566 lines
28 KiB
Plaintext
566 lines
28 KiB
Plaintext
R116 !Short name
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76-16-4 !CAS number
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Hexafluoroethane !Full name
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CF3CF3 !Chemical formula {C2F6}
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FC-116 !Synonym
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138.01182 !Molar mass [g/mol]
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173.1 !Triple point temperature [K]
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195.06 !Normal boiling point [K]
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293.03 !Critical temperature [K]
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3048.0 !Critical pressure [kPa]
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4.444 !Critical density [mol/L]
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0.2566 !Acentric factor
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0.0 !Dipole moment [Debye]; (exactly zero due to symmetry)
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IIR !Default reference state
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10.0 !Version number
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2193 !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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12200. !GWP (IPCC 2007) :GWP:
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97000. !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/C2F6/c3-1(4,5)2(6,7)8 !Standard InChI String :InChi:
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WMIYKQLTONQJES-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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04997260 !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 E.W. Lemmon, NIST Physical and Chemical Properties Division, Boulder, Colorado
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! 12-02-96 EWL, Original version.
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! 05-21-02 MLH, Add coefficients for fit to transport data.
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! 07-11-02 EWL, Add new equation of Lemmon and Span.
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! 01-23-03 EWL, Update cp0 equation.
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! 01-30-04 EWL, Update EOS coefficients.
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! 04-19-04 MLH, Update transport reference.
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! 08-17-10 IDC, Add ancillary equations.
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! 10-15-10 MLH, Revise lower t limits on visc and therm. cond.
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! 10-18-10 MLH, Revise viscosity and thermal conductivity estimation method.
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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-116 of Lemmon and Span (2006).
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:TRUECRITICALPOINT: 293.03 4.444 !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: 10.1021/je050186n
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R.,
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? "Short Fundamental Equations of State for 20 Industrial Fluids,"
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? J. Chem. Eng. Data, 51(3):785-850, 2006. doi: 10.1021/je050186n
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?
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?The uncertainties in the equation are 0.5% in density for liquid and vapor
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? states and 1% in density or pressure for supercritical states. For vapor
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? pressure, the uncertainty is 0.3%, that for vapor phase speed of sounds is
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? 0.2%, and the uncertainty for heat capacities is 5%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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173.1 !Lower temperature limit [K]
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425.0 !Upper temperature limit [K]
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50000.0 !Upper pressure limit [kPa]
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12.31 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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138.01182 !Molar mass [g/mol]
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173.1 !Triple point temperature [K]
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26.08 !Pressure at triple point [kPa]
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12.30 !Density at triple point [mol/L]
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195.06 !Normal boiling point temperature [K]
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0.2566 !Acentric factor
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293.03 3048.0 4.444 !Tc [K], pc [kPa], rhoc [mol/L]
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293.03 4.444 !Reducing parameters [K, mol/L]
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8.314472 !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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1.1632 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-2.8123 1.125 1. 0.
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0.77202 1.5 1. 0.
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-0.14331 1.375 2. 0.
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0.10227 0.25 3. 0.
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0.00024629 0.875 7. 0.
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0.30893 0.625 2. 1.
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-0.028499 1.75 5. 1.
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-0.30343 3.625 1. 2.
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-0.068793 3.625 4. 2.
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-0.027218 14.5 3. 3.
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0.010665 12.0 4. 3.
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-116 of Lemmon and Span (2006).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R., 2006.
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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 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.0 0.0
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2.4818 190.0
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7.0622 622.0
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7.9951 1470.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-116 of Lemmon and Span (2006).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R., 2006.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 2 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-10.7088893891341712 0.0 !aj, ti for [ai*tau**ti] terms
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8.9149145291965084 1.0 !aj, ti for [ai*tau**ti] terms
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2.4818 190.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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7.0622 622.0
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7.9951 1470.0
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#AUX !---Auxiliary function for PH0
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PH0 !Ideal gas Helmholtz form for R-116.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R., 2006.
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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 2 3 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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3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-10.7088650331 0.0 !aj, ti for [ai*tau**ti] terms
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8.9148979056 1.0
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2.4818 -0.648397775 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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7.0622 -2.1226495581
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7.9951 -5.0165512064
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FE1 !Helmholtz equation of state for R-116 of Kozlov (1996).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?private communication from Dr. Alexander D. Kozlov, Director,
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? to E.W. Lemmon, 1996.
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? VNITs SMV Russian Research Center for Standardization Information
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? and Certification of Materials, Nahimovsky prospect, 31, Bld. 2
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? Moscow 117418, Russia. aldrkozlov@mail.ru
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?
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!```````````````````````````````````````````````````````````````````````````````
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176.0 !Lower temperature limit [K]
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425.0 !Upper temperature limit [K]
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50000.0 !Upper pressure limit [kPa]
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12.23 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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138.01 !Molar mass [g/mol]
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176.0 !Triple point temperature [K]
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32.09 !Pressure at triple point [kPa]
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12.231 !Density at triple point [mol/L]
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194.98 !Normal boiling point temperature [K]
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0.25396 !Acentric factor
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293.03 3042.0 4.5069198 !Tc [K], pc [kPa], rhoc [mol/L]
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293.03 4.5069198 !Reducing parameters [K, mol/L]
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8.31451 !Gas constant [J/mol-K]
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23 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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2.1775273 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-5.5052198 1.0 1. 0.
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-1.3675742 3.0 1. 0.
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-0.81284229 4.0 1. 0.
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-0.40207525 0.25 2. 0.
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2.5890073 1.0 2. 0.
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1.4500537 3.50 2. 0.
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-1.0445036 1.50 3. 0.
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0.98965288 2.5 3. 0.
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-0.86794888 3.0 4. 0.
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0.28240917 3.0 5. 0.
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0.04515422 1.0 6. 0.
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-0.030294024 3.0 6. 0.
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-0.017668398 1.0 7. 0.
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0.0020592774 1.0 8. 0.
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4.2059839 2.0 1. 1.
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0.2150038 5.0 1. 2.
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-0.16449561 2.0 4. 2.
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-0.12396086 4.0 4. 2.
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0.15814552 8.0 5. 3.
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-0.14362345 10.0 5. 3.
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0.018637877 10.0 8. 3.
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0.016342835 18.0 4. 4.
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for R-116 of Kozlov (1996).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?private communication with Dr. Alexander D. Kozlov
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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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6 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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27.4009901 0.0
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-2.6057376855e-6 2.0
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9.7501305219e-10 3.0
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-6559.250418 -1.0
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787904.9649 -2.0
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-34166787.86 -3.0
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^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
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#ETA !---Viscosity---
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VS1 !Estimation based on pure fluid viscosity model for R-134a of Huber et al. (2003), scaled to R116.
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:DOI: 10.1021/ie0300880
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?
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?```````````````````````````````````````````````````````````````````````````````
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?The model is based on a scaling of the correlation presented below.
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?Huber, M.L., Laesecke, A., and Perkins, R.A.,
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? "Model for the Viscosity and Thermal Conductivity of Refrigerants, Including
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? a New Correlation for the Viscosity of R134a,"
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? Ind. Eng. Chem. Res., 42(13):3163-3178, 2003. doi: 10.1021/ie0300880
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?
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?The estimated uncertainty in the liquid phase along the saturation boundary is 25 %,
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? and of the vapor phase is 5 %.
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?
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!```````````````````````````````````````````````````````````````````````````````
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173.1 !Lower temperature limit [K]
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425.0 !Upper temperature limit [K]
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50000.0 !Upper pressure limit [kPa]
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12.31 !Maximum density [mol/L]
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1 !Number of terms associated with dilute-gas function
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CI1 !Pointer to reduced effective collision cross-section model
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0.5249 !Lennard-Jones coefficient sigma [nm]
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226.16 !Lennard-Jones coefficient epsilon/kappa [K]
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1.0 1.10 !Reducing parameters for T, eta scaled
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0.25090 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term]
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9 !Number of terms for initial density dependence
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226.16 0.08709 !Reducing parameters for T (=eps/k), etaB2 (= 0.6022137*sigma**3)
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-19.572881 0.0 !Coefficient, power in T* = T/(eps/k)
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219.73999 -0.25
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-1015.3226 -0.5
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2471.0125 -0.75
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-3375.1717 -1.0
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2491.6597 -1.25
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-787.26086 -1.5
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14.085455 -2.5
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-0.34664158 -5.5
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-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
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293.03 4.444 1220.0 !Reducing parameters for T, rho, eta sacling for R116 (Laesecke correlation in terms of mPa-s, convert to uPa-s)
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3.163695635587490 0.0 !Alternative form for del10; numerator term
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-0.08901733752064137 1.0 !Alternative form for del10; denominator terms
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0.1000352946668359 2.0 !Alternative form for del10; denominator terms
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-0.02069007192080741 0.0 1. 0. 0 ! beta1; powers of tau, del, del0; power of del in exponential [0 indicated no exponential term present]
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0.0003560295489828222 -6.0 2. 0. 0 ! beta2
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0.002111018162451597 -2.0 2. 0. 0 ! beta3
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0.01396014148308975 -0.5 2. 0. 0 ! beta4
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-0.004564350196734897 2.0 2. 0. 0 ! beta5
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-0.00351593274583689 0.0 3. 0. 0 ! beta6
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-0.2147633195397038 0.0 0. -1. 0 ! beta7
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0.2147633195397038 0.0 0. 0. 0 ! beta7 in non-simple poly term
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1.0 0.0 0. 1. 0 ! del0 term in denominator
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-1.0 0.0 1. 0. 0 ! -del term in denominator
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NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
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#AUX !---Auxiliary function for the collision integral
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CI1 !Reduced effective collision cross-section model (empirical form in log(T*)) for R-116.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Reduced effective collision cross-section of Wilhelm & Vogel as reported by:
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? Laesecke, A. (laesecke@boulder.nist.gov); Unpublished correlation R134aFitSelDV
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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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3 !Number of terms
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0.355404 0 !Coefficient, power of Tstar
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-0.464337 1
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0.0257353 2
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================================================================================
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#TCX !---Thermal conductivity---
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TC1 !Pure fluid thermal conductivity model for R-134a of Perkins et al. (2000), scaled to R116.
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:DOI: 10.6028/NIST.IR.6605
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:WEB: https://doi.org/10.6028/NIST.IR.6605
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?
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?```````````````````````````````````````````````````````````````````````````````
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?The model is based on a scaling of the correlation presented below.
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? Perkins, R.A., Laesecke, A., Howley, J., Ramires, M.L.V., Gurova, A.N., and
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? Cusco, L., "Experimental Thermal Conductivity Values for the IUPAC
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? Round-Robin Sample of 1,1,1,2-Tetrafluoroethane (R134a),"
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? NISTIR, 2000.
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?
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?The estimated uncertainty in thermal conductivity is 5%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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173.1 !Lower temperature limit [K]
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425.0 !Upper temperature limit [K]
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50000.0 !Upper pressure limit [kPa]
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||
12.31 !Maximum density [mol/L]
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||
2 0 !# terms for dilute gas function: numerator, denominator
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||
1.0 1.05 !Reducing parameters for T, tcx
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||
-0.0105248 0. !Coefficient, power in T
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8.00982e-5 1.
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4 0 !# terms for background gas function: numerator, denominator
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||
1. 4.444 0.00164 !2.055e-3!reducing parameters for T, rho (rho_c), tcx
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1.836526 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
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5.126143 0. 2. 0.
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-1.436883 0. 3. 0.
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0.6261441 0. 4. 0.
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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 R-116 of Olchowy and Sengers (1989).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Olchowy, G.A. and Sengers, J.V.,
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? "A Simplified Representation for the Thermal Conductivity of Fluids in the Critical Region,"
|
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? Int. J. Thermophys., 10:417-426, 1989. doi: 10.1007/BF01133538
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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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||
9 0 0 0 !# terms: CO2-terms, spare, spare, spare
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1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
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0.63 !Nu (universal exponent)
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1.239 !Gamma (universal exponent)
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1.03 !R0 (universal amplitude)
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0.063 !Z (universal exponent--not used for t.c., only viscosity)
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1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
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0.194e-9 !Xi0 (amplitude) [m]
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0.0496 !Gam0 (amplitude) [-]
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||
0.5e-9 !Qd_inverse (modified effective cutoff parameter) [m]; generic number, not fitted to data
|
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439.545 !Tref (reference temperature)=1.5*Tc [K]
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++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
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@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (R134a reference); fitted to limited data for R-116.
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||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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
|
||
?
|
||
?THERMAL CONDUCTIVITY
|
||
? The ECS parameters for thermal conductivity were based in part on the data of:
|
||
? Tauscher, W. (1967). "Thermal conductivity of liquid refrigerants measured by an unsteady state hot wire method".Kaltetechnik, 19:288-292.
|
||
? Gunchuk, B.V., Zhelezny, V.P., Zhosul, I. (1989). "Study of density, viscosity, thermal conductivity, surface tension of refrigerants R116, R132B2, R318, R329 and azeotropic mixtures of R116-R23, R116-R13 at the boiling line", Teplofizicheskiye svoysta veshchestv i materialov, part 28,93-106.
|
||
? Potapov, M.D. (1988). "The thermal conductivity of liquid binary mixtures of halogenated hydrocarbons", PhD Thesis, OTIPP, Odessa.
|
||
? Clifford, A.A., Dickinson, E. and Gray, P. (1976)."Thermal conductivity of gaseous alkanes + perfluoroalkane mixtures", J. Chem. Soc. Far. Trans. I, 1997.doi: 10.1039/f19767201997
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Tauscher: 2.57%; Gunchuk: 1.15%; Potapov: 1.20%; Clifford: 3.93%; Overall: 1.37%
|
||
?
|
||
?VISCOSITY
|
||
? The ECS parameters for viscosity were based in part on the data of:
|
||
? Gunchuk, B.V., Zhelezny, V.P., Zhosul, I. (1989). "Study of density, viscosity, thermal conductivity, surface tension of refrigerants R116, R132B2, R318, R329 and azeotropic mixtures of R116-R23, R116-R13 at the boiling line", Teplofizicheskiye svoysta veshchestv i materialov, part 28,93-106.
|
||
? Dunlop, P.J. (1994). "Viscosities of a series of gaseous fluorocarbons at 25C", J.Chem.Phys. 100(4):3149-3151.
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Gunchuk: 0.88%; Dunlop: 1.06%; Overall: 0.89%
|
||
?
|
||
?The Lennard-Jones parameters were estimated.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
173.1 !Lower temperature limit [K]
|
||
425.0 !Upper temperature limit [K]
|
||
50000.0 !Upper pressure limit [kPa]
|
||
12.31 !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)
|
||
0.5249 !Lennard-Jones coefficient sigma [nm] for ECS method !from scaling R134a
|
||
226.16 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method !from scaling R134a
|
||
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
|
||
1.21996 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
-0.0647835 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
||
1.18041 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
-0.0539975 0. 1. 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-116 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. !
|
||
2 !Number of terms in surface tension model
|
||
293.03 !Critical temperature used in fit (dummy)
|
||
0.047593 1.2666 !Sigma0 and n
|
||
-0.0073402 1.9892
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for R-116 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. !
|
||
293.03 3048.0 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-7.3997 1.0
|
||
2.2554 1.5
|
||
-2.3385 2.2
|
||
-3.5244 4.8
|
||
0.40350 6.2
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for R-116 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. !
|
||
293.03 4.444 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
68.490 0.64
|
||
-247.72 0.79
|
||
358.24 0.95
|
||
-252.90 1.14
|
||
76.880 1.33
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for R-116 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. !
|
||
293.03 4.444 !Reducing parameters
|
||
6 0 0 0 0 0 !Number of terms in equation
|
||
-3.4135 0.428
|
||
-145.29 2.0
|
||
236.51 2.24
|
||
-222.76 3.0
|
||
231.03 4.0
|
||
-174.33 5.0
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
||
|
||
|
||
@EOS !Equation of state specification
|
||
ECS Thermodynamic Extended Corresponding States model w/ T- and rho-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
|
||
?
|
||
?extended by the addition of density-dependent shape factors based on
|
||
? fit by E.W. Lemmon, 12-2-96
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
173.1 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
60000.0 !Upper pressure limit [kPa]
|
||
12.29 !Maximum density [mol/L]
|
||
CPP !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
|
||
0.256 !Acentric factor for fluid used in shape factor correlation
|
||
293.03 !Critical temperature [K]
|
||
3042.0 !Critical pressure [kPa]
|
||
4.5069198 !Critical density [mol/L]
|
||
2 !Number of temperature coefficients for 'f' shape factor
|
||
0.463297447 0. ! alpha1 of Huber & Ely
|
||
-0.511776783 1. ! alpha2 (log(Tr) term)
|
||
1 !Number of density coefficients for 'f' shape factor
|
||
0.00707956644 1. ! rho coefficient and power in temperature
|
||
3 !Number of temperature coefficients for 'h' shape factor
|
||
-4.04678693 0. ! beta1 of Huber & Ely
|
||
-2.3908788 1. ! beta2 (log(Tr) term)
|
||
-0.169059282 1.
|
||
0 !Number of density coefficients for 'h' shape factor
|