548 lines
26 KiB
Plaintext
548 lines
26 KiB
Plaintext
R245fa !Short name
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460-73-1 !CAS number
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1,1,1,3,3-Pentafluoropropane !Full name
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CF3CH2CHF2 !Chemical formula {C3H3F5}
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HFC-245fa !Synonym
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134.04794 !Molar mass [g/mol]
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170.0 !Triple point temperature [K]
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288.198 !Normal boiling point [K]
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427.01 !Critical temperature [K]
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3651.0 !Critical pressure [kPa]
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3.875 !Critical density [mol/L]
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0.3783 !Acentric factor
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1.549 !Dipole moment [Debye]; Goodwin & Mehl (1997) IJT 18:795-806
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IIR !Default reference state
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10.0 !Version number
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???? !UN Number :UN:
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halocb !Family :Family:
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???? !Heating value (upper) [kJ/mol] :Heat:
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1030. !GWP (IPCC 2007) :GWP:
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34000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
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B1 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/C3H3F5/c4-2(5)1-3(6,7)8/h2H,1H2 !Standard InChI String :InChi:
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MSSNHSVIGIHOJA-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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5c322280 !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 E.W. Lemmon, NIST Physical and Chemical Properties Division, Boulder, Colorado
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! 01-24-97 EWL, Original version.
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! 05-17-02 MLH, Add ECS k fit; revised ECS eta fit;.
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! 04-19-04 MLH, Update transport references.
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! 02-18-05 VD, Change CAS number.
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! 01-05-06 EWL, Add Lemmon and Span short EOS.
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! 08-16-06 MLH, Add new k fit based on Wang 2006 data; adjusted transport limits to coincide with new EOS.
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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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! 03-08-13 MLH, Refit ECS viscosity with new data of Meng 2011 and Wang 2010.
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! 02-05-15 EWL, Add Akasaka et al. equation of state.
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! 02-04-16 MLH, Add new viscosity correlation.
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! 03-03-16 MLH, Add new thermal conductivity correlation.
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! 04-14-16 MLH, Correct Ro value in critical enhancement.
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! 02-16-17 KG, Add ancillary equations.
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! 11-14-17 MLH, Update transport references.
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for R-245fa of Akasaka et al. (2015).
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:TRUECRITICALPOINT: 427.01 3.875 !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: 10.1063/1.4913493
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Akasaka, R., Zhou, Y., and Lemmon, E.W.,
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? "A Fundamental Equation of State for 1,1,1,3,3-Pentafluoropropane (R-245fa),"
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? J. Phys. Chem. Ref. Data, 44(1), 013104, 2015.
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? doi: 10.1063/1.4913493
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?
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?The estimated uncertainties are 0.1 % for vapor pressures, 0.1 % for saturated
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? liquid densities, 0.1 % for liquid densities below 70 MPa, 0.2 % for
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? densities at higher pressures, 0.3 % for vapor densities, 0.3 % for liquid
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? sound speeds, and 0.1 % for vapor sound speeds. The uncertainties in the
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? critical region are higher for all properties except vapor pressures.
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?
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!```````````````````````````````````````````````````````````````````````````````
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170.0 !Lower temperature limit [K]
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440. !Upper temperature limit [K]
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200000. !Upper pressure limit [kPa]
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12.29 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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134.04794 !Molar mass [g/mol]
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170.0 !Triple point temperature [K]
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0.01186 !Pressure at triple point [kPa]
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12.28 !Density at triple point [mol/L]
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288.198 !Normal boiling point temperature [K]
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0.3783 !Acentric factor
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427.01 3651.0 3.875 !Tc [K], pc [kPa], rhoc [mol/L]
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427.01 3.875 !Reducing parameters [K, mol/L]
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8.3144598 !Gas constant [J/mol-K]
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10 4 4 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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0.057506623 1.0 4. 0. !a(i),t(i),d(i),l(i)
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1.5615975 0.27 1. 0.
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-2.3614485 0.9 1. 0.
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-0.51773521 1.09 2. 0.
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0.18509788 0.4 3. 0.
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-0.87405626 2.9 1. 2.
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-0.27530955 1.7 3. 2.
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0.57971151 0.8 2. 1.
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-0.39934306 3.6 2. 2.
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-0.033230277 1.05 7. 1.
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0.83210508 1.8 1. 2. 2. -1.011 -1.879 1.081 0.709 0. 0. 0.
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-0.335443 4.0 1. 2. 2. -1.447 -2.454 0.651 0.939 0. 0. 0.
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-0.10117801 4.5 3. 2. 2. -1.079 -1.256 0.468 0.703 0. 0. 0.
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-0.0091495867 2. 3. 2. 2. -7.86 -21.1 1.293 0.777 0. 0. 0.
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eta beta gamma epsilon
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EXP[eta*(delta-epsilon)^2+beta*(tau-gamma)^2]
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for R-245fa of Akasaka et al. (2015).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Akasaka, R., Zhou, Y., and Lemmon, E.W., 2015.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. ! !Doesn't agree well with other sources at high termperatures
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0. !
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0. !
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1.0 8.3144598 !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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4.0 0.0
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5.5728 222.0
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10.385 1010.0
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12.554 2450.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for R-245fa of Akasaka et al. (2015).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Akasaka, R., Zhou, Y., and Lemmon, E.W., 2015.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 2 3 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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-13.3856132851977776 0.0 !aj, ti for [ai*tau**ti] terms
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9.8453764599945881 1.0 !aj, ti for [ai*tau**ti] terms
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5.5728 222.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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10.385 1010.0
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12.554 2450.0
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#AUX !---Auxiliary function for PH0
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PH0 !Ideal gas Helmholtz form for R-245fa.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Akasaka, R., Zhou, Y., and Lemmon, E.W., 2015.
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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 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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3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-13.3856088254 0.0 !aj, ti for [ai*tau**ti] terms
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9.8453743711 1.0
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5.5728 -0.5198941477 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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10.385 -2.3652841854
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12.554 -5.7375705487
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FE1 !Helmholtz equation of state for R-245fa of Lemmon and Span (2006).
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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 estimated uncertainty in the equation of state for density is 0.1% in
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? the liquid phase below 400 K with pressures up to 30 MPa. Above 30 MPa, the
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? uncertainties are 0.2% at temperatures above 310 K and up to 1% for lower
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? temperatures. In the vapor phase and at temperatures above 400 K, the
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? uncertainty is 1% in density, with higher uncertainties in the critical
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? region. The uncertainty in vapor pressure is 0.2% above 250 K, and rises
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? to 0.35% above 370 K. The uncertainties in other properties are 5% in
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? liquid phase heat capacities and 0.2% in liquid phase sound speeds below
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? 360 K, with unknown uncertainties outside of these regions due to a lack of
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? experimental data.
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?
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!```````````````````````````````````````````````````````````````````````````````
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171.05 !Lower temperature limit [K]
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440. !Upper temperature limit [K]
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200000. !Upper pressure limit [kPa]
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12.3 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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134.04794 !Molar mass [g/mol]
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171.05 !Triple point temperature [K]
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0.01251 !Pressure at triple point [kPa]
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12.29 !Density at triple point [mol/L]
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288.29 !Normal boiling point temperature [K]
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0.3776 !Acentric factor
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427.16 3651.0 3.85 !Tc [K], pc [kPa], rhoc [mol/L]
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427.16 3.85 !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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1.2904 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-3.2154 1.25 1. 0.
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0.50693 1.5 1. 0.
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0.093148 0.25 3. 0.
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0.00027638 0.875 7. 0.
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0.71458 2.375 1. 1.
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0.87252 2.0 2. 1.
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-0.015077 2.125 5. 1.
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-0.40645 3.5 1. 2.
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-0.11701 6.5 1. 2.
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-0.13062 4.75 4. 2.
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-0.022952 12.5 2. 3.
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for R-245fa.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R.
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? Coefficients fit to the heat capacity values derived from speed of sound data
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? of J. Scott, NIST, 1999. These have been augmented with spectroscopic values
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? from R. Singh, AlliedSignal, personal communication, 1999.
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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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4.0 0.0
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5.5728 222.0
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10.385 1010.0
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12.554 2450.0
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@AUX !---Auxiliary function for PH0
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PH1 !Ideal gas Helmholtz form for R-245fa.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Span, R.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1 2 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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3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-13.4283638514 0.0 !aj, ti for [ai*tau**ti] terms
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9.87236538 1.0
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5.5728 -0.5197115835 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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10.385 -2.3644536005
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12.554 -5.7355557636
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^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
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#ETA !---Viscosity---
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VS1 !Pure fluid viscosity model for R-245fa of Perkins et al. (2016).
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:DOI: 10.1021/acs.jced.6b00350
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Perkins, R.A., Huber, M.L., and Assael, M.J.,
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? "Measurements of the Thermal Conductivity of 1,1,1,3-3-Pentafluoropropane (R-245fa) and
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? Correlations for the Viscosity and Thermal Conductivity Surfaces,"
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? J. Chem. Eng. Data, 61:3286-3294, 2016. doi: 10.1021/acs.jced.6b00350
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?
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?The estimated uncertainty for the dilute gas region is 2%, for the liquid phase at pressures to 40 MPa is 3%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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170.0 !Lower temperature limit [K]
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700.0 !Upper temperature limit [K]
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200000.0 !Upper pressure limit [kPa]
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15.0 !Maximum density [mol/L]
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1 !Number of terms associated with dilute-gas function
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CI1 !Pointer to reduced effective collision cross-section model
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0.588 !Lennard-Jones coefficient sigma [nm]
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258.15 !Lennard-Jones coefficient epsilon/kappa [K]
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1.0 1.0 !Reducing parameters for T, eta
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0.2472694 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term] for CI1 form
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9 !Number of terms for initial density dependence
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258.15 0.12242852 !Reducing parameters for T (=eps/k), etaB2 (= 0.6022137*sigma**3)
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-19.572881 0.0 !Coefficient, power in T* = T/(eps/k)
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219.73999 -0.25
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-1015.3226 -0.5
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2471.0125 -0.75
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-3375.1717 -1.0
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2491.6597 -1.25
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-787.26086 -1.5
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14.085455 -2.5
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-0.34664158 -5.50
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0 0 3 0 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
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427.01 3.875 1.0 !Reducing parameters for T, rho, eta
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0.83502935 0.5 5.6666666666667 0. 0
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10.245205 -0.5 2.6666666666667 0. 0
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0.00023356206 -2.5 12.6666666666667 0. 0
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NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
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#AUX !---Auxiliary function for the collision integral
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CI1 !Reduced effective collision cross-section model (empirical form in log(T*)) for R-245fa.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Perkins et al., 2016.
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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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3 !Number of terms
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0.250746 0 !Coefficient, power of Tstar
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-0.6031 1
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0.271008 2
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================================================================================
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#TCX !---Thermal conductivity---
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TC1 !Pure fluid thermal conductivity model for R-245fa of Perkins et al. (2016).
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:DOI: 10.1021/acs.jced.6b00350
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Perkins, R.A., Huber, M.L., and Assael, M.J., "Measurements of the Thermal Conductivity of
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? 1,1,1,3-3-Pentafluoropropane (R-245fa) and Correlations for the Viscosity and Thermal Conductivity
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? Surfaces," J. Chem. Eng. Data, 61:3286-3294, 2016. doi: 10.1021/acs.jced.6b00350
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?
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?The estimated uncertainty is 2 % for the liquid phase at pressures to 70 MPa, and 2 % for the vapor phase.
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?
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!```````````````````````````````````````````````````````````````````````````````
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170.0 !Lower temperature limit [K]
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700. !Upper temperature limit [K]
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200000. !Upper pressure limit [kPa]
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15. !Maximum density [mol/L]
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2 0 !# terms for dilute gas function: numerator, denominator
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1.0 1. !Reducing parameters for T, tcx
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-0.0143644 0. !Coefficient, power in T
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0.906916e-4 1.
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10 0 !# terms for background gas function: numerator, denominator
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427.01 3.875 1. !Reducing parameters for T, rho, tcx
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-0.0120505 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
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0.0652392 0. 2. 0.
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-0.0501653 0. 3. 0.
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0.0176338 0. 4. 0.
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-0.00219652 0. 5. 0.
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0.00937193 1. 1. 0.
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-0.0397844 1. 2. 0.
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0.0355883 1. 3. 0.
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-0.0141777 1. 4. 0.
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0.00230154 1. 5. 0.
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TK3 !Pointer to critical enhancement auxiliary function
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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-245fa.
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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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?VISCOSITY
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? The ECS parameters for viscosity were based in part on the data of:
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? Meng, X., Zhang, J., Wu, J.," Compressed Liquid Viscosity of 1,1,1,3,3-Pentafluoropropane (R245fa) and 1,1,1,3,3,3-Hexafluoropropane (R236fa)", J. Chem. Eng. Data, 2011, 56(12), 4956-4964
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? Wang, X., Wu, J., Liu, Z.,"?Viscosity of Gaseous HFC245fa" J. Chem. Eng. Data, 2010, 55(1), 496-499 doi: 10.1021/je900279z
|
||
? Laesecke, A. and R. F. Hafer (1998). "Viscosity of Fluorinated Propane Isomers. 2. Measurements of Three Compounds and Model Comparisons," J. Chem. Eng. Data, 43(1):84-92.
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Laesecke: 0.8%; Wang: 1.3%; Meng: 1.1%
|
||
?
|
||
?THERMAL CONDUCTIVITY
|
||
? The ECS parameters for thermal conductivity were based in part on the data of:
|
||
? Yata, J., Hori, M. Niki, M., Isono, Y. and Yanagitani, Y. (2000). "Coexistence curve of HFC-134a and thermal conductivity of HFC-245fa". Fluid Phase Equilibria, 174:221-229.doi: 10.1016/S0378-3812(00)00429-5
|
||
? Dohrn, R., Treckmann, R., and Heinemann, T. (1999). "Vapor-phase thermal conductivity of 1,1,1,2,2-pentafluoropropane, 1,1,1,3,3-pentafluoropropane, 1,1,2,2,3- pentafluoropropane and carbon dioxide". Fluid Phase Equilibria 158-160:1021-1028
|
||
? Geller, V., Bivens, D.B. and Yokozeki, A. (1999). "Transport properties and surface tension of hydrofluorocarbons HFC236fa and HFC 245fa", Proc. 20th Int. Congress of Refrig, IIR/IIF,Sydney.
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Yata: 1.30%; Dohrn: 2.63%; Geller:7.80%;
|
||
?
|
||
?The Lennard-Jones parameters were taken from a fit to Wang viscosity data.
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
170.0 !Lower temperature limit [K]
|
||
500.0 !Upper temperature limit [K]
|
||
200000.0 !Upper pressure limit [kPa]
|
||
12.3 !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)
|
||
0.58489 !Lennard-Jones coefficient sigma [nm] for ECS method !fit to data
|
||
259.89 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method !fit to data
|
||
2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
|
||
0.0016499 0. 0. 0. !Coefficient, power of T, spare1, spare2
|
||
-3.28868e-7 1. 0. 0. !Coefficient, power of T, spare1, spare2
|
||
3 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
|
||
1.00597 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0187391 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
0.0013349 0. 2. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
||
1.16265 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
-0.0473491 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
TK3 !Pointer to critical enhancement auxiliary function
|
||
|
||
|
||
#AUX !---Auxiliary function for the thermal conductivity critical enhancement
|
||
TK3 !Simplified thermal conductivity critical enhancement for R-245fa of Perkins et al. (2013).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Perkins, R.A., Sengers, J.V., Abdulagatov, I.M., and Huber, M.L.,
|
||
? "Simplified Model for the Critical Thermal-Conductivity Enhancement in Molecular Fluids,"
|
||
? Int. J. Thermophys., 34(2):191-212, 2013. doi: 10.1007/s10765-013-1409-z
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
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)
|
||
1.02 !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)
|
||
0.204e-9 !Xi0 (amplitude) [m]
|
||
0.060 !Gam0 (amplitude) [-]
|
||
0.626e-9 !Qd_inverse (modified effective cutoff parameter) [m]; generic number, not fitted to data
|
||
640.52 !Tref (reference temperature)=1.5*Tc [K]
|
||
|
||
|
||
|
||
|
||
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
|
||
|
||
#STN !---Surface tension---
|
||
ST1 !Surface tension model for R-245fa 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. !
|
||
3 !Number of terms in surface tension model
|
||
427.16 !Critical temperature used in fit (dummy)
|
||
0.073586 1.0983 !Sigma0 and n
|
||
0.0103 0.60033
|
||
-0.02663 0.72765
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for R-245fa of Gao (2017).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Gao, K., 2017.
|
||
?
|
||
?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. !
|
||
427.01 3651.0 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
-7.775 1.0
|
||
1.4832 1.5
|
||
-3.252 2.7
|
||
-2.7634 5.0
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for R-245fa of Akasaka et al. (2015).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Akasaka et al., 2015.
|
||
?
|
||
?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. !
|
||
427.01 3.875 !Reducing parameters
|
||
4 0 0 0 0 0 !Number of terms in equation
|
||
0.46367 0.17
|
||
2.2375 0.5
|
||
-0.27579 1.3
|
||
0.55136 2.5
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for R-245fa of Gao (2017).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Gao, K., 2017.
|
||
?
|
||
?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. !
|
||
427.01 3.875 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-1.3444 0.265
|
||
-6.3533 0.837
|
||
-20.252 2.73
|
||
-60.497 6.25
|
||
-141.82 14.0
|
||
|
||
|
||
@END
|
||
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|
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