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一些优化：CAN和PLC地址的优化

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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 Cachadiña, 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
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