654 lines
34 KiB
Plaintext
654 lines
34 KiB
Plaintext
R152a !Short name
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75-37-6 !CAS number
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1,1-Difluoroethane !Full name
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CHF2CH3 !Chemical formula {C2H4F2}
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HFC-152a !Synonym
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66.051 !Molar mass [g/mol]
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154.56 !Triple point temperature [K]
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249.127 !Normal boiling point [K]
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386.411 !Critical temperature [K]
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4516.75 !Critical pressure [kPa]
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5.571450 !Critical density [mol/L]
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0.27521 !Acentric factor
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2.262 !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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1030 !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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124. !GWP (IPCC 2007) :GWP:
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12000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
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A2 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/C2H4F2/c1-2(3)4/h2H,1H3 !Standard InChI String :InChi:
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NPNPZTNLOVBDOC-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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63f364b0 !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 and S.A. Klein, NIST Thermophysics Division, Boulder, Colorado
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! 11-01-95 MM, Original version.
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! 11-02-98 EWL, Add Tillner-Roth equation of state.
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! 10-06-99 EWL, Fix cp0 part of Tillner-Roth equation of state.
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! 11-01-99 EWL, Add Span 12 term short equation of state.
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! 01-24-00 EWL, Change transport limits to match EOS.
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! 07-09-01 EWL, Add Helmholtz form of BWR equation.
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! 11-28-01 MLH, Add viscosity ECS fit as NIST recommended. Kraus ref has asymptote that occurs at approximately 220 K on the liquid sat line.
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! 07-05-02 MLH, Change crit model to TK6.
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! 09-20-06 EWL, Add Astina and Sato equation.
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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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! 01-04-17 MLH, Update critical enhancement model to TK3.
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________________________________________________________________________________
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#EOS !---Equation of state---
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BWR !MBWR equation of state for R-152a of Outcalt and McLinden (1996).
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:TRUECRITICALPOINT: 386.411 5.57145 !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: 10.1063/1.555979
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Outcalt, S.L. and McLinden, M.O.,
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? "A Modified Benedict-Webb-Rubin Equation of State for the Thermodynamic
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? Properties of R152a (1,1-Difluoroethane),"
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? J. Phys. Chem. Ref. Data, 25(2):605-636, 1996.
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?
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?The uncertainties of the equation of state are 0.1% in density, 2% in heat
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? capacity, and 005% in the vapor speed of sound, except in the critical region.
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? The uncertainty in vapor pressure is 0.1%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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154.56 !Lower temperature limit [K]
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500.0 !Upper temperature limit [K]
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60000.0 !Upper pressure limit [kPa]
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18.07 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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66.051 !Molar mass [g/mol]
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154.56 !Triple point temperature [K]
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0.06413 !Pressure at triple point [kPa]
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18.061 !Density at triple point [mol/L]
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249.127 !Normal boiling point temperature [K]
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0.27521 !Acentric factor
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386.411 4516.75 5.57145 !Tc [K], pc [kPa], rhoc [mol/L]
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386.411 5.57145 !Reducing parameters [K, mol/L]
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5.57145 !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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-0.0101623317192 2.15677129618 -64.8581254334
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12253.5596303 -2068059.88259 -0.000379836507323
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-0.441333232984 158.248874708 564062.216256
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-0.000124115350431 0.494972178825 -208.058039834
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-0.0131403187106 0.212083848812 -151.263785082
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0.0311108025395 -0.00115280979645 0.437040025765
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-0.00965596535032 -242705.525346 -51804251.9989
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-11907.0545681 459333195.257 -71.9317286511
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-8401.0286146 -1.0291095739 -32591.3880841
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-0.0041236218223 1.75102808144 -0.19863662464e-4
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-0.00421363036104 -1.98696760653
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-152a of Outcalt & McLinden (1996).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Outcalt, S.L. and McLinden, M.O., 1996.
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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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27.89465 0.0 !C(i), power of T
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0.09134686 1.0
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0.0002079961 2.0
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-2.317613e-7 3.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-152a of Outcalt & McLinden (1996).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Outcalt, S.L. and McLinden, M.O., 1996.
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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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2.3549563857413802 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-7.9505153063787706 0.0 !aj, ti for [ai*tau**ti] terms
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6.870086795465296 1.0 !aj, ti for [ai*tau**ti] terms
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0.0109865057017895 -1.0
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0.250161892658e-04 -2.0
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-0.278744868067e-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-152a of Outcalt and McLinden (1996).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Outcalt, S.L. and McLinden, M.O.,
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? "A modified Benedict-Webb-Rubin equation of state for the thermodynamic
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? properties of R152a (1,1-difluoroethane),"
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? J. Phys. Chem. Ref. Data, 25(2):605-636, 1996. doi: 10.1063/1.555979
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?
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?The equation here is the same as the Outcalt 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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154.56 !Lower temperature limit [K]
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500.0 !Upper temperature limit [K]
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60000.0 !Upper pressure limit [kPa]
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18.07 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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66.051 !Molar mass [g/mol]
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154.56 !Triple point temperature [K]
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0.0641 !Pressure at triple point [kPa]
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18.061 !Density at triple point [mol/L]
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249.127 !Normal boiling point temperature [K]
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0.27521 !Acentric factor
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386.411 4516.75 5.57145 !Tc [K], pc [kPa], rhoc [mol/L]
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386.411 5.57145 !Reducing parameters [K, mol/L]
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8.314471 !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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-3.54657949982 3.0 0. 0. !a(i),t(i),d(i),l(i)
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-0.36463128062 4.0 0. 0.
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0.0333233335558 5.0 0. 0.
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-0.680968435117 0.0 1. 0.
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7.35212646801 0.5 1. 0.
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-11.2473063838 1.0 1. 0.
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5.49916715657 2.0 1. 0.
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-2.40186327322 3.0 1. 0.
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-0.0709036447042 0.0 2. 0.
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-0.213200886814 1.0 2. 0.
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0.197839736368 2.0 2. 0.
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1.82494769909 3.0 2. 0.
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-0.0860546479693 0.0 3. 0.
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0.88813736654 1.0 3. 0.
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-0.96612734637 2.0 3. 0.
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-0.0985223479324 1.0 4. 0.
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0.0183419368472 2.0 5. 0.
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-0.0338550204252 3.0 5. 0.
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0.0124921101016 2.0 6. 0.
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-0.00221056706423 2.0 7. 0.
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0.00216879133161 3.0 7. 0.
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-0.000233597690478 3.0 8. 0.
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3.54657949982 3.0 0. 2.
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0.36463128062 4.0 0. 2.
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-0.0333233335558 5.0 0. 2.
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2.76133830254 3.0 2. 2.
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-0.069118571188 4.0 2. 2.
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-0.0333233335558 5.0 2. 2.
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0.782761327717 3.0 4. 2.
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-0.034559285594 4.0 4. 2.
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0.137813531906 5.0 4. 2.
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0.186173126153 3.0 6. 2.
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-0.0341119393297 4.0 6. 2.
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0.0459378439687 5.0 6. 2.
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0.0216470012607 3.0 8. 2.
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-0.00852798483242 4.0 8. 2.
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0.00620394038634 5.0 8. 2.
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0.00185210290813 3.0 10. 2.
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0.00101674662734 4.0 10. 2.
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0.00124078807727 5.0 10. 2.
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@EOS !---Equation of state---
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FE2 !Helmholtz equation of state for R-152a of Tillner-Roth (1995).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tillner-Roth, R.,
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? "A Fundamental Equation of State for 1,1-Difluoroethane (HFC-152a),"
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? Int. J. Thermophys., 16(1):91-100, 1995.doi: 10.1007/BF01438960
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?
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?The uncertainties of the equation of state are 0.1% in density, 2% in heat
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? capacity, and 005% in the vapor speed of sound, except in the critical region.
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? The uncertainty in vapor pressure is 0.1%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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154.56 !Lower temperature limit [K]
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435.0 !Upper temperature limit [K]
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30000.0 !Upper pressure limit [kPa]
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18.03 !Maximum density [mol/L]
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CP2 !Pointer to Cp0 model
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66.051 !Molar mass [g/mol]
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154.56 !Triple point temperature [K]
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0.065395176 !Pressure at triple point [kPa]
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18.020671 !Density at triple point [mol/L]
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249.13236 !Normal boiling point temperature [K]
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0.26744 !Acentric factor
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386.41 4495.0 5.5714524 !Tc [K], pc [kPa], rhoc [mol/L]
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386.41 5.5714524 !Reducing parameters [K, mol/L]
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8.314471 !Gas constant [J/mol-K]
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19 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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0.355226 0.0 1. 0. !a(i),t(i),d(i),l(i)
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-1.42566 1.5 1. 0.
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-0.04631621 3.0 1. 0.
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0.06903546 -0.5 1.5 0.
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0.0197571 -0.5 3. 0.
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0.0007486977 -0.5 6. 0.
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0.0004642204 1.5 6. 0.
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-0.2603396 3.0 1. 1.
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-0.07624212 4.0 1. 1.
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0.2233522 3.0 3. 1.
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0.01992515 2.0 4. 1.
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0.344904 4.0 1. 2.
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-0.4963849 5.0 1. 2.
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0.1290719 6.0 1. 2.
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0.000976079 5.0 8. 2.
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0.005066545 12.5 2. 3.
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-0.0140202 25.0 3. 3.
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0.005169918 20.0 5. 3.
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0.0002679087 25.0 6. 3.
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@EOS !---Equation of state---
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FES !Helmholtz equation of state for R-152a 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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154.56 !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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18.1 !Maximum density [mol/L]
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CP2 !Pointer to Cp0 model
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66.051 !Molar mass [g/mol]
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154.56 !Triple point temperature [K]
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0.064093 !Pressure at triple point [kPa]
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18.031 !Density at triple point [mol/L]
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249.11 !Normal boiling point temperature [K]
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0.275 !Acentric factor
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386.41 4519.8 5.5714524 !Tc [K], pc [kPa], rhoc [mol/L]
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386.41 5.5714524 !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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0.95702326 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-2.3707196 1.25 1. 0.
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0.18748463 1.5 1. 0.
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0.063800843 0.25 3. 0.
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0.00016625977 0.875 7. 0.
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0.082208165 2.375 1. 1.
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0.57243518 2.0 2. 1.
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0.0039476701 2.125 5. 1.
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-0.23848654 3.5 1. 2.
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-0.080711618 6.5 1. 2.
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-0.073103558 4.75 4. 2.
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-0.015538724 12.5 2. 3.
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@AUX !---Auxiliary function for Cp0
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CP2 !Ideal gas heat capacity function for R-152a.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tillner-Roth, R.,
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314471 !Reducing parameters for T, Cp0
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3 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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1.4652739 0.25
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0.00002627677 2.0
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-0.29988241e-10 4.0
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@EOS !---Equation of state---
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FE3 !Helmholtz equation of state for R-152a 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 Rigorous Thermodynamic Property Model for Fluid-Phase
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? 1,1-Difluoroethane (R-152a),"
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? Int. J. Thermophys., 25(6):1713-1733, 2004. doi: 10.1007/s10765-004-7731-8
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?
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!```````````````````````````````````````````````````````````````````````````````
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154.56 !Lower temperature limit [K]
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450.0 !Upper temperature limit [K]
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60000.0 !Upper pressure limit [kPa]
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18.04 !Maximum density [mol/L]
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PH3 !Pointer to Cp0 model
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66.050 !Molar mass [g/mol]
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154.56 !Triple point temperature [K]
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0.064 !Pressure at triple point [kPa]
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18.04 !Density at triple point [mol/L]
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249.117 !Normal boiling point temperature [K]
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0.275 !Acentric factor
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386.41 4516.0 5.571536715 !Tc [K], pc [kPa], rhoc [mol/L]
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386.41 5.571536715 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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17 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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1.753847317 0.5 1. 0. !a(i),t(i),d(i),l(i)
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-4.049760759 1.125 1. 0.
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-0.2277389257 2.875 1. 0.
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0.708775195 0.875 2. 0.
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-0.5528619502 1.875 2. 0.
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-0.03025046686 0.5 3. 0.
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0.1396289974 1.875 3. 0.
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1.121238954e-4 4.0 4. 0.
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1.181005890 1.25 1. 1.
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1.535785579 2. 2. 1.
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0.7468363045 2.75 3. 1.
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-0.1252266405 6.0 1. 2.
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-0.03898223986 9.0 2. 2.
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-0.07260588801 6.0 3. 2.
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-0.00265930225 22.0 3. 3.
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0.004210849329 20.0 4. 3.
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2.015953966e-4 32.0 5. 3.
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@AUX !---Auxiliary function for PH0
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PH3 !Helmholtz form for the ideal-gas state
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Astina, I.M. and Sato, H.
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?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
1 4 2 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
|
||
-9.508135074 0.0 !aj, ti for [ai*tau**ti] terms
|
||
6.812068779 1.0
|
||
-7.285916044 -0.5
|
||
6.741130104 0.25
|
||
1.978152028 -1.753741145
|
||
5.880826311 -4.360150337
|
||
|
||
|
||
|
||
|
||
================================================================================
|
||
|
||
#TCX !---Thermal conductivity---
|
||
TC1 !Pure fluid thermal conductivity model for R-152a of Krauss et al. (1996).
|
||
:DOI: 10.1007/BF01439187
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Krauss, R., Weiss, V.C., Edison, T.A., Sengers, J.V., and Stephan, K.,
|
||
? "Transport Properties of 1,1-Difluoroethane (R152a),"
|
||
? Int. J. Thermophys., 17:731-757, 1996. doi: 10.1007/BF01439187
|
||
?
|
||
?The uncertainty in thermal conductivity is 3% in the dilute gas and 5%
|
||
? elsewhere (10% in the critical region).
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
154.56 !Lower temperature limit [K] !Krauss claims only 240 K, but seems to extrapolate fine
|
||
500.0 !Upper temperature limit [K]
|
||
60000.0 !Upper pressure limit [kPa]
|
||
18.07 !Maximum density [mol/L]
|
||
2 0 !# terms for dilute gas function: numerator, denominator
|
||
1.0 0.001 !Reducing parameters for T, tcx [Krauss corr in mW/m.K]
|
||
-14.942 0. !Coefficient, power in T
|
||
0.0973283 1.
|
||
4 0 !# terms for background gas function: numerator, denominator
|
||
1.0 5.57145 0.001115 !Reducing parameters for T, rho (rho_c), tcx
|
||
9.1809 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
|
||
11.8577 0. 2. 0.
|
||
-5.4473 0. 3. 0.
|
||
1.71379 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-152a 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)
|
||
1.075 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
|
||
0.1894e-9 !Xi0 (amplitude) [m]
|
||
0.0487 !Gam0 (amplitude) [-]
|
||
4.37e-10 !Qd_inverse (modified effective cutoff parameter) [m]
|
||
579.617 !Tref (reference temperature) [= 1.5 * 386.411 K]
|
||
|
||
|
||
|
||
|
||
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
||
|
||
@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (Propane reference); fitted to data for R-152a.
|
||
:DOI: 10.1016/S0140-7007(96)00073-4
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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
|
||
?
|
||
?VISCOSITY
|
||
? The ECS parameters for viscosity were based on the data of:
|
||
? vanderGulik, P. S.(1995)"Viscosity of saturated R152a measured with a vibrating wire viscometer" Int. J. Thermophys.,16, 867-76 doi: 10.1007/BF02093469
|
||
? Takahashi, M., Yokoyama, C., and Takahashi, S.(1987)"Viscosities of Gaseous R13B1, R142b, and R152a" J. Chem. Eng. Data,32,98-103. doi: 10.1021/je00047a027
|
||
? Assael, M. J., Polimatidou, S. K., Vogel, E., and Wakeham, W. A.(1994). "Measurements of the viscosity of R11, R12, R141b, and R152a in the temperature range 270-340 K at pressures up to 20 MPa" Int. J. Thermophys.,15,575-89.
|
||
? Karbanov, E.M. (1978). "Investigation of the Dynamic Viscosity of Some Freons of Ethane Type and of the Bromide Freons" Ph.D. Thesis, Groz. Neft. Inst., Grozny, USSR
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? vanderGulik: 4.77%; Takahashi: 1.73%; Assael: 1.62%; Karbanov:5.64%
|
||
? Overall: 2.78%
|
||
?
|
||
?The Lennard-Jones parameters were taken from Krauss, R., Weiss, V.C., Edison, T.A., Sengers, J.V., and Stephan, K., "Transport properties of 1,1-Difluoroethane (R152a),"Int. J. Thermophysics 17:731-757, 1996.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
154.56 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
60000.0 !Upper pressure limit [kPa]
|
||
18.07 !Maximum density [mol/L]
|
||
FEQ PROPANE.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)
|
||
0.46115 !Lennard-Jones coefficient sigma [nm] for ECS method
|
||
354.84 !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
|
||
2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
|
||
0.824547 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0640641 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
1 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
||
1.0 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
TK3 !Pointer to critical enhancement auxiliary function
|
||
|
||
|
||
|
||
|
||
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
|
||
|
||
#STN !---Surface tension---
|
||
ST1 !Surface tension model for R-152a 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
|
||
386.411 !Critical temperature used in fit (dummy)
|
||
0.05808 1.2115 !Sigma0 and n
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for R-152a 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. !
|
||
386.411 4516.75 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-7.4821 1.0
|
||
2.1105 1.5
|
||
-2.0761 2.2
|
||
-3.5539 4.8
|
||
0.58004 6.2
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for R-152a 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. !
|
||
386.411 5.571536715 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
19.914 0.56
|
||
-68.624 0.76
|
||
99.821 0.95
|
||
-77.984 1.20
|
||
29.913 1.40
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for R-152a 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. !
|
||
386.411 5.571536715 !Reducing parameters
|
||
6 0 0 0 0 0 !Number of terms in equation
|
||
-3.3621 0.406
|
||
-8.5985 1.42
|
||
-2.6830 3.6
|
||
-24.140 3.9
|
||
-43.159 8.0
|
||
-28.045 9.0
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
||
|
||
|
||
@ETA !Viscosity model specification
|
||
VS1 pure fluid viscosity model of Krauss et al. (1996).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Krauss, R., Weiss, V.C., Edison, T.A., Sengers, J.V., and Stephan, K.,
|
||
? "Transport properties of 1,1-Difluoroethane (R152a),"
|
||
? Int. J. Thermophysics 17:731-757, 1996.
|
||
?
|
||
?The uncertainty in viscosity is 1% in the dilute gas, and 3% elsewhere above
|
||
? 300 K.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
240.0 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
60000.0 !Upper pressure limit [kPa]
|
||
15.90 !Maximum density [mol/L]
|
||
1 !Number of terms associated with dilute-gas function
|
||
CI1 !Pointer to reduced effective collision cross-section model
|
||
0.46115 !Lennard-Jones coefficient sigma [nm]
|
||
354.84 !Lennard-Jones coefficient epsilon/kappa [K]
|
||
1.0 1.0 !Reducing parameters for T, eta
|
||
0.2169614 0.5 !Chapman-Enskog term
|
||
0 !Number of terms for initial density dependence
|
||
0 5 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
|
||
1.0 5.571537 51.12 !Reducing parameters for T, rho (= 368 kg/m^3, note: Krauss uses MW = 66.05), eta (= the pseudo-critical viscosity)
|
||
-0.139987 0.0 0. 0. 0 ! E5*E6; powers of tau, del, del0; power of del in exponential [0 indicated no exponential term present]
|
||
-0.0737927 0.0 1. 0. 0 ! E1
|
||
0.517924 0.0 2. 0. 0 ! E2
|
||
-0.308875 0.0 3. 0. 0 ! E3
|
||
0.108049 0.0 4. 0. 0 ! E4
|
||
-0.408387 0.0 0. 0. 0 ! E5
|
||
-2.91733 0.0 0. 0. 0 ! -E6 term in denominator
|
||
1.0 0.0 1. 0. 0 !Rho/rhoc 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-152a.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Krauss, R., Weiss, V.C., Edison, T.A., Sengers, J.V., and Stephan, K.,
|
||
? "Transport properties of 1,1-Difluoroethane (R152a),"
|
||
? Int. J. Thermophysics 17:731-757, 1996.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
5 !Number of terms
|
||
0.4425728 0 !Coefficient, power of Tstar
|
||
-0.5138403 1
|
||
0.1547566 2
|
||
-0.02821844 3
|
||
0.001578286 4
|
||
|
||
|