869 lines
44 KiB
Plaintext
869 lines
44 KiB
Plaintext
R134a !Short name
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811-97-2 !CAS number
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1,1,1,2-Tetrafluoroethane !Full name
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CF3CH2F !Chemical formula {C2H2F4}
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HFC-134a !Synonym
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102.032 !Molar mass [g/mol]
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169.85 !Triple point temperature [K]
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247.076 !Normal boiling point [K]
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374.21 !Critical temperature [K]
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4059.28 !Critical pressure [kPa]
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5.017053 !Critical density [mol/L]
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0.32684 !Acentric factor
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2.058 !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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3159 !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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1430. !GWP (IPCC 2007) :GWP:
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50000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
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A1 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/C2H2F4/c3-1-2(4,5)6/h1H2 !Standard InChI String :InChi:
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LVGUZGTVOIAKKC-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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ff1c0560 !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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! 10-10-95 MM, Original version.
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! 11-01-99 EWL, Add Span 12 term short equation of state.
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! 09-26-01 MLH, Add new Laesecke viscosity correlation as default.
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! 04-19-04 MLH, Update viscosity reference.
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! 11-19-04 MLH, Add tPr.
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! 09-20-06 EWL, Add Astina and Sato equation.
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! 10-03-06 EWL, Change maximum density from 17.05 to 20 in TCX and VIS to make it work with RP1.
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! 12-02-06 MLH, Revise LJ for ECS.
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! 03-05-07 MLH, Add VS4.
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! 09-13-10 EWL, Replace ancillary equations.
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! 10-15-10 MLH, Revise limits on TK3 block to be consistent with TC1.
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! 04-11-12 MLH, Add extra blank FT coeff for consistent formatting.
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! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for R-134a of Tillner-Roth and Baehr (1994).
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:TRUECRITICALPOINT: 374.18 5.017053 !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: 10.1063/1.555958
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tillner-Roth, R. and Baehr, H.D.,
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? "An International Standard Formulation of the Thermodynamic Properties
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? of 1,1,1,2-Tetrafluoroethane (HFC-134a) for Temperatures from 170 K
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? to 455 K at Pressures up to 70 MPa,"
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? J. Phys. Chem. Ref. Data, 23:657-729, 1994. doi: 10.1063/1.555958
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?
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?The uncertainties are 0.05% for density, 0.02% for vapor
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? pressure, 0.5-1% for heat capacity, 0.05% for vapor speed of sound,
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? and 1% for liquid speed of sound, except in the critical region.
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?
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!```````````````````````````````````````````````````````````````````````````````
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169.85 !Lower temperature limit [K]
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455.0 !Upper temperature limit [K]
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70000.0 !Upper pressure limit [kPa]
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15.60 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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102.032 !Molar mass [g/mol]
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169.85 !Triple point temperature [K]
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0.3896 !Pressure at triple point [kPa]
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15.5942 !Density at triple point [mol/L]
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247.076 !Normal boiling point temperature [K]
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0.32684 !Acentric factor
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374.21 4059.28 5.017053 !Tc [K], pc [kPa], rhoc [mol/L]
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374.18 4.978830171 !Reducing parameters [K, mol/L]
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8.314471 !Gas constant [J/mol-K]
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21 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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0.05586817 -0.5 2. 0. !a(i),t(i),d(i),l(i)
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0.498223 0.0 1. 0.
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0.02458698 0.0 3. 0.
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0.0008570145 0.0 6. 0.
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0.0004788584 1.5 6. 0.
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-1.800808 1.5 1. 0.
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0.2671641 2.0 1. 0.
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-0.04781652 2.0 2. 0.
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0.01423987 1.0 5. 1.
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0.3324062 3.0 2. 1.
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-0.007485907 5.0 2. 1.
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0.0001017263 1.0 4. 2.
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-0.5184567 5.0 1. 2.
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-0.08692288 5.0 4. 2.
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0.2057144 6.0 1. 2.
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-0.005000457 10.0 2. 2.
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0.0004603262 10.0 4. 2.
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-0.003497836 10.0 1. 3.
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0.006995038 18.0 5. 3.
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-0.01452184 22.0 3. 3.
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-0.0001285458 50.0 10. 4.
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-134a of Tillner-Roth and Baehr (1994).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tillner-Roth, R. and Baehr, H.D., 1994.
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?
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?Note: Tillner-Roth et al. give a Helmholtz form for the ideal gas term; it
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? has been converted to a Cp0 form by the transform:
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?
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?Cp0/R = (1 + a3) - (3/4)*a4*Tr**(1/2) - (21/16)*a5*Tr**(3/4)
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? where the ai are the original coefficients given by T-R and Tr = T/Tc.
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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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374.18 8.314471 !Reducing parameters for T, Cp0
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3 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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-0.629789 0.0
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7.292937 0.5
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5.154411 0.75
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-134a of Tillner-Roth and Baehr (1994).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tillner-Roth, R. and Baehr, H.D., 1994.
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?
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?Note: Tillner-Roth et al. give a Helmholtz form for the ideal gas term; it
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? has been converted to a Cp0 form by the transform:
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?
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?Cp0/R = (1 + a3) - (3/4)*a4*Tr**(1/2) - (21/16)*a5*Tr**(3/4)
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? where the ai are the original coefficients given by T-R and Tr = T/Tc.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 4 0 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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-1.629789 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-1.0195506821162033 0.0 !aj, ti for [ai*tau**ti] terms
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9.0471440883402678 1.0 !aj, ti for [ai*tau**ti] terms
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0.37700296643559 -0.5
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0.0605818461098516 -0.75
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#AUX !---Auxiliary function for PH0
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PH0 !Ideal gas Helmholtz form for R-134a.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tillner-Roth, R. and Baehr, H.D., 1994.
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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 4 0 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
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-1.629789 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-1.019535 0.0 !aj, ti for [ai*tau**ti] terms
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9.047135 1.0
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-9.723916 -0.5
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-3.92717 -0.75
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FES !Helmholtz equation of state for R-134a 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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169.85 !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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15.6 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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102.032 !Molar mass [g/mol]
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169.85 !Triple point temperature [K]
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0.38818 !Pressure at triple point [kPa]
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15.588 !Density at triple point [mol/L]
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247.06 !Normal boiling point temperature [K]
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0.327 !Acentric factor
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374.18 4056.3 4.9788302 !Tc [K], pc [kPa], rhoc [mol/L]
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374.18 4.9788302 !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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1.0663189 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-2.449597 1.25 1. 0.
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0.044645718 1.5 1. 0.
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0.075656884 0.25 3. 0.
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0.00020652089 0.875 7. 0.
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0.42006912 2.375 1. 1.
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0.76739111 2.0 2. 1.
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0.0017897427 2.125 5. 1.
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-0.36219746 3.5 1. 2.
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-0.06780937 6.5 1. 2.
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-0.10616419 4.75 4. 2.
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-0.018185791 12.5 2. 3.
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@EOS !---Equation of state---
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BWR !MBWR equation of state for R-134a of Huber and McLinden (1992).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Huber, M.L. and McLinden, M.O.,
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? "Thermodynamic properties of R134a (1,1,1,2-tetrafluoroethane),"
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? International Refrigeration Conference,
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? West Lafayette, IN, July 14-17, 453-462, 1992.
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?
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?also published in:
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?
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?Huber, M.L. and Ely, J.F.,
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? "A predictive extended corresponding states model for pure and mixed
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? refrigerants including an equation of state for R134a,"
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? Int. J. Refrigeration, 17(1):18-31, 1994. doi: 10.1016/0140-7007(94)90083-3
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?
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!```````````````````````````````````````````````````````````````````````````````
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169.85 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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70000.0 !Upper pressure limit [kPa]
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15.60 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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102.032 !Molar mass [g/mol]
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169.85 !Triple point temperature [K]
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0.3922 !Pressure at triple point [kPa]
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15.60 !Density at triple point [mol/L]
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247.082 !Normal boiling point temperature [K]
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0.32705 !Acentric factor
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374.179 4056.0 5.0308 !Tc [K], pc [kPa], rhoc [mol/L]
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374.179 5.0308 !Reducing parameters [K, mol/L]
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5.0308 !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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0.0965209362217 -4.01824768889 39.5239532858
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1345.3286896 -1394397.41347 -0.00309281355175
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2.92381512283 -1651.46613555 1507060.03118
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0.534973948313e-4 0.543933317622 -211.326049762
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-0.0268191203847 -0.54106712595 -851.731779398
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0.205188253646 -0.00733050188093 3.80655963862
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-0.105832087589 -679243.084424 -126998378.601
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-42623.4431829 0.101973338234e+10 -186.699526782
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-93342.6323419 -5.71735208963 -176762.738787
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-0.0397282752308 14.3016844796 0.80308529426e-4
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-0.171959073552 2.26238385661
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for R-134a of McLinden et al. (1989).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?McLinden, M.O.
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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 1.0 !Reducing parameters for T, Cp0
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3 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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19.4006 0.0
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0.258531 1.0
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-0.000129665 2.0
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@EOS !---Equation of state---
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FE2 !Helmholtz equation of state for R-134a of Astina and Sato (2004).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Astina, I.M. and Sato, H.,
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? "A Fundamental Equation of State for 1,1,1,2-Tetrafluoroethane with an
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? Intermolecular Potential Energy Background and Reliable Ideal-Gas Properties,"
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? Fluid Phase Equilib., 221:103-111, 2004. doi: 10.1016/j.fluid.2004.03.004
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?
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!```````````````````````````````````````````````````````````````````````````````
|
||
169.85 !Lower temperature limit [K]
|
||
460.0 !Upper temperature limit [K]
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70000.0 !Upper pressure limit [kPa]
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||
15.58 !Maximum density [mol/L]
|
||
PH2 !Pointer to Cp0 model
|
||
102.031 !Molar mass [g/mol]
|
||
169.85 !Triple point temperature [K]
|
||
0.327 !Pressure at triple point [kPa]
|
||
15.58 !Density at triple point [mol/L]
|
||
247.087 !Normal boiling point temperature [K]
|
||
0.33 !Acentric factor
|
||
374.083 4048.0 4.988679911 !Tc [K], pc [kPa], rhoc [mol/L]
|
||
374.083 4.988679911 !Reducing parameters [K, mol/L]
|
||
8.314472 !Gas constant [J/mol-K]
|
||
18 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
||
1.832124209 0.5 1. 0. !a(i),t(i),d(i),l(i)
|
||
-2.940698861 1.125 1. 0.
|
||
0.5156071823 3.25 1. 0.
|
||
0.2756965911 0.5 2. 0.
|
||
1.225264939 1.875 2. 0.
|
||
-0.6486749497 2.75 2. 0.
|
||
-0.9286738053 1.625 3. 0.
|
||
0.3920381291 2.125 3. 0.
|
||
0.1056692108 1.125 4. 0.
|
||
-0.7586523371 3.75 1. 1.
|
||
-1.198140136 1.5 2. 1.
|
||
-0.287826039 0.75 3. 1.
|
||
-0.09723032379 9.0 2. 2.
|
||
0.05307113358 8.5 3. 2.
|
||
-0.04681610582 5.5 4. 2.
|
||
-0.009604697902 32.0 4. 3.
|
||
0.006668035048 23.0 5. 3.
|
||
0.00236126629 31.0 6. 3.
|
||
|
||
|
||
@AUX !---Auxiliary function for PH0
|
||
PH2 !Ideal gas Helmholtz form for R-134a.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Astina, I.M. and Sato, H.,
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
1 3 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
|
||
-1.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
||
10.78497786 0.0 !aj, ti for [ai*tau**ti] terms
|
||
8.61297741 1.0
|
||
-24.37548384 -0.25
|
||
7.451784998 -4.103830338
|
||
-4.239239505 -2.561528683
|
||
6.445739825 -2.084607363
|
||
|
||
|
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@EOS !---Cubic equation of state---
|
||
PRT !Translated Peng-Robinson equation for R-134a.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Volume translation of Peng Robinson EOS.
|
||
? Translation computed so that sat. liquid density at Tr=0.7 matches FEQ Helmholtz equation
|
||
? of state for R134a of Tillner-Roth and Baehr (1994).
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
169.85 !Lower temperature limit [K]
|
||
455.0 !Upper temperature limit [K]
|
||
20000.0 !Upper pressure limit [kPa]
|
||
17.05 !Maximum density [mol/L]
|
||
CPP !Pointer to Cp0 model
|
||
102.032 !Molar mass [g/mol]
|
||
0.32684 !Acentric factor
|
||
374.21 !Critical temperature [K]
|
||
4059.28 !Critical pressure [kPa]
|
||
5.017053 !Critical density [mol/L]
|
||
8.314472 !Gas constant [J/mol-K]
|
||
1 !Number of parameters
|
||
0.001032
|
||
|
||
|
||
|
||
|
||
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
||
|
||
#ETA !---Viscosity---
|
||
VS1 !Pure fluid viscosity model for R-134a of Huber et al. (2003).
|
||
:DOI: 10.1021/ie0300880
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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
|
||
?
|
||
?The uncertainty in viscosity is 1.5% along the saturated liquid line, 3% in
|
||
? the liquid phase, 0.5% in the dilute gas, 3-5% in the vapor phase, and 5%
|
||
? in the supercritical region, rising to 8% at pressures above 40 MPa.
|
||
? Below 200 K, the uncertainty is 8%.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
169.85 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
100000.0 !Upper pressure limit [kPa]
|
||
20.0 !Maximum density [mol/L] (rho on melting line at 100 MPa)
|
||
1 !Number of terms associated with dilute-gas function
|
||
CI1 !Pointer to reduced effective collision cross-section model
|
||
0.468932 !Lennard-Jones coefficient sigma [nm]
|
||
299.363 !Lennard-Jones coefficient epsilon/kappa [K]
|
||
1.0 1.0 !Reducing parameters for T, eta
|
||
0.215729 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term]
|
||
9 !Number of terms for initial density dependence
|
||
299.363 0.0620984 !Reducing parameters for T (=eps/k), etaB2 (= 0.6022137*sigma**3)
|
||
-19.572881 0.0 !Coefficient, power in T* = T/(eps/k)
|
||
219.73999 -0.25
|
||
-1015.3226 -0.5
|
||
2471.0125 -0.75
|
||
-3375.1717 -1.0
|
||
2491.6597 -1.25
|
||
-787.26086 -1.5
|
||
14.085455 -2.5
|
||
-0.34664158 -5.50
|
||
-3 7 1 2 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
|
||
374.21 5.0170613 1000.0 !Reducing parameters for T, rho, eta (Laesecke correlation in terms of mPa-s, convert to uPa-s)
|
||
3.163695635587490 0.0 !Alternative form for del10; numerator term
|
||
-0.08901733752064137 1.0 !Alternative form for del10; denominator terms
|
||
0.1000352946668359 2.0 !Alternative form for del10; denominator terms
|
||
-0.02069007192080741 0.0 1. 0. 0 ! beta1; powers of tau, del, del0; power of del in exponential [0 indicated no exponential term present]
|
||
0.0003560295489828222 -6.0 2. 0. 0 ! beta2
|
||
0.002111018162451597 -2.0 2. 0. 0 ! beta3
|
||
0.01396014148308975 -0.5 2. 0. 0 ! beta4
|
||
-0.004564350196734897 2.0 2. 0. 0 ! beta5
|
||
-0.00351593274583689 0.0 3. 0. 0 ! beta6
|
||
-0.2147633195397038 0.0 0. -1. 0 ! beta7
|
||
0.2147633195397038 0.0 0. 0. 0 ! beta7 in non-simple poly term
|
||
1.0 0.0 0. 1. 0 ! del0 term in denominator
|
||
-1.0 0.0 1. 0. 0 ! -del term in denominator
|
||
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
||
|
||
|
||
#AUX !---Auxiliary function for the collision integral
|
||
CI1 !Reduced effective collision cross-section model (empirical form in log(T*)) for R-134a.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Reduced effective collision cross-section of Wilhelm & Vogel as reported by:
|
||
? Laesecke, A. (laesecke@boulder.nist.gov); Unpublished correlation R134aFitSelDV
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
3 !Number of terms
|
||
0.355404 0 !Coefficient, power of Tstar
|
||
-0.464337 1
|
||
0.0257353 2
|
||
|
||
|
||
|
||
|
||
================================================================================
|
||
|
||
#TCX !---Thermal conductivity---
|
||
TC1 !Pure fluid thermal conductivity model for R-134a of Perkins et al. (2000).
|
||
:DOI: 10.6028/NIST.IR.6605
|
||
:WEB: https://doi.org/10.6028/NIST.IR.6605
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Perkins, R.A., Laesecke, A., Howley, J., Ramires, M.L.V., Gurova, A.N., and
|
||
? Cusco, L.,
|
||
? "Experimental Thermal Conductivity Values for the IUPAC Round-Robin
|
||
? Sample of 1,1,1,2-Tetrafluoroethane (R134a),"
|
||
? NISTIR, 2000.
|
||
?
|
||
?The uncertainty in thermal conductivity is 5%.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
169.85 !Lower temperature limit [K]
|
||
455.0 !Upper temperature limit [K]
|
||
20000.0 !Upper pressure limit [kPa]
|
||
20.0 !Maximum density [mol/L]
|
||
2 0 !# terms for dilute gas function: numerator, denominator
|
||
1.0 1.0 !Reducing parameters for T, tcx
|
||
-0.0105248 0. !Coefficient, power in T
|
||
8.00982e-5 1.
|
||
4 0 !# terms for background gas function: numerator, denominator
|
||
1.0 5.049886 0.002055 !Reducing parameters for T, rho (rho_c), tcx
|
||
1.836526 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
|
||
5.126143 0. 2. 0.
|
||
-1.436883 0. 3. 0.
|
||
0.6261441 0. 4. 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-134a of Olchowy and Sengers (1989).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Olchowy, G.A. and Sengers, J.V.,
|
||
? "A Simplified Representation for the Thermal Conductivity of Fluids in the Critical Region,"
|
||
? Int. J. Thermophys., 10:417-426, 1989. doi: 10.1007/BF01133538
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
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)
|
||
1.03 !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) [-]
|
||
5.285356e-10 !Qd_inverse (modified effective cutoff parameter) [m]
|
||
561.411 !Tref (reference temperature) [= 1.5 * 374.274 K]
|
||
|
||
|
||
|
||
|
||
********************************************************************************
|
||
|
||
@ETA !---Viscosity---
|
||
VS4 !Pure fluid generalized friction theory viscosity model for R-134a of Quinones-Cisneros and Deiters (2006).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Quinones-Cisneros, S.E. and Deiters, U.K.,
|
||
? "Generalization of the Friction Theory for Viscosity Modeling,"
|
||
? J. Phys. Chem. B, 110(25):12820-12834, 2006. doi: 10.1021/jp0618577
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
169.85 !Lower temperature limit [K]
|
||
455.0 !Upper temperature limit [K]
|
||
70000.0 !Upper pressure limit [kPa]
|
||
15.60 !Maximum density [mol/L]
|
||
4 0 0 0 0 0 !Number of terms associated with dilute-gas function
|
||
NUL !Pointer to reduced effective collision cross-section model; not used
|
||
0.468932 !Lennard-Jones coefficient sigma [nm] (not used)
|
||
299.363 !Lennard-Jones coefficient epsilon/kappa [K] (not used)
|
||
374.21 1.0 !Reducing parameters for T, eta
|
||
0.0 0.5 !Chapman-Enskog term; not used here
|
||
31.2515 0.0 !Empirical terms for eta0
|
||
-89.6122 0.25
|
||
73.0823 0.50
|
||
0 !Number of terms for initial density dependence
|
||
1.07271318464787e-4 -4.41655360682255e-5 0.0 0. 0. ! a(0),a(1),a(2)
|
||
1.66457266522365e-4 -4.80292908400793e-5 0.0 0. 0. ! b(0),b(1),b(2)
|
||
8.08333416284215e-5 -4.90359549823121e-5 0.0 0. 0. ! c(0),c(1),c(2)
|
||
-2.12476175599662e-8 2.81647242085073e-9 0.0 0. 0. ! A(0),A(1),A(2)
|
||
1.3559352757309e-8 0.0 3.17549774078234e-10 0. 0. ! B(0),B(1),B(2)
|
||
0.0 4.81768878752129e-7 -1.17148596093671e-7 0. 0. ! C(0),C(1),C(2)
|
||
0.0 0.0 0.0 0. 0. ! D(0),D(1),D(2)
|
||
0.0 0.0 0.0 0. 0. ! E(0),E(1),E(2)
|
||
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
||
|
||
|
||
|
||
|
||
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
||
|
||
@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (R134a reference); predictive mode for R-134a.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
169.85 !Lower temperature limit [K]
|
||
600.0 !Upper temperature limit [K]
|
||
70000.0 !Upper pressure limit [kPa]
|
||
15.60 !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)
|
||
0.468932 !Lennard-Jones coefficient sigma [nm]
|
||
299.363 !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
|
||
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 R-134a of Mulero et al. (2012).
|
||
:DOI: 10.1063/1.4768782
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Mulero, A., Cachadi<64>a, I., and Parra, M.I.,
|
||
? "Recommended Correlations for the Surface Tension of Common Fluids,"
|
||
? J. Phys. Chem. Ref. Data, 41(4), 043105, 2012. doi: 10.1063/1.4768782
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
1 !Number of terms in surface tension model
|
||
374.21 !Critical temperature used in fit (dummy)
|
||
0.05801 1.241 !Sigma0 and n
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for R-134a of Lemmon (2010).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Lemmon, E.W., 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. !
|
||
374.21 4059.28 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
-7.7513 1.0
|
||
2.9263 1.5
|
||
-2.6622 1.9
|
||
-3.9711 4.25
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for R-134a of Lemmon (2010).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Lemmon, E.W., 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. !
|
||
374.21 5.017053 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
12.449 0.5
|
||
-41.023 0.7
|
||
73.641 0.9
|
||
-64.635 1.1
|
||
22.551 1.3
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for R-134a of Lemmon (2010).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Lemmon, E.W., 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. !
|
||
374.21 5.017053 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-2.9174 0.383
|
||
-7.2542 1.21
|
||
-23.306 3.3
|
||
5.9840 5.6
|
||
-71.821 7.0
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
||
|
||
|
||
@EOS !Equation of state specification
|
||
ECS Thermodynamic Extended Corresponding States model w/ T-dependent shape factors.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Huber, M.L. and Ely, J.F.,
|
||
? "A predictive extended corresponding states model for pure and mixed
|
||
? refrigerants including an equation of state for R134a,"
|
||
? Int. J. Refrigeration, 17(1):18-31, 1994. doi: 10.1016/0140-7007(94)90083-3
|
||
?
|
||
?the ideal-gas contribution is computed with the polynomial Cp0 fit of:
|
||
? McLinden, M.O., et al.,
|
||
? "Measurement and formulation of the thermodynamic properties of refrigerants
|
||
? 134a (1,1,1,2-tetrafluoroethane) and 123 (1,1-dichloro-2,2,2-trifluoroethane),"
|
||
? ASHRAE Trans. 95(2):263-283, 1989.
|
||
?
|
||
?Shape factors are unity as R134a is the reference fluid
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
169.85 !Lower temperature limit [K]
|
||
600.0 !Upper temperature limit [K]
|
||
70000.0 !Upper pressure limit [kPa]
|
||
15.60 !Maximum density [mol/L]
|
||
CP1 !Pointer to Cp0 model
|
||
R134A.FLD
|
||
BWR !Pointer to reference fluid model
|
||
0.32668 !Acentric factor for R134a used in shape factor correlation
|
||
0.259147 !Critical compressibility for R134a used in correlation
|
||
0.32668 !Acentric factor for fluid used in shape factor correlation
|
||
374.179 !Critical temperature [K]
|
||
4056.0 !Critical pressure [kPa]
|
||
5.0308 !Critical density [mol/L]
|
||
2 !Number of temperature coefficients for 'f' shape factor
|
||
0.0 0. ! alpha1 of Huber & Ely
|
||
0.0 1. ! alpha2 (log(Tr) term)
|
||
0 !Number of density coefficients for 'f' shape factor
|
||
2 !Number of temperature coefficients for 'h' shape factor
|
||
0.0 0. ! beta1 of Huber & Ely
|
||
0.0 1. ! beta2 (log(Tr) term)
|
||
0 !Number of density coefficients for 'h' shape factor
|
||
|
||
|
||
!Older formulation of Laesecke that has been replaced with the 1998
|
||
! unpublished version given above:
|
||
|
||
@ETA !Viscosity model specification
|
||
VS1 pure fluid viscosity model of Laesecke (2000).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Laesecke, A.,
|
||
? "Data reassessment and full surface correlation of
|
||
? the viscosity of HFC-134a (1,1,1,2-tetrafluoroethane)," unpublished
|
||
?
|
||
?The uncertainty in viscosity is 1.5% along the saturated liquid line, 3% in
|
||
? the liquid phase, 0.5% in the dilute gas, 3-5% in the vapor phase, and 5%
|
||
? in the supercritical region, rising to 8% at pressures above 40 MPa.
|
||
? Below 200 K, the uncertainty is 8%.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
169.85 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
100000.0 !Upper pressure limit [kPa]
|
||
17.05 !Maximum density [mol/L] (rho on melting line at 100 MPa)
|
||
1 !Number of terms associated with dilute-gas function
|
||
CI1 !Pointer to reduced effective collision cross-section model
|
||
0.50647 !Lennard-Jones coefficient sigma [nm]
|
||
288.82 !Lennard-Jones coefficient epsilon/kappa [K]
|
||
1.0 1.0 !Reducing parameters for T, eta
|
||
0.215729 0.5 ! =0.021357*SQRT(MW) [Chapman-Enskog term]
|
||
13 !Number of terms for initial density dependence
|
||
288.82 0.07823693 !Reducing parameters for T (=eps/k), etaB2 (= 0.6022137*sigma**3)
|
||
-1.7999496 0.0 !Coefficient, power in T* = T/(eps/k)
|
||
46.692621 -0.5
|
||
-534.60794 -1.0
|
||
3360.4074 -1.5
|
||
-13019.164 -2.0
|
||
33414.23 -2.5
|
||
-58711.743 -3.0
|
||
71426.686 -3.5
|
||
-59834.012 -4.0
|
||
33652.741 -4.5
|
||
-12027.35 -5.0
|
||
2434.8205 -5.5
|
||
-208.07957 -6.0
|
||
2 3 2 2 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
|
||
374.18 4.9788302 1000.0 !Reducing parameters for T, rho, eta (Laesecke correlation in terms of mPa-s, convert to uPa-s)
|
||
3.07383 0.0 ! c4; power of tau for del0
|
||
0.482539055 1.0 ! c3*c4
|
||
-0.0331249 0.0 1. 0. 0 ! c1; powers of tau, del, del0; power of del in exponential [0 indicated no exponential term present]
|
||
-0.000468509 0.0 2. 0. 0 ! c2
|
||
0.306398 0.0 0. -1. 0 ! -c5
|
||
-0.306398 0.0 0. 0. 0 ! c5
|
||
0.215221 0.0 1. 0. 0 ! c6
|
||
1.0 0.0 0. 1. 0 ! del0 term in denominator
|
||
-1.0 0.0 1. 0. 0 ! -del term in denominator
|
||
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
||
|
||
|
||
@AUX !---Reduced effective collision cross-section model specification
|
||
CI1 Reduced effective collision cross-section model (empirical form in log(T*))
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Reduced effective collision cross-section of Wilhelm & Vogel as reported by:
|
||
? Laesecke, A.,
|
||
? "Data reassessment and full surface correlation of
|
||
? the viscosity of HFC-134a (1,1,1,2-tetrafluoroethane),"
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
5 !Number of terms
|
||
0.2218816 0 !Coefficient, power of Tstar
|
||
-0.5079322 1
|
||
0.1285776 2
|
||
-0.008328165 3
|
||
-0.002713173 4
|
||
|
||
|
||
@PS !Vapor pressure equation
|
||
PS5 vapor pressure equation of Tillner-Roth and Baehr (1994).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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. !
|
||
374.18 4056.29 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
-7.686556 1.0
|
||
2.311791 1.5
|
||
-2.039554 2.0
|
||
-3.583758 4.0
|
||
|
||
|
||
@DL !Saturated liquid density equation
|
||
DL2 saturated liquid density equation of Tillner-Roth and Baehr (1994).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Functional Form: D=Dc*[1+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. !
|
||
374.18 5.0787988 !Reducing parameters
|
||
3 0 0 0 0 0 !Number of terms in equation
|
||
1.706155924 1.0
|
||
0.937553068 2.0
|
||
0.373002702 10.0
|
||
|
||
|
||
@DV !Saturated vapor density equation
|
||
DV4 saturated vapor density equation of Tillner-Roth and Baehr (1994).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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. !
|
||
374.18 5.06566567 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-2.837294 1.0
|
||
-7.875988 2.0
|
||
4.478586 1.5
|
||
-14.140125 6.75
|
||
-52.361297 16.5
|
||
|
||
|