616 lines
32 KiB
Plaintext
616 lines
32 KiB
Plaintext
R32 !Short name
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75-10-5 !CAS number
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Difluoromethane !Full name
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CH2F2 !Chemical formula {CH2F2}
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HFC-32 !Synonym
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52.024 !Molar mass [g/mol]
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136.34 !Triple point temperature [K]
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221.499 !Normal boiling point [K]
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351.255 !Critical temperature [K]
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5782. !Critical pressure [kPa]
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8.1500846 !Critical density [mol/L]
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0.2769 !Acentric factor
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1.978 !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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3252 !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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675. !GWP (IPCC 2007) :GWP:
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36000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
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A2L !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/CH2F2/c2-1-3/h1H2 !Standard InChI String :InChi:
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RWRIWBAIICGTTQ-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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7b05bb60 !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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! 11-01-95 MM, Original version.
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! 11-13-97 MM, Enter thermal conductivity shape factor fitted to data.
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! 11-01-99 EWL, Add Span 12 term short equation of state.
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! 05-22-02 MLH, Change transport ref fluid to propane; refit coefficients; added kfit.
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! 07-02-02 MLH, Add dedicated fit for thermal conductivity.
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! 04-19-04 MLH, Update transport reference.
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! 09-01-04 EWL, Add EOS of Astina and Sato.
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! 03-23-05 EWL, Add PRT coefficient.
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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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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for R-32 of Tillner-Roth and Yokozeki (1997).
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:TRUECRITICALPOINT: 351.255 8.1500846 !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: 10.1063/1.556002
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tillner-Roth, R. and Yokozeki, A.,
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? "An International Standard Equation of State for Difluoromethane (R-32)
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? for Temperatures from the Triple Point at 136.34 K to 435 K and Pressures
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? up to 70 MPa,"
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? J. Phys. Chem. Ref. Data, 26(6):1273-1328, 1997.
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?
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?The estimated uncertainties are 0.05% for density, 0.02% for the vapor
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? pressure, and 0.5%-1% for the heat capacity and speed of sound in the
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? liquid phase. In the vapor phase, the uncertainty in the speed of sound
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? is 0.02%
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?
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!```````````````````````````````````````````````````````````````````````````````
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136.340 !Lower temperature limit [K]
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435.0 !Upper temperature limit [K]
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70000.0 !Upper pressure limit [kPa]
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27.4734 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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52.024 !Molar mass [g/mol]
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136.34 !Triple point temperature [K]
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0.0480 !Pressure at triple point [kPa]
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27.4734 !Density at triple point [mol/L]
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221.499 !Normal boiling point temperature [K]
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0.2769 !Acentric factor
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351.255 5782.0 8.1500846 !Tc [K], pc [kPa], rhoc [mol/L]
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351.255 8.1500846 !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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1.046634 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-0.5451165 1.0 2. 0.
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-0.002448595 -0.25 5. 0.
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-0.04877002 -1.0 1. 0.
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0.03520158 2.0 1. 0.
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0.00162275 2.0 3. 0.
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0.2377225e-4 0.75 8. 0.
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0.029149 0.25 4. 0.
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0.003386203 18.0 4. 4.
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-0.004202444 26.0 4. 3.
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0.0004782025 -1.0 8. 1.
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-0.005504323 25.0 3. 4.
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-0.02418396 1.75 5. 1.
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0.4209034 4.0 1. 2.
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-0.4616537 5.0 1. 2.
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-1.200513 1.0 3. 1.
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-2.59155 1.5 1. 1.
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-1.400145 1.0 2. 1.
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0.8263017 0.5 3. 1.
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-32 of Tillner-Roth and Yokozeki (1997).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tillner-Roth, R. and Yokozeki, A., 1997.
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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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1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.004486 0.0
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1.160761 798.0
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2.645151 4185.0
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5.794987 1806.0
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1.129475 11510.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-32 of Tillner-Roth and Yokozeki (1997).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Tillner-Roth, R. and Yokozeki, A., 1997.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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3.004486 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-8.2581043885434511 0.0 !aj, ti for [ai*tau**ti] terms
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6.3531025573429387 1.0 !aj, ti for [ai*tau**ti] terms
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1.160761 798.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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2.645151 4185.0
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5.794987 1806.0
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1.129475 11510.0
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FES !Helmholtz equation of state for R-32 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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136.34 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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27.41 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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52.024 !Molar mass [g/mol]
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136.34 !Triple point temperature [K]
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0.047922 !Pressure at triple point [kPa]
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27.41 !Density at triple point [mol/L]
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221.49 !Normal boiling point temperature [K]
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0.277 !Acentric factor
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351.35 5795.0 8.2077503 !Tc [K], pc [kPa], rhoc [mol/L]
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351.35 8.2077503 !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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0.93080907 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-2.4777491 1.25 1. 0.
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0.41470439 1.5 1. 0.
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0.054859755 0.25 3. 0.
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0.00011475587 0.875 7. 0.
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-0.26225654 2.375 1. 1.
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0.41118822 2.0 2. 1.
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0.0034970526 2.125 5. 1.
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-0.096790506 3.5 1. 2.
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-0.1172821 6.5 1. 2.
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-0.04242838 4.75 4. 2.
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-0.012690083 12.5 2. 3.
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@EOS !---Equation of state---
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BWR !MBWR equation of state for R-32 of Outcalt and McLinden (1995).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Outcalt, S.L. and McLinden, M.O.,
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? "Equations of state for the thermodynamic properties of R32 (difluoromethane)
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? and R125 (pentafluoroethane),"
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? Int. J. Thermophysics, 16:79-89, 1995. doi: 10.1007/BF01438959
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?
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!```````````````````````````````````````````````````````````````````````````````
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136.34 !Lower temperature limit [K]
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500.0 !Upper temperature limit [K]
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60000.0 !Upper pressure limit [kPa]
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27.48 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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52.024 !Molar mass [g/mol]
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136.34 !Triple point temperature [K]
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0.0477 !Pressure at triple point [kPa]
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27.48 !Density at triple point [mol/L]
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221.494 !Normal boiling point temperature [K]
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0.27680 !Acentric factor
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351.35 5795.0 8.2078 !Tc [K], pc [kPa], rhoc [mol/L]
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351.35 8.2078 !Reducing parameters [K, mol/L]
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8.2078 !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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-0.000131275405202 0.899927934911 -28.1400805178
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4360.91182784 -837235.280004 -0.782176408963e-6
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-1.11226606825 539.331431878 288600.276863
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-0.352264609289e-4 0.189661830119 -68.6549003993
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-0.00349007064245 -0.0749983559476 -32.1524283063
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0.00913057921906 -0.000171082181849 0.0503986984347
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-0.000830354867752 -245522.676708 -10785905.6038
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-4295.14279646 80872472.9567 -12.5945229993
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-1057.35009761 -0.0904064745354 -1835.78733048
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-0.000169690612464 0.0639250820631 -0.20492576744e-6
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-0.00016562970087 -0.00932607493424
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for R-32 of Outcalt and McLinden (1995).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Outcalt, S.L. and McLinden, M.O.,
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? "Equations of state for the thermodynamic properties of R32 (difluoromethane)
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? and R125 (pentafluoroethane),"
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? Int. J. Thermophysics, 16:79-89, 1995.doi: 10.1007/BF01438959
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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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36.79959 0.0
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-0.06304821 1.0
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0.0003757936 2.0
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-3.219812e-7 3.0
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@EOS !---Equation of state---
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FE2 !Helmholtz equation of state for R-32 of Astina and Sato (2003).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Astina, I.M. and Sato, H.
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? "A Rational Helmholtz Fundamental Equation of State for Difluoromethane with
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? an Intermolecular Potential Background,"
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? Int. J. Thermophys., 24(4):963-990, 2003. doi: 10.1023/A:1025096716493
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?
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?The estimated uncertainties of calculated properties from the equation of
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? state are 0.07% in density for the liquid phase, 0.1% in pressure for the
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? gaseous phase, 0.35% in pressure for the supercritical region, 0.07% in
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? vapor pressure, 0.2% in saturated-liquid density, 0.7% in saturated-vapor
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? density, 0.01% in speed of sound for the gaseous phase, 0.7% in speed of
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? sound for the liquid phase, and 0.6% in isochoric specific heat for the
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? liquid phase.
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?
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!```````````````````````````````````````````````````````````````````````````````
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136.34 !Lower temperature limit [K]
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450.0 !Upper temperature limit [K]
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72000.0 !Upper pressure limit [kPa]
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27.48 !Maximum density [mol/L]
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CP2 !Pointer to Cp0 model
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52.023 !Molar mass [g/mol]
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136.34 !Triple point temperature [K]
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0.0485 !Pressure at triple point [kPa]
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27.47 !Density at triple point [mol/L]
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221.488 !Normal boiling point temperature [K]
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0.277 !Acentric factor
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351.255 5782.0 8.150241 !Tc [K], pc [kPa], rhoc [mol/L]
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351.255 8.150241 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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18 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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2.118688 0.5 1. 0. !a(i),t(i),d(i),l(i)
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-4.531096 1.125 1. 0.
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1.442456 1.625 1. 0.
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0.2053906 0.875 3. 0.
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-0.1311675 1.5 3. 0.
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0.01022272 1.75 4. 0.
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0.4873982 1.75 1. 1.
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-1.062213 2.75 1. 1.
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-0.004542051 0.25 5. 1.
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-6.933347e-4 3.75 5. 1.
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-0.03510307 1.0 6. 1.
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-0.05606161 6.5 1. 2.
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0.08849625 2.5 2. 2.
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-0.01850758 7.5 5. 2.
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0.007878071 7.5 6. 2.
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-0.03384115 11.0 2. 3.
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1.641979e-4 16.0 2. 3.
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-0.001459172 13.0 8. 3.
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@AUX !---Auxiliary function for Cp0
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CP2 !Ideal gas heat capacity function for R-32 of Astina and Sato (2003).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Astina, I.M. and Sato, H.
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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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351.255 8.314472 !Reducing parameters for T, Cp0
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1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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3.99966 0.0
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3.12115 1601.64447
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0.9994221 760.3926
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2.412721 4336.89982
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3.055435 2064.64246
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@AUX !---Auxiliary function for PH0
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PH2 !Ideal gas Helmholtz form for R-32 of Astina and Sato (2003).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Astina, I.M. and Sato, H.
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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 4 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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2.99966 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-8.253834 0.0 !aj, ti for [ai*tau**ti] terms
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6.351918 1.0
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3.12115 -4.559777 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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0.9994221 -2.164788
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2.412721 -12.34687
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3.055435 -5.877902
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@EOS !---Cubic equation of state---
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PRT !Translated Peng-Robinson equation for R-32.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Volume translation of Peng Robinson EOS.
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?
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!```````````````````````````````````````````````````````````````````````````````
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136.340 !Lower temperature limit [K]
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435.0 !Upper temperature limit [K]
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70000.0 !Upper pressure limit [kPa]
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27.4734 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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52.024 !Molar mass [g/mol]
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0.2769 !Acentric factor
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351.255 !Critical temperature [K]
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5782.0 !Critical pressure [kPa]
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8.1500846 !Critical density [mol/L]
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8.314472 !Gas constant [J/mol-K]
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1 !Number of parameters
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0.00585
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================================================================================
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#TCX !---Thermal conductivity---
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TC1 !Pure fluid thermal conductivity model for R-32 of Perkins and Huber (2005) (unpublished)
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:DOI: 10.1021/je010001m
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Unpublished; however the fit uses the functional form found in:
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? Marsh, K., Perkins, R., and Ramires, M.L.V.,
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? "Measurement and Correlation of the Thermal Conductivity of Propane
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? from 86 to 600 K at Pressures to 70 MPa,"
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? J. Chem. Eng. Data, 47(4):932-940, 2002.
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?
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?The estimated uncertainty of the correlation is 5%, except for the dilute gas and points
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? approaching critical where the uncertainty rises to 10%.
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?
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?THERMAL CONDUCTIVITY
|
||
? Comparisons with specific data sets are given below.
|
||
? Le Neindre, B. and Garrabos, Y., "Measurement of Thermal Conductivity of HFC-32 (Difluoromethane) in the Temperature Range from 300 to 465 K at Pressures up to 50 MPa," Int. J. Thermophysics 22(3):701-722, 2001.
|
||
? Gao, X., Iojima, H., Nagasaka, Y., and Nagashima, A., "Thermal Conductivity of HFC-32 in the Liquid Phase," Paper C1c4, Proceedings 4th Asian Thermophysical Properties Conference, Tokyo, 1995.
|
||
? Ro, S.T., Kim, J.Y., and Kim, D.S., "Thermal Conductivity of R32 and its Mixture with R134a," Int. J. Thermophysics 16(5):1193-1201, 1995. doi: 10.1007/BF02081287
|
||
? Tanaka, Y., Matsuo, S., and Taya, S., "Gaseous Thermal Conductivity of Difluoromethane (HFC-32), Pentafluoroethane (HFC), and Their Mixtures," Int. J. Thermophys., 16(1):121-131, 1995. doi: 10.1007/BF01438963
|
||
? Papadaki, M. and Wakeham, W.A., "Thermal Conductivity of R32 and R125 in the Liquid Phase at the Saturation Vapor Pressure," Int. J. Thermophys., 14(6):1215-1220, 1993. doi: 10.1007/BF02431285
|
||
? Assael, M.J. and Karagiannidis, L., "Measurements of the Thermal Conductivity of Liquid R32, R124, R125 and R141b," Int. J. Thermophys., 16(4):851-865, 1995. doi: 10.1007/BF02093468
|
||
? Gross, U. and Song, Y.W., "Thermal Conductivities of New Refrigerants R125 and R32 Measured by the Transient Hot-Wire Method," Int. J. Thermophys., 17(3):607-619, 1996. doi: 10.1007/BF01441507
|
||
? Yata, J., Hori, M., Kobayashi, K., and Minimiyama, T., "Thermal Conductivity of Alternative Refrigerants in the Liquid Phase," Int. J. Thermophys., 17(3):561-571, 1996. doi: 10.1007/BF01441503
|
||
? Perkins, R.A., 2002, unpublished data. 325 Broadway, Boulder, CO 80305, perkins@boulder.nist.gov
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Le Neindre: 2.13%; Gao: 1.66%; Ro: 2.26%; Tanaka: 2.85%; Papadaki: 3.12%;
|
||
? Assael: 2.90%; Gross: 3.85%; Yata: 2.86%; Perkins: 1.69%.
|
||
? Overall: 1.93%.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
136.340 !Lower temperature limit [K]
|
||
435.0 !Upper temperature limit [K]
|
||
70000.0 !Upper pressure limit [kPa]
|
||
27.4734 !Maximum density [mol/L]
|
||
3 0 !# terms for dilute gas function: numerator, denominator
|
||
351.255 1.0 !Reducing parameters for T, tcx
|
||
0.0106548 0. !Coefficient, power in T
|
||
-0.0194174 1.
|
||
0.0254295 2.
|
||
10 0 !# terms for background gas function: numerator, denominator
|
||
351.255 8.1500846 1. !Reducing parameters for T, rho, tcx
|
||
0.0221878 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
|
||
-0.0215336 1. 1. 0.
|
||
0.283523 0. 2. 0.
|
||
-0.169164 1. 2. 0.
|
||
-0.297237 0. 3. 0.
|
||
0.191614 1. 3. 0.
|
||
0.105727 0. 4. 0.
|
||
-0.0665397 1. 4. 0.
|
||
-0.0123172 0. 5. 0.
|
||
0.00766378 1. 5. 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-32 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: CO2-terms, spare, spare, spare
|
||
1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
|
||
0.63 !Nu (universal exponent)
|
||
1.239 !Gamma (universal exponent)
|
||
1.03 !R0 (universal amplitude)
|
||
0.063 !Z (universal exponent--not used for t.c., only viscosity)
|
||
1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
|
||
0.194e-9 !Xi0 (amplitude) [m]
|
||
0.0496 !Gam0 (amplitude) [-]
|
||
5.582925e-10 !Qd_inverse (modified effective cutoff parameter) [m]; fitted to data
|
||
526.8825 !Tref (reference temperature)=1.5*Tc [K]
|
||
|
||
|
||
|
||
|
||
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
||
|
||
@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (Propane reference); fitted to data for R-32.
|
||
:DOI: 10.1021/ie0300880
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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:
|
||
? Le Neindre, B. and Garrabos, Y. (2001) "Measurement of Thermal Conductivity of HFC-32 (Difluoromethane) in the temperature range from 300 to 465 K at pressures up to 50 MPa", Int. J. Thermophysics 22(3): 701-722. doi: 10.1023/A:1010766730306
|
||
? Gao, X., Iojima, H., Nagasaka, Y. and Nagashima, A. (1995). "Thermal conductivity of HFC-32 in the liquid phase", Paper C1c4, Proceedings 4th Asian Thermophysical Properties Conference, Tokyo.
|
||
? Perkins, R.A.,(2002) personal communication. 325 Broadway, Boulder, CO 80305, perkins@boulder.nist.gov
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? LeNeindre: 2.75%; Gao: 3.92%; Perkins: 4.81% Overall: 4.23%
|
||
?
|
||
?VISCOSITY
|
||
? The ECS parameters for viscosity were based in part on the data of:
|
||
? Laesecke, A., Luddecke, T.O.D., Hafer, R.F. and Morris, D.J. (1999). Viscosity measurements of ammonia, R32, and R134a. Vapor buoyancy and radial acceleration in capillary viscometers, Int. J. Thermophys. 20(2):401-434. doi: 10.1023/A:1022644718603
|
||
? Bivens, D.B., Yokozeki, A., Geller, V.Z., and Paulaitis, M.E. (1993). Transport properties and heat transfer of alternatives for R502 and R22. ASHRAE/NIST Refrigerants Conference, August 19-20, Gaithersburg, MD, 73-84.
|
||
? Shibasaki-Kitakawa, N., Takahashi, M., Yokoyama, C., and Takahashi, S., (1995). Gas viscosity of difluoromethane from 298.15 K to 423.15 K and up to 10 MPa. J. Chem. Eng. Data, 40:900-902. doi: 10.1021/je00020a036
|
||
? Oliveira, C. M. B. P., and Wakeham, W. A. (1993). "The viscosity of R32 and R125 at saturation", Int. J. Thermophys.14: 1131-43.doi: 10.1007/BF02431279
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Laesecke: 0.66; Bivens: 4.43%; Takahashi: 2.65%; Oliveira: 2.80%; Overall: 2.17%
|
||
?
|
||
?The Lennard-Jones parameters were based on the low-density viscosity data of Takahashi.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
136.34 !Lower temperature limit [K]
|
||
435.0 !Upper temperature limit [K]
|
||
70000.0 !Upper pressure limit [kPa]
|
||
27.4734 !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)
|
||
0.4098 !Lennard-Jones coefficient sigma [nm] for ECS method
|
||
289.65 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
|
||
2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
|
||
4.36654e-4 0. 0. 0. !Coefficient, power of T, spare1, spare2
|
||
1.78134e-6 1. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
|
||
0.795399 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0542658 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
|
||
1.29424 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
-0.0924549 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-32 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
|
||
351.255 !Critical temperature used in fit (dummy)
|
||
0.07147 1.246 !Sigma0 and n
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for R-32 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. !
|
||
351.255 5782.0 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-7.4883 1.0
|
||
1.9697 1.5
|
||
-1.7496 2.2
|
||
-4.0224 4.8
|
||
1.5209 6.2
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for R-32 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. !
|
||
351.255 8.1500846 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
1.2584 0.27
|
||
4.6410 0.8
|
||
-5.4870 1.1
|
||
3.3115 1.5
|
||
-0.61370 1.8
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for R-32 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. !
|
||
351.255 8.1500846 !Reducing parameters
|
||
6 0 0 0 0 0 !Number of terms in equation
|
||
-2.2002 0.336
|
||
-5.9720 0.98
|
||
-14.571 2.7
|
||
-42.598 5.7
|
||
4.2686 6.5
|
||
-73.373 11.0
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
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