510 lines
25 KiB
Plaintext
510 lines
25 KiB
Plaintext
Dodecane !Short name
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112-40-3 !CAS number
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Dodecane !Full name
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CH3-10(CH2)-CH3 !Chemical formula {C12H26}
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n-Dodecane !Synonym
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170.33484 !Molar mass [g/mol]
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263.6 !Triple point temperature [K]
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489.442 !Normal boiling point [K]
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658.1 !Critical temperature [K]
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1817.0 !Critical pressure [kPa]
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1.33 !Critical density [mol/L]
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0.574 !Acentric factor
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0.0 !Dipole moment [Debye]; Dornte, R.W. and C.P. Smyth, J. Am. Chem. Soc. 52, 3546-3552 (1930)
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NBP !Default reference state
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10.0 !Version number
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???? !UN Number :UN:
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n-alkane !Family :Family:
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8147.19 !Heating value (upper) [kJ/mol] :Heat:
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1S/C12H26/c1-3-5-7-9-11-12-10-8-6-4-2/h3-12H2,1-2H3 :InChi: !Standard InChI String
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SNRUBQQJIBEYMU-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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111888d0 (decane) !Alternative fluid for mixing rules :AltID:
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8bc8dec0 !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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! 05-28-03 EWL, Original version.
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! 07-14-03 MLH, Add ECS viscosity fit.
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! 07-28-03 MLH, Add ECS thermal conductivity fit.
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! 10-03-03 MLH, Add surface tension, dipole moment.
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! 11-05-03 EWL, Add final EOS fit.
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! 11-06-03 MLH, Add final TC1 and VS1 fits.
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! 04-19-04 MLH, Update transport and EOS references.
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! 12-02-06 MLH, Update LJ for ECS.
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! 06-10-10 CKL, Add ancillary equations.
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! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
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! 06-27-17 MLH, Remove TK6 model for the ECS section and make it TK3.
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for dodecane of Lemmon (2004).
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:TRUECRITICALPOINT: 658.1 1.33 !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/ef0341062
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W. and Huber, M.L.,
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? "Thermodynamic Properties of n-Dodecane,"
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? Energy & Fuels, 18(4):960-967, 2004. doi: 10.1021/ef0341062
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?
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?The uncertainties (where the uncertainties can be considered as estimates
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? of a combined expanded uncertainty with a coverage factor of 2) of density
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? values calculated with the equation of state in the liquid phase
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? (including at saturation) are 0.2% for pressures less than 200 MPa, and
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? 0.5% for higher pressures. The uncertainty for heat capacities is 1%, and
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? that for sound speeds is 0.5%. The estimated uncertainties of vapor
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? pressures calculated with the Maxwell criterion are 0.2% for temperatures
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? above 350 K and approach 5% as the temperature decreases to the triple
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? point temperature. These estimated uncertainties for calculated
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? properties are consistent with the experimental accuracies of the various
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? available experimental data.
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?
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!```````````````````````````````````````````````````````````````````````````````
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263.6 !Lower temperature limit [K]
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700.0 !Upper temperature limit [K]
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700000.0 !Upper pressure limit [kPa]
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4.53 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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170.33484 !Molar mass [g/mol]
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263.6 !Triple point temperature [K]
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0.0006262 !Pressure at triple point [kPa]
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4.53 !Density at triple point [mol/L]
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489.442 !Normal boiling point temperature [K]
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0.574 !Acentric factor
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658.1 1817.0 1.33 !Tc [K], pc [kPa], rhoc [mol/L]
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658.1 1.33 !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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1.38031 0.32 1. 0. !a(i),t(i),d(i),l(i)
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-2.85352 1.23 1. 0.
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0.288897 1.5 1. 0.
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-0.165993 1.4 2. 0.
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0.0923993 0.07 3. 0.
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2.82772e-4 0.8 7. 0.
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0.956627 2.16 2. 1.
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0.0353076 1.1 5. 1.
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-0.445008 4.1 1. 2.
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-0.118911 5.6 4. 2.
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-0.0366475 14.5 3. 3.
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0.0184223 12.0 4. 3.
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#AUX !---Auxiliary function for Cp0
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CPP !Ideal gas heat capacity function for dodecane of Lemmon (2004).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W.,
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? Based on "TRC Thermodynamic Properties of Substances in the Ideal Gas State,"
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? Version 1.0M, 1994.
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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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23.085 0.0
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37.776 1280.0
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29.369 2399.0
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12.461 5700.0
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7.7733 13869.0
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for dodecane of Lemmon (2004).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Lemmon, E.W.,
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? Based on "TRC Thermodynamic Properties of Substances in the Ideal Gas State,"
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? Version 1.0M, 1994.
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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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22.085 1.0 !ai, ti for [ai*log(tau**ti)] terms
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20.5642558466316814 0.0 !aj, ti for [ai*tau**ti] terms
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-15.593070164198167 1.0 !aj, ti for [ai*tau**ti] terms
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37.776 1280.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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29.369 2399.0
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12.461 5700.0
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7.7733 13869.0
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--------------------------------------------------------------------------------
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@EOS !---Cubic equation of state---
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PRT !Translated Peng-Robinson equation for dodecane.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?
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!```````````````````````````````````````````````````````````````````````````````
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263.6 !Lower temperature limit [K]
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700.0 !Upper temperature limit [K]
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700000.0 !Upper pressure limit [kPa]
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4.53 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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170.33484 !Molar mass [g/mol]
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0.574 !Acentric factor
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658.1 !Critical temperature [K]
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1817.0 !Critical pressure [kPa]
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1.33 !Critical density [mol/L]
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8.314472 !Gas constant [J/mol-K]
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1 !Number of parameters
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0.0
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^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
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#ETA !---Viscosity---
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VS1 !Pure fluid viscosity model for dodecane of Huber et al. (2004).
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:DOI: 10.1021/ef034109e
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Huber, M.L., Laesecke, A., and Perkins, R.A.,
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? "Transport Properties of n-Dodecane,"
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? Energy & Fuels, 18:968-975, 2004.
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?
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?The estimated uncertainty in viscosity is 0.5% along the saturated liquid line,
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? 2% in compressed liquid to 200 MPa, 5% in vapor and supercritical regions.
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?
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?DATA SOURCES FOR VISCOSITY
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? The parameters for viscosity were based on the data of:
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? Knapstad, B. Skolsvik, P.A., and Oye, H.A., "Viscosity of Pure Hydrocarbons," J. Chem. Eng. Data, 34:37-43, 1989. doi: 10.1021/je00055a013
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? Knapstad, B., Skjolsvik, P.A., and Oye, H.A., "Viscosity of Three Binary Hydrocarbon Mixtures," J. Chem. Eng. Data, 36(1):84-88, 1991. doi: 10.1021/je00001a025
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? Dymond, J.H. and Young, K.J., "Transport Properties of Nonelectrolyte Liquid Mixtures- I. Viscosity Coefficients for n-Alkane Mixtures at Saturation Pressure from 283 to 378 K," Int. J. Thermophys., 1(4):331-344, 1980. doi: 10.1007/BF00516562
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? Caudwell, D.R., Trusler, J.P.M., Vesovic, V., and Wakeham, W.A., "The Viscosity and Density of n-Dodecane and n-Octadecane at Pressures up to 200 MPa and Temperatures up to 473 K," Int. J. Thermophys., 25(5):1339-1352, 2004. doi: 10.1007/s10765-004-5742-0
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? Lyusternik, V.E. and Zhdanov, A.G., Teplofiz. Svoistva Veshchestv Mater, No.7, Rabinovich, V.A. ed., Standards Publishing, Moscow, 1973.
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? Giller, E.B. and Drickamer, H.G., "Viscosity of Normal Paraffins near the Freezing Point," Ind. Eng. Chem., 41(9):2067-2069, 1949. doi: 10.1021/ie50477a056
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? Average absolute deviations of the fit from the experimental data are:
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? Knapstad, 1989: avg 0.35% (max 0.66); Knapstad, 1991: avg 0.29% (max 0.73);
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? Caudwell: avg 1.11% (max 3.44); Lyusternik: 0.92% (max 2.14) Giller: 0.70% (max 1.17%).
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? Overall: 0.95%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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200.0 !Lower temperature limit [K] allow for extrapolation to low T
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1000.0 !Upper temperature limit [K]
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700000.00 !Upper pressure limit [kPa]
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7.0 !Maximum density [mol/L]
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1 !Number of terms associated with dilute-gas function
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CI1 !Pointer to reduced effective collision cross-section model
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0.735639 !Lennard-Jones coefficient sigma [nm]
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522.592 !Lennard-Jones coefficient epsilon/kappa [K]
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1.0 1.0 !Reducing parameters for T, eta
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0.2787353 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term]
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9 !Number of terms for initial density dependence
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522.592 0.2397238 !Reducing parameters for T (=eps/k), etaB2 (= 0.6022137*sigma**3)
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-19.572881 0.0 !Coefficient, power in T* = T/(eps/k)
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219.73999 -0.25
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-1015.3226 -0.5
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2471.0125 -0.75
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-3375.1717 -1.0
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2491.6597 -1.25
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-787.26086 -1.5
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14.085455 -2.5
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-0.34664158 -5.50
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2 5 1 2 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
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658.1 1.33 1000.0 !Reducing parameters for T, rho, eta (Laesecke correlation in terms of mPa-s, convert to uPa-s)
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2.32661 0.0 0. 0. 0 ! c1
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2.23089 0.5 0. 0. 0 ! c8
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-0.0471703 -1.0 2. 0. 0 ! beta16; powers of tau, del, del0; power of del in exponential [0= no exp.]
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0.00827816 -1.0 3. 0. 0 ! beta17; powers of tau, del, del0; power of del in exponential [0= no exp.]
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0.0298429 -2.0 2. 0. 0 ! beta18; powers of tau, del, del0; power of del in exponential [0= no exp.]
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-0.0134156 -2.0 3. 0. 0 ! beta19; powers of tau, del, del0; power of del in exponential [0= no exp.]
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-0.503109 0.0 1. -1. 0 ! beta7 over del0 term
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0.503109 0.0 1. 0. 0 ! beta7 in non-simple poly term
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1.0 0.0 0. 1. 0 ! del0 term in denominator
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-1.0 0.0 1. 0. 0 ! -del term in denominator
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NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
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#AUX !---Auxiliary function for the collision integral
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CI1 !Reduced effective collision cross-section model (empirical form in log(T*)) for dodecane.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Huber, M.L., Laesecke, A., and Perkins, R.A.,
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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3 !Number of terms
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0.382987 0 !Coefficient, power of Tstar
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-0.561050 1
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0.0313962 2
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================================================================================
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#TCX !---Thermal conductivity---
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TC1 !Pure fluid thermal conductivity model for dodecane of Huber et al. (2004).
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:DOI: 10.1021/ef034109e
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Huber, M.L., Laesecke, A., and Perkins, R.A.,
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? "Transport Properties of n-Dodecane,"
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? Energy & Fuels, 18:968-975, 2004.
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?
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?Uncertainty in thermal conductivity is 3%, except in the supercritical region
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? and dilute gas which have an uncertainty of 5%.
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?
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?DATA SOURCES FOR THERMAL CONDUCTIVITY
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? Tanaka, T., Itani, Y., Kubota, H., and Makita, T., "Thermal Conductivity of Five Normal Alkanes in the Temperature Range 283-373 K at Pressures up to 250 MPa," Int. J. Thermophys., 9(3):331-350, 1988. doi: 10.1007/BF00513075
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? Mustafaev, R.A., "Thermal Conductivity of Vapors of Normal Saturated Hydrocarbons at High Temperatures," Izv. Vyssh. Uchebn. Zaved., Neft Gaz., 16(11):71-74, 1973.
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? Average absolute deviations of the fit from the experimental data are:
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? Tanaka: 0.35% (max 1.45); Mustafaev: 1.71% (max 4.43).
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? Overall: 0.75%.
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?
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!```````````````````````````````````````````````````````````````````````````````
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200.0 !Lower temperature limit [K] allow for extrapolation to low T
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1000.0 !Upper temperature limit [K]
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700000.0 !Upper pressure limit [kPa]
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7.0 !Maximum density [mol/L]
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4 0 !# terms for dilute gas function: numerator, denominator
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658.1 1.0 !Reducing parameters for T, tcx
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0.00436343 0. !Coefficient, power in T
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-0.0264054 1. !(2)
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0.0922394 2. !(3)
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-0.0291756 3. !(16)
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10 0 !# terms for background gas function: numerator, denominator
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658.1 1.33 1. !Reducing parameters for T, rho, tcx
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0.0693347 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
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-0.0280792 1. 1. 0.
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-0.0331695 0. 2. 0.
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0.00173922 1. 2. 0.
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0.00676165 0. 3. 0.
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0.00309558 1. 3. 0.
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0.0 0. 4. 0.
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0.0 1. 4. 0.
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0.0 0. 5. 0.
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0.0 1. 5. 0.
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TK3 !Pointer to critical enhancement auxiliary function
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#AUX !---Auxiliary function for the thermal conductivity critical enhancement
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TK3 !Simplified thermal conductivity critical enhancement for dodecane of Olchowy and Sengers (1989).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Olchowy, G.A. and Sengers, J.V.,
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? "A Simplified Representation for the Thermal Conductivity of Fluids in the Critical Region,"
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? Int. J. Thermophys., 10:417-426, 1989. doi: 10.1007/BF01133538
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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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9 0 0 0 !# terms: CO2-terms, spare, spare, spare
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1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
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0.63 !Nu (universal exponent)
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1.239 !Gamma (universal exponent)
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1.03 !R0 (universal amplitude)
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0.063 !Z (universal exponent--not used for t.c., only viscosity)
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1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
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0.194e-9 !Xi0 (amplitude) [m]
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0.0496 !Gam0 (amplitude) [-]
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1.52e-9 !Qd_inverse (modified effective cutoff parameter) [m]; estimated
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987.15 !Tref (reference temperature)=1.5*Tc [K]
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++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
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@TRN !---ECS Transport---
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ECS !Extended Corresponding States model (Nitrogen reference); fitted to data for dodecane.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Klein, S.A., McLinden, M.O., and Laesecke, A., "An Improved Extended Corresponding States Method for Estimation of Viscosity of Pure Refrigerants and Mixtures," Int. J. Refrigeration, 20(3):208-217, 1997. doi: 10.1016/S0140-7007(96)00073-4.
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?McLinden, M.O., Klein, S.A., and Perkins, R.A., "An Extended Corresponding States Model for the Thermal Conductivity of Refrigerants and Refrigerant Mixtures," Int. J. Refrigeration, 23(1):43-63, 2000. doi: 10.1016/S0140-7007(99)00024-9
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?
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!```````````````````````````````````````````````````````````````````````````````
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263.6 !Lower temperature limit [K]
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1000.0 !Upper temperature limit [K]
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700000.0 !Upper pressure limit [kPa]
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4.54 !Maximum density [mol/L]
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FEQ NITROGEN.FLD
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VS1 !Model for reference fluid viscosity
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TC1 !Model for reference fluid thermal conductivity
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NUL !Large molecule identifier
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1 !Lennard-Jones flag (0 or 1) (0 => use estimates)
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0.735639 !Lennard-Jones coefficient sigma [nm]
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522.592 !Lennard-Jones coefficient epsilon/kappa [K]
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2 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2
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0.000789804 0. 0. 0. !Coefficient, power of T, spare1, spare2
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0.611329e-6 1. 0. 0. !Coefficient, power of T, spare1, spare2
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2 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
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0.9756 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
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-0.0095246 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2
|
||
1.32283 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
|
||
-0.0221478 0. 0. 1. !Coefficient, power of Tr, power of Dr, spare
|
||
TK3 !Pointer to critical enhancement auxiliary function
|
||
|
||
|
||
|
||
|
||
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
|
||
|
||
#STN !---Surface tension---
|
||
ST1 !Surface tension model for dodecane of Mulero et al. (2012).
|
||
:DOI: 10.1063/1.4768782
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Mulero, A., Cachadi<64>a, I., and Parra, M.I.,
|
||
? "Recommended Correlations for the Surface Tension of Common Fluids,"
|
||
? J. Phys. Chem. Ref. Data, 41(4), 043105, 2012. doi: 10.1063/1.4768782
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
0. !
|
||
10000. !
|
||
0. !
|
||
0. !
|
||
2 !Number of terms in surface tension model
|
||
658.1 !Critical temperature used in fit (dummy)
|
||
0.0154 4.18 !Sigma0 and n
|
||
0.048 1.17
|
||
|
||
|
||
#PS !---Vapor pressure---
|
||
PS5 !Vapor pressure equation for dodecane of Lemmon (2010).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Lemmon, C.K. and Lemmon, E.W., 2010.
|
||
?
|
||
?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. !
|
||
658.1 1817.0 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
-9.4217 1.0
|
||
-4.1890 1.5
|
||
5.4999 1.359
|
||
-6.7789 3.56
|
||
-1.7161 9.2
|
||
|
||
|
||
#DL !---Saturated liquid density---
|
||
DL1 !Saturated liquid density equation for dodecane of Lemmon (2010).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Lemmon, C.K. and Lemmon, E.W., 2010.
|
||
?
|
||
?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. !
|
||
658.1 1.33 !Reducing parameters
|
||
5 0 0 0 0 0 !Number of terms in equation
|
||
0.92236 0.21
|
||
0.92047 0.49
|
||
5.5713 1.08
|
||
-9.2253 1.49
|
||
5.1763 1.9
|
||
|
||
|
||
#DV !---Saturated vapor density---
|
||
DV3 !Saturated vapor density equation for dodecane of Lemmon (2010).
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Lemmon, C.K. and Lemmon, E.W., 2010.
|
||
?
|
||
?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. !
|
||
658.1 1.33 !Reducing parameters
|
||
6 0 0 0 0 0 !Number of terms in equation
|
||
-1.7859 0.298
|
||
-7.5436 0.91
|
||
-22.848 2.8
|
||
-81.355 6.0
|
||
92.283 9.0
|
||
-217.25 11.0
|
||
|
||
|
||
@END
|
||
c 1 2 3 4 5 6 7 8
|
||
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
||
|
||
|
||
@EOS !Equation of state specification
|
||
ECS Thermodynamic Extended Corresponding States model w/ T-dependent shape factors.
|
||
?
|
||
?```````````````````````````````````````````````````````````````````````````````
|
||
?Huber, M.L. and Ely, J.F.,
|
||
? "A predictive extended corresponding states model for pure and mixed
|
||
? refrigerants including an equation of state for R134a,"
|
||
? Int. J. Refrigeration, 17(1):18-31, 1994. doi: 10.1016/0140-7007(94)90083-3
|
||
?
|
||
?DATA SOURCES
|
||
? Liquid density: Francis, A.W., "Pressure-Temperature-Liquid Density Relations of Pure Hydrocarbons", Ind. Eng. Chem., 49(10):1779-1786 (1957) doi: 10.1021/ie50574a048
|
||
? Vapor pressure: Morgan, D.L. and Kobayashi, R., "Direct Vapor Pressure Measurements of Ten n-Alkanes m the 10-C28 Range", Fluid Phase Equilibria 97:211 (1994)
|
||
? Average absolute deviations of the fit from the experimental data are:
|
||
? Francis: avg 0.55% (max 3.0); Morgan: avg 3.28% (max. -13.0)
|
||
?
|
||
!```````````````````````````````````````````````````````````````````````````````
|
||
263.6 !Lower temperature limit [K]
|
||
1000.0 !Upper temperature limit [K]
|
||
100000.0 !Upper pressure limit [kPa]
|
||
10.0 !Maximum density [mol/L]
|
||
CPP !Pointer to Cp0 model
|
||
PROPANE.FLD
|
||
FEQ !Pointer to reference fluid model
|
||
0.1524 !Acentric factor for c3 used in shape factor correlation
|
||
0.2787 !Critical compressibility for c3 used in correlation
|
||
0.574 !Acentric factor for fluid used in shape factor correlation
|
||
658.1 !Critical temperature [K]
|
||
1817.0 !Critical pressure [kPa]
|
||
1.33 !Critical density [mol/L]
|
||
2 !Number of temperature coefficients for 'f' shape factor
|
||
0.0532961 0. ! alpha1 of Huber & Ely
|
||
-0.769446 1. ! alpha2 (log(Tr) term)
|
||
0 !Number of density coefficients for 'f' shape factor
|
||
2 !Number of temperature coefficients for 'h' shape factor
|
||
-0.202751 0. ! beta1 of Huber & Ely
|
||
0.2270890 1. ! beta2 (log(Tr) term)
|
||
0 !Number of density coefficients for 'h' shape factor
|