525 lines
26 KiB
Plaintext
525 lines
26 KiB
Plaintext
R123 !Short name
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306-83-2 !CAS number
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2,2-Dichloro-1,1,1-trifluoroethane !Full name
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CHCl2CF3 !Chemical formula {C2HCl2F3}
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HCFC-123 !Synonym
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152.931 !Molar mass [g/mol]
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166.0 !Triple point temperature [K]
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300.973 !Normal boiling point [K]
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456.831 !Critical temperature [K]
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3661.8 !Critical pressure [kPa]
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3.596417 !Critical density [mol/L]
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0.28192 !Acentric factor
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1.356 !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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???? !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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77. !GWP (IPCC 2007) :GWP:
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0.01 !ODP (WMO 2010) :ODP:
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9100. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
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B1 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/C2HCl2F3/c3-1(4)2(5,6)7/h1H !Standard InChI String :InChi:
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OHMHBGPWCHTMQE-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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efdfede0 !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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! 08-17-10 IDC, Add ancillary equations.
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! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
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! 04-25-18 MLH, Add TK3 block to replace TK1 block.
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________________________________________________________________________________
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#EOS !---Equation of state---
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BWR !MBWR equation of state for R-123 of Younglove and McLinden (1994).
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:TRUECRITICALPOINT: 456.831 3.596417 !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: 10.1063/1.555950
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Younglove, B.A. and McLinden, M.O.,
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? "An International Standard Equation of State for the Thermodynamic
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? Properties of Refrigerant 123 (2,2-Dichloro-1,1,1-Trifluoroethane),"
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? J. Phys. Chem. Ref. Data, 23:731-779, 1994.
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?
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?The uncertainties of the equation of state are 0.1% in density, 1.5% in heat
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? capacity, and 2% in the speed of sound, except in the critical region.
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? The uncertainty in vapor pressure is 0.1%. Uncertainties are greater below
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? 180 K.
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?
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!```````````````````````````````````````````````````````````````````````````````
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166.0 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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40000.0 !Upper pressure limit [kPa]
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11.60 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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152.931 !Molar mass [g/mol]
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166.0 !Triple point temperature [K]
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0.004202 !Pressure at triple point [kPa]
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11.58 !Density at triple point [mol/L]
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300.973 !Normal boiling point temperature [K]
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0.28192 !Acentric factor
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456.831 3661.8 3.596417 !Tc [K], pc [kPa], rhoc [mol/L]
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456.831 3.596417 !Reducing parameters [K, mol/L]
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3.596417 !gamma
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0.08314510 !Gas constant [L-bar/mol-K]
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32 1 !Nterm, Ncoeff per term
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-0.00657453133659 2.93479845842 -98.9140469845
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20102.9776013 -3835665.27886 0.00227587641969
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-9.0872681945 4341.81417995 3541164.64954
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-0.00063539484967 3.20786715274 -1312.76484299
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-0.116360713718 -11.3354409016 -5375.43457327
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2.5811241612 -0.106148632128 50.0026133667
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-2.04326706346 -2494383.45685 -463962781.113
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-284903.429588 0.974392239902e+10 -6373.14379308
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314121.189813 -145.747968225 -8438302.61449
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-2.41138441593 1085.08031257 -0.0106653193965
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-12.1343571084 -257.51038324
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-123 of Younglove & McLinden (1994).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Younglove, B.A. and McLinden, M.O., 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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1.0 1.0 !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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17.01154 0.0
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0.4046308 1.0
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-0.0004644803 2.0
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2.347418e-7 3.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-123 of Younglove & McLinden (1994).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Younglove, B.A. and McLinden, M.O., 1994.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 5 0 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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1.0460186721932314 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-13.2327874222552726 0.0 !aj, ti for [ai*tau**ti] terms
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10.948194603389112 1.0 !aj, ti for [ai*tau**ti] terms
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0.0486659157339362 -1.0
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-0.558641584869e-04 -2.0
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0.282329586824e-07 -3.0
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FE1 !Helmholtz transformation of MBWR EOS for R-123 of Younglove & McLinden (1994).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Younglove, B.A. and McLinden, M.O.,
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? "An International Standard Equation of State for the Thermodynamic
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? Properties of Refrigerant 123 (2,2-Dichloro-1,1,1-trifluoroethane),"
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? J. Phys. Chem. Ref. Data, 23:731-779, 1994.
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?
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?The equation here is the same as the Younglove and McLinden BWR equation,
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? but has been transformed into the fundamental Helmholtz energy form.
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?
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!```````````````````````````````````````````````````````````````````````````````
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166.0 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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40000.0 !Upper pressure limit [kPa]
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11.60 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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152.931 !Molar mass [g/mol]
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166.0 !Triple point temperature [K]
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0.0042 !Pressure at triple point [kPa]
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11.60 !Density at triple point [mol/L]
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300.973 !Normal boiling point temperature [K]
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0.28192 !Acentric factor
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456.831 3661.8 3.596417 !Tc [K], pc [kPa], rhoc [mol/L]
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456.831 3.596417 !Reducing parameters [K, mol/L]
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8.314510 !Gas constant [J/mol-K]
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40 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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-10.0242647494 3.0 0. 0. !a(i),t(i),d(i),l(i)
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-0.280607656419 4.0 0. 0.
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0.0206814471606 5.0 0. 0.
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-0.284379431451 0.0 1. 0.
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5.93928110321 0.5 1. 0.
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-9.36560389528 1.0 1. 0.
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4.16660793675 2.0 1. 0.
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-1.74023292951 3.0 1. 0.
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0.177019905365 0.0 2. 0.
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-1.5472169226 1.0 2. 0.
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1.6182049559 2.0 2. 0.
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2.88903529383 3.0 2. 0.
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-0.118493874757 0.0 3. 0.
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1.30952266209 1.0 3. 0.
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-1.17308103711 2.0 3. 0.
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-0.12812513195 1.0 4. 0.
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-0.0786087387513 2.0 5. 0.
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-0.0816000499305 3.0 5. 0.
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0.0536451054311 2.0 6. 0.
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-0.00680078211929 2.0 7. 0.
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0.00701264082191 3.0 7. 0.
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-0.000901762397311 3.0 8. 0.
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10.0242647494 3.0 0. 2.
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0.280607656419 4.0 0. 2.
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-0.0206814471606 5.0 0. 2.
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7.98923878145 3.0 2. 2.
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-0.547972072476 4.0 2. 2.
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-0.0206814470584 5.0 2. 2.
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2.49142724365 3.0 4. 2.
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-0.273986034884 4.0 4. 2.
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0.236001863614 5.0 4. 2.
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0.540528251211 3.0 6. 2.
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-0.0600457561959 4.0 6. 2.
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0.0786672874826 5.0 6. 2.
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0.0708085874508 3.0 8. 2.
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-0.0150114389748 4.0 8. 2.
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0.00182205199477 5.0 8. 2.
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0.00314978575163 3.0 10. 2.
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0.00784455573794 4.0 10. 2.
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0.000364410397155 5.0 10. 2.
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@EOS !---Equation of state---
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FES !Helmholtz equation of state for R-123 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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166.0 !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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11.62 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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152.931 !Molar mass [g/mol]
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166.0 !Triple point temperature [K]
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0.0041534 !Pressure at triple point [kPa]
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11.613 !Density at triple point [mol/L]
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300.96 !Normal boiling point temperature [K]
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0.283 !Acentric factor
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456.82 3672.0 3.6160098 !Tc [K], pc [kPa], rhoc [mol/L]
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456.82 3.6160098 !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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1.116973 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-3.074593 1.25 1. 0.
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0.51063873 1.5 1. 0.
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0.094478812 0.25 3. 0.
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0.00029532752 0.875 7. 0.
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0.66974438 2.375 1. 1.
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0.96438575 2.0 2. 1.
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-0.014865424 2.125 5. 1.
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-0.49221959 3.5 1. 2.
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-0.022831038 6.5 1. 2.
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-0.1407486 4.75 4. 2.
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-0.025117301 12.5 2. 3.
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^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
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#ETA !---Viscosity---
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VS1 !Pure fluid viscosity model for R-123 of Tanaka and Sotani (1995).
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:DOI: 10.1007/BF01443394
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tanaka, Y. and Sotani, T.,
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? "Transport Properties (Thermal Conductivity and Viscosity),"
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? in McLinden, M.O., editor. R123--Thermodynamic and Physical
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? Properties. Paris, International Institute of Refrigeration, 1995.
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?
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?see also: Int. J. Thermophys., 17(2):293-328, 1996. doi: 10.1007/BF01443394
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?
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?The uncertainty in viscosity is 5%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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166.0 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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40000.0 !Upper pressure limit [kPa]
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15.90 !Maximum density [mol/L]
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4 !Number of terms associated with dilute-gas function
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NUL !Pointer to collision integral model
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0.5909 !Lennard-Jones coefficient sigma [nm]
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275.16 !Lennard-Jones coefficient epsilon/kappa [K]
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1.0 1.0 !Reducing parameters for T, eta
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0.0 0.5 !Chapman-Enskog term (not used here)
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-2.273638 0.0 !Polynomial term: Coefficient, power of T
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0.05099859 1.0
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-2.402786e-5 2.0
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0 !# initial density terms (these are merged with residual term)
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1 6 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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1.0 0.006538897 1.0 !Reducing parameters for T, rho (= 1/MW), eta
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1828.263 0.0 0. 0. 0 ! rho_0; powers of tau, del, del0; power of del in exponential [0 indicated no exponential term present]
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-176.2849 0.0 0. 0. 0 ! d0/rho_0
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-0.02226484 0.0 1. 0. 0 ! const term in Eqn 2.8 (the initial density term)
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5.550623e-5 1.0 1. 0. 0 !Temperature term in Eqn 2.8
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-0.1009812 0.0 1. 0. 0 ! d1 in Eqn 2.9
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6.161902e-5 0.0 2. 0. 0 ! d2
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-8.84048e-8 0.0 3. 0. 0 ! d3
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-322295.1 0.0 0. 0. 0 ! d0 in numerator of rational polynomial
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1.0 0.0 1. 0. 0 ! rho in denominator of rational polynomial
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-1.0 0.0 0. 1. 0 ! rho_0 in denominator of rational polynomial
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NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
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================================================================================
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#TCX !---Thermal conductivity---
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TC1 !Pure fluid thermal conductivity model for R-123 of Laesecke et al. (1996).
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:DOI: 10.1016/0140-7007(96)00019-9
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Laesecke, A., Perkins, R.A., and Howley, J.B.,
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? "An Improved Correlation for the Thermal Conductivity of HCFC123
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? (2,2-Dichloro-1,1,1-Trifluoroethane),"
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? Int. J. Refrig., 19:231-238, 1996. doi: 10.1016/0140-7007(96)00019-9
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?
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?The uncertainty in thermal conductivity is 2%, according to Laesecke et al, 1996. However, data published after 1996 (Perkins, R., Cusco, L., Howley, J., Laesecke, A., Matthes, S., Ramires, M.L.V., "Thermal Conductivities of Alternatives to CFC-11 for Foam Insulation," J. Chem. Eng. Data, 46:428-432, 2001. doi: 10.1021/je990337k)
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? suggest that the uncertainty in gas phase thermal conductivity may be 10-20%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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166.0 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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67000.0 !Upper pressure limit [kPa]
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12.42 !Maximum density [mol/L] (= 1900 kg/m^3)
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2 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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-0.00778 0. !Coefficient, power in T
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5.695e-5 1.
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12 0 !# terms for background gas function: numerator, denominator
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456.831 3.596417 1. !Reducing parameters for T (= Tc), rho (= Dc), tcx
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0.0642894 -1.5 1. 0. !Coefficient, powers of Tau=T/Tc (= -powers of Tc/T), del, spare for future use
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-0.0530474 -2. 1. 0.
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0.453522e-4 -6. 1. 0.
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-0.139928 0. 2. 0.
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0.16654 -0.5 2. 0.
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-0.0162656 -1.5 2. 0.
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0.136819 0. 3. 0.
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-0.183291 -0.5 3. 0.
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0.0357146 -1.5 3. 0.
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-0.023121 0. 4. 0.
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0.0341945 -0.5 4. 0.
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-0.00757341 -1.5 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 R123 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. !
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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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1.02 !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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0.216e-9 !Xi0 (amplitude) [m]
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0.058 !Gam0 (amplitude) [-]
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||
0.643e-9 !Qd_inverse (modified effective cutoff parameter) [m]
|
||
685.25 !Tref (reference temperature)=1.5*Tc [K]
|
||
|
||
|
||
|
||
|
||
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
||
|
||
@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (R134a reference); predictive mode for R-123.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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
|
||
?
|
||
?Thermal conductivity data used in the development of the extended corresponding
|
||
? states method were taken from:
|
||
? Assael, M. J. and Karagiannidis, E., "Measurements of the Thermal Conductivity of R22, R123, and R134a in the Temperature Range 250-340 K at Pressures up to 30 MPa," J Int. J. Thermophysics, V 14, N 2. P 183-197, 1993.
|
||
?
|
||
?The Lennard-Jones parameters were taken from Nabizadeh, H. and Mayinger, F., "Viscosity of gaseous R123, R134a and R142b," High Temperatures - High Pressures, 24:221, 1992.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
166.0 !Lower temperature limit [K]
|
||
600.0 !Upper temperature limit [K]
|
||
40000.0 !Upper pressure limit [kPa]
|
||
11.60 !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)
|
||
0.5909 !Lennard-Jones coefficient sigma [nm] for ECS method
|
||
275.16 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
|
||
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
|
||
NUL !Pointer to critical enhancement auxiliary function
|
||
|
||
|
||
|
||
|
||
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
|
||
|
||
#STN !---Surface tension---
|
||
ST1 !Surface tension model for R-123 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
|
||
456.831 !Critical temperature used in fit (dummy)
|
||
0.056151 1.2367 !Sigma0 and n
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for R-123 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. !
|
||
456.831 3661.8 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
-7.4610 1.0
|
||
2.0293 1.5
|
||
-2.1897 2.25
|
||
-3.4945 4.5
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for R-123 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. !
|
||
456.831 3.596417 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
1.9996 0.345
|
||
0.41823 0.74
|
||
0.24849 1.2
|
||
0.18831 2.6
|
||
0.13737 7.2
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for R-123 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. !
|
||
456.831 3.596417 !Reducing parameters
|
||
6 0 0 0 0 0 !Number of terms in equation
|
||
-3.0205 0.3905
|
||
-7.4537 1.29
|
||
-21.880 3.4
|
||
-57.430 7.0
|
||
11.239 12.0
|
||
-166.40 15.0
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
||
|
||
|
||
@AUX !---Auxiliary function for the thermal conductivity critical enhancement
|
||
TK1 !Pure fluid thermal conductivity model for R-123 of Laesecke et al. (1996).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Laesecke, A., Perkins, R.A., and Howley, J.B.,
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
1 0 2 0 !# terms: polynomial-numerator, poly-denom, exp, spare
|
||
-456.831 3.596417 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)] (-Tc indicates tau = Tred/t), rho (= Dc), tcx in polynomial term
|
||
0.00486742 0. 0. 0. 0. 0 ! a13
|
||
-456.831 3.596417 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)] (-Tc indicates tau = Tred/t), rho (= Dc), tcx in exponential term
|
||
-100.0 -1. 4. 0. 0. 0 ! a14*(tau - 1)**4
|
||
-7.08535 0. 0. -1. 2. 0 ! a15*(del - 1)**2
|