850 lines
45 KiB
Plaintext
850 lines
45 KiB
Plaintext
R125 !Short name
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354-33-6 !CAS number
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Pentafluoroethane !Full name
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CHF2CF3 !Chemical formula {C2HF5}
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HFC-125 !Synonym
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120.0214 !Molar mass [g/mol]
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172.52 !Triple point temperature [K]
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225.06 !Normal boiling point [K]
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339.173 !Critical temperature [K]
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3617.7 !Critical pressure [kPa]
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4.779 !Critical density [mol/L]
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0.3052 !Acentric factor
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1.563 !Dipole moment [Debye]; Meyer & Morrison (1991) J. Phys. Chem. 95:3860-3866.
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IIR !Default reference state
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10.0 !Version number
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3220 !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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3500. !GWP (IPCC 2007) :GWP:
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75000. !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/C2HF5/c3-1(4)2(5,6)7/h1H !Standard InChI String :InChi:
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GTLACDSXYULKMZ-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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25c5a3a0 !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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! 7-29-98 EWL, Add equation of state of Sunaga.
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! 10-28-98 EWL, Add equation of state of Piao.
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! 11-01-99 EWL, Add Span 12 term short equation of state.
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! 02-11-02 EWL, Add equation of state of Lemmon and Jacobsen.
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! 05-08-02 MLH, Change LJ parameters to Le Neindre, refit visc and k w/ propane ref., added kfit.
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! 06-17-02 EWL, Add ancillary equations.
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! 07-05-02 MLH, Update coefficients on Tc1 model.
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! 04-19-04 MLH, Update transport references.
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! 09-01-04 EWL, Add EOS of Astina and Sato.
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! 09-15-04 MLH, Add VS1, update coefficients on TC1.
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! 11-30-04 MLH, Add tPr coef.
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! 09-30-05 MLH, Update viscosity coefficients.
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! 12-02-06 MLH, Update LJ coef in ECS model, references for transport.
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! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
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! 06-27-17 MLH, Remove TK6 model for the ECS section and make it TK3.
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for R-125 of Lemmon and Jacobsen (2005).
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:TRUECRITICALPOINT: 339.173 4.779 !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: 10.1063/1.1797813
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Jacobsen, R.T,
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? "A New Functional Form and New Fitting Techniques for Equations of State
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? with Application to Pentafluoroethane (HFC-125),"
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? J. Phys. Chem. Ref. Data, 34(1):69-108, 2005. doi: 10.1063/1.1797813
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?
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?The uncertainty in density is 0.1% at temperatures from the triple point
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? to 400 K at pressures up to 60 MPa, except in the critical region, where
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? an uncertainty of 0.2% in pressure is generally attained. In the limited
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? region between 340 and 400 K and at pressures from 4 to 10 MPa, as well as
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? for all states above 400 K, the uncertainty in density increases to 0.5%.
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? At temperatures below 330 K and pressures below 30 MPa, the uncertainty in
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? density in the liquid phase may be as low as 0.04%. In the vapor and
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? supercritical region, speed of sound data are represented within 0.05% at
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? pressures below 1 MPa. The estimated uncertainty for heat capacities is
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? 0.5% and the estimated uncertainty for the speed of sound in the liquid
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? phase is 0.5% for T>250 K. The estimated uncertainties of vapor pressures
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? and saturated liquid densities calculated with the Maxwell criterion are
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? 0.1% for each property, and the estimated uncertainty for saturated vapor
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? densities is 0.2%. The uncertainty in density increases as the critical
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? point is approached, while the accompanying uncertainty in calculated
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? pressures is 0.2%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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172.52 !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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14.09 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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120.0214 !Molar mass [g/mol]
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172.52 !Triple point temperature [K]
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2.914 !Pressure at triple point [kPa]
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14.086 !Density at triple point [mol/L]
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225.06 !Normal boiling point temperature [K]
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0.3052 !Acentric factor
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339.173 3617.7 4.779 !Tc [K], pc [kPa], rhoc [mol/L]
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339.173 4.779 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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15 4 3 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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0.01451899 1.0 4. 0. !a(i),t(i),d(i),l(i)
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5.28076 0.669 1. 0.
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-8.67658 1.05 1. 0.
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0.7501127 2.75 1. 0.
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0.7590023 0.956 2. 0.
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4.777189 2.0 1. 1.
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-3.330988 2.75 1. 1.
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3.775673 2.38 2. 1.
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-2.290919 3.37 2. 1.
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0.8888268 3.47 3. 1.
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-0.6234864 2.63 4. 1.
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-0.04127263 3.45 5. 1.
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-0.08455389 0.72 1. 2.
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-0.1308752 4.23 5. 2.
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0.008344962 0.2 1. 3.
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-1.532005 4.5 2. 2. 1.7 -1. -1. 0. 0. 0. 0. 0.
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-0.05883649 29.0 3. 3. 7.0 -1. -1. 0. 0. 0. 0. 0.
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0.02296658 24.0 5. 3. 6.0 -1. -1. 0. 0. 0. 0. 0.
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-125 of Lemmon and Jacobsen (2005).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Jacobsen, R.T, 2005.
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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 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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3.063 0.1
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2.303 314.0
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5.086 756.0
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7.3 1707.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-125 of Lemmon and Jacobsen (2005).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Jacobsen, R.T, 2005.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 3 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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-1.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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37.267394939995441 0.0 !aj, ti for [ai*tau**ti] terms
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8.884053082097827 1.0 !aj, ti for [ai*tau**ti] terms
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3.063 -0.1
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2.303 314.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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5.086 756.0
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7.3 1707.0
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#AUX !---Auxiliary function for PH0
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PH0 !Ideal gas Helmholtz form for R-125.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Jacobsen, R.T, 2005.
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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 3 3 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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-1.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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37.2674 0.0 !aj, ti for [ai*tau**ti] terms
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8.88404 1.0
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-49.8651 -0.1
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2.303 -0.92578 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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5.086 -2.22895
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7.3 -5.03283
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FE1 !Helmholtz equation of state for R-125 of Sunaga et al. (1998).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Sunaga, H., Tillner-Roth, R., Sato, H., and Watanabe, K.,
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? "A Thermodynamic Equation of State for Pentafluoroethane (R-125),"
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? Int. J. Thermophys., 19(6):1623-1635, 1998. doi: 10.1007/BF03344914
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?
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?The uncertainties of the equation of state are 0.05% in density, 1% in heat
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? capacity, 0.5% in the liquid speed of sound, and 0.02% in the vapor speed
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? of sound. Uncertainties are higher in the critical region. The uncertainty
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? in vapor pressure is 0.05%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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172.52 !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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14.09 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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120.022 !Molar mass [g/mol]
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172.52 !Triple point temperature [K]
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2.943 !Pressure at triple point [kPa]
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14.088 !Density at triple point [mol/L]
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225.018 !Normal boiling point temperature [K]
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0.3061 !Acentric factor
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339.165 3629.0 4.7324657 !Tc [K], pc [kPa], rhoc [mol/L]
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339.165 4.7324657 !Reducing parameters [K, mol/L]
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8.314471 !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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0.1243922 -0.5 1. 0. !a(i),t(i),d(i),l(i)
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0.27922179 0.0 2. 0.
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-1.1822597 1.5 2. 0.
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0.23616512 1.5 3. 0.
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-0.01157181 3.0 2. 0.
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1.225177 0.5 1. 1.
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-2.147964 1.0 1. 1.
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-0.298138 3.0 1. 1.
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0.3391211 2.75 3. 1.
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-0.0006322995 2.0 8. 1.
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0.0001271747 -1.0 10. 1.
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0.5026962e-5 1.25 12. 1.
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-0.1667058 4.0 1. 2.
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-0.0733275 4.0 2. 2.
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-0.0637878 3.0 4. 2.
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0.683311e-5 0.25 15. 2.
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-0.01995426 23.0 3. 3.
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0.01260026 14.0 4. 3.
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for R-125.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Sunaga, H., Tillner-Roth, R., Sato, H., and Watanabe, K.,
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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 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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5.911212 0.0
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6.856764 670.10271
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4.885985 1626.81842
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3.292859 1863.11546
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@EOS !---Equation of state---
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FE2 !Helmholtz equation of state for R-125 of Piao and Noguchi (1998).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Piao, C.-C. and Noguchi, M.,
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? "An international standard equation of state for the thermodynamic
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? properties of HFC-125 (pentafluoroethane),"
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? J. Phys. Chem. Ref. Data, 27(4):775-806, 1998. doi: 10.1063/1.556021
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?
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!```````````````````````````````````````````````````````````````````````````````
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172.52 !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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14.11 !Maximum density [mol/L]
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CP2 !Pointer to Cp0 model
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120.022 !Molar mass [g/mol]
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172.52 !Triple point temperature [K]
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2.9562 !Pressure at triple point [kPa]
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14.1 !Density at triple point [mol/L]
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225.054 !Normal boiling point temperature [K]
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0.305 !Acentric factor
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339.165 3617.5 4.7324657 !Tc [K], pc [kPa], rhoc [mol/L]
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339.165 4.7324657 !Reducing parameters [K, mol/L]
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8.314471 !Gas constant [J/mol-K]
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20 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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0.085393382372 1.0 0. 0. !a(i),t(i),d(i),l(i)
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-0.133260499658 2.0 0. 0.
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0.257817782488 0.0 1. 0.
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-0.735018179542 1.0 1. 0.
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-0.787454743426 3.0 1. 0.
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-0.0190320468891 4.0 1. 0.
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0.388329449013 0.0 2. 0.
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-0.631901774641 1.0 2. 0.
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0.623842653447 3.0 2. 0.
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0.109925047828 1.0 3. 0.
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-0.0993099630896 3.0 3. 0.
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-0.0104601585904 1.0 4. 0.
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-0.0769998709731 2.0 4. 0.
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0.0149829594347 1.0 5. 0.
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0.0166640927925 2.0 5. 0.
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-0.00181492321758 1.0 6. 0.
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-0.085393382372 1.0 0. 2.
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0.133260499658 2.0 0. 2.
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0.410983574575 1.0 2. 2.
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-0.45298892633 2.0 2. 2.
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@AUX !---Auxiliary function for Cp0
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CP2 !Ideal gas heat capacity function for R-125 of Piao and Noguchi (1998).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Piao, C.-C. and Noguchi, M.,
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314471 !Reducing parameters for T, Cp0
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3 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.3987 0.0
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0.0242728 1.0
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-0.000004099 2.0
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@EOS !---Equation of state---
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BWR !MBWR equation of state for R-125 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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172.52 !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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14.10 !Maximum density [mol/L]
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CP3 !Pointer to Cp0 model
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120.022 !Molar mass [g/mol]
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172.52 !Triple point temperature [K]
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2.921 !Pressure at triple point [kPa]
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14.095 !Density at triple point (max density)
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225.006 !Normal boiling point temperature [K]
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0.30349 !Acentric factor
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339.33 3629.0 4.75996 !Tc [K], pc [kPa], rhoc [mol/L]
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339.33 4.75996 !Reducing parameters [K, mol/L]
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4.75996 !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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-0.052336960705 3.78761878904 -80.715281899
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11565.4605248 -1521756.19161 0.00597541484451
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-1.45990589966 -992.338995652 -399180.535687
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-0.000722591037504 0.358108080969 -108.627994573
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0.022982162657 1.49537670449 911.199833952
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-0.254479949722 0.0102433894096 -6.45583164735
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0.218649963191 1147487.21552 -118389825.386
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30653.9775027 542870289.406 903.502635609
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-153646.507435 3.14617903718 429297.546671
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0.109652021582 -32.9350271819 -0.000338796950505
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0.384533651902 -49.1511706857
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@AUX !---Auxiliary function for Cp0
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CP3 !Ideal gas heat capacity function for R-125 of Outcalt & 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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?
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?The Cp0/R(Tr) function of Outcalt & McLinden has been transformed to Cp0(T).
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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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25.87069 0.0
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0.2690914 1.0
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-0.0001331388 2.0
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4.10133e-9 3.0
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@EOS !---Equation of state---
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FES !Helmholtz equation of state for R-125 of Span and Wagner (2003).
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?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Span, R. and Wagner, W.
|
||
? "Equations of State for Technical Applications. III. Results for Polar Fluids,"
|
||
? Int. J. Thermophys., 24(1):111-162, 2003. doi: 10.1023/A:1022362231796
|
||
?
|
||
?The uncertainties of the equation of state are approximately 0.2% (to
|
||
? 0.5% at high pressures) in density, 1% (in the vapor phase) to 2% in
|
||
? heat capacity, 1% (in the vapor phase) to 2% in the speed of sound, and
|
||
? 0.2% in vapor pressure, except in the critical region.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
172.52 !Lower temperature limit [K]
|
||
600.0 !Upper temperature limit [K]
|
||
100000.0 !Upper pressure limit [kPa]
|
||
14.1 !Maximum density [mol/L]
|
||
CPS !Pointer to Cp0 model
|
||
120.022 !Molar mass [g/mol]
|
||
172.52 !Triple point temperature [K]
|
||
2.9213 !Pressure at triple point [kPa]
|
||
14.096 !Density at triple point [mol/L]
|
||
225.03 !Normal boiling point temperature [K]
|
||
0.304 !Acentric factor
|
||
339.33 3629.0 4.7599607 !Tc [K], pc [kPa], rhoc [mol/L]
|
||
339.33 4.7599607 !Reducing parameters [K, mol/L]
|
||
8.31451 !Gas constant [J/mol-K]
|
||
12 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
||
1.1290996 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
||
-2.8349269 1.25 1. 0.
|
||
0.29968733 1.5 1. 0.
|
||
0.087282204 0.25 3. 0.
|
||
0.00026347747 0.875 7. 0.
|
||
0.61056963 2.375 1. 1.
|
||
0.90073581 2.0 2. 1.
|
||
-0.0068788457 2.125 5. 1.
|
||
-0.44211186 3.5 1. 2.
|
||
-0.035041493 6.5 1. 2.
|
||
-0.1269863 4.75 4. 2.
|
||
-0.025185874 12.5 2. 3.
|
||
|
||
|
||
@AUX !---Auxiliary function for Cp0
|
||
CPS !Ideal gas heat capacity function for R-125 of Outcalt & McLinden (1995).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Outcalt, S.L. and McLinden, M.O.,
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
339.33 8.314471 !Reducing parameters for T, Cp0
|
||
4 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
||
3.111514 0.0
|
||
10.982115 1.0
|
||
-1.843797 2.0
|
||
0.019273 3.0
|
||
|
||
|
||
@EOS !---Equation of state---
|
||
FE4 !Helmholtz equation of state for R-125 of Astina and Sato (2004).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Astina, I.M. and Sato, H.
|
||
? "A Rational Fundamental Equation of State for Pentafluoroethane with
|
||
? Theoretical and Experimental Bases,"
|
||
? Int. J. Thermophys., 25(1):113-131, 2004. doi: 10.1023/B:IJOT.0000022330.46522.68
|
||
?
|
||
?The estimated uncertainties of the equation are 0.1% for the vapor
|
||
? pressure, 0.15% in density for the saturated-liquid phase, 0.5% in density
|
||
? for the saturated-vapor phase, 0.1% in density for the liquid phase, 0.1%
|
||
? in pressure for the gaseous phase, 0.5% in density for the supercritical
|
||
? region, 0.01% in speed of sound for the gaseous phase, 0.9% in speed of
|
||
? sound for the liquid phase, 0.5% in isobaric specific heat for the liquid
|
||
? phase, and 1.2% in isochoric specific heat for the liquid phase.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
172.52 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
70000.0 !Upper pressure limit [kPa]
|
||
14.1 !Maximum density [mol/L]
|
||
CP4 !Pointer to Cp0 model
|
||
120.022 !Molar mass [g/mol]
|
||
172.52 !Triple point temperature [K]
|
||
2.94 !Pressure at triple point [kPa]
|
||
14.1 !Density at triple point [mol/L]
|
||
225.03 !Normal boiling point temperature [K]
|
||
0.305 !Acentric factor
|
||
339.165 3617.5 4.7324657 !Tc [K], pc [kPa], rhoc [mol/L]
|
||
339.165 4.7324657 !Reducing parameters [K, mol/L]
|
||
8.314472 !Gas constant [J/mol-K]
|
||
17 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
||
1.51628822 0.5 1. 0. !a(i),t(i),d(i),l(i)
|
||
-1.49598050 0.75 1. 0.
|
||
-1.28939650 2.25 1. 0.
|
||
1.47295195 0.5 2. 0.
|
||
-2.22976436 0.875 2. 0.
|
||
1.02082011 2. 2. 0.
|
||
-0.00961695881 3.0 3. 0.
|
||
0.0414142522 0.5 4. 0.
|
||
0.14621749 4.0 3. 1.
|
||
-0.0656486371 2.0 6. 1.
|
||
-0.0918319727 3.25 4. 1.
|
||
-0.0290343386 9.5 2. 2.
|
||
-0.0174343357 4.5 4. 2.
|
||
-8.77406498e-4 10.5 4. 2.
|
||
-0.00510648362 25.0 3. 3.
|
||
0.00352425947 5.0 5. 3.
|
||
4.9802285e-4 28.0 7. 3.
|
||
|
||
|
||
@AUX !---Auxiliary function for Cp0
|
||
CP4 !Ideal gas heat capacity function for R-125 of Astina and Sato (2003).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Astina, I.M. and Sato, H.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
339.165 8.314472 !Reducing parameters for T, Cp0
|
||
2 2 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
||
12.990267052 0.0
|
||
-5.2262199 -0.25
|
||
7.028445731 1664.325535
|
||
4.58663536 705.7406967
|
||
|
||
|
||
@EOS !---Cubic equation of state---
|
||
PRT !Translated Peng-Robinson equation for R-125.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Volume translation of Peng Robinson EOS.
|
||
? Translation computed so that sat. liquid density at Tr=0.7 matches FEQ Helmholtz equation
|
||
? of state for R125 of Lemmon and Jacobsen (2004).
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
172.52 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
60000.0 !Upper pressure limit [kPa]
|
||
14.09 !Maximum density [mol/L]
|
||
CPP !Pointer to Cp0 model
|
||
120.0214 !Molar mass [g/mol]
|
||
0.3052 !Acentric factor
|
||
339.173 !Critical temperature [K]
|
||
3617.7 !Critical pressure [kPa]
|
||
4.779 !Critical density [mol/L]
|
||
8.314472 !Gas constant [J/mol-K]
|
||
1 !Number of parameters
|
||
-0.00247
|
||
|
||
|
||
|
||
|
||
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
||
|
||
#ETA !---Viscosity---
|
||
VS1 !Pure fluid viscosity model for R-125 of Huber and Laesecke (2006).
|
||
:DOI: 10.1021/ie051367l
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Huber, M.L. and Laesecke, A.,
|
||
? "Correlation for the Viscosity of Pentafluoroethane (R125) from the Triple
|
||
? Point to 500 K at Pressures up to 60 MPa,"
|
||
? Ind. Eng. Chem. Res., 45:4447-4453, 2006. doi: 10.1021/ie051367l
|
||
?
|
||
?The estimated uncertainty in viscosity is 3.0% in the liquid phase,
|
||
? 0.8% in the vapor.
|
||
?
|
||
?DATA SOURCES FOR VISCOSITY
|
||
? The parameters for viscosity were based in part on the data of:
|
||
? Takahashi, M., Shibasaki-Kitakawa, N., and Yokoyama, C., "Viscosity of Gaseous HFC-125 (Pentafluoroethane) Under High Pressures," Int. J. Thermophys., 20(2):445-453, 1999.
|
||
? Diller, D.E. and Peterson, S.M., "Measurements of the Viscosities of Saturated and Compressed Fluid 1-Chloro-1,2,2,2-Tetrafluoroethane (R124) and Pentafluoroethane (R125) at Temperatures between 120 and 420 K," Int. J. Thermophys, 14(1):55-66, 1993.
|
||
? Ripple, D. and Defibaugh, D., "Viscosity of the Saturated Liquid Phase of Three Fluorinated Ethanes: R152a, R143a, and R125," J. Chem. Eng. Data, 42:360-364, 1997.
|
||
? Assael, M.J. and Polimatidou, S.K., "Measurements of the Viscosity of Liquid R22, R124, and R125 in the Temperature Range 273-333 K," Int. J. Thermophys., 15(5):779-790, 1994.
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Takahashi: avg 0.30% (max -1.22); Diller: avg 1.19% (max. -15.38);
|
||
? Ripple: avg 0.73% (max 1.21); Assael: 0.61% (max -4.62).
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
172.52 !Lower temperature limit [K]
|
||
1000.0 !Upper temperature limit [K]
|
||
60000.0 !Upper pressure limit [kPa]
|
||
18.0 !Maximum density [mol/L]
|
||
1 !Number of terms associated with dilute-gas function
|
||
CI0 !Pointer to reduced effective collision cross-section model
|
||
0.5235 !Lennard-Jones coefficient sigma [nm]
|
||
237.077 !Lennard-Jones coefficient epsilon/kappa [K]
|
||
1.0 1.0 !Reducing parameters for T, eta
|
||
0.2924206 0.5 !=0.026692*SQRT(MW) [Chapman-Enskog term]for LJ CI0
|
||
9 !Number of terms for initial density dependence
|
||
237.077 0.0863974 !Reducing parameters for T (=eps/k), etaB2 (= 0.6022137*sigma**3)
|
||
-19.572881 0.0 !Coefficient, power in T* = T/(eps/k)
|
||
219.73999 -0.25
|
||
-1015.3226 -0.5
|
||
2471.0125 -0.75
|
||
-3375.1717 -1.0
|
||
2491.6597 -1.25
|
||
-787.26086 -1.5
|
||
14.085455 -2.5
|
||
-0.34664158 -5.50
|
||
2 5 1 2 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
|
||
339.173 4.779 1000.0 !Reducing parameters for T, rho, eta (Laesecke correlation in terms of mPa-s, convert to uPa-s)
|
||
3.03379692 0.0 0. 0. 0 ! c1
|
||
0.299246403 0.5 0. 0. 0 ! c8
|
||
0.0 -1.0 2. 0. 0 ! beta16; powers of tau, del, del0; power of del in exponential [0= no exp.]
|
||
-0.00509666198 -1.0 3. 0. 0 ! beta17; powers of tau, del, del0; power of del in exponential [0= no exp.]
|
||
0.0056774484 -2.0 2. 0. 0 ! beta18; powers of tau, del, del0; power of del in exponential [0= no exp.]
|
||
0.0 -2.0 3. 0. 0 ! beta19; powers of tau, del, del0; power of del in exponential [0= no exp.]
|
||
-0.141256365 0.0 1. -1. 0 ! beta7 over del0 term
|
||
0.141256365 0.0 1. 0. 0 ! beta7 in non-simple poly term
|
||
1.0 0.0 0. 1. 0 ! del0 term in denominator
|
||
-1.0 0.0 1. 0. 0 ! -del term in denominator
|
||
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
||
|
||
|
||
|
||
|
||
================================================================================
|
||
|
||
#TCX !---Thermal conductivity---
|
||
TC1 !Pure fluid thermal conductivity model for R-125 of Perkins and Huber (2006).
|
||
:DOI: 10.1021/je050372t
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Perkins, R.A. and Huber, M.L.,
|
||
? "Measurement and Correlation of the Thermal Conductivity of Pentafluoroethane (R125)
|
||
? from 190 K to 512 K at Pressures to 70 MPa,"
|
||
? J. Chem. Eng. Data, 51:898-904, 2006.
|
||
?
|
||
?The estimated uncertainty of the correlation is 3%, except for the dilute gas and points
|
||
? approaching critical where the uncertainty rises to 5%.
|
||
?
|
||
?DATA SOURCES FOR THERMAL CONDUCTIVITY
|
||
?The parameters for thermal conductivity were based on the data of:
|
||
? Perkins, R.A. and Huber, M.L., "Measurement and Correlation of the Thermal Conductivity of Pentafluoroethane (R125) from 190 K to 512 K at Pressures to 70 MPa," J. Chem. Eng. Data, 51:898-904, 2006.
|
||
? LeNeindre, B. and Garrabos, Y., "Measurements of the Thermal Conductivity of HFC-125 in the Temperature Range from 300 to 515 K at Pressures up to 53 MPa," Int. J. Thermophys., 20:375-399, 1999. doi: 10.1023/A:1022692601764
|
||
? Yata, J., Hori, M., Kobayashi, K., and Minamiyama, T., "Thermal Conductivity of Alternative Refrigerants in the Liquid Phase," Int. J. Thermophys., 17:561-571, 1996.
|
||
? Assael, M.J., Malamataris, N., and Karagiannidis, L., "Measurements of the Thermal Conductivity of Refrigerants in the Vapor Phase," Int. J. Thermophys., 18:341-352, 1997.
|
||
? Kim, D.S., Yang, M.H., Kim, M.S., and Ro, S.T., "Thermal Conductivities of Pentafluoroethane (R125) and its Mixtures with Difluoromethane (R32) in the Liquid Phase," Proc. 4th Asian Thermophysical Properties Conference, Tokyo Japan, paper C1c1, 1995.
|
||
? Gao, X., Yamada, T., Nagasaka, Y., and Nagashima, A., "The Thermal Conductivity of CFC Alternatives HFC-125 and HCFC-141b in the Liquid Phase," Int. J. Thermophys., 17:279-292, 1996.
|
||
? Assael, M.J. and Karagiannidis, L., "Measurements of the Thermal Conductivity of Liquid R32, R124, R125, and R141b," Int. J. Thermophys., 16:851-65, 1995.
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Perkins: 0.76% (max -4.1); LeNeindre: 0.66% (max 3.8); Yata: 1.54% (max 3.6);
|
||
? Assael, 1997: 1.23% (max -3.48); Kim: 1.37 (max 2.48); Gao: 1.17% (max 2.4);
|
||
? Assael, 1995: 1.30% (max -3.58).
|
||
? Overall AAD: 0.76%.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
172.52 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
60000.0 !Upper pressure limit [kPa]
|
||
14.09 !Maximum density [mol/L]
|
||
3 0 !# terms for dilute gas function: numerator, denominator
|
||
339.173 1.0 !Reducing parameters for T, tcx
|
||
-0.0046082 0. !Coefficient, power in T
|
||
0.0168688 1.
|
||
0.00488345 2.
|
||
10 0 !# terms for background gas function: numerator, denominator
|
||
339.173 4.779 1. !Reducing parameters for T, rho, tcx
|
||
-0.0072941 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
|
||
0.0110497 1. 1. 0.
|
||
0.0416339 0. 2. 0.
|
||
-0.0289236 1. 2. 0.
|
||
-0.0311487 0. 3. 0.
|
||
0.0278399 1. 3. 0.
|
||
0.0112682 0. 4. 0.
|
||
-0.01211 1. 4. 0.
|
||
-0.00138322 0. 5. 0.
|
||
0.00211196 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-125 of Perkins and Huber (2005).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Perkins, R.A. and Huber, M.L., 2006.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
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) [-]
|
||
5.834646e-10 !Qd_inverse (modified effective cutoff parameter) [m]; fitted to data
|
||
508.7475 !Tref (reference temperature)=1.5*Tc [K]
|
||
|
||
|
||
|
||
|
||
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
||
|
||
@TRN !---ECS Transport---
|
||
ECS !Extended Corresponding States model (Propane reference); fitted to data for R-125.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?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:
|
||
? Perkins, R.A.,(2002) personal communication. 325 Broadway, Boulder, CO 80305, perkins@boulder.nist.gov
|
||
? LeNeindre, B. and Garrabos, Y. (1999). Measurements of the thermal conductivity of HFC-125 in the temperature range from 300 to 515 K at pressures up to 53 MPa, Int. J. Thermophys. 20:375-399.
|
||
? Yata, J., Hori, M., Kobayashi, K. and Minamiyama, T. (1996). Thermal conductivity of alternative refrigerants in the liquid phase, Int. J. Thermophys 17:561-571.
|
||
? Assael, M.J., Malamataris, N., and Karagiannidis, L. (1997). Measurements of the thermal conductivity of refrigerants in the vapor phase, Int. J. Thermophys. 18:341-352.
|
||
? Kim, D.S., Kim, M.S., Ro, S.T. and Yang, M.H..Thermal conductivities of pentafluoroethane (R125) and its mixtures with difluoromethane (R32) in the liquid phase, Proc. 4th Asian Thermophysical Properties Conference, Tokyo Japan, paper C1c1
|
||
? Gao, X., Yamada, T., Nagasaka, Y. and Nagashima, A (1996). The thermal conductivity of CFC alternatives HFC-125 and HCFC-141b in the liquid phase, Int. J. Thermophys. 17:279-292. doi: 10.1007/BF01443393
|
||
? Assael, M.J. and Karagiannidis, L. (1995). Measurements of the thermal conductivity of liquid R32, R124, R125, and R141b, Int. J. Thermohpys 16:851-65.
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Perkins:2.00%; LeNeindre: 2.22%; Yata: 1.98; Assael(1997): 1.21%
|
||
? Kim: 1.66%; Gao: 1.38%; Assael (1995): 1.16%
|
||
? Overall: 2.04%
|
||
?
|
||
?VISCOSITY
|
||
? The ECS parameters for viscosity were based in part on the data of:
|
||
? Diller, D.E. and Peterson, S.M. (1993). Measurements of the viscosities of saturated and compressed fluid 1-chloro-1,2,2,2-tetrafluoroethane (R124) and pentafluoroethane (R125) at temperatures between 120 and 420 K. Int. J. Thermophysics, 14:55-66.
|
||
? Ripple, D. and Matar, O., (1993). Viscosity of the saturated liquid phase of six halogenated compounds and three mixtures, J. Chem. Eng. data 38:560-564.
|
||
? Wilson, L.C., Wilding, W.V., Wilson, G.M., Rowley, R.L., Felix, V.M., and Chilsom-Carter, T. (1992). Thermophysical properties of HFC-125. Fluid Phase Equilibria 80:167-177. doi: 10.1016/0378-3812(92)87065-U
|
||
? Ripple, D. and Defibaugh, D., Viscosity of the saturated liquid phase of three fluorinated ethanes: R152a, R143a and R125, J. Chem. Eng. Data, 1997, 42, 360-364. doi: 10.1021/je960284w
|
||
? Assael, M.J., and Polimatidou, S. (1994).Measurements of the viscosity of liquid R22, R124, and R125 in the temperature range 273-333 K at pressures up to 17 MPa, Int. J. Thermophys 15: 779-790.
|
||
? Assael, M.J., and Polimatidou, S. (1997).Measurements of the viscosity of refrigerants in the vapor phase, Int. J. Thermophys 18: 353-366.
|
||
? Dunlop, P.J. (1994) Viscosities of a series of gaseous fluorocarbons at 25C, J. Chem. Phys. 100:3149-3151.
|
||
? Takahashi, M., Shibasaki-Kitakawa, N., and Yokoyama, C., Viscosity of Gaseous HFC-125 (pentafluoroethane) under high pressures, Int. J. Thermophysics, 1999, 20(2), 445-453. doi: 10.1023/A:1022648819511
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Diller: 2.85%; Ripple(1993): 2.31%; Wilson: 2.53%; Ripple(1997): 0.70%
|
||
? Assael (1994): 1.26%; Assael (1997): 1.01%; Dunlop: -0.15%; Takahashi:1.45%
|
||
? Overall: 1.87%
|
||
?
|
||
?The Lennard-Jones parameters were taken from Le Neindre (1999)
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
172.52 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
60000.0 !Upper pressure limit [kPa]
|
||
14.10 !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)
|
||
0.5235 !Lennard-Jones coefficient sigma [nm]
|
||
237.077 !Lennard-Jones coefficient epsilon/kappa [K]
|
||
2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
|
||
0.00118189 0. 0. 0. !Coefficient, power of T, spare1, spare2
|
||
0.663334e-6 1. 0. 0. !Coefficient, power of T, spare1, spare2
|
||
2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
|
||
1.00907 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0193968 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
|
||
1.21594 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
-0.056531 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-125 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
|
||
339.173 !Critical temperature used in fit (dummy)
|
||
0.05252 1.237 !Sigma0 and n
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for R-125 of Lemmon and Jacobsen (2004).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Lemmon, E.W. and Jacobsen, R.T, 2005.
|
||
?
|
||
?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. !
|
||
339.173 3617.7 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
-7.5295 1.0
|
||
1.9026 1.5
|
||
-2.2966 2.3
|
||
-3.4480 4.6
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for R-125 of Gao and Lemmon (2017).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Gao, K. and Lemmon, E.W., 2017.
|
||
?
|
||
?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. !
|
||
339.173 4.779 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
2.0408 0.343
|
||
2.5341 1.35
|
||
-3.6390 1.85
|
||
2.0924 2.5
|
||
4.8676 16.0
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for R-125 of Lemmon and Jacobsen (2004).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Lemmon, E.W. and Jacobsen, R.T, 2005.
|
||
?
|
||
?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. !
|
||
339.173 4.779 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
-2.8403 0.38
|
||
-7.2738 1.22
|
||
-21.890 3.3
|
||
-58.825 6.9
|
||
|
||
|
||
@END
|
||
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|
||
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