545 lines
26 KiB
Plaintext
545 lines
26 KiB
Plaintext
Decane !Short name
|
|
124-18-5 !CAS number
|
|
Decane !Full name
|
|
CH3-8(CH2)-CH3 !Chemical formula {C10H22}
|
|
n-Decane !Synonym
|
|
142.28168 !Molar mass [g/mol]
|
|
243.5 !Triple point temperature [K]
|
|
447.27 !Normal boiling point [K]
|
|
617.7 !Critical temperature [K]
|
|
2103.0 !Critical pressure [kPa]
|
|
1.64 !Critical density [mol/L]
|
|
0.4884 !Acentric factor
|
|
0.07 !Dipole moment [Debye]; (estimated value)
|
|
NBP !Default reference state
|
|
10.0 !Version number
|
|
2247 !UN Number :UN:
|
|
n-alkane !Family :Family:
|
|
6829.77 !Heating value (upper) [kJ/mol] :Heat:
|
|
1S/C10H22/c1-3-5-7-9-10-8-6-4-2/h3-10H2,1-2H3 :InChi: !Standard InChI String
|
|
DIOQZVSQGTUSAI-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
|
|
???? !Alternative fluid for mixing rules :AltID:
|
|
111888d0 !Hash number from InChI Key :Hash:
|
|
|
|
|
|
|
|
|
|
!The fluid files contain general information about the fluid in the first 15 to 20 lines, followed by sections for the
|
|
! equations of state, transport equations, and auxiliary equations. Equations of state are listed first. The NIST recommended
|
|
! equations begin with a hash mark (#). The secondary equations begin with the @ symbol. These symbols can be swapped to
|
|
! select a secondary equation as primary and the primary as secondary. The equation of state section also contains auxiliary
|
|
! equations for the ideal gas heat capacity or ideal gas Helmholtz energy. Below the equations of state (both primary and
|
|
! secondary) are the transport equations, first viscosity and then thermal conductivity. These are then followed by the
|
|
! secondary equations if available. The transport section also contains auxiliary equations required to calculate either the
|
|
! dilute gas state or the critical enhancement. At the end of the file are additional but not necessary auxiliary equations,
|
|
! including simple equations for the vapor pressure, saturated liquid and vapor densities, melting line (for some fluids), and
|
|
! sublimation line (for even fewer fluids). This section also contains the equations for dielectric constant and surface
|
|
! tension if available. The sections are divided by different symbols (these being _-+=^*~) to aid the eye in locating a
|
|
! particular section. Secondary equations are indented 10 spaces to avoid confusion with the NIST recommended equations. The
|
|
! end of the fluid file is marked with @END. Anything below that is ignored.
|
|
|
|
|
|
! compiled by E.W. Lemmon, NIST Physical and Chemical Properties Division, Boulder, Colorado
|
|
! 02-07-01 EWL, Original version.
|
|
! 03-13-03 EWL, Replace cp0 equation.
|
|
! 02-09-04 EWL, Revise EOS fit.
|
|
! 02-28-04 MLH, Add viscosity VS1 fit.
|
|
! 03-18-04 MLH, Add thermal conductivity TC1 fit.
|
|
! 04-19-04 MLH, Add TC1, VS1 references.
|
|
! 07-07-04 AHH, Update dipole moment.
|
|
! 08-05-04 EWL, Add Harvey and Lemmon dielectric correlation.
|
|
! 10-13-04 MLH, Add family.
|
|
! 11-14-09 EWL, Duplicate FEQ as FEK and use PHK so as to work with GERG-2008.
|
|
! 06-21-10 CKL, Add ancillary equations.
|
|
! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
|
|
|
|
|
|
|
|
|
|
________________________________________________________________________________
|
|
|
|
#EOS !---Equation of state---
|
|
FEQ !Helmholtz equation of state for decane of Lemmon and Span (2006).
|
|
:TRUECRITICALPOINT: 617.7 1.64 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
|
|
:DOI: 10.1021/je050186n
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Lemmon, E.W. and Span, R.,
|
|
? "Short Fundamental Equations of State for 20 Industrial Fluids,"
|
|
? J. Chem. Eng. Data, 51(3):785-850, 2006. doi: 10.1021/je050186n
|
|
?
|
|
?The uncertainties in density are 0.05% in the saturated liquid density
|
|
? between 290 and 320 K, 0.2% in the liquid phase at temperatures to 400 K
|
|
? (with somewhat higher uncertainties above 100 MPa, up to 0.5%), 1% in the
|
|
? liquid phase up to 500 K, and 2% at higher temperatures as well as in the
|
|
? vapor phase. Vapor pressures have an uncertainty of 0.2% and the
|
|
? uncertainties in liquid heat capacities and liquid sound speeds are 1%.
|
|
? The uncertainty in heat capacities may be higher at pressures above 10 MPa.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
243.5 !Lower temperature limit [K]
|
|
675.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
5.41 !Maximum density [mol/L]
|
|
CPP !Pointer to Cp0 model
|
|
142.28168 !Molar mass [g/mol]
|
|
243.5 !Triple point temperature [K]
|
|
0.001404 !Pressure at triple point [kPa]
|
|
5.41 !Density at triple point [mol/L]
|
|
447.27 !Normal boiling point temperature [K]
|
|
0.4884 !Acentric factor
|
|
617.7 2103.0 1.64 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
617.7 1.64 !Reducing parameters [K, mol/L]
|
|
8.314472 !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
|
|
1.0461 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
|
-2.4807 1.125 1. 0.
|
|
0.74372 1.5 1. 0.
|
|
-0.52579 1.375 2. 0.
|
|
0.15315 0.25 3. 0.
|
|
0.00032865 0.875 7. 0.
|
|
0.84178 0.625 2. 1.
|
|
0.055424 1.75 5. 1.
|
|
-0.73555 3.625 1. 2.
|
|
-0.18507 3.625 4. 2.
|
|
-0.020775 14.5 3. 3.
|
|
0.012335 12.0 4. 3.
|
|
|
|
|
|
#AUX !---Auxiliary function for Cp0
|
|
CPP !Ideal gas heat capacity function for decane of Lemmon and Span (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Lemmon, E.W. and Span, R., 2006.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1.0 8.314472 !Reducing parameters for T, Cp0
|
|
1 4 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
|
|
19.109 0.0
|
|
25.685 1193.0
|
|
28.233 2140.0
|
|
12.417 4763.0
|
|
10.035 10862.0
|
|
|
|
|
|
#AUX !---Auxiliary function for PX0
|
|
PX0 !Helmholtz energy ideal-gas function for decane of Lemmon and Span (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Lemmon, E.W. and Span, R., 2006.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
|
|
18.109 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
|
13.936202857079877 0.0 !aj, ti for [ai*tau**ti] terms
|
|
-10.5265173263752523 1.0 !aj, ti for [ai*tau**ti] terms
|
|
25.685 1193.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
|
|
28.233 2140.0
|
|
12.417 4763.0
|
|
10.035 10862.0
|
|
|
|
|
|
#AUX !---Auxiliary function for PH0
|
|
PH0 !Ideal gas Helmholtz form for decane.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Lemmon, E.W. and Span, R., 2006.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1 2 4 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
|
|
18.109 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
|
13.9361966549 0.0 !aj, ti for [ai*tau**ti] terms
|
|
-10.5265128286 1.0
|
|
25.685 -1.9313582645 !aj, ti for [ai*log(1-exp(ti*tau)] terms
|
|
28.233 -3.4644649506
|
|
12.417 -7.7108628784
|
|
10.035 -17.5845879877
|
|
|
|
|
|
|
|
|
|
--------------------------------------------------------------------------------
|
|
|
|
@EOS !---Equation of state---
|
|
FEK !Helmholtz equation of state for decane of Lemmon and Span (2006).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Lemmon, E.W. and Span, R.,
|
|
? "Short Fundamental Equations of State for 20 Industrial Fluids,"
|
|
? J. Chem. Eng. Data, 51(3):785-850, 2006. doi: 10.1021/je050186n
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
243.5 !Lower temperature limit [K]
|
|
675.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
5.41 !Maximum density [mol/L]
|
|
PHK !Pointer to Cp0 model
|
|
142.28168 !Molar mass [g/mol]
|
|
243.5 !Triple point temperature [K]
|
|
0.0014 !Pressure at triple point [kPa]
|
|
5.41 !Density at triple point [mol/L]
|
|
447.27 !Normal boiling point temperature [K]
|
|
0.4884 !Acentric factor
|
|
617.7 2103.0 1.64 !Tc [K], pc [kPa], rhoc [mol/L]
|
|
617.7 1.64 !Reducing parameters [K, mol/L]
|
|
8.314472 !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
|
|
1.0461 0.25 1. 0. !a(i),t(i),d(i),l(i)
|
|
-2.4807 1.125 1. 0.
|
|
0.74372 1.5 1. 0.
|
|
-0.52579 1.375 2. 0.
|
|
0.15315 0.25 3. 0.
|
|
0.00032865 0.875 7. 0.
|
|
0.84178 0.625 2. 1.
|
|
0.055424 1.75 5. 1.
|
|
-0.73555 3.625 1. 2.
|
|
-0.18507 3.625 4. 2.
|
|
-0.020775 14.5 3. 3.
|
|
0.012335 12.0 4. 3.
|
|
|
|
|
|
@AUX !---Auxiliary function for PH0
|
|
PHK !Ideal gas Helmholtz form for decane of Kunz and Wagner (2004).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Kunz, O., Klimeck, R., Wagner, W., Jaeschke, M.
|
|
? "The GERG-2004 Wide-Range Equation of State for Natural Gases
|
|
? and Other Mixtures," GERG Technical Monograph 15,
|
|
? Fortschritt-Berichte VDI, VDI-Verlag, Düsseldorf, 2007.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
1 2 0 1 2 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
|
|
3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
|
|
15.870791919 0.0 !aj, ti for [ai*tau**ti] terms
|
|
-108.858547525 1.0
|
|
-43.4931 1.353835195 !aj, ti for cosh and sinh terms
|
|
21.0069 0.267034159
|
|
58.3657 2.833479035
|
|
|
|
|
|
|
|
|
|
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
|
|
|
|
#ETA !---Viscosity---
|
|
VS1 !Pure fluid viscosity model for decane of Huber et al. (2004).
|
|
:DOI: 10.1016/j.fluid.2005.03.008
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Huber, M.L., Laesecke, A., and Xiang, H.W.,
|
|
? "Viscosity Correlations for Minor Constituent Fluids in Natural
|
|
? Gas: n-Octane, n-Nonane and n-Decane,"
|
|
? Fluid Phase Equilib., 224:263-270, 2004.
|
|
?
|
|
?The estimated uncertainty in viscosity is 1% along the saturated liquid line,
|
|
? 2% in compressed liquid to 200 MPa, and 5% in vapor and supercritical regions.
|
|
?
|
|
?DATA SOURCES FOR VISCOSITY
|
|
? The parameters for viscosity were based in part on the data of:
|
|
? Knapstad, B., Skolsvik, P.A., and Oye, H.A., "Viscosity of Pure Hydrocarbons," J. Chem. Eng. Data, 34:37-43, 1989.
|
|
? Knapstad, B., Skjolsvik, P.A., and Oye, H.A., "Viscosity of Three Binary Hydrocarbon Mixtures," J. Chem. Eng. Data, 36:84-88, 1991.
|
|
? 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.
|
|
? 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," paper presented at 15th Symposium on Thermophysical Properties, Boulder CO 80303, June, 2003.
|
|
? Lyusternik, V.E. and Zhdanov, A.G., Teplofiz. Svoistva Veshchestv Mater, No.7, Rabinovich, V.A. ed., Standards Publishing, Moscow, 1973.
|
|
? Average absolute deviations of the fit from the experimental data are:
|
|
? Knapstad, 1989: avg 0.33% (max 0.93); Knapstad, 1991: avg 0.65% (max. 1.72);
|
|
? Caudwell: avg 1.05% (max 1.97); Lyusternik: 0.76% (max 1.60).
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
243.5 !Lower temperature limit [K]
|
|
1000.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
8.0 !Maximum density [mol/L]
|
|
1 !Number of terms associated with dilute-gas function
|
|
CI1 !Pointer to reduced effective collision cross-section model
|
|
0.6860 !Lennard-Jones coefficient sigma [nm]
|
|
490.51 !Lennard-Jones coefficient epsilon/kappa [K]
|
|
1.0 1.0 !Reducing parameters for T, eta
|
|
0.2547503 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term]
|
|
9 !Number of terms for initial density dependence
|
|
490.51 0.194412 !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
|
|
2471.0125 -0.75
|
|
-3375.1717 -1.0
|
|
2491.6597 -1.25
|
|
-787.26086 -1.5
|
|
14.085455 -2.5
|
|
-0.34664158 -5.50
|
|
3 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
|
|
617.7 1.64 1000.0 !Reducing parameters for T, rho, eta (Laesecke correlation in terms of mPa-s, convert to uPa-s)
|
|
2.55105 0.0 0. 0. 0 ! c10
|
|
1.71465 0.5 0. 0. 0 ! c8
|
|
0.0 1.0 0. 0. 0 ! c22
|
|
-0.0402094 -1.0 2. 0. 0 ! beta16; powers of tau, del, del0; power of del in exponential [0= no exp.]
|
|
0.0 -1.0 3. 0. 0 ! beta17; powers of tau, del, del0; power of del in exponential [0= no exp.]
|
|
0.0404435 -2.0 2. 0. 0 ! beta18; powers of tau, del, del0; power of del in exponential [0= no exp.]
|
|
-0.0142063 -2.0 3. 0. 0 ! beta19; powers of tau, del, del0; power of del in exponential [0= no exp.]
|
|
-0.453387 0.0 1. -1. 0 ! beta7 over del0 term
|
|
0.453387 0.0 1. 0. 0 ! beta7 in non-simple poly term
|
|
1.0 0.0 0. 1. 0 ! del0 term in denominator
|
|
-1.0 0.0 1. 0. 0 ! -del term in denominator
|
|
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
|
|
|
|
|
|
#AUX !---Auxiliary function for the collision integral
|
|
CI1 !Reduced effective collision cross-section model (empirical form in log(T*)) for decane.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Huber, M.L., Laesecke, A., and Xiang, H.W., 2004.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
2 !Number of terms
|
|
0.343267 0 !Coefficient, power of Tstar
|
|
-0.460514 1
|
|
|
|
|
|
|
|
|
|
================================================================================
|
|
|
|
#TCX !---Thermal conductivity---
|
|
TC1 !Pure fluid thermal conductivity model for decane of Huber and Perkins (2005).
|
|
:DOI: 10.1016/j.fluid.2004.10.031
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Huber, M.L. and Perkins, R.A., "Thermal Conductivity Correlations for
|
|
? Minor Constituent Fluids in Natural Gas: n-Octane, n-Nonane and n-Decane,"
|
|
? Fluid Phase Equilib., 227:47-55, 2005.
|
|
?
|
|
?Uncertainty in thermal conductivity is 3%, except in the supercritical region
|
|
? and dilute gas which have an uncertainty of 5%.
|
|
?
|
|
?DATA SOURCES FOR THERMAL CONDUCTIVITY
|
|
? Tanaka, Y., 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.
|
|
? Mustafaev, R.A., "Thermal Conductivity of Vapors of Normal Saturated Hydrocarbons at High Temperatures," Izv. Vyssh. Ucheb. Zaved., Neft Gaz, 16(11):71-74, 1973.
|
|
? Watanabe, H., Seong, D.J., "The Thermal Conductivity and Thermal Diffusivity of Liquid n-Alkanes: CnH2n+2 (n=5 to 10) and Toluene," Int. J. Thermophys., 23:337-356, 2002.
|
|
? Average absolute deviations of the fit from the experimental data are:
|
|
? Tanaka et al.: 0.82% (max -2.31); Mustafaev: 0.82% (max -2.69);
|
|
? Watanabe and Seong: 0.11% (max 0.20).
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
243. !Lower temperature limit [K]
|
|
1000. !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
8.0 !Maximum density [mol/L]
|
|
4 0 !# terms for dilute gas function: numerator, denominator
|
|
617.7 1.0 !Reducing parameters for T, tcx
|
|
0.0105543 0. !Coefficient, power in T
|
|
-0.051453 1. !(2)
|
|
0.118979 2. !(3)
|
|
-0.0372442 3. !(16)
|
|
10 0 !# terms for background gas function: numerator, denominator
|
|
617.7 1.64 1. !Reducing parameters for T, rho, tcx
|
|
-0.0294394 0. 1. 0. !Coefficient, powers of T, rho, spare for future use
|
|
0.0150509 1. 1. 0.
|
|
0.0499245 0. 2. 0.
|
|
0.0 1. 2. 0.
|
|
-0.01427 0. 3. 0.
|
|
-0.0138857 1. 3. 0.
|
|
0.00150828 0. 4. 0.
|
|
0.00433326 1. 4. 0.
|
|
0.0 0. 5. 0.
|
|
0.0 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 decane of Olchowy and Sengers (1989).
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Olchowy, G.A. and Sengers, J.V.,
|
|
? "A Simplified Representation For the Thermal Conductivity of Fluids in the Critical Region,"
|
|
? Int. J. Thermophys., 10:417-426, 1989. doi: 10.1007/BF01133538
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
0. !
|
|
10000. !
|
|
0. !
|
|
0. !
|
|
9 0 0 0 !# terms: CO2-terms, spare, spare, spare
|
|
1.0 1.0 1.0 !Reducing parameters for T, rho, tcx [mW/(m-K)]
|
|
0.63 !Nu (universal exponent)
|
|
1.239 !Gamma (universal exponent)
|
|
1.03 !R0 (universal amplitude)
|
|
0.063 !Z (universal exponent--not used for t.c., only viscosity)
|
|
1.0 !C (constant in viscosity eqn = 1/[2 - (alpha + gamma)/(2*nu)], but often set to 1)
|
|
0.194e-9 !Xi0 (amplitude) [m]
|
|
0.0496 !Gam0 (amplitude) [-]
|
|
7.086368e-10 !Qd_inverse (modified effective cutoff parameter) [m]; fitted to data
|
|
926.55 !Tref (reference temperature)=1.5*Tc [K]
|
|
|
|
|
|
|
|
|
|
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
|
|
|
|
@TRN !---ECS Transport---
|
|
ECS !Extended Corresponding States model (Nitrogen reference); predictive mode for decane.
|
|
?
|
|
?```````````````````````````````````````````````````````````````````````````````
|
|
?Klein, S.A., McLinden, M.O., and Laesecke, A., "An Improved Extended Corresponding States Method for Estimation of Viscosity of Pure Refrigerants and Mixtures," Int. J. Refrigeration, 20(3):208-217, 1997. doi: 10.1016/S0140-7007(96)00073-4.
|
|
?McLinden, M.O., Klein, S.A., and Perkins, R.A., "An Extended Corresponding States Model for the Thermal Conductivity of Refrigerants and Refrigerant Mixtures," Int. J. Refrigeration, 23(1):43-63, 2000. doi: 10.1016/S0140-7007(99)00024-9
|
|
?
|
|
?The Lennard-Jones parameters were estimated with the method of Chung.
|
|
?
|
|
!```````````````````````````````````````````````````````````````````````````````
|
|
243. !Lower temperature limit [K]
|
|
1000.0 !Upper temperature limit [K]
|
|
800000.0 !Upper pressure limit [kPa]
|
|
8.0 !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)
|
|
0.686 !Lennard-Jones coefficient sigma [nm] for ECS method
|
|
490.51 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method
|
|
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 decane 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
|
|
617.7 !Critical temperature used in fit (dummy)
|
|
0.05473 1.29 !Sigma0 and n
|
|
|
|
|
|
#DE !---Dielectric constant---
|
|
DE3 !Dielectric constant model for decane 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
|
|
0.10924 -1. 1. 0. !Coefficient, T exp, D exp
|
|
49.32 0. 1. 0.
|
|
0.050 1. 1. 0.
|
|
220.15 0. 2. 0.
|
|
-316.3 1. 2. 0.
|
|
-88358.0 0. 3. 0.
|
|
53511.0 1. 3. 0.
|
|
|
|
|
|
#PS !---Vapor pressure---
|
|
PS5 !Vapor pressure equation for decane 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. !
|
|
617.7 2103.0 !Reducing parameters
|
|
5 0 0 0 0 0 !Number of terms in equation
|
|
-8.7738 1.0
|
|
4.0864 1.5
|
|
-4.0775 1.93
|
|
-6.4910 4.14
|
|
1.5598 4.7
|
|
|
|
|
|
#DL !---Saturated liquid density---
|
|
DL1 !Saturated liquid density equation for decane 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. !
|
|
617.7 1.64 !Reducing parameters
|
|
5 0 0 0 0 0 !Number of terms in equation
|
|
9.2435 0.535
|
|
-16.288 0.74
|
|
20.445 1.0
|
|
-17.624 1.28
|
|
7.3796 1.57
|
|
|
|
|
|
#DV !---Saturated vapor density---
|
|
DV3 !Saturated vapor density equation for decane 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. !
|
|
617.7 1.64 !Reducing parameters
|
|
6 0 0 0 0 0 !Number of terms in equation
|
|
-5.0378 0.4985
|
|
-3.4694 1.33
|
|
-15.906 2.43
|
|
-82.894 5.44
|
|
29.336 5.8
|
|
-109.85 11.0
|
|
|
|
|
|
@END
|
|
c 1 2 3 4 5 6 7 8
|
|
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
|