1105 lines
54 KiB
Plaintext
1105 lines
54 KiB
Plaintext
Propane !Short name
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74-98-6 !CAS number
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Propane !Full name
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CH3CH2CH3 !Chemical formula {C3H8}
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R-290 !Synonym
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44.09562 !Molar mass [g/mol]
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85.525 !Triple point temperature [K]
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231.036 !Normal boiling point [K]
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369.89 !Critical temperature [K]
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4251.2 !Critical pressure [kPa]
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5.0 !Critical density [mol/L]
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0.1521 !Acentric factor
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0.084 !Dipole moment [Debye]; R.D. Nelson, D.R. Lide, and A.A. Maryott, "Selected Values of Electric Dipole Moments for Molecules in the Gas Phase," NSRDS-NBS 10, National Reference Data Series, US Government Printing Office, Washington, 1967.
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IIR !Default reference state
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10.0 !Version number
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1075, 1978 !UN Number :UN:
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n-alkane !Family :Family:
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2219.17 !Heating value (upper) [kJ/mol] :Heat:
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3.3 !GWP (IPCC 2007) :GWP:
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5300. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
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A3 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/C3H8/c1-3-2/h3H2,1-2H3 !Standard InChI String :InChi:
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ATUOYWHBWRKTHZ-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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70c6aac0 !Hash number from InChI Key :Hash:
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!The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the
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! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended
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! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to
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! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary
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! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and
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! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the
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! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the
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! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations,
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! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and
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! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface
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! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a
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! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The
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! end of the fluid file is marked with @END. Anything below that is ignored.
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! compiled by M. McLinden, NIST Physical and Chemical Properties Division, Boulder, Colorado
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! 02-01-96 MM, Original version.
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! 05-18-99 EWL, Add Span equation of state.
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! 11-22-99 EWL, Add viscosity equation of Vogel et al.
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! 03-01-00 EWL, Add Marsh thermal conductivity equation.
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! 5-02-01 EWL, Add Miyamoto and Watanabe equation of state.
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! 04-19-04 AHH, Change dipole moment.
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! 08-05-04 EWL, Add Harvey and Lemmon dielectric correlation.
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! 09-14-04 EWL, Add Buecker and Wagner EOS.
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! 10-13-04 MLH, Add family.
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! 12-13-04 EWL, Update melting line.
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! 09-03-06 MLH, Allow transport equations TC1, TK1, VC1 to be extrapolated to higher rho for use as ref. fluid.
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! 01-10-07 EWL, Add Lemmon et al. equation of state.
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! 03-05-07 MLH, Add VS4 model.
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! 02-12-08 EWL, Change the triple point temperature to that of Perkins et al. (2008), including in MLT.
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! 09-11-08 EWL, Update ancillary equations for VLE properties.
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! 04-11-12 MLH, Add extra blank FT coeff for consistent formatting.
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! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
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! 09-25-13 EWL, Change reducing pressure from ..17 to ..173 in melting line equation.
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! 01-11-17 MLH, Add Vogel viscosity model (2016).
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! 05-08-17 EWL, Update VS7 to the new reverse Polish notation.
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for propane of Lemmon et al. (2009).
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:TRUECRITICALPOINT: 369.89 5.0 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
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:DOI: 10.1021/je900217v
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W., McLinden, M.O., and Wagner, W.,
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? "Thermodynamic Properties of Propane. III. A Reference Equation of State
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? for Temperatures from the Melting Line to 650 K and Pressures up to 1000 MPa,"
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? J. Chem. Eng. Data, 54:3141-3180, 2009.
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?
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?The uncertainties below 350 K in density are 0.01% in the liquid phase and
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? 0.03% in the vapor phase (including saturated states for both phases). The
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? liquid phase value also applies at temperatures greater than 350 K (to about
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? 500 K) at pressures greater than 10 MPa. In the extended critical region, the
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? uncertainties increase to 0.1% in density, except very near the critical point
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? where the uncertainties in density increase rapidly as the critical point is
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? approached. However, in this same region, the uncertainty in pressure
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? calculated from density and temperature is 0.04%, even at the critical point.
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?
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?The uncertainties in the speed of sound are 0.01% in the vapor phase at
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? pressures up to 1 MPa, 0.03% in the liquid phase between 260 and 420 K and 0.1%
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? in the liquid phase at temperatures below 260 K. The uncertainty in vapor
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? pressure is 0.02% above 180 K, 0.1% between 120 and 180 K, and increases
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? steadily below 120 K. Below 115 K, vapor pressures are less than 1 Pa and
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? uncertainty values might be as low as 3% at the triple point. Uncertainties
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? in heat capacities are 0.5% in the liquid phase, 0.2% in the vapor phase, and
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? higher in the supercritical region.
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?
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!```````````````````````````````````````````````````````````````````````````````
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85.525 !Lower temperature limit [K]
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650.0 !Upper temperature limit [K]
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1000000.0 !Upper pressure limit [kPa]
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20.6 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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44.09562 !Molar mass [g/mol]
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85.525 !Triple point temperature [K]
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0.000000172 !Pressure at triple point [kPa]
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16.63 !Density at triple point [mol/L]
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231.036 !Normal boiling point temperature [K]
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0.1521 !Acentric factor
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369.89 4251.2 5.0 !Tc [K], pc [kPa], rhoc [mol/L]
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369.89 5.0 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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11 4 7 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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0.042910051 1.0 4. 0. !a(i),t(i),d(i),l(i)
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1.7313671 0.33 1. 0.
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-2.4516524 0.8 1. 0.
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0.34157466 0.43 2. 0.
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-0.46047898 0.90 2. 0.
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-0.66847295 2.46 1. 1.
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0.20889705 2.09 3. 1.
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0.19421381 0.88 6. 1.
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-0.22917851 1.09 6. 1.
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-0.60405866 3.25 2. 2.
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0.066680654 4.62 3. 2.
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0.017534618 0.76 1. 2. 2. -0.963 -2.33 0.684 1.283 0. 0. 0.
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0.33874242 2.50 1. 2. 2. -1.977 -3.47 0.829 0.6936 0. 0. 0.
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0.22228777 2.75 1. 2. 2. -1.917 -3.15 1.419 0.788 0. 0. 0.
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-0.23219062 3.05 2. 2. 2. -2.307 -3.19 0.817 0.473 0. 0. 0.
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-0.09220694 2.55 2. 2. 2. -2.546 -0.92 1.5 0.8577 0. 0. 0.
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-0.47575718 8.40 4. 2. 2. -3.28 -18.8 1.426 0.271 0. 0. 0.
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-0.017486824 6.75 1. 2. 2. -14.6 -547.8 1.093 0.948 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 propane of Lemmon et al. (2009).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W., McLinden, M.O., and Wagner, W., 2009.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314472 !Reducing parameters for T, Cp0
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1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.0 0.0
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3.043 393.0
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5.874 1237.0
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9.337 1984.0
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7.922 4351.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for propane of Lemmon et al. (2009).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W., McLinden, M.O., and Wagner, W., 2009.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-4.9705912033525124 0.0 !aj, ti for [ai*tau**ti] terms
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4.293524424315649 1.0 !aj, ti for [ai*tau**ti] terms
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3.043 393.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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5.874 1237.0
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9.337 1984.0
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7.922 4351.0
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#AUX !---Auxiliary function for PH0
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PH0 !Ideal gas Helmholtz form for propane.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W., McLinden, M.O., and Wagner, W., 2009.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
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3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-4.970583 0.0 !aj, ti for [ai*tau**ti] terms
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4.29352 1.0
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3.043 -1.062478 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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5.874 -3.344237
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9.337 -5.363757
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7.922 -11.762957
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FEK !Helmholtz equation of state for propane of Kunz and Wagner (2004).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Kunz, O., Klimeck, R., Wagner, W., Jaeschke, M.
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? "The GERG-2004 Wide-Range Equation of State for Natural Gases
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? and Other Mixtures," GERG Technical Monograph 15,
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? Fortschritt-Berichte VDI, VDI-Verlag, Düsseldorf, 2007.
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?
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!```````````````````````````````````````````````````````````````````````````````
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85.48 !Lower temperature limit [K]
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500.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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17.41 !Maximum density [mol/L]
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PHK !Pointer to Cp0 model
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44.09562 !Molar mass [g/mol]
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85.48 !Triple point temperature [K]
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0.00000017 !Pressure at triple point [kPa]
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16.62 !Density at triple point [mol/L]
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231.08 !Normal boiling point temperature [K]
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0.1538 !Acentric factor
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369.825 4255.5 5.000043088 !Tc [K], pc [kPa], rhoc [mol/L]
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369.825 5.000043088 !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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1.0403973107358 0.25 1. 0. !a(i),t(i),d(i),l(i)
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-2.8318404081403 1.125 1. 0.
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0.84393809606294 1.5 1. 0.
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-0.076559591850023 1.375 2. 0.
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0.09469737305728 0.25 3. 0.
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0.00024796475497006 0.875 7. 0.
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0.27743760422870 0.625 2. 1.
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-0.043846000648377 1.75 5. 1.
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-0.26991064784350 3.625 1. 2.
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-0.06931341308986 3.625 4. 2.
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-0.029632145981653 14.5 3. 3.
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0.01404012675138 12.0 4. 3.
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@AUX !---Auxiliary function for PH0
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PHK !Ideal gas Helmholtz form for propane of Kunz and Wagner (2004).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Kunz, O., Klimeck, R., Wagner, W., Jaeschke, M.
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? "The GERG-2004 Wide-Range Equation of State for Natural Gases
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? and Other Mixtures," GERG Technical Monograph 15,
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? Fortschritt-Berichte VDI, VDI-Verlag, Düsseldorf, 2007.
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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 0 2 2 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
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3.02939 1.0 !ai, ti for [ai*log(tau**ti)] terms
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31.602908195 0.0 !aj, ti for [ai*tau**ti] terms
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-84.463284382 1.0
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-3.197 0.543210978 !aj, ti for cosh and sinh terms
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8.37267 2.777773271
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6.60569 1.297521801
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19.1921 2.583146083
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@EOS !---Equation of state---
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FE1 !Helmholtz equation of state for propane of Buecker and Wagner (2006).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Bücker, D. and Wagner, W.,
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? "Reference equations of state for the thermodynamic properties of fluid
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? phase n-butane and isobutane,"
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? J. Phys. Chem. Ref. Data, 35(1):929-1019, 2006. doi: 10.1063/1.1901687
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?
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?Typical uncertainties in density are 0.02% in the liquid phase, 0.05% in the
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? vapor phase and at supercritical temperatures, and 0.1% in the critical
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? region, except very near the critical point, where the uncertainty in
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? pressure is 0.1%. For vapor pressures, the uncertainty is 0.02% above 180
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? K, 0.05% above 1 Pa (115 K), and dropping to 0.001 mPa at the triple point.
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? The uncertainty in heat capacity (isobaric, isochoric, and saturated) is
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? 0.5% at temperatures above 125 K and 2% at temperatures below 125 K for the
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? liquid, and is 0.5% for all vapor states. The uncertainty in the liquid
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? phase speed of sound is 0.5%, and that for the vapor phase is 0.05%. The
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? uncertainties are higher for all properties very near the critical point
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? except pressure (saturated vapor/liquid and single phase).
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?
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!```````````````````````````````````````````````````````````````````````````````
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85.48 !Lower temperature limit [K]
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500.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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17.41 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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44.09562 !Molar mass [g/mol]
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85.48 !Triple point temperature [K]
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0.00000017 !Pressure at triple point [kPa]
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16.62 !Density at triple point [mol/L]
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231.034 !Normal boiling point temperature [K]
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0.1524 !Acentric factor
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369.825 4247.66 5.000043088 !Tc [K], pc [kPa], rhoc [mol/L] (218.5 kg/m^3)
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369.825 5.000043088 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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23 4 2 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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2.1933784906951 0.5 1. 0.
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-3.8432884604893 1.0 1. 0.
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0.56820219711755 1.5 1. 0.
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0.11235233289697 0.0 2. 0.
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-0.013246623110619 0.5 3. 0.
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0.014587076590314 0.5 4. 0.
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0.019654925217128 0.75 4. 0.
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0.73811022854042 2.0 1. 1.
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-0.85976999811290 2.5 1. 1.
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0.14331675665712 2.5 2. 1.
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-0.023280677426427 1.5 7. 1.
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-0.98713669399783e-4 1.0 8. 1.
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0.0045708225999895 1.5 8. 1.
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-0.027766802597861 4.0 1. 2.
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-0.10523131087952 7.0 2. 2.
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0.097082793466314 3.0 3. 2.
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0.020710537703751 7.0 3. 2.
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-0.054720320371501 3.0 4. 2.
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0.00064918009057295 1.0 5. 2.
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0.0074471355056336 6.0 5. 2.
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-0.00027504616979066 0.0 10. 2.
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-0.0077693374632348 6.0 2. 3.
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-0.0017367624932157 13.0 6. 3.
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-0.038248057095416 2.0 1. 2. 2. -10.0 -150.0 1.16 0.85 0. 0. 0.
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-0.006879725443549 0.0 2. 2. 2. -10.0 -200.0 1.13 1.0 0. 0. 0.
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for propane of Buecker and Wagner (2005).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Bücker, D. and Wagner, W.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314472 !Reducing parameters for T, Cp0
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1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.02256195 0.0
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2.90591124 388.87291
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4.68495401 1145.03868
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10.2971154 1880.40472
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8.08977905 4228.18881
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@AUX !---Auxiliary function for PH0
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PH1 !Ideal gas Helmholtz form for propane of Buecker and Wagner (2005).
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?
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?```````````````````````````````````````````````````````````````````````````````
|
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?Bücker, D. and Wagner, W.
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?
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!```````````````````````````````````````````````````````````````````````````````
|
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0. !
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10000. !
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0. !
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0. !
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1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
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3.02256195 1.0 !ai, ti for [ai*log(tau**ti)] terms
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10.14394255 0.0 !aj, ti for [ai*tau**ti] terms
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-4.79513693 1.0
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2.90591124 -1.0515052038 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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4.68495401 -3.0961635368
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10.2971154 -5.0845797877
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8.08977905 -11.4329447982
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|
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@EOS !---Equation of state---
|
|
FE2 !Helmholtz equation of state for propane of Miyamoto and Watanabe (2000).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Miyamoto, H., and Watanabe, K.,
|
|
? "A Thermodynamic Property Model for Fluid-Phase Propane,"
|
|
? Int. J. Thermophys., 21(5):1045-1072, 2000.
|
|
?
|
|
?Typical uncertainties are 0.05% for density, 0.02% for the vapor
|
|
? pressure, and 0.5%-1% for the heat capacity and speed of sound in the
|
|
? liquid phase. In the vapor phase, the uncertainty in the speed of sound
|
|
? is 0.02%
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.48 !Lower temperature limit [K]
|
|
623.0 !Upper temperature limit [K]
|
|
103000.0 !Upper pressure limit [kPa]
|
|
17.41 !Maximum density [mol/L]
|
|
CP2 !Pointer to Cp0 model
|
|
44.09562 !Molar mass [g/mol]
|
|
85.48 !Triple point temperature [K]
|
|
0.00000017 !Pressure at triple point [kPa]
|
|
16.64 !Density at triple point [mol/L]
|
|
231.06 !Normal boiling point temperature [K]
|
|
0.1524 !Acentric factor
|
|
369.825 4247.09 4.9551406693 !Tc [K], pc [kPa], rhoc [mol/L] (218.5 kg/m^3)
|
|
369.825 4.9551406693 !Reducing parameters [K, mol/L]
|
|
8.314472 !Gas constant [J/mol-K]
|
|
19 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
0.2698378 -0.25 1. 0. !a(i),t(i),d(i),l(i)
|
|
-1.339252 1.5 1. 0.
|
|
-0.02273858 -0.75 2. 0.
|
|
0.2414973 0.0 2. 0.
|
|
-0.03321461 1.25 3. 0.
|
|
0.002203323 1.5 5. 0.
|
|
5.935588e-5 0.5 8. 0.
|
|
-1.137457e-6 2.5 8. 0.
|
|
-2.379299 1.5 3. 1.
|
|
2.337373 1.75 3. 1.
|
|
0.001242344 -0.25 8. 1.
|
|
-0.007352787 3.0 5. 1.
|
|
0.001965751 3.0 6. 1.
|
|
-0.1402666 4.0 1. 2.
|
|
-0.0209336 2.0 5. 2.
|
|
-2.475221e-4 -1.0 7. 2.
|
|
-0.01482723 2.0 2. 3.
|
|
-0.01303038 19.0 3. 3.
|
|
3.63467e-5 5.0 15. 3.
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CP2 !Ideal gas heat capacity function for propane of Miyamoto and Watanabe (2000).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Miyamoto, H., and Watanabe, K.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 8.314472 !Reducing parameters for T, Cp0
|
|
1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
4.021394 0.0
|
|
2.88998 387.69088
|
|
4.474243 1129.1386
|
|
10.48251 1864.95906
|
|
8.139803 4224.43701
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
BWR !MBWR equation of state for propane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.,
|
|
? "Thermophysical properties of fluids. II. Methane, ethane, propane,
|
|
? isobutane and normal butane,"
|
|
? J. Phys. Chem. Ref. Data, 16:577-798, 1987.
|
|
?
|
|
?The uncertainties in density are 0.1% in the liquid, 0.04% in the vapor
|
|
? and 1.5% in the supercritical and critical regions. The uncertainty is
|
|
? 2% for heat capacities, 1% for the speed of sound in the vapor, and 0.5%
|
|
? for the speed of sound in the liquid.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.47 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
17.36 !Maximum density [mol/L]
|
|
CP3 !Pointer to Cp0 model
|
|
44.0956 !Molar mass [g/mol]
|
|
85.47 !Triple point temperature [K]
|
|
1.685e-7 !Pressure at triple point [kPa]
|
|
16.617 !Density at triple point [mol/L]
|
|
231.063 !Normal boiling point temperature [K]
|
|
0.15243 !Acentric factor
|
|
369.85 4247.66 5.0 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
369.85 5.0 !Reducing parameters [K, mol/L]
|
|
5.0 !gamma
|
|
0.0831434 !Gas constant [L-bar/mol-K]
|
|
32 1 !Nterm, Ncoeff per term
|
|
-0.002804337729 1.180666107 -37.5632586
|
|
5624.374521 -935475.9605 -0.0004557405505
|
|
1.530044332 -1078.107476 221807.2099
|
|
0.6629473971e-4 -0.06199354447 67.54207966
|
|
0.00647283757 -0.6804325262 -97.26162355
|
|
0.05097956459 -0.0010046559 0.4363693352
|
|
-0.01249351947 264475.5879 -79442372.7
|
|
-7299.920845 538109500.3 34.50217377
|
|
9936.666689 -2.166699036 -161210.3424
|
|
-0.00363312699 11.08612343 -0.0001330932838
|
|
-0.03157701101 1.423083811
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CP3 !Ideal gas heat capacity function for propane of Younglove and Ely.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 8.31434 !Reducing parameters for T, Cp0
|
|
7 1 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
3125245.0099 -3.0
|
|
-114152.53638 -2.0
|
|
1497.165072 -1.0
|
|
-5.4041204338 0.0
|
|
0.039215452897 1.0
|
|
-0.000021738913926 2.0
|
|
4.8274541303e-9 3.0
|
|
3.1907016349 1500.0
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
FES !Helmholtz equation of state for propane of Span and Wagner (2003).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Span, R. and Wagner, W.
|
|
? "Equations of State for Technical Applications. II. Results for Nonpolar Fluids,"
|
|
? Int. J. Thermophys., 24(1):41-109, 2003. doi: 10.1023/A:1022310214958
|
|
?
|
|
?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.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.47 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
17.36 !Maximum density [mol/L]
|
|
CPS !Pointer to Cp0 model
|
|
44.097 !Molar mass [g/mol]
|
|
85.47 !Triple point temperature [K]
|
|
0.00000015304 !Pressure at triple point [kPa]
|
|
16.706 !Density at triple point [mol/L]
|
|
231.08 !Normal boiling point temperature [K]
|
|
0.153 !Acentric factor
|
|
369.825 4248.0 4.9998866 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
369.825 4.9998866 !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
|
|
1.0403973 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
|
-2.8318404 1.125 1. 0.
|
|
0.84393810 1.5 1. 0.
|
|
-0.076559592 1.375 2. 0.
|
|
0.094697373 0.25 3. 0.
|
|
0.00024796475 0.875 7. 0.
|
|
0.27743760 0.625 2. 1.
|
|
-0.043846001 1.75 5. 1.
|
|
-0.26991065 3.625 1. 2.
|
|
-0.069313413 3.625 4. 2.
|
|
-0.029632146 14.5 3. 3.
|
|
0.014040127 12.0 4. 3.
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CPS !Ideal gas heat capacity function for propane of Jaeschke and Schley (1995).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Jaeschke, M. and Schley, P.
|
|
? "Ideal-Gas Thermodynamic Properties for Natural-Gas Applications,"
|
|
? Int. J. Thermophys., 16(6):1381-1392, 1995. doi: 10.1007/BF02083547
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 8.31451 !Reducing parameters for T, Cp0
|
|
1 0 2 2 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
4.02939 0.0
|
|
129024.5 -2.0 200.893 -1.0 -2.0
|
|
-8835886.0 -2.0 1027.29 -1.0 -2.0
|
|
1521038.0 -2.0 479.856 -1.0 -2.0
|
|
17515110.0 -2.0 955.312 -1.0 -2.0
|
|
|
|
|
|
|
|
|
|
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
|
|
|
#ETA !---Viscosity---
|
|
VS7 !Pure fluid viscosity model for propane of Vogel and Herrmann (2016).
|
|
:DOI: 10.1063/1.4966928
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Vogel, E. and Herrmann, S.,
|
|
? "New Formulation for the Viscosity of Propane,"
|
|
? J. Phys. Chem. Ref. Data, 45, 043103, 2016.
|
|
? doi: 10.1063/1.4966928
|
|
?
|
|
?The viscosity at low pressures (< 0.2 MPa) has an expanded uncertainty
|
|
? (at 95% confidence) of 0.5% for 273 < T < 625 K.
|
|
? The uncertainty is 1.5% for the vapor phase at subcritical temperatures T = 273 K
|
|
? as well as in the supercritical thermodynamic region T = 423 K at pressures
|
|
? up to 30 MPa. For additional information on uncertainty consult the referenced manuscript.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.525 !Lower temperature limit [K]
|
|
650.0 !Upper temperature limit [K]
|
|
1000000.0 !Upper pressure limit [kPa]
|
|
20.6 !Maximum density [mol/L]
|
|
NUL !Omega model
|
|
!
|
|
!Dilute gas function
|
|
$DG RED SUM:4
|
|
!
|
|
!Residual function
|
|
$RF RED SUM:11 CMPLX:2 +
|
|
!
|
|
!Coefficients
|
|
$CF
|
|
1.0 369.89 1. 0. 0 !Reducing parameters for eta, T, rho
|
|
9.9301297115406 1. 0. 0. 0 !Dilute gas terms
|
|
0.72658798096248 2. 0. 0. 0
|
|
-0.74692506744427 3. 0. 0. 0
|
|
0.10156334572774 4. 0. 0. 0
|
|
!Simple polynomial/exponential terms
|
|
1.0 369.89 4.999997732 0. 0 !Reducing parameters for eta, T, rho
|
|
12.514603628320 0. 1. 0. 0
|
|
1.5922183980545 0. 2. 0. 0
|
|
-0.017976570855233 -3. 4. 0. 0
|
|
0.099769818327437 0. 7. 0. 0
|
|
1.0361434810683e-5 -2. 14. 0. 0
|
|
-1.4863884140117e-9 -6. 19. 0. 0
|
|
4.840568643174e-10 -6. 20. 0. 0
|
|
-13.029665878806 -1. 1. 0. 1
|
|
1.8734125698089 -2. 1. 0. 1
|
|
2.3303894474483 -1. 4. 0. 1
|
|
3.4631192496757 0. 5. 0. 1
|
|
^12TERMS !Complex polynomial/exponential terms
|
|
3.2587396573174 1. 1. 2. 1. -20. -250. 1. 1. 0. 0. 0.
|
|
0.21724931048783 1. 1. 2. 1. -100. -100. 1. 1. 0. 0. 0.
|
|
^END12TERMS
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
|
|
|
|
================================================================================
|
|
|
|
#TCX !---Thermal conductivity---
|
|
TC1 !Pure fluid thermal conductivity model for propane of Marsh et al. (2002).
|
|
:DOI: 10.1021/je010001m
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Marsh, K., Perkins, R., and Ramires, M.L.V.,
|
|
? "Measurement and Correlation of the Thermal Conductivity of Propane
|
|
? from 86 to 600 K at Pressures to 70 MPa,"
|
|
? J. Chem. Eng. Data, 47(4):932-940, 2002.
|
|
?
|
|
?Uncertainty in thermal conductivity is 3%, except in the critical region
|
|
? and dilute gas which have an uncertainty of 5%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.47 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
20.6 !Maximum density [mol/L]
|
|
3 0 !# terms for dilute gas function: numerator, denominator
|
|
369.85 1.0 !Reducing parameters for T, tcx
|
|
-0.00124778 0. !Coefficient, power in T
|
|
0.00816371 1.
|
|
0.0199374 2.
|
|
10 0 !# terms for background gas function: numerator, denominator
|
|
369.85 5. 1. !Reducing parameters for T, rho, tcx
|
|
-0.03695 0. 1. 0. !Coefficient, powers of t, rho, spare for future use
|
|
0.0482798 1. 1. 0.
|
|
0.148658 0. 2. 0.
|
|
-0.135636 1. 2. 0.
|
|
-0.119986 0. 3. 0.
|
|
0.117588 1. 3. 0.
|
|
0.0412431 0. 4. 0.
|
|
-0.0436911 1. 4. 0.
|
|
-0.00486905 0. 5. 0.
|
|
0.00616079 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 propane of Marsh et al. (2002).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Marsh, K., Perkins, R., and Ramires, M.L.V., 2002.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
9 0 0 0 !# terms: 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) [-]
|
|
0.716635e-9 !Qd_inverse (modified effective cutoff parameter) [m]
|
|
554.73 !Tref (reference temperature) [K]
|
|
|
|
|
|
|
|
|
|
********************************************************************************
|
|
|
|
@TCX !---Thermal conductivity---
|
|
TC2 !Pure fluid thermal conductivity model for propane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.,
|
|
? "Thermophysical properties of fluids. II. Methane, ethane, propane,
|
|
? isobutane and normal butane,"
|
|
? J. Phys. Chem. Ref. Data, 16:577-798, 1987.
|
|
?
|
|
?The uncertainty in thermal conductivity is 2%, except in the critical region
|
|
? which is 10%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.47 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
17.36 !Maximum density [mol/L]
|
|
CI2 !Pointer to collision integral model
|
|
0.47 !Lennard-Jones coefficient sigma [nm]
|
|
358.9 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
0.177273976 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12
|
|
1.422605 !Dilute gas terms (Eq 27): Gt(1)
|
|
-0.179749 ! Gt(2)
|
|
0.003113890422 !Residual terms (Eqs 26, 28-30): Et(1)
|
|
-0.2257559730
|
|
56.74370999
|
|
-0.7840963643e-4
|
|
0.02291785465
|
|
-2.52793989
|
|
-0.06265334654
|
|
2.518064809 !Et(8)
|
|
TK2 !Pointer to critical enhancement model (follows immediately)
|
|
3.98 !Critical enhancement terms (Eqs D1-D4): X1
|
|
5.450
|
|
0.468067
|
|
1.08 !X4
|
|
8.117e-10 !Z
|
|
1.38054e-23 !Boltzmann's constant, k
|
|
0.0 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1)
|
|
0.0 !Fv(2)
|
|
1.12 !Fv(3)
|
|
359.0 !Fv(4)
|
|
-14.113294896 !Coefficients for residual viscosity, eqs (22 - 25)
|
|
968.22940153 !Ev(2) (the viscosity is also used in conductivity correlation)
|
|
13.686545032 !Ev(3)
|
|
-12511.628378 !Ev(4)
|
|
0.0168910864 !Ev(5)
|
|
43.527109444 !Ev(6)
|
|
7659.4543472 !Ev(7)
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS1 !Pure fluid viscosity model for propane of Vogel et al. (1998).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Vogel, E., Kuechenmeister, C., Bich, E., and Laesecke, A.,
|
|
? "Reference Correlation of the Viscosity of Propane,"
|
|
? J. Phys. Chem. Ref. Data, 27(5):947-970, 1998.
|
|
?
|
|
?The uncertainty in viscosity varies from 0.4% in the dilute gas between
|
|
? room temperature and 600 K, to about 2.5% from 100 to 475 K up to about 30 MPa,
|
|
? and to about 4% outside this range.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.47 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
20.6 !Maximum density [mol/L]
|
|
1 !Number of terms associated with dilute-gas function
|
|
CI1 !Pointer to reduced effective collision cross-section model
|
|
0.49748 !Lennard-Jones coefficient sigma [nm]
|
|
263.88 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
1.0 1.0 !Reducing parameters for T, eta
|
|
0.141824 0.5 !Chapman-Enskog term
|
|
9 !Number of terms for initial density dependence
|
|
263.88 0.0741445 !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
|
|
2471.01251 -0.75
|
|
-3375.1717 -1.0
|
|
2491.6597 -1.25
|
|
-787.26086 -1.5
|
|
14.085455 -2.5
|
|
-0.34664158 -5.5
|
|
2 13 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
|
|
369.82 5.0 1.0 !Reducing parameters for T, rho, eta
|
|
2.50053938863 0.0 0. 0. 0
|
|
2.15175430074 0.5 0. 0. 0
|
|
35.9873030195 0.0 2. 0. 0
|
|
-180.512188564 -1.0 2. 0. 0
|
|
87.7124888223 -2.0 2. 0. 0
|
|
-105.773052525 0.0 3. 0. 0
|
|
205.319740877 -1.0 3. 0. 0
|
|
-129.210932610 -2.0 3. 0. 0
|
|
58.9491587759 0.0 4. 0. 0
|
|
-129.740033100 -1.0 4. 0. 0
|
|
76.6280419971 -2.0 4. 0. 0
|
|
-9.59407868475 0.0 5. 0. 0
|
|
21.0726986598 -1.0 5. 0. 0
|
|
-14.3971968187 -2.0 5. 0. 0
|
|
-1616.88405374 0.0 1. -1. 0
|
|
1616.88405374 0.0 1. 0. 0
|
|
1.0 0.0 0. 1. 0
|
|
-1.0 0.0 1. 0. 0
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
@AUX !---Auxiliary function for the collision integral
|
|
CI1 !Collision integral model for propane of Vogel et al. (1998).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Vogel, E., Kuechenmeister, C., Bich, E., and Laesecke, A.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
3 !Number of terms
|
|
0.25104574 0 !Coefficient, power of Tstar
|
|
-0.47271238 1
|
|
0.060836515 3
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS2 !Pure fluid viscosity model for propane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.,
|
|
? "Thermophysical properties of fluids. II. Methane, ethane, propane,
|
|
? isobutane and normal butane,"
|
|
? J. Phys. Chem. Ref. Data, 16:577-798, 1987.
|
|
?
|
|
?The uncertainty in viscosity is 2%, except in the critical region which is 5%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.47 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
17.36 !Maximum density [mol/L]
|
|
CI2 !Pointer to collision integral model
|
|
0.47 !Lennard-Jones coefficient sigma [nm]
|
|
358.9 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
0.177273976 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12
|
|
0.5 !Exponent in Eq 19 for T
|
|
0.0 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1)
|
|
0.0 !Fv(2)
|
|
1.12 !Fv(3)
|
|
359.0 !Fv(4)
|
|
-14.113294896 !Coefficients for residual viscosity, eqs (22 - 25)
|
|
968.22940153 !Ev(2)
|
|
13.686545032 !Ev(3)
|
|
-12511.628378 !Ev(4)
|
|
0.0168910864 !Ev(5)
|
|
43.527109444 !Ev(6)
|
|
7659.45434720 !Ev(7)
|
|
5.0 !Ev(8)
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
@AUX !---Auxiliary function for the collision integral
|
|
CI2 !Collision integral model for propane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
9 !Number of terms
|
|
-3.0328138281 0 !Omega (eq 20): coeffs of {(e/kT)**((4-n)/3)}
|
|
16.918880086 0 !There is misprint in Younglove and Ely, the exponent
|
|
-37.189364917 0 ! is ((4-n)/3) not ((n+2)/3)
|
|
41.288861858 0
|
|
-24.61592114 0
|
|
8.948843096 0
|
|
-1.8739245042 0
|
|
0.209661014 0 !Wrong sign in Younglove and Ely, Table 2
|
|
-0.009657044 0
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS4 !Pure fluid generalized friction theory viscosity model for propane of Quinones-Cisneros and Deiters (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Quinones-Cisneros, S.E. and Deiters, U.K.,
|
|
? "Generalization of the Friction Theory for Viscosity Modeling,"
|
|
? J. Phys. Chem. B, 110(25):12820-12834, 2006. doi: 10.1021/jp0618577
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.47 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
55000.0 !Upper pressure limit [kPa]
|
|
17.36 !Maximum density [mol/L]
|
|
4 0 0 0 0 0 !Number of terms associated with dilute-gas function
|
|
NUL !Pointer to reduced effective collision cross-section model; not used
|
|
0.47 !Lennard-Jones coefficient sigma [nm];not used
|
|
358.9 !Lennard-Jones coefficient epsilon/kappa [K];not used
|
|
369.825 1.0 !Reducing parameters for T, eta
|
|
0.0 0.5 !Chapman-Enskog term; not used here
|
|
12.3057 0.0 !Empirical terms for eta0
|
|
-42.5793 0.25
|
|
40.3486 0.50
|
|
0 !Number of terms for initial density dependence
|
|
-9.34267734206329e-6 -4.93309341792654e-5 1.46749885301233e-13 0. 0. ! a(0),a(1),a(2)
|
|
9.60710434008784e-5 -8.18030722274335e-5 3.00126073333685e-12 0. 0. ! b(0),b(1),b(2)
|
|
7.68800436177747e-5 -4.18871321795657e-5 -7.2008794976648e-15 0. 0. ! c(0),c(1),c(2)
|
|
-8.49308621313605e-9 -4.91414639525551e-10 0.0 0. 0. ! A(0),A(1),A(2)
|
|
2.08794813407621e-8 9.21785453914614e-10 0.0 0. 0. ! B(0),B(1),B(2)
|
|
-4.0594410922187e-7 1.31730904193479e-7 0.0 0. 0. ! C(0),C(1),C(2)
|
|
0.0 0.0 0.0 0. 0. ! D(0),D(1),D(2)
|
|
0.0 0.0 0.0 0. 0. ! E(0),E(1),E(2)
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
|
|
|
|
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
|
|
|
@TRN !---ECS Transport---
|
|
ECS !Extended Corresponding States model (R134a reference); fitted to data for propane.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Klein, S.A., McLinden, M.O., and Laesecke, A., "An Improved Extended Corresponding States Method for Estimation of Viscosity of Pure Refrigerants and Mixtures," Int. J. Refrigeration, 20(3):208-217, 1997. doi: 10.1016/S0140-7007(96)00073-4.
|
|
?McLinden, M.O., Klein, S.A., and Perkins, R.A., "An Extended Corresponding States Model for the Thermal Conductivity of Refrigerants and Refrigerant Mixtures," Int. J. Refrigeration, 23(1):43-63, 2000. doi: 10.1016/S0140-7007(99)00024-9
|
|
?
|
|
?THERMAL CONDUCTIVITY
|
|
? The ECS parameters for thermal conductivity were based on the data of:
|
|
? Aggarwal, M.C. and Springer, G.S., "High temperature-high pressure thermal conductivities of ethylene and propane," J. Chem. Phys., 70:3948-3951, 1979.
|
|
? Mann, W.B. and Dickins, B.G., "The thermal conductivities of the saturated hydrocarbons in the gaseous state," Proc. Royal Soc. (London), Series A134:77-96, 1932.
|
|
? Roder, H.M., "Experimental thermal conductivity values for hydrogen, methane, ethane and propane," National Bureau of Standards NBSIR 84-3006, 1984.
|
|
? Tufeu, R. and LeNeindre, B., "Thermal conductivity of propane in the temperature range 25-305øC and pressure range 1-70 MPa," Int. J. Thermophys., 8:27-38, 1987.
|
|
? Average absolute deviations of the fit from the experimental data are:
|
|
? Aggarwal: 2.89%; Mann: 0.23%; Roder: 1.18%; Tufeu: 3.13%; Overall: 1.86%
|
|
?
|
|
?The Lennard-Jones parameters were taken from Vogel, E., Kuchenmeister, C., Bich, E., and Laesecke, A., "Reference correlation of the viscosity of propane," J. Phys. Chem. Ref. Data, 27:947-970, 1998.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.47 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
17.36 !Maximum density [mol/L]
|
|
FEQ R134A.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)
|
|
0.49748 !Lennard-Jones coefficient sigma [nm] for ECS method
|
|
263.88 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
|
|
2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
|
|
0.0010398 0. 0. 0. !Coefficient, power of T, spare1, spare2
|
|
5.4024e-7 1. 0. 0. !Coefficient, power of T, spare1, spare2
|
|
1 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
|
|
1.0 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
|
2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
|
0.81477 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
|
0.051039 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 propane of Mulero et al. (2012).
|
|
:DOI: 10.1063/1.4768782
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Mulero, A., Cachadiña, 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. !
|
|
2 !Number of terms in surface tension model
|
|
369.89 !Critical temperature used in fit (dummy)
|
|
0.05334 1.235 !Sigma0 and n
|
|
-0.01748 4.404
|
|
|
|
|
|
#DE !---Dielectric constant---
|
|
DE4 !Dielectric constant model for propane of Harvey and Lemmon (2005).
|
|
:DOI: 10.1007/s10765-005-2351-5
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Harvey, A.H. and Lemmon, E.W.,
|
|
? "Method for Estimating the Dielectric Constant of Natural Gas Mixtures,"
|
|
? Int. J. Thermophys., 26(1):31-46, 2005. doi: 10.1007/s10765-005-2351-5
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
273.16 1000.0 1.0 !Reducing parameters for T and D
|
|
1 2 4 0 0 0 !Number of terms in dielectric constant model
|
|
0.1573071 -1. 1. 0. !Coefficient, T exp, D exp
|
|
15.850 0. 1. 0.
|
|
0.036 1. 1. 0.
|
|
172.75 0. 2. 0.
|
|
505.67 1. 2. 0.
|
|
-388.21 0. 2.35 0.
|
|
-2078.8 1. 2.35 0.
|
|
|
|
|
|
#MLT !---Melting line---
|
|
ML1 !Melting line model for propane of Reeves et al. (1964).
|
|
:DOI: 10.1063/1.1725068
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Reeves, L.E., Scott, G.J., and Babb, S.E., Jr.,
|
|
? "Melting Curves of Pressure-Transmitting Fluids,"
|
|
? J. Chem. Phys., 40(12):3662-6, 1964.
|
|
?
|
|
?Coefficients have been modified, 2004.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
85.525 !Lower temperature limit [K]
|
|
2000.0 !Upper temperature limit [K]
|
|
0. !
|
|
0. !
|
|
85.525 0.00000017205 !Reducing temperature and pressure
|
|
2 0 0 0 0 0 !Number of terms in melting line equation
|
|
-4230000000000. 0. !Coefficients and exponents
|
|
4230000000001. 1.283
|
|
|
|
|
|
#PS !---Vapor pressure---
|
|
PS5 !Vapor pressure equation for propane of Gao and Lemmon (2017).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Gao, K. and Lemmon, E.W., 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. !
|
|
369.89 4251.2 !Reducing parameters
|
|
5 0 0 0 0 0 !Number of terms in equation
|
|
-6.7524 1.0
|
|
1.6741 1.5
|
|
-0.97245 2.0
|
|
-2.6052 4.1
|
|
-0.72255 16.5
|
|
|
|
|
|
#DL !---Saturated liquid density---
|
|
DL1 !Saturated liquid density equation for propane of Lemmon et al. (2009).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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. !
|
|
369.89 5.0 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
1.82205 0.345
|
|
0.65802 0.74
|
|
0.21109 2.6
|
|
0.083973 7.2
|
|
|
|
|
|
#DV !---Saturated vapor density---
|
|
DV3 !Saturated vapor density equation for propane of Gao and Lemmon (2017).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Gao, K. and Lemmon, E.W., 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. !
|
|
369.89 5.0 !Reducing parameters
|
|
6 0 0 0 0 0 !Number of terms in equation
|
|
-2.6016 0.385
|
|
-5.5659 1.13
|
|
-15.487 3.0
|
|
-45.572 6.6
|
|
-95.789 14.5
|
|
-207.58 30.0
|
|
|
|
|
|
@END
|
|
c 1 2 3 4 5 6 7 8
|
|
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|