1179 lines
56 KiB
Plaintext
1179 lines
56 KiB
Plaintext
Butane !Short name
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106-97-8 !CAS number
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n-Butane !Full name
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CH3-2(CH2)-CH3 !Chemical formula {C4H10}
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R-600 !Synonym
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58.1222 !Molar mass [g/mol]
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134.895 !Triple point temperature [K]
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272.660 !Normal boiling point [K]
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425.125 !Critical temperature [K]
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3796.0 !Critical pressure [kPa]
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3.922769613 !Critical density [mol/L]
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0.201 !Acentric factor
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0.05 !Dipole moment [Debye]; Harvey, A.H., Lemmon, E.W., Int. J. Thermophys., 26(1):31-46, 2005.
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IIR !Default reference state
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10.0 !Version number
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1011 !UN Number :UN:
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n-alkane !Family :Family:
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2877.40 !Heating value (upper) [kJ/mol] :Heat:
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4. !GWP (IPCC 2007) :GWP:
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1000. !RCL (ppm v/v, ASHRAE Standard 34, 2010) :RCL:
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A3 !Safety Group (ASHRAE Standard 34, 2010) :Safety:
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1S/C4H10/c1-3-4-2/h3-4H2,1-2H3 !Standard InChI String :InChi:
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IJDNQMDRQITEOD-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
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47ade7e0 (isobutane) !Alternative fluid for mixing rules :AltID:
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7b3b4080 !Hash number from InChI Key :Hash:
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!The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the
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! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended
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! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to
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! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary
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! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and
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! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the
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! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the
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! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations,
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! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and
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! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface
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! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a
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! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The
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! end of the fluid file is marked with @END. Anything below that is ignored.
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! compiled by M. McLinden, NIST Physical and Chemical Properties Division, Boulder, Colorado
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! 02-01-96 MM, Original version.
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! 10-17-96 MM, Add thermal conductivity model of Younglove and Ely.
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! 11-18-98 EWL, Add equation of state of Polt et al. (1992).
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! 11-01-99 EWL, Add Span 12 term short equation of state.
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! 07-17-00 EWL, Add Vogel viscosity equation.
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! 03-30-01 MLH, Add Perkins et al. thermal conductivity equation (2001).
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! 06-01-01 EWL, Add Miyamoto and Watanabe equation.
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! 07-07-04 AHH, Update dipole moment.
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! 08-05-04 EWL, Add Harvey and Lemmon dielectric correlation.
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! 09-02-04 EWL, Add Buecker and Wagner equation.
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! 10-13-04 MLH, Add family.
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! 08-08-05 EWL, Change Ptrp in melting line equation slightly to match EOS at Ttrp.
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! 12-02-06 MLH, Update LJ in ECS.
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! 03-05-07 MLH, Add VS4 model.
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! 09-13-10 EWL, Replace ancillary equations.
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! 10-21-10 EWL, Increase upper pressure limit to 200 MPa based on data of Miyamoto (2008).
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! 10-21-10 MLH, Revise upper limit of pressure on vis. and therm. cond. to 200 MPa.
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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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! 04-01-18 EWL, Add Herrmann and Vogel viscosity equation.
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________________________________________________________________________________
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#EOS !---Equation of state---
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FEQ !Helmholtz equation of state for butane of Buecker and Wagner (2006).
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:TRUECRITICALPOINT: 425.125 3.922769613 !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: 10.1063/1.1901687
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Bücker, D. and Wagner, W.,
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? "Reference Equations of State for the Thermodynamic Properties of Fluid
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? Phase n-Butane and Isobutane,"
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? J. Phys. Chem. Ref. Data, 35(1):929-1019, 2006. doi: 10.1063/1.1901687
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?
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?The uncertainties in density are 0.02% at temperatures below 340 K and
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? pressures below 12 MPa (both liquid and vapor states), 0.1% at temperatures
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? below 270 K and pressures above 12 MPa, 0.2% between 340 and 515 K at
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? pressures less than 0.6 MPa, and 0.4% elsewhere. Above the upper pressure
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? limit of 69 MPa as given in the original formulation, new data up to 200 MPa
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? show that the uncertainty in density is 0.3%. In the critical region,
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? deviations in pressure are 0.5%. At temperatures above 500 K, the
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? uncertainties in density increase up to 1%. Uncertainties in heat capacities
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? are typically 1%, rising to 5% in the critical region and at pressures above
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? 30 MPa. Uncertainties in the speed of sound are typically 0.5%, rising to 1%
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? at temperatures below 200 K and to 4% in a large area around the critical point.
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?
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!```````````````````````````````````````````````````````````````````````````````
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134.895 !Lower temperature limit [K]
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575.0 !Upper temperature limit [K]
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200000.0 !Upper pressure limit [kPa]
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13.86 !Maximum density [mol/L]
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CPP !Pointer to Cp0 model
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58.1222 !Molar mass [g/mol]
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134.895 !Triple point temperature [K]
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0.0006656 !Pressure at triple point [kPa]
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12.645 !Density at triple point [mol/L]
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272.660 !Normal boiling point temperature [K]
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0.201 !Acentric factor
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425.125 3796.0 3.922769613 !Tc [K], pc [kPa], rhoc [mol/L]
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425.125 3.922769613 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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23 4 2 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
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2.5536998241635 0.5 1. 0. !a(i),t(i),d(i),l(i)
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-4.4585951806696 1.0 1. 0.
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0.82425886369063 1.5 1. 0.
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0.11215007011442 0.0 2. 0.
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-0.035910933680333 0.5 3. 0.
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0.016790508518103 0.5 4. 0.
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0.032734072508724 0.75 4. 0.
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0.95571232982005 2.0 1. 1.
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-1.0003385753419 2.5 1. 1.
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0.085581548803855 2.5 2. 1.
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-0.025147918369616 1.5 7. 1.
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-0.0015202958578918 1.0 8. 1.
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0.004706068232642 1.5 8. 1.
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-0.097845414174006 4.0 1. 2.
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-0.04831790415876 7.0 2. 2.
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0.17841271865468 3.0 3. 2.
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0.018173836739334 7.0 3. 2.
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-0.11399068074953 3.0 4. 2.
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0.019329896666669 1.0 5. 2.
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0.001157587740101 6.0 5. 2.
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0.00015253808698116 0.0 10. 2.
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-0.043688558458471 6.0 2. 3.
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-0.0082403190629989 13.0 6. 3.
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-0.028390056949441 2.0 1. 2. 2. -10.0 -150.0 1.16 0.85 0. 0. 0.
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0.0014904666224681 0.0 2. 2. 2. -10.0 -200.0 1.13 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 butane of Buecker and Wagner (2006).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Bücker, D. and Wagner, W., 2006.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314472 !Reducing parameters for T, Cp0
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1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.24680487 0.0
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5.54913289 329.40404
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11.4648996 1420.17366
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7.59987584 2113.08938
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9.66033239 4240.8573
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#AUX !---Auxiliary function for PX0
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PX0 !Helmholtz energy ideal-gas function for butane of Buecker and Wagner (2006).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Bücker, D. and Wagner, W., 2006.
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?
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!```````````````````````````````````````````````````````````````````````````````
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1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
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3.24680487 1.0 !ai, ti for [ai*log(tau**ti)] terms
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-5.4249697888268713 0.0 !aj, ti for [ai*tau**ti] terms
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4.9194999371032626 1.0 !aj, ti for [ai*tau**ti] terms
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5.54913289 329.40404 !aj, ti for [ai*log(1-exp(-ti/T)] terms
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11.4648996 1420.17366
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7.59987584 2113.08938
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9.66033239 4240.8573
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#AUX !---Auxiliary function for PH0
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PH0 !Ideal gas Helmholtz form for butane.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Bücker, D. and Wagner, W., 2006.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
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3.24680487 1.0 !ai, ti for [ai*log(tau**ti)] terms
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12.54882924 0.0 !aj, ti for [ai*tau**ti] terms
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-5.46976878 1.0
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5.54913289 -0.7748404445 !aj, ti for [ai*log(1-exp(ti*tau)] terms
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11.4648996 -3.3406025522
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7.59987584 -4.9705130961
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9.66033239 -9.9755537783
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--------------------------------------------------------------------------------
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@EOS !---Equation of state---
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FEK !Helmholtz equation of state for butane of Kunz and Wagner (2007).
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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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134.895 !Lower temperature limit [K]
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575.0 !Upper temperature limit [K]
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69000.0 !Upper pressure limit [kPa]
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13.2 !Maximum density [mol/L]
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PHK !Pointer to Cp0 model
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58.1222 !Molar mass [g/mol]
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134.895 !Triple point temperature [K]
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0.0006507 !Pressure at triple point [kPa]
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12.67 !Density at triple point [mol/L]
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272.62 !Normal boiling point temperature [K]
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0.2038 !Acentric factor
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425.125 3830.3 3.920016792 !Tc [K], pc [kPa], rhoc [mol/L]
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425.125 3.920016792 !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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1.0626277411455 0.25 1. 0.
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-2.8620951828350 1.125 1. 0.
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0.88738233403777 1.5 1. 0.
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-0.12570581155345 1.375 2. 0.
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0.10286308708106 0.250 3. 0.
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0.00025358040602654 0.875 7. 0.
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0.32325200233982 0.625 2. 1.
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-0.037950761057432 1.75 5. 1.
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-0.32534802014452 3.625 1. 2.
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-0.079050969051011 3.625 4. 2.
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-0.020636720547775 14.5 3. 3.
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0.005705380933475 12.0 4. 3.
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@AUX !---Auxiliary function for PH0
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PHK !Ideal gas Helmholtz form for butane of Kunz and Wagner (2007).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Kunz, O., Klimeck, R., Wagner, W., Jaeschke, M.
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? "The GERG-2004 Wide-Range Equation of State for Natural Gases
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? and Other Mixtures," GERG Technical Monograph 15,
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? Fortschritt-Berichte VDI, VDI-Verlag, Düsseldorf, 2007.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1 2 0 2 2 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
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3.33944 1.0 !ai, ti for [ai*log(tau**ti)] terms
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20.884143364 0.0 !aj, ti for [ai*tau**ti] terms
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-91.638478026 1.0
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-6.89406 0.43195766 !aj, ti for cosh and sinh terms
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-14.7824 2.124516319
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9.44893 1.101487798
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24.4618 4.502440459
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@EOS !---Equation of state---
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FE1 !Helmholtz equation of state for butane of Miyamoto and Watanabe (2001).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Miyamoto, H. and Watanabe, K.
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? "A Thermodynamic Property Model for Fluid-Phase n-Butane,"
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? Int. J. Thermophys., 22(2):459-475, 2001. doi: 10.1023/A:1010722814682
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?
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?The uncertainties of the equation of state are approximately 0.2%
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? in density, 1% in heat capacity, 1% 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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134.87 !Lower temperature limit [K]
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589.0 !Upper temperature limit [K]
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69000. !Upper pressure limit [kPa]
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13.15 !Maximum density [mol/L]
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CP1 !Pointer to Cp0 model
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58.1222 !Molar mass [g/mol]
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134.87 !Triple point temperature [K]
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0.000688 !Pressure at triple point [kPa]
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12.652 !Density at triple point [mol/L]
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272.6 !Normal boiling point temperature [K]
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0.2 !Acentric factor
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425.125 3796.0 3.92001679 !Tc [K], pc [kPa], rhoc [mol/L]
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425.125 3.92001679 !Reducing parameters [K, mol/L]
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8.314472 !Gas constant [J/mol-K]
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19 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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0.2952054 -0.25 1. 0. !a(i),t(i),d(i),l(i)
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-1.326360 1.50 1. 0.
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-0.002031317 -0.75 2. 0.
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0.2240301 0.0 2. 0.
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-0.03635425 1.25 3. 0.
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0.001905841 1.5 5. 0.
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7.409154e-5 0.5 8. 0.
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-1.401175e-6 2.5 8. 0.
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-2.492172 1.50 3. 1.
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2.386920 1.75 3. 1.
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0.001424009 -0.25 8. 1.
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-0.009393388 3.0 5. 1.
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0.00261659 3.0 6. 1.
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-0.1977323 4.0 1. 2.
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-0.03809534 2.0 5. 2.
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0.001523948 -1.0 7. 2.
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-0.02391345 2.0 2. 3.
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-0.009535229 19.0 3. 3.
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3.928384e-5 5.0 15. 3.
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@AUX !---Auxiliary function for Cp0
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CP1 !Ideal gas heat capacity function for butane.
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Miyamoto, H. and Watanabe, K., 2001.
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?
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!```````````````````````````````````````````````````````````````````````````````
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0. !
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10000. !
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0. !
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0. !
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1.0 8.314472 !Reducing parameters for T, Cp0
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1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
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4.240207 0.0
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5.513671 327.55988
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7.38845 1319.06935
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10.25063 4138.63184
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11.06101 1864.36783
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@EOS !---Equation of state---
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BWR !MBWR equation of state for butane of Younglove and Ely (1987).
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?
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?```````````````````````````````````````````````````````````````````````````````
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?Younglove, B.A. and Ely, J.F.,
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? "Thermophysical properties of fluids. II. Methane, ethane, propane,
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? isobutane and normal butane,"
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? J. Phys. Chem. Ref. Data, 16:577-798, 1987.
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?
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?The uncertainties in density are 0.05% in the liquid, 0.4% in the vapor
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? and 0.06% in the supercritical and critical regions. The uncertainty is
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? 2% for heat capacities, 1% for the speed of sound in the vapor, and 2%
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? for the speed of sound in the liquid. All temperatures are given on IPTS-68.
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?
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!```````````````````````````````````````````````````````````````````````````````
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134.86 !Lower temperature limit [K]
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500.0 !Upper temperature limit [K]
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70000.0 !Upper pressure limit [kPa]
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13.20 !Maximum density [mol/L]
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CP2 !Pointer to Cp0 model
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58.1222 !Molar mass [g/mol]
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134.86 !Triple point temperature [K]
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6.736e-4 !Pressure at triple point [kPa]
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12.650 !Density at triple point [mol/L]
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272.613 !Normal boiling point temperature [K]
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0.199586 !Acentric factor
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425.16 3796.0 3.920 !Tc [K], pc [kPa], rhoc [mol/L]
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425.16 3.920 !Reducing parameters [K, mol/L]
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3.920 !gamma
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0.0831434 !Gas constant [L-bar/mol-K]
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32 1 !Nterm, Ncoeff per term
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0.0153740104603 -0.160980034611 -9.7978245901
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499.660674504 -1021156.07687 0.00236032147756
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-1.37475757093 -907.038733865 385421.748213
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-0.3494537107e-4 0.157361122714 102.301474068
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0.0182335737331 -4.04114307787 1.87979855783
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0.36208879504 -0.00738762248266 -2.18618590563
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0.118802729027 706854.198713 -219469885.796
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-18245.4361268 0.206790377277e+10 111.757550145
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55877.9925986 -15.9579054026 -1480342.14622
|
|
-0.245206328201 218.305259309 -0.923990627338e-4
|
|
-2.05267776639 38.763904482
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CP2 !Ideal gas heat capacity function for butane of Younglove and Ely.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F., 1987.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
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
|
|
388023.10194 -3.0
|
|
-154442.9689 -2.0
|
|
2845.5082239 -1.0
|
|
-13.491511376 0.0
|
|
0.066142595353 1.0
|
|
-0.000024307965028 2.0
|
|
1.5044248429e-10 3.0
|
|
-8.3933423467 3000.0
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
FES !Helmholtz equation of state for butane of Span and Wagner (2003).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Span, R. and Wagner, W.
|
|
? "Equations of State for Technical Applications. II. Results for Nonpolar Fluids,"
|
|
? Int. J. Thermophys., 24(1):41-109, 2003. doi: 10.1023/A:1022310214958
|
|
?
|
|
?The uncertainties of the equation of state are approximately 0.2% (to
|
|
? 0.5% at high pressures) in density, 1% (in the vapor phase) to 2% in
|
|
? heat capacity, 1% (in the vapor phase) to 2% in the speed of sound, and
|
|
? 0.2% in vapor pressure, except in the critical region.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.86 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
100000.0 !Upper pressure limit [kPa]
|
|
13.20 !Maximum density [mol/L]
|
|
CPS !Pointer to Cp0 model
|
|
58.123 !Molar mass [g/mol]
|
|
134.86 !Triple point temperature [K]
|
|
0.00064578 !Pressure at triple point [kPa]
|
|
12.671 !Density at triple point [mol/L]
|
|
272.62 !Normal boiling point temperature [K]
|
|
0.2 !Acentric factor
|
|
425.125 3796.0 3.9199628 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
425.125 3.9199628 !Reducing parameters [K, mol/L]
|
|
8.31451 !Gas constant [J/mol-K]
|
|
12 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
1.0626277 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
|
-2.8620952 1.125 1. 0.
|
|
0.88738233 1.5 1. 0.
|
|
-0.12570581 1.375 2. 0.
|
|
0.10286309 0.25 3. 0.
|
|
0.00025358041 0.875 7. 0.
|
|
0.323252 0.625 2. 1.
|
|
-0.037950761 1.75 5. 1.
|
|
-0.32534802 3.625 1. 2.
|
|
-0.079050969 3.625 4. 2.
|
|
-0.020636721 14.5 3. 3.
|
|
0.0057053809 12.0 4. 3.
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CPS !Ideal gas heat capacity function for butane of Jaeschke and Schley (1995).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Jaeschke, M. and Schley, P.
|
|
? "Ideal-Gas Thermodynamic Properties for Natural-Gas Applications,"
|
|
? Int. J. Thermophys., 16(6):1381-1392, 1995. doi: 10.1007/BF02083547
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 8.31451 !Reducing parameters for T, Cp0
|
|
1 0 2 2 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
4.33944 0.0
|
|
232482.7 -2.0 183.636 -1.0 -2.0
|
|
12058640.0 -2.0 903.185 -1.0 -2.0
|
|
2071931.0 -2.0 468.27 -1.0 -2.0
|
|
89622620.0 -2.0 1914.1 -1.0 -2.0
|
|
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
FE3 !Helmholtz equation of state for butane of Sarin et al. (2007).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Sarin, C., Astina, I.M., Darmanto, P.S., Sato, H.
|
|
? Thermodynamic property model of wide-fluid phase n-butane.
|
|
? Jurnal Teknik Mesin, 22(2):44-54, 2007.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.895 !Lower temperature limit [K]
|
|
589.0 !Upper temperature limit [K]
|
|
69000.0 !Upper pressure limit [kPa]
|
|
12.648 !Maximum density [mol/L]
|
|
CPP !Pointer to Cp0 model
|
|
58.1222 !Molar mass [g/mol]
|
|
134.895 !Triple point temperature [K]
|
|
0.000677 !Pressure at triple point [kPa]
|
|
12.648 !Density at triple point [mol/L]
|
|
272.664 !Normal boiling point temperature [K]
|
|
0.201 !Acentric factor
|
|
425.125 3796.0 3.9200167922 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
425.125 3.9200167922 !Reducing parameters [K, mol/L]
|
|
8.314472 !Gas constant [J/mol-K]
|
|
18 4 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
0.7558424814 0.25 1. 0.
|
|
0.2874737492 0.25 2. 0.
|
|
-0.0001142684008 0.5 8. 0.
|
|
-1.811241776 1.25 1. 0.
|
|
0.01149143018 1.5 5. 0.
|
|
-0.000004140496922 2.5 8. 0.
|
|
0.002458991872 3.5 2. 0.
|
|
-0.005092499231 0.25 7. 1.
|
|
0.01042207957 0.5 8. 1.
|
|
-0.03210318054 1. 7. 1.
|
|
-3.055326240 1.5 3. 1.
|
|
2.730293235 1.75 3. 1.
|
|
-0.01139148850 2. 7. 1.
|
|
-0.04337857953 2. 5. 2.
|
|
-0.1875707093 4. 1. 2.
|
|
-0.006890261888 5. 7. 2.
|
|
-0.009547267340 7. 2. 3.
|
|
-0.01219583966 18. 3. 3.
|
|
|
|
|
|
|
|
@EOS !---Equation of state---
|
|
FE4 !Helmholtz equation of state for butane of Polt et al. (1992).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Polt, A., Platzer, B., and Maurer, G.,
|
|
? "Parameter der thermischen Zustandsgleichung von Bender fuer 14
|
|
? mehratomige reine Stoffe,"
|
|
? Chem. Tech. (Leipzig), 44(6):216-224, 1992.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
140.0 !Lower temperature limit [K]
|
|
589.0 !Upper temperature limit [K]
|
|
30000.0 !Upper pressure limit [kPa]
|
|
12.81 !Maximum density [mol/L]
|
|
CP4 !Pointer to Cp0 model
|
|
58.124 !Molar mass [g/mol]
|
|
140.0 !Triple point temperature [K]
|
|
0.00161 !Pressure at triple point [kPa]
|
|
12.573 !Density at triple point [mol/L]
|
|
272.62 !Normal boiling point temperature [K]
|
|
0.1984 !Acentric factor
|
|
425.14 3783.85 3.9192072 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
425.14 3.9192072 !Reducing parameters [K, mol/L]
|
|
8.3143 !Gas constant [J/mol-K]
|
|
22 5 0 0 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
|
|
-0.504188295325 3. 0. 0. 0. !a(i),t(i),d(i),l(i)
|
|
0.541067401063 4. 0. 0. 0.
|
|
-0.0760421383062 5. 0. 0. 0.
|
|
0.846035653528 0. 1. 0. 0.
|
|
-1.91317317203 1. 1. 0. 0.
|
|
0.521441860186 2. 1. 0. 0.
|
|
-0.783511318207 3. 1. 0. 0.
|
|
0.0689697797175 4. 1. 0. 0.
|
|
0.0947825461055 0. 2. 0. 0.
|
|
-0.141401831669 1. 2. 0. 0.
|
|
0.382675021672 2. 2. 0. 0.
|
|
-0.0423893176684 0. 3. 0. 0.
|
|
0.0677591792029 1. 3. 0. 0.
|
|
0.056794336334 0. 4. 0. 0.
|
|
-0.131517698401 1. 4. 0. 0.
|
|
0.0221136942526 1. 5. 0. 0.
|
|
0.504188295325 3. 0. 2. 1.08974964
|
|
-0.541067401063 4. 0. 2. 1.08974964
|
|
0.0760421383062 5. 0. 2. 1.08974964
|
|
-0.061910953546 3. 2. 2. 1.08974964
|
|
0.423035373804 4. 2. 2. 1.08974964
|
|
-0.390505508895 5. 2. 2. 1.08974964
|
|
|
|
|
|
@AUX !---Auxiliary function for Cp0
|
|
CP4 !Ideal gas heat capacity function for butane.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Polt, A., Platzer, B., and Maurer, G., 1992.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 58.124 !Reducing parameters for T, Cp0
|
|
5 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
0.801601 0.0
|
|
0.000655936 1.0
|
|
0.000012277 2.0
|
|
-0.165626e-7 3.0
|
|
0.67736e-11 4.0
|
|
|
|
|
|
|
|
|
|
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
|
|
|
#ETA !---Viscosity---
|
|
VS7 !Pure fluid viscosity model for butane of Herrman and Vogel (2018).
|
|
:DOI: 10.1063/1.5020802
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Herrmann, S. and Vogel, E.,
|
|
? "New Formulation for the Viscosity of n-Butane,"
|
|
? J. Phys. Chem. Ref. Data, 47, 013104, 2018.
|
|
? doi: 10.1063/1.5020802
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.895 !Lower temperature limit [K]
|
|
575.0 !Upper temperature limit [K]
|
|
200000.0 !Upper pressure limit [kPa]
|
|
13.86 !Maximum density [mol/L]
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
!
|
|
$VR RED TRED TEMP / =TR TR =TAU DENS DRED / =DEL
|
|
!
|
|
!Dilute gas
|
|
$DG CNST TR SQRT / SUMLOGT:3 EXP /
|
|
!
|
|
!Initial density viscosity
|
|
$VV CNST SUMTAU:9 DRED / *
|
|
!
|
|
!Residual function
|
|
$RF SUMTAUDEL:8
|
|
!
|
|
!Critical enhancement
|
|
$CE 30 SIGN DEL 1 - SQR * 220 TAU 1 - ABS * - EXP SUMTAUDEL:1 *
|
|
$CE 5 SIGN DEL 1 - SQR * 400 TAU 1 - ABS * - EXP SUMTAUDEL:1 * +
|
|
!
|
|
!Coefficients
|
|
$CF
|
|
1.0 425.125 3.922769613 0. 0 !Reducing parameters for eta, T, rho
|
|
1.0546549635209e3 0. 0. 0. 0 !Dilute gas terms
|
|
4.6147656002208 0. 0. 0. 0
|
|
4.5743185910390e-1 1. 0. 0. 0
|
|
3.0851104723224e-2 2. 0. 0. 0
|
|
4.89736312734e-1 0. 0. 0. 0 !Initial density terms
|
|
-1.95728810000e1 0. 0. 0. 0
|
|
1.98887362343e2 0.25 0. 0. 0
|
|
-8.31764209120e2 0.50 0. 0. 0
|
|
1.83218450345e3 0.75 0. 0. 0
|
|
-2.26510439059e3 1. 0. 0. 0
|
|
1.51348864395e3 1.25 0. 0. 0
|
|
-4.32819866497e2 1.5 0. 0. 0
|
|
5.19698852489 2.5 0. 0. 0
|
|
-3.86579291550e-2 5.5 0. 0. 0
|
|
2.3460864383872 2. 2. 0. 0 !Residual function
|
|
7.8632175809804e-1 5. 2. 0. 0
|
|
1.5823593499816e1 0. 2.5 0. 0
|
|
-9.4670516989296 0. 3. 0. 0
|
|
1.0511496276340 0. 5. 0. 0
|
|
-1.9355799491084e-2 4. 7.5 0. 0
|
|
1.4895031937816e-4 5. 10. 0. 0
|
|
1.2280342363570e-3 2.5 10.733333333333333 0. 0
|
|
1.2790911462043 1. 1. 0. 0
|
|
2.5581822924086e-1 1. 1. 0. 0
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
|
================================================================================
|
|
|
|
#TCX !---Thermal conductivity---
|
|
TC1 !Pure fluid thermal conductivity model for butane of Perkins et al. (2002).
|
|
:DOI: 10.1021/je0101202
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Perkins, R.A, Ramires, M.L.V., Nieto de Castro, C.A., and Cusco, L.,
|
|
? "Measurement and Correlation of the Thermal Conductivity of Butane
|
|
? from 135 K to 600 K at Pressures to 70 MPa,"
|
|
? J. Chem. Eng. Data, 47(5):1263-1271, 2002. doi: 10.1021/je0101202
|
|
?
|
|
?Uncertainty in thermal conductivity is 3%, except in the critical region
|
|
? and dilute gas which have an uncertainty of 5%.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.86 !Lower temperature limit [K]
|
|
600.0 !Upper temperature limit [K]
|
|
200000.0 !Upper pressure limit [kPa]
|
|
13.86 !Maximum density [mol/L]
|
|
3 0 !# terms for dilute gas function: numerator, denominator
|
|
425.16 1.0 !Reducing parameters for T, tcx
|
|
0.00162676 0. !Coefficient, power in T
|
|
9.75703e-4 1.
|
|
0.0289887 2.
|
|
10 0 !# terms for background gas function: numerator, denominator
|
|
425.16 3.92 1. !Reducing parameters for T, rho, tcx
|
|
-0.0304337 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
|
|
0.0418357 1. 1. 0.
|
|
0.16582 0. 2. 0.
|
|
-0.147163 1. 2. 0.
|
|
-0.148144 0. 3. 0.
|
|
0.133542 1. 3. 0.
|
|
0.05255 0. 4. 0.
|
|
-0.0485489 1. 4. 0.
|
|
-0.00629367 0. 5. 0.
|
|
0.00644307 1. 5. 0.
|
|
TK3 !Pointer to critical enhancement auxiliary function
|
|
|
|
|
|
#AUX !---Auxiliary function for the thermal conductivity critical enhancement
|
|
TK3 !Simplified thermal conductivity critical enhancement for butane of Perkins et al. (2002).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Perkins, R.A., Ramires, M.L.V., Castro de Nieto, C.A., and Cusco, L., 2002.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
9 0 0 0 !# terms: terms, spare, spare, spare
|
|
1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
|
|
0.63 !Nu (universal exponent)
|
|
1.239 !Gamma (universal exponent)
|
|
1.03 !R0 (universal amplitude)
|
|
0.063 !Z (universal exponent--not used for t.c., only viscosity)
|
|
1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
|
|
0.194e-9 !Xi0 (amplitude) [m]
|
|
0.0496 !Gam0 (amplitude) [-]
|
|
0.87535e-9 !Qd_inverse (modified effective cutoff parameter) [m]
|
|
637.68 !Tref (reference temperature) [K]
|
|
|
|
|
|
|
|
|
|
********************************************************************************
|
|
|
|
@TCX !---Thermal conductivity---
|
|
TC2 !Pure fluid thermal conductivity model for butane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.,
|
|
? "Thermophysical properties of fluids. II. Methane, ethane, propane,
|
|
? isobutane and normal butane,"
|
|
? J. Phys. Chem. Ref. Data, 16:577-798, 1987.
|
|
?
|
|
?The uncertainty in thermal conductivity is 2%, except in the critical region
|
|
? which is 10%. All temperatures on IPTS-68
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.86 !Lower temperature limit [K]
|
|
500.0 !Upper temperature limit [K]
|
|
70000.0 !Upper pressure limit [kPa]
|
|
13.86 !Maximum density [mol/L]
|
|
CI2 !Pointer to collision integral model
|
|
0.503103 !Lennard-Jones coefficient sigma [nm]
|
|
440.0 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
0.203525266 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12
|
|
1.530992335 !Dilute gas terms (Eq 27): Gt(1)
|
|
-0.2114511021 ! Gt(2)
|
|
0.004024170074 !Residual terms (Eqs 26, 28-30): Et(1)
|
|
1.561435847
|
|
-600.4381127
|
|
-0.0007547260841
|
|
-0.02069676662
|
|
93.82534978
|
|
-0.1711371457
|
|
36.47724935 !Et(8)
|
|
TK2 !Pointer to critical enhancement model (follows immediately)
|
|
0.000769608 !Critical enhancement terms (Eqs D1-D4): X1
|
|
13.2533
|
|
0.485554
|
|
1.01021 !X4
|
|
9.10218e-10 !Z
|
|
1.38054e-23 !Boltzmann's constant, k
|
|
1.630521851 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1)
|
|
0.0 !Fv(2)
|
|
1.40 !Fv(3)
|
|
425.16 !Fv(4)
|
|
-27.24386845 !Coefficients for residual viscosity, eqs (22 - 25)
|
|
801.2766611 !Ev(2) (the viscosity is also used in conductivity correlation)
|
|
25.03978646 !Ev(3)
|
|
-13097.04275 !Ev(4)
|
|
-0.08313305258 !Ev(5)
|
|
66.36975027 !Ev(6)
|
|
9849.317662 !Ev(7)
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS1 !Pure fluid viscosity model for butane of Vogel et al. (1999).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Vogel, E., Kuechenmeister, C., and Bich, E.,
|
|
? "Viscosity for n-Butane in the Fluid Region,"
|
|
? High Temp. - High Pressures, 31(2):173-186, 1999.
|
|
?
|
|
?The uncertainty in viscosity varies from 0.4% in the dilute gas between
|
|
? room temperature and 600 K, to 3.0% over the rest of the fluid surface.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.86 !Lower temperature limit [K]
|
|
500.0 !Upper temperature limit [K]
|
|
200000.0 !Upper pressure limit [kPa]
|
|
13.86 !Maximum density [mol/L]
|
|
1 !Number of terms associated with dilute-gas function
|
|
CI1 !Pointer to reduced effective collision cross-section model
|
|
0.57335 !Lennard-Jones coefficient sigma [nm]
|
|
280.51 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
1.0 1.0 !Reducing parameters for T, eta
|
|
0.1628213 0.5 !Chapman-Enskog term
|
|
9 !Number of terms for initial density dependence
|
|
280.51 0.1135034 !Reducing parameters for T (= eps/k), etaB2 (= 0.6022137*sigma**3)
|
|
-19.572881 0.0 !Coefficient, power in T* = T/(eps/k)
|
|
219.73999 -0.25
|
|
-1015.3226 -0.5
|
|
2471.01251 -0.75
|
|
-3375.1717 -1.0
|
|
2491.6597 -1.25
|
|
-787.26086 -1.5
|
|
14.085455 -2.5
|
|
-0.34664158 -5.5
|
|
2 13 1 2 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
|
|
425.125 3.92 1.0 !Reducing parameters for T, rho, eta
|
|
2.30873963359 0.0 0. 0. 0
|
|
2.03404037254 0.5 0. 0. 0
|
|
-54.7737770846 0.0 2. 0. 0
|
|
58.0898623034 -1.0 2. 0. 0
|
|
0.0 -2.0 2. 0. 0
|
|
35.2658446259 0.0 3. 0. 0
|
|
-39.6682203832 -1.0 3. 0. 0
|
|
0.0 -2.0 3. 0. 0
|
|
-1.83729542151 0.0 4. 0. 0
|
|
0.0 -1.0 4. 0. 0
|
|
0.0 -2.0 4. 0. 0
|
|
-0.833262985358 0.0 5. 0. 0
|
|
1.93837020663 -1.0 5. 0. 0
|
|
0.0 -2.0 5. 0. 0
|
|
-188.075903903 0.0 1. -1. 0
|
|
188.075903903 0.0 1. 0. 0
|
|
1.0 0.0 0. 1. 0
|
|
-1.0 0.0 1. 0. 0
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
@AUX !---Auxiliary function for the collision integral
|
|
CI1 !Collision integral model for butane of Vogel et al. (1999).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Vogel, E., Kuechenmeister, C., and Bich, E., 1999.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
3 !Number of terms
|
|
0.17067154 0 !Coefficient, power of Tstar
|
|
-0.48879666 1
|
|
0.039038856 2
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS2 !Pure fluid viscosity model for butane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F., 1987.
|
|
?
|
|
?The uncertainty in viscosity is 2%, except in the critical region which is 5%.
|
|
? All temperatures are given on IPTS-68.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.86 !Lower temperature limit [K]
|
|
500.0 !Upper temperature limit [K]
|
|
70000.0 !Upper pressure limit [kPa]
|
|
13.86 !Maximum density [mol/L]
|
|
CI2 !Pointer to collision integral model
|
|
0.503103 !Lennard-Jones coefficient sigma [nm]
|
|
440.0 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
0.20352457 !Const in Eq 19 = 5/16*(k*MW/1000/pi/Na)**0.5*1.0d12
|
|
0.5 !Exponent in Eq 19 for T
|
|
1.630521851 !Coefficient for initial density dependence of viscosity (eq 21); Fv(1)
|
|
0.0 !Fv(2)
|
|
1.40 !Fv(3)
|
|
425.16 !Fv(4)
|
|
-27.24386845 !Coefficients for residual viscosity, eqs (22 - 25)
|
|
801.2766611 !Ev(2)
|
|
25.03978646 !Ev(3)
|
|
-13097.04275 !Ev(4)
|
|
-0.08313305258 !Ev(5)
|
|
66.36975027 !Ev(6)
|
|
9849.317662 !Ev(7)
|
|
3.920 !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 butane of Younglove and Ely (1987).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Younglove, B.A. and Ely, J.F.,
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
9 !Number of terms
|
|
-3.0328138281 0 !Omega (eq 20): coeffs of {(e/kT)**((4-n)/3)}
|
|
16.918880086 0 !There is misprint in Younglove and Ely, the exponent
|
|
-37.189364917 0 ! is ((4-n)/3) not ((n+2)/3)
|
|
41.288861858 0
|
|
-24.61592114 0
|
|
8.948843096 0
|
|
-1.8739245042 0
|
|
0.209661014 0 !Wrong sign in Younglove and Ely, Table 2
|
|
-0.009657044 0
|
|
|
|
|
|
@ETA !---Viscosity---
|
|
VS4 !Pure fluid generalized friction theory viscosity model for butane of Quinones-Cisneros and Deiters (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Quinones-Cisneros, S.E. and Deiters, U.K.,
|
|
? "Generalization of the Friction Theory for Viscosity Modeling,"
|
|
? J. Phys. Chem. B, 110(25):12820-12834, 2006. doi: 10.1021/jp0618577
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.895 !Lower temperature limit [K]
|
|
500.0 !Upper temperature limit [K]
|
|
68000.0 !Upper pressure limit [kPa]
|
|
13.86 !Maximum density [mol/L]
|
|
4 0 0 0 0 0 !Number of terms associated with dilute-gas function
|
|
NUL !Pointer to reduced effective collision cross-section model; not used
|
|
0.503103 !Lennard-Jones coefficient sigma [nm] (not used)
|
|
440.0 !Lennard-Jones coefficient epsilon/kappa [K] (not used)
|
|
425.125 1.0 !Reducing parameters for T, eta
|
|
0.0 0.5 !Chapman-Enskog term; not used here
|
|
18.3983 0.0 !Empirical terms for eta0
|
|
-57.1255 0.25
|
|
49.3197 0.5
|
|
0 !Number of terms for initial density dependence
|
|
-1.34110938674421e-5 -8.56587924603951e-5 -6.45720639242339e-13 0. 0. ! a(0),a(1),a(2)
|
|
1.49859653515567e-4 -1.71133855507542e-4 7.37953726544736e-13 0. 0. ! b(0),b(1),b(2)
|
|
3.53018109777015e-7 -1.93040375218067e-5 -1.26469933968355e-14 0. 0. ! c(0),c(1),c(2)
|
|
-3.63389393526204e-9 -7.73717469888952e-10 0.0 0. 0. ! A(0),A(1),A(2)
|
|
3.70980259815724e-8 2.07658634467549e-9 0.0 0. 0. ! B(0),B(1),B(2)
|
|
-1.12495594619911e-7 7.66906137372152e-8 0.0 0. 0. ! C(0),C(1),C(2)
|
|
0.0 0.0 0.0 0. 0. ! D(0),D(1),D(2)
|
|
0.0 0.0 0.0 0. 0. ! E(0),E(1),E(2)
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
|
|
|
|
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
|
|
|
@TRN !---ECS Transport---
|
|
ECS !Extended Corresponding States model (Nitrogen reference); predictive mode for butane.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Klein, S.A., McLinden, M.O., and Laesecke, A., "An Improved Extended Corresponding States Method for Estimation of Viscosity of Pure Refrigerants and Mixtures," Int. J. Refrigeration, 20(3):208-217, 1997. doi: 10.1016/S0140-7007(96)00073-4.
|
|
?McLinden, M.O., Klein, S.A., and Perkins, R.A., "An Extended Corresponding States Model for the Thermal Conductivity of Refrigerants and Refrigerant Mixtures," Int. J. Refrigeration, 23(1):43-63, 2000. doi: 10.1016/S0140-7007(99)00024-9
|
|
?
|
|
?Thermal conductivity and viscosity data used in the development of the
|
|
? extended corresponding states correlations were taken from:
|
|
? 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(4):577-798, 1987. doi: 10.1063/1.555785
|
|
?
|
|
?The Lennard-Jones parameters were taken from Reid, R.C., Prausnitz, J.M., and Poling, B.E., "The Properties of Gases and Liquids," 4th edition, New York, McGraw-Hill Book Company, 1987.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.86 !Lower temperature limit [K]
|
|
500.0 !Upper temperature limit [K]
|
|
70000.0 !Upper pressure limit [kPa]
|
|
13.86 !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)
|
|
0.57335 !Lennard-Jones coefficient sigma [nm]
|
|
280.51 !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
|
|
|
|
|
|
|
|
|
|
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
|
|
|
|
#STN !---Surface tension---
|
|
ST1 !Surface tension model for butane 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. !
|
|
1 !Number of terms in surface tension model
|
|
425.125 !Critical temperature used in fit (dummy)
|
|
0.05138 1.209 !Sigma0 and n
|
|
|
|
|
|
#DE !---Dielectric constant---
|
|
DE3 !Dielectric constant model for butane of Harvey and Lemmon (2005).
|
|
:DOI: 10.1007/s10765-005-2351-5
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Harvey, A.H. and Lemmon, E.W.,
|
|
? "Method for Estimating the Dielectric Constant of Natural Gas Mixtures,"
|
|
? Int. J. Thermophys., 26(1):31-46, 2005. doi: 10.1007/s10765-005-2351-5
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
273.16 1000.0 1.0 !Reducing parameters for T and D
|
|
1 2 4 0 0 0 !Number of terms in dielectric constant model
|
|
0.0557549 -1. 1. 0. !Coefficient, T exp, D exp
|
|
20.611 0. 1. 0.
|
|
0.020 1. 1. 0.
|
|
66.64 0. 2. 0.
|
|
24.44 1. 2. 0.
|
|
-7461.2 0. 3. 0.
|
|
-1983.6 1. 3. 0.
|
|
|
|
|
|
#MLT !---Melting line---
|
|
ML1 !Melting line model for butane of Buecker and Wagner (2005).
|
|
:DOI: 10.1063/1.1901687
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Bücker, D. and Wagner, W.,
|
|
? "Reference Equations of State for the Thermodynamic Properties of Fluid
|
|
? Phase n-Butane and Isobutane,"
|
|
? J. Phys. Chem. Ref. Data, 35(1):929-1019, 2006. doi: 10.1063/1.1901687
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
134.895 !Lower temperature limit [K]
|
|
575.0 !Upper temperature limit [K]
|
|
0. !
|
|
0. !
|
|
134.895 0.00066566 !Reducing temperature and pressure
|
|
2 0 0 0 0 0 !Number of terms in melting line equation
|
|
-558558235.4 0.0 !Coefficients and exponents
|
|
558558236.4 2.206
|
|
|
|
|
|
#PS !---Vapor pressure---
|
|
PS5 !Vapor pressure equation for butane of Lemmon (2010).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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. !
|
|
425.125 3796.0 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
-7.1897 1.0
|
|
2.6122 1.5
|
|
-2.1729 2.0
|
|
-2.7230 4.5
|
|
|
|
|
|
#DL !---Saturated liquid density---
|
|
DL1 !Saturated liquid density equation for butane of Lemmon (2010).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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. !
|
|
425.125 3.922769613 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
5.2341 0.44
|
|
-6.2011 0.60
|
|
3.6063 0.76
|
|
0.22137 5.0
|
|
|
|
|
|
#DV !---Saturated vapor density---
|
|
DV3 !Saturated vapor density equation for butane of Lemmon (2010).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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. !
|
|
425.125 3.922769613 !Reducing parameters
|
|
5 0 0 0 0 0 !Number of terms in equation
|
|
-2.7390 0.391
|
|
-5.7347 1.14
|
|
-16.408 3.0
|
|
-46.986 6.5
|
|
-100.90 14.0
|
|
|
|
|
|
@END
|
|
c 1 2 3 4 5 6 7 8
|
|
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|
|
|
|
|
|
@PS !Vapor pressure equation
|
|
PS5 vapor pressure equation of Buecker and Wagner (2005).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Functional Form: P=Pc*EXP[SUM(Ni*Theta^ti)*Tc/T] where Theta=1-T/Tc, Tc and Pc
|
|
? are the reducing parameters below, which are followed by rows containing Ni and ti.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
425.125 3796.0 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
-7.17616903 1.0
|
|
2.53635336 1.5
|
|
-2.07532869 2.0
|
|
-2.82241113 4.5
|
|
|
|
|
|
@DL !Saturated liquid density equation
|
|
DL1 saturated liquid density equation of Buecker and Wagner (2005).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?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. !
|
|
425.125 3.922769613 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
1.97874515 0.345
|
|
0.856799510 1.0
|
|
-0.341871887 1.5
|
|
0.304337558 3.0
|
|
|
|
|
|
@DV !Saturated vapor density equation
|
|
DV6 saturated vapor density equation of Buecker and Wagner (2005).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Functional Form: D=Dc*EXP[SUM(Ni*Theta^(ti/3))*Tc/T] 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. !
|
|
425.125 3.922769613 !Reducing parameters
|
|
4 0 0 0 0 0 !Number of terms in equation
|
|
-2.07770057 1.035
|
|
-3.08362490 2.5
|
|
-0.485645266 9.5
|
|
-3.83167519 12.5
|
|
|
|
|