348 lines
16 KiB
Plaintext
348 lines
16 KiB
Plaintext
R142b !Short name
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75-68-3 !CAS number
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1-Chloro-1,1-difluoroethane !Full name
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CClF2CH3 !Chemical formula {C2H3ClF2}
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HCFC-142b !Synonym
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100.49503 !Molar mass [g/mol]
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142.72 !Triple point temperature [K]
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264.03 !Normal boiling point [K]
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410.26 !Critical temperature [K]
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4055.0 !Critical pressure [kPa]
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4.438 !Critical density [mol/L]
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0.2321 !Acentric factor
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2.14 !Dipole moment [Debye]; value from REFPROP v5.0
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IIR !Default reference state
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10.0 !Version number
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2517 !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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2310. !GWP (IPCC 2007) :GWP:
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0.06 !ODP (WMO 2010) :ODP:
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20000. !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/C2H3ClF2/c1-2(3,4)5/h1H3 !Standard InChI String :InChi:
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BHNZEZWIUMJCGF-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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f2a8b2e0 !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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! 05-23-96 MM, Original version.
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! 04-12-01 EWL, Add Lemmon and Span short EOS.
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! 05-08-02 MLH, Add LJ parameters, k, eta fits.
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! 03-13-03 EWL, Replace cp0 equation.
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! 01-27-04 EWL, Add final coefficients to EOS.
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! 04-19-04 MLH, Update transport references.
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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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! 01-05-16 MLH, Change TK6 to TK3.
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for R-142b of Lemmon and Span (2006).
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:TRUECRITICALPOINT: 410.26 4.438 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
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:DOI: 10.1021/je050186n
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R.,
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? "Short Fundamental Equations of State for 20 Industrial Fluids,"
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? J. Chem. Eng. Data, 51(3):785-850, 2006. doi: 10.1021/je050186n
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?
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?The uncertainties in density are 0.3% in the liquid phase below 370 K, 1%
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? at higher temperatures in the liquid and supercritical regions, and 0.5% in
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? the vapor phase. Uncertainties for other properties are 0.5% for vapor
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? pressure, 2% for heat capacities and liquid sound speeds, and 0.2% for
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? vapor sound speeds.
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?
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!```````````````````````````````````````````````````````````````````````````````
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142.72 !Lower temperature limit [K]
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470.0 !Upper temperature limit [K]
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60000.0 !Upper pressure limit [kPa]
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14.44 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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100.49503 !Molar mass [g/mol]
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142.72 !Triple point temperature [K]
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0.003632 !Pressure at triple point [kPa]
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14.44 !Density at triple point [mol/L]
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264.03 !Normal boiling point temperature [K]
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0.2321 !Acentric factor
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410.26 4055.0 4.438 !Tc [K], pc [kPa], rhoc [mol/L]
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410.26 4.438 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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12 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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1.0038 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-2.7662 1.25 1. 0.
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0.42921 1.5 1. 0.
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0.081363 0.25 3. 0.
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0.00024174 0.875 7. 0.
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0.48246 2.375 1. 1.
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0.75542 2.0 2. 1.
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-0.007430 2.125 5. 1.
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-0.41460 3.5 1. 2.
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-0.016558 6.5 1. 2.
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-0.10644 4.75 4. 2.
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-0.021704 12.5 2. 3.
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-142b of Lemmon and Span (2006).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R., 2006.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314472 !Reducing parameters for T, Cp0
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1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.0 0.0
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5.0385 473.0
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6.8356 1256.0
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4.0591 2497.0
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2.8136 6840.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-142b of Lemmon and Span (2006).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R., 2006.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-12.6016704500950851 0.0 !aj, ti for [ai*tau**ti] terms
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8.316026972375175 1.0 !aj, ti for [ai*tau**ti] terms
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5.0385 473.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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6.8356 1256.0
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4.0591 2497.0
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2.8136 6840.0
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#AUX !---Auxiliary function for PH0
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PH0 !Ideal gas Helmholtz form for R-142b.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R., 2006.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1 2 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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3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-12.6016527149 0.0 !aj, ti for [ai*tau**ti] terms
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8.3160183265 1.0
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5.0385 -1.1529274119 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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6.8356 -3.0614732121
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4.0591 -6.0863842441
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2.8136 -16.6723541169
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++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
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#TRN !---ECS Transport---
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ECS !Extended Corresponding States model (Propane reference); fitted to data for R-142b.
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:DOI: 10.1021/ie0300880
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Unpublished; uses method described in the following reference:
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?Huber, M.L., Laesecke, A., and Perkins, R.A.,
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? "Model for the Viscosity and Thermal Conductivity of Refrigerants, Including
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? a New Correlation for the Viscosity of R134a,"
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? Ind. Eng. Chem. Res., 42(13):3163-3178, 2003. doi: 10.1021/ie0300880
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?
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?THERMAL CONDUCTIVITY
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? The ECS parameters for thermal conductivity were based in part on the data of:
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? Perkins, R.A., Laesecke, A., and Nieto de Castro, C.A., "Polarized Transient Hot Wire Thermal Conductivity Measurements," Fluid Phase Equilib., 80:275-286, 1992. doi: 10.1016/0378-3812(92)87074-W
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? Sousa, A.T., Fialho, P.S., Nieto de Castro, C.A., Tufeu, R., and LeNeindre, B., "The Thermal Conductivity of 1-Chloro-1,1-Difluoroethane," Int. J. Thermophys., 13(3):383, 1992. doi: 10.1007/BF00503878
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? Tanaka, Y., Nakata, M., and Makita, T., "Thermal Conductivity of Gaseous HFC-134a, HFC-143a, HCFC-141b, and HCFC-142b," Int. J. Thermophys., 12:949-963, 1991.
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? Yata, J., Hori, M., Kurahashi, T., and Minamiyama, T., "Thermal Conductivity of Alternative Fluorocarbons in Liquid Phase," Fluid Phase Equilib., 80:287-296, 1992.
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? Kim, S.H., Kim, D.S., Kim, M.S., and Ro, S.T., "The Thermal Conductivity of R22, R142b, R152a, and Their Mixtures in the Liquid State," Int. J. Thermophys., 14:937-50, 1993. doi: 10.1007/BF00502116
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? Average absolute deviations of the fit from the experimental data are:
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? Perkins: 0.93%; Sousa: 2.53%; Tanaka: 2.77%; Yata: 1.72%; Kim: 0.76%.
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? Overall: 1.99%.
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?
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?VISCOSITY
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? The ECS parameters for viscosity were based in part on the data of:
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? Kumagai, A. and Yokoyama, C., "Revised Viscosities of Saturated Liquid Halocarbon Refrigerants from 273 to 353 K," Int. J. Thermophys., 21(4):909-912, 2000.
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? Arnemann, M. and Kruse, H., "Liquid Viscosities of the Non-Azeotropic Binary Refrigerant Mixtures R22/R114, R22/R152a, R22/R142b," Actes Congr. Int. Froid, 18(2):379-383, 1991.
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? Average absolute deviations of the fit from the experimental data are:
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? Kumagai: 2.26%; Arnemann: 2.27%.
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? Overall: 2.26%.
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?
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?The Lennard-Jones parameters were taken from Nabizadeh, H. and Mayinger, F., "Viscosity of Gaseous R123, R134a and R142b," High Temp.-High Press., 24:221, 1992.
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?
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!```````````````````````````````````````````````````````````````````````````````
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142.72 !Lower temperature limit [K]
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470.0 !Upper temperature limit [K]
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60000.0 !Upper pressure limit [kPa]
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14.44 !Maximum density [mol/L]
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FEQ PROPANE.FLD
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VS1 !Model for reference fluid viscosity
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TC1 !Model for reference fluid thermal conductivity
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NUL !Large molecule identifier
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1 !Lennard-Jones flag (0 or 1) (0 => use estimates)
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0.5362 !Lennard-Jones coefficient sigma [nm] for ECS method
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278.20 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
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2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
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0.000940725 0. 0. 0. !Coefficient, power of T, spare1, spare2
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0.988196e-6 1. 0. 0. !Coefficient, power of T, spare1, spare2
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2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
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0.971602 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
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0.019181 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
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2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
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1.07494 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
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-0.0177916 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
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TK3 !Pointer to critical enhancement auxiliary function
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#AUX !---Auxiliary function for the thermal conductivity critical enhancement
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TK3 !Simplified thermal conductivity critical enhancement for R-142b of Olchowy and Sengers (1989).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Olchowy, G.A. and Sengers, J.V.,
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? "A Simplified Representation for the Thermal Conductivity of Fluids in the Critical Region,"
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? Int. J. Thermophys., 10:417-426, 1989. doi: 10.1007/BF01133538
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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9 0 0 0 !# terms: CO2-terms, spare, spare, spare
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1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
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0.63 !Nu (universal exponent)
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1.239 !Gamma (universal exponent)
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1.03 !R0 (universal amplitude)
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0.063 !Z (universal exponent--not used for t.c., only viscosity)
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1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
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0.194e-9 !Xi0 (amplitude) [m]
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0.0496 !Gam0 (amplitude) [-]
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0.615654e-9 !Qd_inverse (modified effective cutoff parameter) [m]; fitted to data
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615.39 !Tref (reference temperature)=1.5*Tc [K]
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~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
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#STN !---Surface tension---
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ST1 !Surface tension model for R-142b of Mulero et al. (2012).
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:DOI: 10.1063/1.4768782
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Mulero, A., Cachadiña, I., and Parra, M.I.,
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? "Recommended Correlations for the Surface Tension of Common Fluids,"
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? J. Phys. Chem. Ref. Data, 41(4), 043105, 2012. doi: 10.1063/1.4768782
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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 !Number of terms in surface tension model
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410.26 !Critical temperature used in fit (dummy)
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0.05685 1.237 !Sigma0 and n
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#PS !---Vapor pressure---
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PS5 !Vapor pressure equation for R-142b of Cullimore (2010).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Cullimore, I.D., 2010.
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?
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?Functional Form: P=Pc*EXP[SUM(Ni*Theta^ti)*Tc/T] where Theta=1-T/Tc, Tc and Pc
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? are the reducing parameters below, which are followed by rows containing Ni and ti.
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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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410.26 4055.0 !Reducing parameters
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5 0 0 0 0 0 !Number of terms in equation
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-7.3074 1.0
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2.3186 1.5
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-2.3278 2.2
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-3.2761 4.8
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0.42103 6.2
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#DL !---Saturated liquid density---
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DL1 !Saturated liquid density equation for R-142b of Cullimore (2010).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Cullimore, I.D., 2010.
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?
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?Functional Form: D=Dc*[1+SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are
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? the reducing parameters below, which are followed by rows containing Ni and ti.
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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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410.26 4.438 !Reducing parameters
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5 0 0 0 0 0 !Number of terms in equation
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17.162 0.53
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-47.495 0.71
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57.171 0.9
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-25.404 1.1
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1.5855 2.3
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#DV !---Saturated vapor density---
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DV3 !Saturated vapor density equation for R-142b of Cullimore (2010).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Cullimore, I.D., 2010.
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?
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?Functional Form: D=Dc*EXP[SUM(Ni*Theta^ti)] where Theta=1-T/Tc, Tc and Dc are
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? the reducing parameters below, which are followed by rows containing Ni and ti.
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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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410.26 4.438 !Reducing parameters
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6 0 0 0 0 0 !Number of terms in equation
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-3.1460 0.408
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-6.5221 1.28
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-18.006 3.2
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-46.694 6.6
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-2.6087 7.0
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-110.20 14.0
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@END
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