1033 lines
50 KiB
Plaintext
1033 lines
50 KiB
Plaintext
Methane !Short name
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74-82-8 !CAS number
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Methane !Full name
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CH4 !Chemical formula {CH4}
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R-50 !Synonym
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16.0428 !Molar mass [g/mol]
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90.6941 !Triple point temperature [K]
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111.667 !Normal boiling point [K]
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190.564 !Critical temperature [K]
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4599.2 !Critical pressure [kPa]
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10.139 !Critical density [mol/L]
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0.01142 !Acentric factor
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0.0 !Dipole moment [Debye]; (exactly zero due to symmetry)
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NBP !Default reference state
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10.0 !Version number
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1971, 1972 !UN Number :UN:
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n-alkane !Family :Family:
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890.58 !Heating value (upper) at 25 C [kJ/mol] (ISO 6976:2016) :Heat:
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25. !GWP (IPCC 2007) :GWP:
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A3 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/CH4/h1H4 !Standard InChI String :InChi:
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VNWKTOKETHGBQD-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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???? !Alternative fluid for mixing rules :AltID:
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8ae7a700 !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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! 01-22-97 EWL, Original version.
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! 06-24-98 EWL, Add Younglove and Ely BWR equation of state.
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! 11-18-98 EWL, Add equation of state of Friend et al. (1989).
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! 11-01-99 EWL, Add Span 12 term short equation of state.
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! 01-26-00 EWL, Add Friend transport equations, but keep Younglove viscosity eq. as default since Friend eq. has an anomaly above 100 MPa.
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! 07-23-02 EWL, Add sublimation line.
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! 08-05-04 EWL, Add Harvey and Lemmon dielectric correlation.
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! 10-13-04 MLH, Add family.
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! 07-14-05 MLH, Add Vogel(2000) viscosity correlation.
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! 12-02-06 MLH, Update LJ for ECS.
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! 01-05-07 MLH, Add VS4 model, new VS1 model of Vogel, moved Friend VS1 model to EOF.
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! 03-05-07 EWL, Add ancillary equations.
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! 03-09-07 MLH, Add final FT model coefficients.
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! 02-14-08 MLH, Add TK6 block for ECS for mixture calculations.
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! 09-02-10 MLH, Add new VS4 model for viscosity feb2010 model.
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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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! 05-15-17 EWL, Change the hard coded CH4 model to the TK7 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 methane of Setzmann and Wagner (1991).
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:TRUECRITICALPOINT: 190.564 10.139128 !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: 10.1063/1.555898
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Setzmann, U. and Wagner, W.,
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? "A New Equation of State and Tables of Thermodynamic Properties for Methane
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? Covering the Range from the Melting Line to 625 K at Pressures up to 1000 MPa,"
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? J. Phys. Chem. Ref. Data, 20(6):1061-1151, 1991.
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?
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?The uncertainties in density are 0.03% for pressures below 12 MPa and
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? temperatures below 350 K and up to 0.07% for pressures less than 50 MPa.
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? For the speed of sound, the uncertainty ranges from 0.03% (in the vapor
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? phase) to 0.3% depending on temperature and pressure. Heat capacities
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? may be generally calculated within an uncertainty of 1%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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90.6941 !Lower temperature limit [K]
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625.0 !Upper temperature limit [K]
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1000000.0 !Upper pressure limit [kPa]
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40.072 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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16.0428 !Molar mass [g/mol]
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90.6941 !Triple point temperature [K]
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11.696 !Pressure at triple point [kPa]
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28.142 !Density at triple point [mol/L]
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111.667 !Normal boiling point temperature [K]
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0.01142 !Acentric factor
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190.564 4599.2 10.139128 !Tc [K], pc [kPa], rhoc [mol/L]
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190.564 10.139128 !Reducing parameters [K, mol/L]
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8.31451 !Gas constant [J/mol-K]
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36 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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0.04367901028 -0.5 1. 0. !a(i),t(i),d(i),l(i)
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0.6709236199 0.5 1. 0.
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-1.765577859 1.0 1. 0.
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0.8582330241 0.5 2. 0.
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-1.206513052 1.0 2. 0.
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0.512046722 1.5 2. 0.
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-0.0004000010791 4.5 2. 0.
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-0.01247842423 0.0 3. 0.
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0.03100269701 1.0 4. 0.
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0.001754748522 3.0 4. 0.
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-0.3171921605e-5 1.0 8. 0.
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-0.224034684e-5 3.0 9. 0.
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0.2947056156e-6 3.0 10. 0.
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0.1830487909 0.0 1. 1.
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0.1511883679 1.0 1. 1.
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-0.4289363877 2.0 1. 1.
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0.06894002446 0.0 2. 1.
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-0.01408313996 0.0 4. 1.
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-0.0306305483 2.0 5. 1.
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-0.02969906708 2.0 6. 1.
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-0.01932040831 5.0 1. 2.
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-0.1105739959 5.0 2. 2.
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0.09952548995 5.0 3. 2.
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0.008548437825 2.0 4. 2.
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-0.06150555662 4.0 4. 2.
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-0.04291792423 12.0 3. 3.
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-0.0181320729 8.0 5. 3.
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0.0344590476 10.0 5. 3.
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-0.00238591945 10.0 8. 3.
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-0.01159094939 10.0 2. 4.
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0.06641693602 14.0 3. 4.
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-0.0237154959 12.0 4. 4.
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-0.03961624905 18.0 4. 4.
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-0.01387292044 22.0 4. 4.
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0.03389489599 18.0 5. 4.
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-0.002927378753 14.0 6. 4.
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0.9324799946e-4 2.0 2. 2. 2. -20.0 -200.0 1.07 1.0 0. 0. 0.
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-6.287171518 0.0 0. 2. 2. -40.0 -250.0 1.11 1.0 0. 0. 0.
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12.71069467 1.0 0. 2. 2. -40.0 -250.0 1.11 1.0 0. 0. 0.
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-6.423953466 2.0 0. 2. 2. -40.0 -250.0 1.11 1.0 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 methane of Setzmann and Wagner (1991).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Setzmann, U. and Wagner, W., 1991.
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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 8.31451 !Reducing parameters for T, Cp0
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1 5 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.0016 0.0
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0.008449 648.0
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4.6942 1957.0
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3.4865 3895.0
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1.6572 5705.0
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1.4115 15080.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for methane of Setzmann and Wagner (1991).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Setzmann, U. and Wagner, W., 1991.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 2 5 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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3.0016 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-2.9705496667947529 0.0 !aj, ti for [ai*tau**ti] terms
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2.8907453831087553 1.0 !aj, ti for [ai*tau**ti] terms
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0.008449 648.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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4.6942 1957.0
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3.4865 3895.0
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1.6572 5705.0
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1.4115 15080.0
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#AUX !---Auxiliary function for PH0
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PH0 !Ideal gas Helmholtz form for methane.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Setzmann, U. and Wagner, W., 1991.
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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 5 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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3.0016 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-2.9705496668 0.0 !aj, ti for [ai*tau**ti] terms
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2.8907453831 1.0
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0.008449 -3.4004324007 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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4.6942 -10.2695157532
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3.4865 -20.43932747
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1.6572 -29.9374488361
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1.4115 -79.1335194475
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FEK !Helmholtz equation of state for methane 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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90.6941 !Lower temperature limit [K]
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625.0 !Upper temperature limit [K]
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1000000.0 !Upper pressure limit [kPa]
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40.072 !Maximum density [mol/L]
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PHK !Pointer to Cp0 model
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16.04246 !Molar mass [g/mol]
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90.6941 !Triple point temperature [K]
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11.698 !Pressure at triple point [kPa]
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28.146 !Density at triple point [mol/L]
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111.66 !Normal boiling point temperature [K]
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0.0114 !Acentric factor
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190.564 4599.2 10.139342719 !Tc [K], pc [kPa], rhoc [mol/L]
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190.564 10.139342719 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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24 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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0.57335704239162 0.125 1. 0.
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-1.6760687523730 1.125 1. 0.
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0.23405291834916 0.375 2. 0.
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-0.21947376343441 1.125 2. 0.
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0.016369201404128 0.625 4. 0.
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0.01500440638928 1.5 4. 0.
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0.098990489492918 0.625 1. 1.
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0.58382770929055 2.625 1. 1.
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-0.74786867560390 2.75 1. 1.
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0.30033302857974 2.125 2. 1.
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0.20985543806568 2.0 3. 1.
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-0.018590151133061 1.75 6. 1.
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-0.15782558339049 4.50 2. 2.
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0.12716735220791 4.75 3. 2.
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-0.032019743894346 5.0 3. 2.
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-0.068049729364536 4.0 4. 2.
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0.024291412853736 4.5 4. 2.
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0.0051440451639444 7.5 2. 3.
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-0.019084949733532 14.0 3. 3.
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0.0055229677241291 11.5 4. 3.
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-0.0044197392976085 26.0 5. 6.
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0.040061416708429 28.0 6. 6.
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-0.033752085907575 30.0 6. 6.
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-0.0025127658213357 16.0 7. 6.
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@AUX !---Auxiliary function for PH0
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PHK !Ideal gas Helmholtz form for methane 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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?
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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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3.00088 1.0 !ai, ti for [ai*log(tau**ti)] terms
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19.597508817 0.0 !aj, ti for [ai*tau**ti] terms
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-83.959667892 1.0
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-0.0046 0.936220902 !aj, ti for cosh and sinh terms
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4.46921 5.722644361
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0.76315 4.306474465
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8.74432 5.577233895
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@EOS !---Equation of state---
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FE1 !Helmholtz equation of state for methane of Friend et al. (1989).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Friend, D.G., Ely, J.F., and Ingham, H.,
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? "Thermophysical Properties of Methane,"
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? J. Phys. Chem. Ref. Data, 18(2):583-638, 1989.
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?
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!```````````````````````````````````````````````````````````````````````````````
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90.6854 !Lower temperature limit [K]
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620.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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29.714 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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16.043 !Molar mass [g/mol]
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90.6854 !Triple point temperature [K]
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11.694 !Pressure at triple point [kPa]
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28.145 !Density at triple point [mol/L]
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111.66 !Normal boiling point temperature [K]
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0.0086 !Acentric factor
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190.551 4599.2 10.139 !Tc [K], pc [kPa], rhoc [mol/L]
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190.551 10.139 !Reducing parameters [K, mol/L]
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8.31451 !Gas constant [J/mol-K]
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32 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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0.384436099659 0.0 1. 0. !a(i),t(i),d(i),l(i)
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-1.796925988 1.5 1. 0.
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0.329444947369 2.5 1. 0.
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0.0226312728442 -0.5 2. 0.
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0.0759236768798 1.5 2. 0.
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0.0693758447259 2.0 2. 0.
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0.0241163263947 0.0 3. 0.
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0.0107009920854 1.0 3. 0.
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-0.0380933275164 2.5 3. 0.
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0.000471537561143 0.0 6. 0.
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0.000556607678805 2.0 7. 0.
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0.548759346533e-6 5.0 7. 0.
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-0.999632699967e-4 2.0 8. 0.
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-0.128087979280 5.0 1. 2.
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0.0380198873377 6.0 1. 2.
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0.139226650551 3.5 2. 2.
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-0.0874996348859 5.5 2. 2.
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-0.0033489416576 3.0 3. 2.
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-0.0517576297122 7.0 3. 2.
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0.0252835179116 6.0 5. 2.
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0.00051870320595 8.5 6. 2.
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-0.00166770594525 4.0 7. 2.
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-0.000607401927389 6.5 8. 2.
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-0.972915359991e-4 5.5 10. 2.
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-0.298844010462e-4 22.0 2. 4.
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-0.0130940111124 11.0 3. 4.
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0.0198175833798 18.0 3. 4.
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0.0208465762327 11.0 4. 4.
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-0.0358025052631 23.0 4. 4.
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-0.203486851741 17.0 5. 4.
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0.215964755088 18.0 5. 4.
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-0.00429340628249 23.0 5. 4.
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for methane.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Friend, D.G., Ely, J.F., and Ingham, H.,
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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 8.31451 !Reducing parameters for T, Cp0
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4 1 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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3.5998324 0.0
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0.2614717613495 0.3333333333333
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-0.05671028952515 0.6666666666667
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0.004105505612671 1.0
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4.7206715 2009.15202
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@EOS !---Equation of state---
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FES !Helmholtz equation of state for methane of Span and Wagner (2003).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Span, R. and Wagner, W.
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? "Equations of State for Technical Applications. II. Results for Nonpolar Fluids,"
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? Int. J. Thermophys., 24(1):41-109, 2003. doi: 10.1023/A:1022310214958
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?
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?The uncertainties of the equation of state are approximately 0.2% (to
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? 0.5% at high pressures) in density, 1% (in the vapor phase) to 2% in
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? heat capacity, 1% (in the vapor phase) to 2% in the speed of sound, and
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? 0.2% in vapor pressure, except in the critical region.
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?
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!```````````````````````````````````````````````````````````````````````````````
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90.6941 !Lower temperature limit [K]
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600.0 !Upper temperature limit [K]
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100000.0 !Upper pressure limit [kPa]
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40.072 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
|
|
16.043 !Molar mass [g/mol]
|
|
90.6941 !Triple point temperature [K]
|
|
11.661 !Pressure at triple point [kPa]
|
|
28.167 !Density at triple point [mol/L]
|
|
111.66 !Normal boiling point temperature [K]
|
|
0.011 !Acentric factor
|
|
190.564 4599.0 10.139001 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
190.564 10.139001 !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
|
|
0.89269676 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
|
-2.5438282 1.125 1. 0.
|
|
0.64980978 1.5 1. 0.
|
|
0.020793471 1.375 2. 0.
|
|
0.070189104 0.25 3. 0.
|
|
0.00023700378 0.875 7. 0.
|
|
0.16653334 0.625 2. 1.
|
|
-0.043855669 1.75 5. 1.
|
|
-0.1572678 3.625 1. 2.
|
|
-0.035311675 3.625 4. 2.
|
|
-0.029570024 14.5 3. 3.
|
|
0.014019842 12.0 4. 3.
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
BWR !MBWR equation of state for methane 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.
|
|
? All temperatures on IPTS-68
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.68 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
200000.0 !Upper pressure limit [kPa]
|
|
36.2029 !Maximum density [mol/L]
|
|
CP2 !Pointer to Cp0 model
|
|
16.043 !Molar mass [g/mol]
|
|
90.68 !Triple point temperature [K]
|
|
11.744 !Pressure at triple point [kPa]
|
|
28.147 !Density at triple point [mol/L]
|
|
111.667 !Normal boiling point temperature [K]
|
|
0.011 !Acentric factor
|
|
190.53 4597.97 10.15 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
190.53 10.15 !Reducing parameters [K, mol/L]
|
|
10.15 !gamma
|
|
0.0831434 !Gas constant [L-bar/mol-K]
|
|
32 1 !Nterm, Ncoeff per term
|
|
0.9898937956e-4 0.2199608275 -5.322788
|
|
202.1657962 -22343.98926 0.000106794028
|
|
0.001457922469 -9.265816666 2915.364732
|
|
0.2313546209e-5 0.001387214274 0.04780467451
|
|
0.0001176103833 -0.00198209673 -0.2512887756
|
|
0.9748899826e-4 -0.1202192137e-5 0.0004128353939
|
|
-0.7215842918e-5 5081.738255 -919890.3192
|
|
-27.32264677 749902.4351 0.01114060908
|
|
10.83955159 -0.0004490960312 -13.80337847
|
|
-0.2371902232e-6 0.0003761652197 -0.2375166954e-8
|
|
-0.123764079e-6 0.6766926453e-5
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CP2 !Ideal gas heat capacity function for methane 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
|
|
-1804475.0507 -3.0
|
|
77426.666393 -2.0
|
|
-1324.1658754 -1.0
|
|
15.438149595 0.0
|
|
-0.051479005257 1.0
|
|
0.00010809172196 2.0
|
|
-0.65501783437e-7 3.0
|
|
-6.7490056171 3000.0
|
|
|
|
|
|
|
|
|
|
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
|
|
|
#ETA !---Viscosity---
|
|
VS4 !Pure fluid generalized friction theory viscosity model for methane of Quinones-Cisneros et al. (2011). unpublished
|
|
:DOI:
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Quinones-Cisneros, S.E., Huber, M.L., and Deiters, U.K.,
|
|
? unpublished work, 2011.
|
|
?
|
|
?Detailed uncertainty analysis will be found in a future publication; however
|
|
? in general the estimated uncertainty in viscosity varies from less than 0.3%
|
|
? between 200-400 K for pressures less than 30 MPa, to less than 2% over the
|
|
? rest of the fluid surface up to 100 MPa, increasing up to 5%
|
|
? for 100 to 500 MPa, and 10% at 500 to 1000 MPa for temperatures to 625 K.
|
|
? Above uncertainties are valid when used with the equation of state of
|
|
? Setzmann, U. and Wagner, W., J. Phys. Chem. Ref. Data, 20(6):1061-1151, 1991.
|
|
? The use of other equations of state may result in larger uncertainties.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.68 !Lower temperature limit [K]
|
|
1200.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
40.072 !Maximum density [mol/L]
|
|
6 0 0 0 0 0 !Number of terms associated with dilute-gas function
|
|
NUL !Pointer to reduced effective collision cross-section model; not used
|
|
0.36652 !Lennard-Jones coefficient sigma [nm];not used
|
|
174.0 !Lennard-Jones coefficient epsilon/kappa [K];not used
|
|
190.564 1.0 !Reducing parameters for T, eta
|
|
0.0 0.5 !Chapman-Enskog term; not used here
|
|
58.343920516258155 0.0
|
|
-199.92388279110893 0.25
|
|
240.35409195445984 0.5
|
|
-113.08166560748158 0.75
|
|
21.645948012444557 1.0
|
|
0 !Number of terms for initial density dependence
|
|
-0.00002946520026265898 0.000011850361299482738 0.0 0.0 0.0 ! a(0),a(1),a(2)
|
|
0.00002700022529490106 -0.000032677520832951284 0.0 0.0 0.0 ! b(0),b(1),b(2)
|
|
0.00002904479739920783 -0.00001018049342159992 -3.095500930526404e-8 0.0 0.0 ! c(0),c(1),c(2)
|
|
1.55372118714633e-8 -1.944037783173382e-9 0.0 0.0 0.0 ! A(0),A(1),A(2)
|
|
-2.6710447337075816e-9 3.2621373142076857e-9 0.0 0.0 0.0 ! B(0),B(1),B(2)
|
|
5.207541202169661e-9 1.5949945307134116e-7 3.687831977089463e-10 0.0 0.0 ! C(0),C(1),C(2)
|
|
3.0218122078964884e-12 0.0 0.0 0.0 0.0 ! D(0),D(1),D(2)
|
|
0.0 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)
|
|
|
|
|
|
|
|
|
|
================================================================================
|
|
|
|
#TCX !---Thermal conductivity---
|
|
TC1 !Pure fluid thermal conductivity model for methane of Friend et al. (1989).
|
|
:DOI:
|
|
:WEB: https://nvlpubs.nist.gov/nistpubs/Legacy/TN/nbstechnicalnote1325.pdf
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Friend, D.G., Ely, J.F., and Ingham, H.,
|
|
? "Tables for the Thermophysical Properties of Methane,"
|
|
? NIST Technical Note 1325, 1989.
|
|
?
|
|
?The uncertainty in thermal conductivity of the dilute gas between 130
|
|
? and 625 K is 2.5%. For temperatures below 130 K, the uncertainty is
|
|
? less than 10%. Excluding the dilute gas, the uncertainty is 2% between
|
|
? 110 and 725 K at pressures up to 70 MPa, except near the critical
|
|
? point which has an uncertainty of 5% or greater. For the vapor at lower
|
|
? temperatures and the dense liquid near the triple point, an uncertainty of
|
|
? 10% is possible.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.6941 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
1000000.0 !Upper pressure limit [kPa]
|
|
40.072 !Maximum density [mol/L]
|
|
3 0 !# terms for dilute gas function: numerator, denominator
|
|
174.0 0.001 !Reducing parameters for T, tcx
|
|
1.45885 0. !Coefficient, power in T
|
|
-0.4377162 -1.
|
|
0. -96. !Coefficient, power in T
|
|
8 0 !# terms for background gas function: numerator, denominator
|
|
190.551 10.139 0.00629638 !Reducing parameters for T, rho, tcx
|
|
1.5554612 0. 2. 0. !Coefficient, powers of T, rho, exp(rho)
|
|
1.0 0. 0. -99. !The order here is important
|
|
2.4149207 0. 1. 0.
|
|
0.55166331 0. 3. 0.
|
|
-0.52837734 0. 4. 0.
|
|
0.073809553 -1. 4. 0.
|
|
0.24465507 0. 5. 0.
|
|
-0.047613626 -1. 5. 0.
|
|
TK7 !Pointer to critical enhancement auxiliary function
|
|
|
|
|
|
#AUX !---Auxiliary function for the thermal conductivity critical enhancement
|
|
TK7 !Thermal conductivity critical enhancement for methane of Friend et al. (1989).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Friend, D.G., Ely, J.F., and Ingham, H., 1989.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
$CE RED 1 TR - =TAU 1 DR - =DEL
|
|
$CE 1 DPDT RGAS / DENS / CNST DENS POP< =V1
|
|
$CE CNST CNST DENS * DRED / TRED * DPDD / RGAS * DUP 0 POP> =V2
|
|
$CE CNST ETA / TRED TEMP / SQR / V1 SQR * V2 CNST POWR *
|
|
$CE TAU ABS SQRT CNST * CNST DEL SQR * + CNST DEL * - SIGN EXP *
|
|
$CF
|
|
0.001 190.564 10.139128 0. 0
|
|
1.E-12 0. 0. 0. 0
|
|
1.e5 0. 0. 0. 0
|
|
0.28631 0. 0. 0. 0
|
|
91.855 0. 0. 0. 0
|
|
0.4681 0. 0. 0. 0
|
|
2.646 0. 0. 0. 0
|
|
2.678 0. 0. 0. 0
|
|
0.637 0. 0. 0. 0
|
|
|
|
|
|
|
|
|
|
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
|
|
|
@TRN !---ECS Transport---
|
|
ECS !Extended Corresponding States model (Nitrogen reference); predictive mode for methane.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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
|
|
?
|
|
?The Lennard-Jones parameters were taken from Friend, D.G., Ely, J.F., and Ingham, H., "Tables for the Thermophysical Properties of Methane," NIST Technical Note 1325, 1989.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.6941 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
1000000.0 !Upper pressure limit [kPa]
|
|
40.072 !Maximum density [mol/L]
|
|
FEQ NITROGEN.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)
|
|
0.36652 !Lennard-Jones coefficient sigma [nm]
|
|
174.0 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
|
|
0.00132 0. 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
|
|
1 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
|
1.0 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
|
TK3 !Pointer to critical enhancement auxiliary function
|
|
|
|
|
|
|
|
|
|
********************************************************************************
|
|
|
|
@TCX !---Thermal conductivity---
|
|
TC2 !Pure fluid thermal conductivity model for methane 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 5% in the liquid, 4% in the vapor,
|
|
? 3% at T>Tc, and 8% in the critical region.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.6941 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
1000000.0 !Upper pressure limit [kPa]
|
|
40.072 !Maximum density [mol/L]
|
|
CI2 !Pointer to collision integral model
|
|
0.368 !Lennard-Jones coefficient sigma [nm]
|
|
168.0 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
0.1069188 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12
|
|
1.346953698 !Dilute gas terms (Eq 27): Gt(1)
|
|
-0.3254677753 ! Gt(2)
|
|
0.002325800819 !Residual terms (Eqs 26, 28-30): Et(1)
|
|
-0.2477927999
|
|
38.80593713
|
|
-0.1579519146e-6
|
|
0.003717991328
|
|
-0.9616989434
|
|
-0.03017352774
|
|
0.4298153386 !Et(8)
|
|
TK2 !Pointer to critical enhancement model (follows immediately)
|
|
37.42368 !Critical enhancement terms (Eqs D1-D4): X1
|
|
3.16714
|
|
0.78035
|
|
0.60103 !X4
|
|
6.512707e-10 !Z
|
|
1.38054e-23 !Boltzmann's constant, k
|
|
0.16969859271 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1)
|
|
-0.013337234608 !Fv(2)
|
|
1.4 !Fv(3)
|
|
168. !Fv(4)
|
|
-16.20427429 !Coefficients for residual viscosity, eqs (22 - 25)
|
|
427.0589027 !Ev(2) (the viscosity is also used in conductivity correlation)
|
|
14.02596278 !Ev(3)
|
|
-3916.837745 !Ev(4)
|
|
-0.0347709909 !Ev(5)
|
|
21.36542674 !Ev(6)
|
|
1436.802482 !Ev(7)
|
|
|
|
|
|
@AUX !---Auxiliary function for the thermal conductivity critical enhancement
|
|
TK3 !Simplified thermal conductivity critical enhancement for methane of Olchowy and Sengers (1989).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Olchowy, G.A. and Sengers, J.V.,
|
|
? "A simplified representation for the thermal conductivity of fluids in the critical region,"
|
|
? Int. J. Thermophysics, 10:417-426, 1989. doi: 10.1007/BF01133538
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
9 0 0 0 !# terms: CO2-terms, spare, spare, spare
|
|
1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
|
|
0.63 !Nu (universal exponent)
|
|
1.239 !Gamma (universal exponent)
|
|
1.03 !R0 (universal amplitude)
|
|
0.063 !Z (universal exponent--not used for t.c., only viscosity)
|
|
1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
|
|
0.194e-9 !Xi0 (amplitude) [m]
|
|
0.0496 !Gam0 (amplitude) [-]
|
|
0.4e-9 !Qd_inverse (modified effective cutoff parameter) [m]; estmated value from matching Friend at 50 bar
|
|
285.846 !Tref (reference temperature)=1.5*Tc [K]
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS1 !Pure fluid viscosity model for methane of Vogel et al. (2000).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Vogel, E., Wilhelm, J., Kuechenmeister, C., and Jaesche, M.,
|
|
? "High-precision viscosity measurements on methane,"
|
|
? High Temp. - High Pressures, 32(1):73-81, 2000.
|
|
?
|
|
?The uncertainty in viscosity varies from 0.3% in the dilute gas between
|
|
? 260-360 K, to 3.0% over the rest of the fluid surface, increasing up to 5 %
|
|
? from 620 K and 100 MPa.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.6941 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
40.072 !Maximum density [mol/L]
|
|
1 !Number of terms associated with dilute-gas function
|
|
CI1 !Pointer to reduced effective collision cross-section model
|
|
0.37333 !Lennard-Jones coefficient sigma [nm]
|
|
160.78 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
1.0 1.0 !Reducing parameters for T, eta
|
|
0.0855422 0.5 !Chapman-Enskog term sqrt[MW]*0.021357
|
|
9 !Number of terms for initial density dependence
|
|
159.7 0.0306525 !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
|
|
1 9 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
|
|
190.564 10.139 1.0 !Reducing parameters for T, rho, eta
|
|
3.10860501398 0. 0. 0. 0
|
|
-3.02256904347 0. 2. 0. 0
|
|
17.6965130175 -1. 2. 0. 0
|
|
3.11150846518 0. 3. 0. 0
|
|
-21.5685107769 -1. 3. 0. 0
|
|
0.672852409238 0. 4. 0. 0
|
|
10.2387524315 -1. 4. 0. 0
|
|
-1.09330775541 0. 5. 0. 0
|
|
-1.20030749419 -1. 5. 0. 0
|
|
-21.1009923406 0. 1. -1. 0
|
|
21.1009923406 0. 1. 0. 0
|
|
1.0 0. 0. 1. 0
|
|
-1.0 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 methane of Vogel et al. (2000).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Vogel, E., Wilhelm, J., Kuechenmeister, C., and Jaesche, M.,
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
5 !Number of terms
|
|
0.215309028 0 !Coefficient, power of Tstar
|
|
-0.46256942 1
|
|
0.051313823 2
|
|
0.030320660 3
|
|
-0.0070047029 4
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS2 !Pure fluid viscosity model for methane 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.
|
|
? All temperatures on IPTS-68
|
|
?
|
|
?The uncertainty in viscosity is 2%, except in the critical region which is 5%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.6941 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
1000000.0 !Upper pressure limit [kPa]
|
|
40.072 !Maximum density [mol/L]
|
|
CI2 !Pointer to collision integral model
|
|
0.368 !Lennard-Jones coefficient sigma [nm]
|
|
168.0 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
0.1069188 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12
|
|
0.5 !Exponent in Eq 19 for T
|
|
0.16969859271 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1)
|
|
-0.013337234608 !Fv(2)
|
|
1.4 !Fv(3)
|
|
168.0 !Fv(4)
|
|
-16.20427429 !Coefficients for residual viscosity, eqs (22 - 25)
|
|
427.0589027 !Ev(2)
|
|
14.02596278 !Ev(3)
|
|
-3916.837745 !Ev(4)
|
|
-0.0347709909 !Ev(5)
|
|
21.36542674 !Ev(6)
|
|
1436.802482 !Ev(7)
|
|
10.15 !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 methane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Friend, D.G., Ely, J.F., and Ingham, H.,
|
|
? "Tables for the Thermophysical Properties of Methane,"
|
|
? NIST Technical Note 1325, 1989.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
9 !Number of terms
|
|
-3.0328138281 0
|
|
16.918880086 0
|
|
-37.189364917 0
|
|
41.288861858 0
|
|
-24.615921140 0
|
|
8.9488430959 0
|
|
-1.8739245042 0
|
|
0.20966101390 0
|
|
-0.009657043707 0
|
|
|
|
|
|
|
|
|
|
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
|
|
|
|
#STN !---Surface tension---
|
|
ST1 !Surface tension model for methane 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. !
|
|
3 !Number of terms in surface tension model
|
|
190.564 !Critical temperature used in fit (dummy)
|
|
0.03825 1.191 !Sigma0 and n
|
|
-0.006024 5.422
|
|
-0.0007065 0.6161
|
|
|
|
|
|
#DE !---Dielectric constant---
|
|
DE3 !Dielectric constant model for methane 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
|
|
0 2 4 0 0 0 !Number of terms in dielectric constant model
|
|
6.5443 0. 1. 0. !Coefficient, T exp, D exp
|
|
0.0133 1. 1. 0.
|
|
8.4578 0. 2. 0.
|
|
3.7196 1. 2. 0.
|
|
-352.97 0. 3. 0.
|
|
-100.65 1. 3. 0.
|
|
|
|
|
|
#MLT !---Melting line---
|
|
ML1 !Melting line model for methane of Setzmann and Wagner (1991).
|
|
:DOI: 10.1063/1.555898
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Setzmann, U. and Wagner, W.,
|
|
? "A New Equation of State and Tables of Thermodynamic Properties for Methane
|
|
? Covering the Range from the Melting Line to 625 K at Pressures up to 1000 MPa,"
|
|
? J. Phys. Chem. Ref. Data, 20(6):1061-1151, 1991.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.6941 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
0. !
|
|
0. !
|
|
90.6941 11.696 !Reducing temperature and pressure
|
|
5 0 0 0 0 0 !Number of terms in melting line equation
|
|
1.0 0.0 !Coefficients and exponents
|
|
24756.8 1.85
|
|
-7366.02 2.1
|
|
-24756.8 0.0
|
|
7366.02 0.0
|
|
|
|
|
|
#SBL !---Sublimation line---
|
|
SB3 !Sublimation line model for methane of Lemmon (2002).
|
|
:DOI:
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Lemmon, E.W., 2002.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
90.6941 !Upper temperature limit [K]
|
|
0. !
|
|
0. !
|
|
90.6941 11.696 !Reducing temperature and pressure
|
|
0 1 0 0 0 0 !Number of terms in sublimation line equation
|
|
-12.84 1. !Coefficients and exponents
|
|
|
|
|
|
#PS !---Vapor pressure---
|
|
PS5 !Vapor pressure equation for methane of Setzmann and Wagner (1991).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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. !
|
|
190.564 4599.2 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
-6.036219 1.0
|
|
1.409353 1.5
|
|
-0.4945199 2.0
|
|
-1.443048 4.5
|
|
|
|
|
|
#DL !---Saturated liquid density---
|
|
DL4 !Saturated liquid density equation for methane of Setzmann and Wagner (1991).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Functional Form: D=Dc*EXP[SUM(Ni*Theta^(ti/3))] 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. !
|
|
190.564 10.139128 !Reducing parameters
|
|
3 0 0 0 0 0 !Number of terms in equation
|
|
1.9906389 1.062
|
|
-0.78756197 1.5
|
|
0.036976723 7.5
|
|
|
|
|
|
#DV !---Saturated vapor density---
|
|
DV4 !Saturated vapor density equation for methane of Setzmann and Wagner (1991).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Functional Form: D=Dc*EXP[SUM(Ni*Theta^(ti/3))] 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. !
|
|
190.564 10.139128 !Reducing parameters
|
|
6 0 0 0 0 0 !Number of terms in equation
|
|
-1.8802840 1.062
|
|
-2.8526531 2.5
|
|
-3.0006480 4.5
|
|
-5.2511690 7.5
|
|
-13.191859 12.5
|
|
-37.553961 23.5
|
|
|
|
|
|
@END
|
|
c 1 2 3 4 5 6 7 8
|
|
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
|
|
|
!Can't have two vs1 models in at the same time so put Friend here
|
|
!It is limited to low p
|
|
|
|
@ETA !Viscosity model specification
|
|
VS1 pure fluid viscosity model of Friend et al. (1989).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Friend, D.G., Ely, J.F., and Ingham, H.,
|
|
? "Tables for the Thermophysical Properties of Methane,"
|
|
? NIST Technical Note 1325, 1989.
|
|
?
|
|
?The uncertainty in viscosity is 0.5% between 270 and 600 K, and 1% above
|
|
? 600 K. Below 270 K, the uncertainty is 2%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
90.6941 !Lower temperature limit [K]
|
|
625.0 !Upper temperature limit [K]
|
|
1000000.0 !Upper pressure limit [kPa]
|
|
40.072 !Maximum density [mol/L]
|
|
1 !Number of terms associated with dilute-gas function
|
|
CI2 !Pointer to reduced effective collision cross-section model
|
|
0.36652 !Lennard-Jones coefficient sigma [nm]
|
|
174.0 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
174. 10.0 !Reducing parameters for T, eta
|
|
0.14105376 0.5 !Chapman-Enskog term
|
|
0 !Number of terms for initial density dependence
|
|
0 0 9 3 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
|
|
190.551 10.139 12.149 !Reducing parameters for T, rho, eta
|
|
0.41250137 0. 1. 0. 0
|
|
-0.14390912 -1. 1. 0. 0
|
|
0.10366993 0. 2. 0. 0
|
|
0.40287464 -1. 2. 0. 0
|
|
-0.24903524 -1.5 2. 0. 0
|
|
-0.12953131 0. 3. 0. 0
|
|
0.06575776 -2. 3. 0. 0
|
|
0.02566628 0. 4. 0. 0
|
|
-0.03716526 -1. 4. 0. 0
|
|
1.0 0. 0. 0. 0
|
|
-0.38798341 0. 1. 0. 0
|
|
0.03533815 -1. 1. 0. 0
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|