze(E)]," ? Int. J. Thermophys., 37:28, 2016. doi: 10.1007/s10765-016-2040-6 ? ?The uncertainty in density in the liquid and vapor phases is 0.1% from 200 K to ? 420 K at all pressures. The uncertainty increases outside of this temperature ? region and in the critical region. In the gaseous phase, speeds of sound can be ? calculated with an uncertainty of 0.05%. In the liquid phase, the uncertainty ? in speed of sound increases to 0.1%. The estimated uncertainty for liquid heat ? capacities is 5%. The uncertainty in vapor pressure is 0.1%. ? !``````````````````````````````````````````````````````````````````````````````` 169.0 !Lower temperature limit [K] 420.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 13.25 !Maximum density [mol/L] CPP !Pointer to Cp0 model 114.0416 !Molar mass [g/mol] 169.0 !Triple point temperature [K] 0.2286 !Pressure at triple point [kPa] 13.25 !Density at triple point [mol/L] 254.177 !Normal boiling point temperature [K] 0.313 !Acentric factor 382.513 3634.9 4.29 !Tc [K], pc [kPa], rhoc [mol/L] 382.513 4.29 !Reducing parameters [K, mol/L] 8.3144598 !Gas constant [J/mol-K] 10 4 6 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.03982797 1.0 4. 0. !a(i),t(i),d(i),l(i) 1.812227 0.223 1. 0. -2.537512 0.755 1. 0. -0.5333254 1.24 2. 0. 0.1677031 0.44 3. 0. -1.323801 2.0 1. 2. -0.6694654 2.2 3. 2. 0.8072718 1.2 2. 1. -0.7740229 1.5 2. 2. -0.01843846 0.9 7. 1. 1.407916 1.33 1. 2. 2. -1.0 -1.21 0.943 0.728 0. 0. 0. -0.4237082 1.75 1. 2. 2. -1.61 -1.37 0.642 0.87 0. 0. 0. -0.2270068 2.11 3. 2. 2. -1.24 -0.98 0.59 0.855 0. 0. 0. -0.805213 1.0 3. 2. 2. -9.34 -171. 1.2 0.79 0. 0. 0. 0.00994318 1.5 2. 2. 2. -5.78 -47.4 1.33 1.3 0. 0. 0. -0.008798793 1.0 1. 2. 2. -3.08 -15.4 0.64 0.71 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 R-1234ze(E) of Thol and Lemmon (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M. and Lemmon, E.W., 2016. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.3144598 !Reducing parameters for T, Cp0 1 2 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.0 0.0 9.3575 513.0 10.717 1972.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for R-1234ze(E) of Thol and Lemmon (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M. and Lemmon, E.W., 2016. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 2 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 -12.5583513312376738 0.0 !aj, ti for [ai*tau**ti] terms 8.7912317462661171 1.0 !aj, ti for [ai*tau**ti] terms 9.3575 513.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms 10.717 1972.0 #AUX !---Auxiliary function for PH0 PH0 !Ideal gas Helmholtz form for R-1234ze(E) of Thol and Lemmon (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M. and Lemmon, E.W., 2016. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 2 2 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh 3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms -12.558347537 0.0 !aj, ti for [ai*tau**ti] terms 8.7912297624 1.0 9.3575 -1.3411308897 !aj, ti for [ai*log(1-exp(ti*tau)] terms 10.717 -5.15538034 -------------------------------------------------------------------------------- @EOS !---Equation of state--- FE1 !Helmholtz equation of state for R-1234ze(E) of McLinden et al. (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?unpublished equation, but similar to the form given in: ? McLinden, M.O., Thol, M., and Lemmon, E.W. ? "Thermodynamic Properties of trans-1,3,3,3-Tetrafluoropropene [R1234ze(E)]: ? Measurements of Density and Vapor Pressure and a Comprehensive Equation of State," ? International Refrigeration and Air Conditioning Conference at Purdue, ? July 12-15, 2010. ? ?The uncertainty in density in the liquid phase of the equation of state is ? 0.1% from 240 K to 320 K and pressures up to 10 MPa. The uncertainty ? increases outside of this region and in the vapor phase to 0.5%, and even ? higher in the critical region. In the gaseous region, the speed of sound can ? be calculated with an uncertainty of 0.1%. In the liquid phase, the ? uncertainty increases to 0.5%. The estimated uncertainty for heat capacities ? is 5%. The estimated uncertainty in vapor pressure is 0.1%. ? !``````````````````````````````````````````````````````````````````````````````` 168.62 !Lower temperature limit [K] 420.0 !Upper temperature limit [K] 20000.0 !Upper pressure limit [kPa] 13.20 !Maximum density [mol/L] CP1 !Pointer to Cp0 model 114.0415928 !Molar mass [g/mol] 168.62 !Triple point temperature [K] 0.2312 !Pressure at triple point [kPa] 13.19 !Density at triple point [mol/L] 254.2 !Normal boiling point temperature [K] 0.313 !Acentric factor 382.52 3636.25 4.29 !Tc [K], pc [kPa], rhoc [mol/L] 382.52 4.29 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 10 4 5 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.04434245 1.0 4. 0. !a(i),t(i),d(i),l(i) 1.646369 0.31 1. 0. -2.437488 0.923 1. 0. -0.5170560 1.06 2. 0. 0.1815626 0.44 3. 0. -1.210104 2.08 1. 2. -0.5944653 2.32 3. 2. 0.7521992 1.25 2. 1. -0.6747216 2.0 2. 2. -0.02448183 1.0 7. 1. 1.379434 0.93 1. 2. 2. -1.0 -1.64 1.13 0.711 0. 0. 0. -0.4697024 1.93 1. 2. 2. -1.4 -1.57 0.61 0.856 0. 0. 0. -0.2036158 2.69 3. 2. 2. -1.134 -1.49 0.65 0.753 0. 0. 0. -0.08407447 1.0 3. 2. 2. -7.68 -257.0 1.13 0.772 0. 0. 0. 0.0005109529 2.0 2. 2. 2. -24.0 -45.0 1.34 1.88 0. 0. 0. @AUX !---Auxiliary function for Cp0 CP1 !Ideal gas heat capacity function for R-1234ze(E). ? ?``````````````````````````````````````````````````````````````````````````````` ? McLinden, M.O., Thol, M., and Lemmon, E.W. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.314472 !Reducing parameters for T, Cp0 1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 6.259 0.0 7.303 691.0 8.597 1705.0 2.333 4216.0 @EOS !---Equation of state--- FE2 !Helmholtz equation of state for R-1234ze(E) of McLinden et al. (2010). ? ?``````````````````````````````````````````````````````````````````````````````` ?McLinden, M.O., Thol, M., and Lemmon, E.W. ? "Thermodynamic Properties of trans-1,3,3,3-Tetrafluoropropene [R1234ze(E)]: ? Measurements of Density and Vapor Pressure and a Comprehensive Equation of State," ? International Refrigeration and Air Conditioning Conference at Purdue, ? July 12-15, 2010. ? !``````````````````````````````````````````````````````````````````````````````` 168.62 !Lower temperature limit [K] 420.0 !Upper temperature limit [K] 20000.0 !Upper pressure limit [kPa] 13.20 !Maximum density [mol/L] CP2 !Pointer to Cp0 model 114.0415928 !Molar mass [g/mol] 168.62 !Triple point temperature [K] 0.23 !Pressure at triple point [kPa] 13.19 !Density at triple point [mol/L] 254.2 !Normal boiling point temperature [K] 0.313 !Acentric factor 382.52 3636.25 4.29 !Tc [K], pc [kPa], rhoc [mol/L] 382.52 4.29 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 10 4 4 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.0555630 1.0 4. 0. !a(i),t(i),d(i),l(i) 1.66927 0.34 1. 0. -2.53408 0.91 1. 0. -0.475075 1.23 2. 0. 0.190055 0.46 3. 0. -1.25154 2.26 1. 2. -0.742195 2.50 3. 2. 0.537902 2.0 2. 1. -0.741246 2.24 2. 2. -0.0355064 0.90 7. 1. 1.58506 1.06 1. 2. 2. -1.02 -1.19 1.140 0.711 0. 0. 0. -0.502086 1.79 1. 2. 2. -1.34 -2.29 0.667 0.914 0. 0. 0. -0.191360 3.75 3. 2. 2. -1.08 -1.15 0.505 0.694 0. 0. 0. -0.975576 0.92 3. 2. 2. -6.41 -131.8 1.220 0.731 0. 0. 0. @AUX !---Auxiliary function for Cp0 CP2 !Ideal gas heat capacity function for R-1234ze(E). ? ?``````````````````````````````````````````````````````````````````````````````` ?McLinden, M.O., Thol, M., and Lemmon, E.W. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.314472 !Reducing parameters for T, Cp0 1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 5.8887 0.0 7.0804 620.0 9.3371 1570.0 2.5577 3953.0 @EOS !---Equation of state--- FE3 !Helmholtz equation of state for R-1234ze(E) of Akasaka (2011). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R., ? "New Fundamental Equations of State with a Common Functional Form for ? 2,3,3,3-Tetrafluoropropene (R-1234yf) and trans-1,3,3,3-Tetrafluoropropene ? (R-1234ze(E))," ? Int. J. Thermophys., 32(6):1125-1147, 2011. ? !``````````````````````````````````````````````````````````````````````````````` 240.0 !Lower temperature limit [K] 420.0 !Upper temperature limit [K] 15000.0 !Upper pressure limit [kPa] 13.20 !Maximum density [mol/L] CP3 !Pointer to Cp0 model 114.042 !Molar mass [g/mol] 168.62 !Triple point temperature [K] 0.23 !Pressure at triple point [kPa] 13.19 !Density at triple point [mol/L] 254.2 !Normal boiling point temperature [K] 0.313 !Acentric factor 382.51 3632.0 4.261587836 !Tc [K], pc [kPa], rhoc [mol/L] 382.52 4.261587836 !Reducing parameters [K, mol/L] 8.314472 !Gas constant [J/mol-K] 17 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 8.5579765 0.66886 1. 0. !a(i),t(i),d(i),l(i) -9.4701332 0.83392 1. 0. -0.25013623 1.6982 1. 0. 0.13789870 1.8030 2. 0. 0.012177113 0.36657 5. 0. -0.14227996 3.8666 1. 1. 0.10096648 1.0194 3. 1. 0.017504319 0.0 5. 1. -0.017627303 1.1655 7. 1. -0.01470512 8.3101 1. 2. 0.37202269 6.1459 2. 2. -0.30138266 8.3495 2. 2. -0.092927274 6.0422 3. 2. 0.087051177 7.444 4. 2. 0.01811377 15.433 2. 3. -0.016018424 21.543 3. 3. 0.005380986 15.499 5. 3. @AUX !---Auxiliary function for Cp0 CP3 !Ideal gas heat capacity function for R-1234ze(E) of Akasaka (2011). ? ?``````````````````````````````````````````````````````````````````````````````` ?Akasaka, R., ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.314472 !Reducing parameters for T, Cp0 1 2 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.0 0.0 6.07536 289.0 9.95795 1303.0 ^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^ #ETA !---Viscosity--- VS7 !Pure fluid viscosity model for R-1234ze(E) of Huber and Assael (2016). :DOI: 10.1016/j.ijrefrig.2016.08.007 ? ?``````````````````````````````````````````````````````````````````````````````` ?Huber, M.L. and Assael, M.J., ? "Correlations for the Viscosity of 2,3,3,3-Tetrafluoroprop-1-ene (R1234yf) ? and trans-1,2,2,2-Tetrafluoropropene (R1234ze(E))," ? Int. J. Refrig., 71:39-45, 2016. ? doi: 10.1016/j.ijrefrig.2016.08.007 ? ?The estimated uncertainty for the dilute gas region is 3%, for the liquid phase at pressures to 30 MPa is 3.5%. ? !``````````````````````````````````````````````````````````````````````````````` 169.0 !Lower temperature limit [K] 420.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 14.0 !Maximum density [mol/L] NUL !Omega model ! !Dilute gas function $DG SUM:4 SUM:3 / ! !Second viscosity virial function $VV RED SUM:9 ! !Residual function $RF RED SUMDTHRD:5 ! !Coefficients $CF -963382.0 0. 0. 0. 0 !Dilute gas terms 9614.09 1. 0. 0. 0 !Coefficient, power in T -13.233 2. 0. 0. 0 0.0360562 3. 0. 0. 0 122059. 0. 0. 0. 0 -224.741 1. 0. 0. 0 1.0 2. 0. 0. 0 !Virial terms 0.075276713 340. 1. 0. 0 !Reducing parameters for T (= eps/k), rho, etaB2 (= 0.6022137*sigma**3) -19.572881 0. 0. 0. 0 !Coefficient, power in T* = T/(eps/k) 219.73999 -0.25 0. 0. 0 -1015.3226 -0.5 0. 0. 0 2471.01251 -0.75 0. 0. 0 -3375.1717 -1. 0. 0. 0 2491.6597 -1.25 0. 0. 0 -787.26086 -1.5 0. 0. 0 14.085455 -2.5 0. 0. 0 -0.34664158 -5.5 0. 0. 0 !Background gas function 1.0 382.513 4.29 0. 0 !Reducing parameters for T, rho, eta 8.61691913 0.5 2. 0. 0 20.83024738 0.5 8. 0. 0 0.54243690 -0.5 20. 0. 0 -10.49684841 1.5 5. 0. 0 -1.38137689 0.5 17. 0. 0 NUL !Pointer to the viscosity critical enhancement auxiliary function (none used) ================================================================================ #TCX !---Thermal conductivity--- TC1 !Pure fluid thermal conductivity model for R-1234ze(E) of Perkins and Huber (2011). :DOI: 10.1021/je200811n ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A. and Huber, M.L., ? "Measurement and Correlation of the Thermal Conductivity of ? 2,3,3,3-Tetrafluoroprop-1-ene (R1234yf) and trans-1,3,3,3-Tetrafluoropeopene (R1234ze)," ? J. Chem. Eng. Data, 56(12):4868-4874, 2011. doi: 10.1021/je200811n ? ?The estimated uncertainty of the correlation is 1 % for the liquid phase, ? and 3 % for the vapor at pressures less than 1 MPa, larger in the critical region. ? !``````````````````````````````````````````````````````````````````````````````` 168.62 !Lower temperature limit [K] 420. !Upper temperature limit [K] 20000. !Upper pressure limit [kPa] 14. !Maximum density [mol/L] 4 0 !# terms for dilute gas function: numerator, denominator 382.52 1.0 !Reducing parameters for T, tcx -0.0103589 0. 0.0308929 1. 0.000230348 2. 0.0 3. 10 0 !# terms for background gas function: numerator, denominator 382.52 4.29 1. !Reducing parameters for T, rho, tcx -0.0428296 0. 1. 0. 0.0927099 0. 2. 0. -0.0702107 0. 3. 0. 0.0249708 0. 4. 0. -0.00301838 0. 5. 0. 0.0434288 1. 1. 0. -0.0605844 1. 2. 0. 0.0440187 1. 3. 0. -0.0155082 1. 4. 0. 0.0021019 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 R-1234ze(E) of Perkins and Huber (2011). ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A. and Huber, M.L., 2011. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 9 0 0 0 !# terms: CO2-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) 1.03 !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) 0.194e-9 !Xi0 (amplitude) [m] 0.0496 !Gam0 (amplitude) [-] 5.835e-10 !Qd_inverse (modified effective cutoff parameter) [m]; R125 value 573.78 !Tref (reference temperature)=1.5*Tc [K] ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ @TRN !---ECS Transport--- ECS !Extended Corresponding States model (R134a reference) for R-1234ze(E). ? ?``````````````````````````````````````````````````````````````````````````````` ?*** ESTIMATION METHOD *** NOT STANDARD REFERENCE QUALITY *** ?Unpublished; uses method described in the following reference: ?Huber, M.L., Laesecke, A., and Perkins, R.A. ? "Model for the Viscosity and Thermal Conductivity of Refrigerants, Including ? a New Correlation for the Viscosity of R134a," ? Ind. Eng. Chem. Res., 42(13):3163-3178, 2003. doi: 10.1021/ie0300880 ? ?Estimated uncertainty for liquid viscosity is 3 % based on comparisons with ? Grebenkov, A.J., Hulse, R., Pham, H. and Singh, R., "Physical Properties and Equation of State for trans-1,3,3,3-tetrafluoropropene" paper presented at 3rd IIR Conference on Thermophysical Properties and Transfer Processes of Refrigerants, Boulder CO June 2009. ? ?No data for thermal conductivity was found. Based on family comparisons, ? the estimated uncertainty for ECS estimation model is 20% ? ?The Lennard-Jones parameters were estimated with the method of Chung. ? !``````````````````````````````````````````````````````````````````````````````` 168.62 !Lower temperature limit [K] 1000.0 !Upper temperature limit [K] 20000.0 !Upper pressure limit [kPa] 14.0 !Maximum density [mol/L] FEQ R134A.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) 0.5017 !Lennard-Jones coefficient sigma [nm] 292.11 !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 2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 1.02599432 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.0101642107 0. 1. 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 ******************************************************************************** @TCX !---Thermal conductivity--- TC5 !Pure fluid thermal conductivity model for R-1234ze(E) of Chung et al. (1988). ? ?``````````````````````````````````````````````````````````````````````````````` ?Chung, T-H., Ajlan, M., Lee, L.L. and Starling, K.E. ? "Generalized Multiparameter Correlation for Nonpolar and Polar Fluid Transport Properties" ? Ind. Eng. Chem. Res. 1998, 27, 671-679. ? !``````````````````````````````````````````````````````````````````````````````` 168.62 !Lower temperature limit [K] 2000. !Upper temperature limit [K] 200000. !Upper pressure limit [kPa] 13.20 !Maximum density [mol/L] 0.50 !Lennard-Jones coefficient sigma [nm] =0.809vc*(1/3)A 303.8 !Lennard-Jones coefficient epsilon/kappa [K] =Tc/1.2593 0.313 0. 0. !w, mur, kappa for Chung 0 !Additional parameters for Chung TK3 !Pointer to critical enhancement auxiliary function ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for R-1234ze(E) of Mulero et al. (2014). :DOI: 10.1063/1.4878755 ? ?``````````````````````````````````````````````````````````````````````````````` ?Mulero, A. and Cachadiņa, I., ? "Recommended Correlations for the Surface Tension of Several Fluids ? Included in the REFPROP Program," ? J. Phys. Chem. Ref. Data, 43, 023104, 2014. ? doi: 10.1063/1.4878755 ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 !Number of terms in surface tension model 382.51 !Critical temperature used in fit (dummy) 0.06158 1.281 !Sigma0 and n -0.8247 6.505 #PS !---Vapor pressure--- PS5 !Vapor pressure equation for R-1234ze(E) of Thol and Lemmon (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M. and Lemmon, E.W., 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. ! 382.513 3634.9 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation -7.5888 1.0 1.9696 1.5 -2.0827 2.2 -4.1238 4.6 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for R-1234ze(E) of Thol and Lemmon (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M. and Lemmon, E.W., 2017. ? ?Functional Form: D=Dc*[1+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. ! 382.513 4.29 !Reducing parameters 4 0 0 0 0 0 !Number of terms in equation 1.1913 0.27 2.2456 0.70 -1.7747 1.25 1.3096 1.90 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for R-1234ze(E) of Thol and Lemmon (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Thol, M. and Lemmon, E.W., 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. ! 382.513 4.29 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -1.0308 0.24 -5.0422 0.72 -11.5 2.1 -37.499 4.8 -77.945 9.5 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890