371 lines
18 KiB
Plaintext
371 lines
18 KiB
Plaintext
R12 !Short name
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75-71-8 !CAS number
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Dichlorodifluoromethane !Full name
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CCl2F2 !Chemical formula {CCl2F2}
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CFC-12 !Synonym
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120.913 !Molar mass [g/mol]
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116.099 !Triple point temperature [K]
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243.398 !Normal boiling point [K]
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385.12 !Critical temperature [K]
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4136.1 !Critical pressure [kPa]
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4.672781 !Critical density [mol/L] (565 kg/m**3)
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0.17948 !Acentric factor
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0.510 !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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1028 !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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10900. !GWP (IPCC 2007) :GWP:
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0.82 !ODP (WMO 2010) :ODP:
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18000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
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A1 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/CCl2F2/c2-1(3,4)5 !Standard InChI String :InChi:
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PXBRQCKWGAHEHS-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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98829b70 !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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! 02-29-96 MM, Original version.
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! 11-01-99 EWL, Add Span 12 term short equation of state.
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! 09-04-03 EWL, Modify cp0 coeffs by 8.31451/8.314472 to use same R as EOS but to leave calculated values unchanged.
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! 11-13-06 MLH, Add LJ parameters.
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! 08-17-10 IDC, Add ancillary equations.
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! 10-15-10 MLH, Revise lower temp limits on vis and therm. cond.
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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-12 of Marx et al. (1992).
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:TRUECRITICALPOINT: 385.12 4.672781 !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:
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Marx, V., Pruss, A., and Wagner, W.,
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? "Neue Zustandsgleichungen fuer R 12, R 22, R 11 und R 113. Beschreibung
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? des thermodynamishchen Zustandsverhaltens bei Temperaturen bis 525 K und
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? Druecken bis 200 MPa,"
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? Duesseldorf, VDI Verlag, Series 19 (Waermetechnik/Kaeltetechnik), No. 57, 1992.
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?
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?The uncertainties in density are 0.2% below the critical point temperature and
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? increases to 1% in and above the critical region. The uncertainties for vapor
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? pressures are 0.2% above 200 K and greater than 1% below 200 K. The
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? uncertainties in heat capacities and sound speeds are 1% each.
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?
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!```````````````````````````````````````````````````````````````````````````````
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116.099 !Lower temperature limit [K]
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525.0 !Upper temperature limit [K]
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200000.0 !Upper pressure limit [kPa]
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15.13 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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120.913 !Molar mass [g/mol]
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116.099 !Triple point temperature [K]
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0.0002425 !Pressure at triple point [kPa]
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15.1253 !Density at triple point [mol/L]
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243.398 !Normal boiling point temperature [K]
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0.17948 !Acentric factor
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385.12 4136.1 4.672781 !Tc [K], pc [kPa], rhoc [mol/L]
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385.12 4.672781 !Reducing parameters [K, mol/L]
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8.314471 !Gas constant [J/mol-K]
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22 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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2.075343402 0.5 1. 0. !a(i),t(i),d(i),l(i)
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-2.962525996 1.0 1. 0.
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0.01001589616 2.0 1. 0.
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0.01781347612 2.5 2. 0.
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0.02556929157 -0.5 4. 0.
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0.002352142637 0.0 6. 0.
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-0.8495553314e-4 0.0 8. 0.
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-0.01535945599 -0.5 1. 1.
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-0.2108816776 1.5 1. 1.
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-0.01654228806 2.5 5. 1.
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-0.0118131613 -0.5 7. 1.
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-0.416029583e-4 0.0 12. 1.
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0.2784861664e-4 0.5 12. 1.
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0.1618686433e-5 -0.5 14. 1.
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-0.1064614686 4.0 1. 2.
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0.0009369665207 4.0 9. 2.
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0.02590095447 2.0 1. 3.
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-0.04347025025 4.0 1. 3.
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0.1012308449 12.0 3. 3.
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-0.1100003438 14.0 3. 3.
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-0.003361012009 0.0 5. 3.
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0.0003789190008 14.0 9. 4.
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-12 of Marx et al. (1992).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Marx, V., Pruss, A., and Wagner, W., 1992.
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?
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?Note: Marx et al. give a Helmholtz form for the ideal gas term; it
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? has been converted to a Cp0 form, by the transform:
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?
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?Cp0/R = (1 + a_3) + SUM{a_i*U_i*exp(U_i)/[1 - exp(U_i)]**2}
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? where U_i = omega_i*T_n/T, T_n = Tcrit,
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? and the a_i and omega_i are the original coefficients given by Marx.
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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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4.003638529 0.0 ! 1 + a_3; power in T
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3.160638395 1433.4342 ! omega_4 * T_n (T_n = 385.12 K)
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0.3712598774 2430.0498 ! omega_5 * T_n
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3.562277099 685.65952 ! omega_6 * T_n
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2.121533311 412.41579 ! omega_7 * T_n
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-12 of Marx et al. (1992).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Marx, V., Pruss, A., and Wagner, W., 1992.
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?
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?Note: Marx et al. give a Helmholtz form for the ideal gas term; it
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? has been converted to a Cp0 form, by the transform:
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?
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?Cp0/R = (1 + a_3) + SUM{a_i*U_i*exp(U_i)/[1 - exp(U_i)]**2}
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? where U_i = omega_i*T_n/T, T_n = Tcrit,
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? and the a_i and omega_i are the original coefficients given by Marx.
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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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3.003638529 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-14.7178947415560639 0.0 !aj, ti for [ai*tau**ti] terms
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9.4030125798124899 1.0 !aj, ti for [ai*tau**ti] terms
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3.160638395 1433.4342 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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0.3712598774 2430.0498
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3.562277099 685.65952
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2.121533311 412.41579
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FES !Helmholtz equation of state for R-12 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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173.0 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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13.9 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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120.914 !Molar mass [g/mol]
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173.0 !Triple point temperature [K]
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1.1633 !Pressure at triple point [kPa]
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13.892 !Density at triple point [mol/L]
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243.41 !Normal boiling point temperature [K]
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0.179 !Acentric factor
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385.12 4136.1 4.6727426 !Tc [K], pc [kPa], rhoc [mol/L]
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385.12 4.6727426 !Reducing parameters [K, mol/L]
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8.31451 !Gas constant [J/mol-K]
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12 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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1.0557228 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-3.3312001 1.25 1. 0.
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1.0197244 1.5 1. 0.
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0.084155115 0.25 3. 0.
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0.00028520742 0.875 7. 0.
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0.39625057 2.375 1. 1.
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0.63995721 2.0 2. 1.
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-0.021423411 2.125 5. 1.
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-0.36249173 3.5 1. 2.
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0.001934199 6.5 1. 2.
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-0.092993833 4.75 4. 2.
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-0.024876461 12.5 2. 3.
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++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
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#TRN !---ECS Transport---
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ECS !Extended Corresponding States model (R134a reference); fitted to data for R-12.
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:DOI: 10.1016/S0140-7007(96)00073-4
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?
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?```````````````````````````````````````````````````````````````````````````````
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?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. Refrig., 20(3):208-217, 1997. doi: 10.1016/S0140-7007(96)00073-4.
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?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. Refrig., 23(1):43-63, 2000. doi: 10.1016/S0140-7007(99)00024-9
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?
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?THERMAL CONDUCTIVITY
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? The ECS parameters for thermal conductivity were based on the data of:
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? Donaldson, A.B., "On the Estimation of Thermal Conductivity of Organic Vapors," Ind. Eng. Chem., 14:325-328, 1975. doi: 10.1021/i160056a008
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? Geller, V.Z., Artamonov, S.D., Zaporozhan, G.V., and Peredrii, V.G., "Thermal Conductivity of Freon-12," J. Eng. Phys., 27:842-846, 1974. doi: 10.1007/BF00827625
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? Keyes, F.G., "Thermal Conductivity of Gases," Trans. ASME, 76:809-816, 1954.
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? Makita, T., Tanaka, Y., Morimoto, Y., Noguchi, M., and Kubota, H., "Thermal Conductivity of Gaseous Fluorocarbon Refrigerants R12, R13, R22, and R23 under Pressure," Int. J. Thermophys., 2:249-268, 1981. doi: 10.1007/BF00504188
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? Shankland, I.R., "Transport Properties of CFC Alternatives," paper presented at AIChE Spring National Meeting, Orlando, Florida, 1990.
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? Sherratt, G.G. and Griffiths, E., "A Hot Wire Method for the Thermal Conductivity of Gases," Phil. Mag., 27:68-75, 1939. doi: 10.1080/14786443908562205
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? Venart, J.E.S. and Mani, N., "The Thermal Conductivity of R12," Trans. Canadian Soc. Mech. Engrs., 3:1-9, 1975.
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? Yata, J., Minamiyama, T., and Tanaka, S., "Measurement of Thermal Conductivity of Liquid Fluorocarbons," Int. J. Thermophys., 5:209-218, 1984.
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? Average absolute deviations of the fit from the experimental data are:
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? Donaldson: 2.18%; Geller: 1.86%; Keyes: 1.36%; Makita: 0.73%;
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? Shankland: 1.70%; Sherratt: 1.55%; Venart: 1.29%; Yata: 2.32%.
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? Overall: 1.36%.
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?
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?VISCOSITY
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? The ECS parameters for viscosity were based on the data of:
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? Assael, M.J., Polimatidou, S.K., Vogel, E., and Wakeham, W.A., "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(4):575-589, 1994.
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? Kumagai, A. and Takahashi, S., "Viscosity of Saturated Liquid Fluorocarbon Refrigerants from 273 to 353 K," Int. J. Thermophys., 12(1):105-117, 1991.
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? Average absolute deviations of the fit from the experimental data are:
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? Assael: 0.64%; Kumagai: 2.45%. Overall: 1.00%.
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?
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?The Lennard-Jones parameters were estimated from corresponding states with R134a and 298 K as a reference.
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?
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!```````````````````````````````````````````````````````````````````````````````
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116.0 !Lower temperature limit [K]
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525.0 !Upper temperature limit [K]
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200000.0 !Upper pressure limit [kPa]
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15.13 !Maximum density [mol/L]
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FEQ R134A.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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0.5186 !Lennard-Jones coefficient sigma [nm] for ECS method
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297.24 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
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1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
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0.001344 0. 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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1.0524907 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
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-0.0252897 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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0.99103 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
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0.0029509 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
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NUL !Pointer to critical enhancement auxiliary function
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~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
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#STN !---Surface tension---
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ST1 !Surface tension model for R-12 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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2 !Number of terms in surface tension model
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385.12 !Critical temperature used in fit (dummy)
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-0.000124 0.4318 !Sigma0 and n
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0.05662 1.263
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#PS !---Vapor pressure---
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PS5 !Vapor pressure equation for R-12 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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385.12 4136.1 !Reducing parameters
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5 0 0 0 0 0 !Number of terms in equation
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-7.0834 1.0
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4.3562 1.5
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-3.5249 1.67
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-2.8872 4.14
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-0.89926 10.0
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#DL !---Saturated liquid density---
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DL1 !Saturated liquid density equation for R-12 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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385.12 4.672781 !Reducing parameters
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5 0 0 0 0 0 !Number of terms in equation
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32.983 0.57
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-109.97 0.72
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170.67 0.89
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-133.42 1.07
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42.525 1.25
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#DV !---Saturated vapor density---
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DV3 !Saturated vapor density equation for R-12 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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385.12 4.672781 !Reducing parameters
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6 0 0 0 0 0 !Number of terms in equation
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-3.1530 0.418
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-6.4734 1.32
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-17.346 3.3
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-15.918 6.6
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-32.492 7.0
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-120.72 15.0
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@END
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