558 lines
28 KiB
Plaintext
558 lines
28 KiB
Plaintext
R143a !Short name
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420-46-2 !CAS number
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1,1,1-Trifluoroethane !Full name
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CF3CH3 !Chemical formula {C2H3F3}
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HFC-143a !Synonym
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84.041 !Molar mass [g/mol]
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161.34 !Triple point temperature [K]
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225.909 !Normal boiling point [K]
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345.857 !Critical temperature [K]
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3761.0 !Critical pressure [kPa]
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5.12845 !Critical density [mol/L]
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0.2615 !Acentric factor
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2.340 !Dipole moment [Debye]; Meyer & Morrison (1991) J. Chem. Eng. Data 36:409-413.
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IIR !Default reference state
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10.0 !Version number
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2035 !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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4470. !GWP (IPCC 2007) :GWP:
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21000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
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A2L !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/C2H3F3/c1-2(3,4)5/h1H3 !Standard InChI String :InChi:
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UJPMYEOUBPIPHQ-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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0deae990 !Hash number from InChI Key :Hash:
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!The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the
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! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended
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! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to
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! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary
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! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and
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! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the
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! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the
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! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations,
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! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and
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! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface
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! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a
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! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The
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! end of the fluid file is marked with @END. Anything below that is ignored.
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! compiled by M. McLinden, NIST Physical and Chemical Properties Division, Boulder, Colorado
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! 12-01-95 MM, Original version.
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! 07-29-98 EWL, Add equation of state of Lemmon.
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! 10-06-99 EWL, Add newest equation of state of Lemmon.
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! 10-12-99 EWL, Add equation of Li et al.
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! 11-01-99 EWL, Add Span 12 term short equation of state.
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! 05-30-00 EWL, Change TRN reference fluid from BWR to FEQ R134a.
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! 11-13-06 MLH, Add LJ parameters.
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! 01-18-07 MLH, Refit viscosity with updated dataset of Kumagai and Yokoyama.
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! 08-17-10 IDC, Add ancillary equations.
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! 10-07-10 EWL, Refit surface tension data.
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! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
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! 05-07-14 EWL, Add surface tension coefficients of Mulero et al. (2014).
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! 11-26-17 MLH, Revise ECS viscosity and thermal conductivity.
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! 12-03-17 MLH, Add preliminary full fit with 1994 Perkin's data from ARTI report.
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for R-143a of Lemmon and Jacobsen (2000).
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:TRUECRITICALPOINT: 345.857 5.12845 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
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:DOI: 10.1063/1.1318909
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Jacobsen, R.T,
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? "An International Standard Formulation for the Thermodynamic Properties
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? of 1,1,1-Trifluoroethane (HFC-143a) for Temperatures from 161
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? to 450 K and Pressures to 50 MPa,"
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? J. Phys. Chem. Ref. Data, 29(4):521-552, 2000. doi: 10.1063/1.1318909
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?
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?The estimated uncertainties of properties calculated with the equation
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? of state are 0.1% in density, 0.5% in heat capacities, 0.02% in the
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? speed of sound for the vapor at pressures less than 1 MPa, 0.5% in speed
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? of sound elsewhere, and 0.1% in vapor pressure, except in the critical
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? region.
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?
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!```````````````````````````````````````````````````````````````````````````````
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161.34 !Lower temperature limit [K]
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650.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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15.85 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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84.041 !Molar mass [g/mol]
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161.34 !Triple point temperature [K]
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1.0749 !Pressure at triple point [kPa]
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15.832 !Density at triple point [mol/L]
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225.91 !Normal boiling point temperature [K]
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0.2615 !Acentric factor
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345.857 3761.0 5.12845 !Tc [K], pc [kPa], rhoc [mol/L]
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345.857 5.12845 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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17 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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7.7736443 0.67 1. 0. !a(i),t(i),d(i),l(i)
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-8.70185 0.833 1. 0.
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-0.27779799 1.7 1. 0.
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0.14609220 1.82 2. 0.
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0.0089581616 0.35 5. 0.
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-0.20552116 3.9 1. 1.
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0.10653258 0.95 3. 1.
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0.023270816 0.0 5. 1.
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-0.013247542 1.19 7. 1.
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-0.04279387 7.2 1. 2.
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0.36221685 5.9 2. 2.
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-0.25671899 7.65 2. 2.
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-0.092326113 7.5 3. 2.
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0.083774837 7.45 4. 2.
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0.017128445 15.5 2. 3.
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-0.01725611 22.0 3. 3.
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0.0049080492 19.0 5. 3.
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-143a of Lemmon and Jacobsen (2000).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Jacobsen, R.T, 2000.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314472 !Reducing parameters for T, Cp0
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1 2 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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1.0578 0.33
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4.4402 1791.0
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3.7515 823.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-143a of Lemmon and Jacobsen (2000).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Jacobsen, R.T, 2000.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 3 2 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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-1.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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5.9030332880254637 0.0 !aj, ti for [ai*tau**ti] terms
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7.3072591981034742 1.0 !aj, ti for [ai*tau**ti] terms
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1.0578 -0.33
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4.4402 1791.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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3.7515 823.0
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FE1 !Helmholtz equation of state for R-143a of Li et al. (1997).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Li, J., Tillner-Roth, R., Sato, H., and Watanabe, K.,
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? "An Equation of State for 1,1,1-Trifluoroethane (R-143a),"
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? Int. J. Thermophys., 20(6):1639-1651, 1999. doi: 10.1023/A:1022645626800
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?
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!```````````````````````````````````````````````````````````````````````````````
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161.34 !Lower temperature limit [K]
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650.0 !Upper temperature limit [K]
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50000.0 !Upper pressure limit [kPa]
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15.84 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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84.041 !Molar mass [g/mol]
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161.34 !Triple point temperature [K]
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1.0808 !Pressure at triple point [kPa]
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15.819 !Density at triple point [mol/L]
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225.89 !Normal boiling point temperature [K]
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0.2618 !Acentric factor
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345.86 3764.0 5.164146 !Tc [K], pc [kPa], rhoc [mol/L]
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345.86 5.164146 !Reducing parameters [K, mol/L]
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8.31451 !Gas constant [J/mol-K]
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19 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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0.01606645 0.0 5. 0. !a(i),t(i),d(i),l(i)
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4.163515 0.5 1. 0.
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-5.031058 0.75 1. 0.
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-0.01920208 2.5 2. 0.
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0.001470093 2.5 4. 0.
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0.1775429 0.25 3. 1.
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-0.007316069 0.25 8. 1.
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-0.09555916 2.0 3. 1.
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-0.5822518 3.0 1. 1.
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-0.0004211022 3.0 10. 2.
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-0.02059847 8.0 1. 2.
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0.03711325 8.0 4. 2.
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0.0001799723 8.0 8. 2.
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-0.04145922 10.0 2. 2.
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0.7682566e-4 8.0 12. 3.
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-0.002089695 17.0 8. 3.
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0.001958633 20.0 2. 3.
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-0.3198325e-5 35.0 5. 3.
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-0.005376561 27.0 3. 4.
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@EOS !---Equation of state---
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FES !Helmholtz equation of state for R-143a of Span and Wagner (2003).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Span, R. and Wagner, W.
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? "Equations of State for Technical Applications. III. Results for Polar Fluids,"
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? Int. J. Thermophys., 24(1):111-162, 2003. doi: 10.1023/A:1022362231796
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?
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?The uncertainties of the equation of state are approximately 0.2% (to
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? 0.5% at high pressures) in density, 1% (in the vapor phase) to 2% in
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? heat capacity, 1% (in the vapor phase) to 2% in the speed of sound, and
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? 0.2% in vapor pressure, except in the critical region.
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?
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!```````````````````````````````````````````````````````````````````````````````
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161.34 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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15.82 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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84.04 !Molar mass [g/mol]
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161.34 !Triple point temperature [K]
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1.072 !Pressure at triple point [kPa]
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15.816 !Density at triple point [mol/L]
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225.9 !Normal boiling point temperature [K]
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0.262 !Acentric factor
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345.86 3764.0 5.1653974 !Tc [K], pc [kPa], rhoc [mol/L]
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345.86 5.1653974 !Reducing parameters [K, mol/L]
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8.31451 !Gas constant [J/mol-K]
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12 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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1.0306886 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-2.9497307 1.25 1. 0.
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0.69435230 1.5 1. 0.
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0.071552102 0.25 3. 0.
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0.00019155982 0.875 7. 0.
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0.079764936 2.375 1. 1.
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0.56859424 2.0 2. 1.
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-0.0090946566 2.125 5. 1.
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-0.24199452 3.5 1. 2.
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-0.070610813 6.5 1. 2.
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-0.075041709 4.75 4. 2.
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-0.016411241 12.5 2. 3.
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for R-143a.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Li, J., Tillner-Roth, R., Sato, H., and Watanabe, K.,
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? "An Equation of State for 1,1,1-Trifluoroethane (R-143a),"
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? Int. J. Thermophys., 20(6):1639-1651, 1999. doi: 10.1023/A:1022645626800
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.31451 !Reducing parameters for T, Cp0
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4 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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0.1000206 0.0
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-0.00096337511 1.5
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318.22397 -1.25
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0.04691762 1.0
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@EOS !---Equation of state---
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BWR !MBWR equation of state for R-143a of Outcalt and McLinden (1996).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Outcalt, S.L. and McLinden, M.O.,
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? "An equation of state for the thermodynamic properties of
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? R143a (1,1,1-trifluoroethane),"
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? Int. J. Thermophys., 18(6):1445-1463, 1997. doi: 10.1007/BF02575344
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?
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!```````````````````````````````````````````````````````````````````````````````
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161.34 !Lower temperature limit [K]
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500.0 !Upper temperature limit [K]
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60000.0 !Upper pressure limit [kPa]
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15.84 !Maximum density [mol/L]
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CP2 !Pointer to Cp0 model
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84.041 !Molar mass [g/mol]
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161.34 !Triple point temperature [K]
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1.069 !Pressure at triple point [kPa]
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15.8328 !Density at triple point [mol/L]
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225.928 !Normal boiling point temperature [K]
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0.26113 !Acentric factor
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346.04 3775.6 5.151118 !Tc [K], pc [kPa], rhoc [mol/L]
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346.04 5.151118 !Reducing parameters [K, mol/L]
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5.151118 !gamma
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0.08314471 !Gas constant [L-bar/mol-K]
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32 1 !Nterm, Ncoeff per term
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-0.0240561786316 2.62345913719 -65.0858041394
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9959.52053681 -1475364.64961 0.00135498153308
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-2.81726617426 1343.71062574 850286.316514
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-0.000180516636446 0.618889066246 -223.083798271
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-0.0119095922349 -1.73933336877 -420.84760118
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0.213502079796 -0.00565708555185 1.854422968
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-0.0520377059921 -846735.696108 -20796448.3848
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-34997.7290513 576427827.667 -389.131863941
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10307.4054089 -4.47627052215 -106673.161101
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-0.0219511369081 6.42186519493 -0.938317030843e-4
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-0.0478594713528 -2.06555883874
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@AUX !---Auxiliary function for Cp0
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CP2 !Ideal gas heat capacity function for R-143a of Outcalt & McLinden (1996).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Outcalt, S.L. and McLinden, M.O.,
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? "An equation of state for the thermodynamic properties of
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? R143a (1,1,1-trifluoroethane),"
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? Int. J. Thermophys., 18(6):1445-1463, 1997. doi: 10.1007/BF02575344
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?
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?fit to (corrected) data of Gillis and Chen
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314471 !Reducing parameters for T, Cp0
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4 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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1.838736 0.0
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0.0301994 1.0
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-0.0000178455 2.0
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4.42442e-9 3.0
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================================================================================
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#TCX !---Thermal conductivity---
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TC1 !Pure fluid preliminary thermal conductivity model for R143A of Huber (2018).
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:DOI: 10.6028/NIST.IR.8209
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Huber, M.L., "Models for the Viscosity, Thermal Conductivity, and Surface Tension
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? of Selected Pure Fluids as Implemented in REFPROP v10.0," NISTIR 8209, 2018.
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? doi: 10.6028/NIST.IR.8209
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?
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?Uncertainty in thermal conductivity is 5%, except in the critical region where the uncertainty is larger.
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?
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!```````````````````````````````````````````````````````````````````````````````
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161.34 !Lower temperature limit [K]
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650.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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20. !Maximum density [mol/L]
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3 0 !# terms for dilute gas function: numerator, denominator
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1.0 1.0 !Reducing parameters for T, tcx
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-7.00852e-3 0. !Coefficient, power in T
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6.56307e-5 1.
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2.62499e-8 2.
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10 0 !# terms for background gas function: numerator, denominator
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345.857 5.12845 1.0 !reducing par for T, rho, tcx
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-0.81221200E-01 .00E+00 .10E+01 .00E+00
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-0.16665200E-01 .00E+00 .20E+01 .00E+00
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0.87447700E-01 .00E+00 .30E+01 .00E+00
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-0.35146800E-01 .00E+00 .40E+01 .00E+00
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0.39957000E-02 .00E+00 .50E+01 .00E+00
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0.76235500E-01 .10E+01 .10E+01 .00E+00
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-0.22766200E-01 .10E+01 .20E+01 .00E+00
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-0.17572600E-01 .10E+01 .30E+01 .00E+00
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0.37946700E-02 .10E+01 .40E+01 .00E+00
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0.77691900E-03 .10E+01 .50E+01 .00E+00
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TK3 !Pointer to critical enhancement auxiliary function
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#AUX !---Auxiliary function for the thermal conductivity critical enhancement
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TK3 !Simplified thermal conductivity critical enhancement for R143a of Perkins et al. (2013).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Perkins, R.A., Sengers, J.V., Abdulagatov, I.M., and Huber, M.L.,
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? "Simplified Model for the Critical Thermal-Conductivity Enhancement in Molecular Fluids,"
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? Int. J. Thermophys., 34(2):191-212, 2013. doi: 10.1007/s10765-013-1409-z
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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||
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)
|
||
1.02 !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)
|
||
0.193e-9 !Xi0 (amplitude) [m]
|
||
0.055 !Gam0 (amplitude) [-]
|
||
0.23e-9 !Qd_inverse (modified effective cutoff parameter) [m] fit to data
|
||
518.79 !Tref (reference temperature)=1.5*Tc [K]
|
||
|
||
|
||
|
||
|
||
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
||
|
||
@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (R134a reference); fitted to data for R-143a.
|
||
:DOI: 10.6028/NIST.IR.8209
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Huber, M.L., "Models for the Viscosity, Thermal Conductivity, and Surface Tension
|
||
? of Selected Pure Fluids as Implemented in REFPROP v10.0," NISTIR 8209, 2018.
|
||
? doi: 10.6028/NIST.IR.8209
|
||
?
|
||
?THERMAL CONDUCTIVITY
|
||
? The ECS parameters for thermal conductivity were based in part on the data of:
|
||
? Tanaka, Y., Nakata, M., and Makita, T., "Thermal Conductivity of Gaseous HFC-134a, HFC-143a, HCFC-141b, and HCFC-142b," Int. J. Thermophys., 12:949-963, 1991.
|
||
? Yata, J., Hori, M., Kobayashi, K., and Minamiyama, T., "Thermal Conductivity of Alternative Fluorocarbons in the Liquid Phase," Int. J. Thermophys., 17(3):561-571, 1996.
|
||
? Le Neindre et al., Int. J. Thermophys., 22:723-748, 2001.
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Tanaka: 4.8%; Yata: 2.9%; Le Niendre:1.6%
|
||
?
|
||
?Estimated uncertainty for viscosity over full region of validity is <10%, except
|
||
? near the critical region where deviations can be much larger.
|
||
?
|
||
?VISCOSITY
|
||
? The ECS parameters for viscosity were based on the data of:
|
||
? Avelino et al. J. Chem. Eng. Data, 51:1672-1677, 2006.
|
||
? Ripple, D. and Defibaugh, D., "Viscosity of the Saturated Liquid Phase of Three Fluorinated Ethanes: R152a, R143a, and R125," J. Chem. Eng. Data, 42:360-364, 1997.
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Avelino: 0.4%; Ripple: 1.2%
|
||
?
|
||
?Estimated uncertainty for viscosity over full region of validity is <10%
|
||
?
|
||
?The Lennard-Jones parameters were obtained by fitting gas phase viscosity data of Takahashi et al., Int. J. Thermophys., 20:435-443, 1999, and Wang et al., J. Eng. Thermophys., 30(4):1455-1458, 2009.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
161.34 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
60000.0 !Upper pressure limit [kPa]
|
||
20. !Maximum density [mol/L]
|
||
FEQ R134A.FLD
|
||
VS1 !Model for reference fluid viscosity
|
||
TC1 !Model for reference fluid thermal conductivity
|
||
BIG !Large molecule identifier
|
||
0.992 0. 0. 0. !Large molecule parameters 0.99
|
||
1 !Lennard-Jones flag (0 or 1) (0 => use estimates)
|
||
0.4827 !Lennard-Jones coefficient sigma [nm] for ECS method
|
||
301.76 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
|
||
2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
|
||
7.74846e-4 0. 0. 0. !Coefficient, power of T, spare1, spare2
|
||
1.51546e-6 1. 0. 0. !Coefficient, power of T, spare1, spare2
|
||
2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
|
||
0.942896 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0142114 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
3 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
||
1.38978 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
-0.367658 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0804516 0. 2. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
TK3 !Pointer to critical enhancement auxiliary function
|
||
|
||
|
||
|
||
|
||
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
|
||
|
||
#STN !---Surface tension---
|
||
ST1 !Surface tension model for R-143a of Mulero et al. (2014).
|
||
:DOI: 10.1063/1.4878755
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Mulero, A. and Cachadi<64>a, 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
|
||
345.857 !Critical temperature used in fit (dummy)
|
||
0.0537 1.25 !Sigma0 and n
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for R-143a of Cullimore (2010).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Cullimore, I.D., 2010.
|
||
?
|
||
?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. !
|
||
345.857 3761.0 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-7.3938 1.0
|
||
1.9948 1.5
|
||
-1.8487 2.2
|
||
-4.1927 4.8
|
||
1.4862 6.2
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for R-143a of Cullimore (2010).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Cullimore, I.D., 2010.
|
||
?
|
||
?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. !
|
||
345.857 5.12845 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
2.1135 0.348
|
||
10.2 1.6
|
||
-30.836 2.0
|
||
39.909 2.4
|
||
-18.557 2.7
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for R-143a of Cullimore (2010).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Cullimore, I.D., 2010.
|
||
?
|
||
?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. !
|
||
345.857 5.12845 !Reducing parameters
|
||
6 0 0 0 0 0 !Number of terms in equation
|
||
-2.8673 0.384
|
||
-6.3818 1.17
|
||
-16.314 3.0
|
||
-45.947 6.2
|
||
-1.3956 7.0
|
||
-246.71 15.0
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
||
?The Lennard-Jones parameters were taken from Takahashi, M., Shibasaki-Kitakawa, N. and
|
||
?Yokoyama, C., Int. J. Thermophys. 20(2) 1999 p435-443.doi: 10.1023/A:1022696702673
|
||
0.4885 !Lennard-Jones coefficient sigma [nm] for ECS method
|
||
365.58 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
|
||
these do not work as well as ECS estimated values
|