TyroneGit/CapMachine
1
0
Fork 0
Code Issues Pull Requests Actions Packages Projects Releases Wiki Activity

一些优化：CAN和PLC地址的优化

Browse Source
This commit is contained in:
Tyrone CT
2025-01-01 13:11:13 +08:00
parent 8b21846424
commit 26569135d3
182 changed files with 87934 additions and 261 deletions
Download Patch File Download Diff File Expand all files Collapse all files

628
CapMachine.Wpf/PPCalculation/REFPROP/FLUIDS/BENZENE.FLD Normal file
View File

@@ -0,0 +1,628 @@
Benzene !Short name
71-43-2 !CAS number
Benzene !Full name
C6H6 !Chemical formula {C6H6}
Benzene !Synonym
78.11184 !Molar mass [g/mol]
278.674 !Triple point temperature [K]; Reid, Prausnitz, & Poling, McGraw-Hill (1987)
353.219 !Normal boiling point [K]
562.02 !Critical temperature [K]
4907.277 !Critical pressure [kPa]
3.901 !Critical density [mol/L]
0.211 !Acentric factor
0.0 !Dipole moment [Debye]; (exactly zero due to symmetry)
NBP !Default reference state
10.0 !Version number
1114 !UN Number :UN:
aromatic !Family :Family:
3301.43 !Heating value (upper) [kJ/mol] :Heat:
1S/C6H6/c1-2-4-6-5-3-1/h1-6H !Standard InChI String :InChi:
UHOVQNZJYSORNB-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
cb03ba40 (hexane) !Alternative fluid for mixing rules :AltID:
f2cfb460 !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
! 11-13-98 EWL, Original version.
! 10-14-99 EWL, Add L-J parameters.
! 11-08-01 EWL, Change dmax.
! 08-08-05 EWL, Change tlow to ttrp.
! 08-18-10 EWL, Add equation of state of Thol et al.
! 08-19-10 IDC, Add ancillary equations.
! 07-10-12 MLH, Add transport.
! 12-06-12 EWL, Add surface tension coefficients of Mulero et al. (2012).
! 02-20-13 EWL, Add final equation of state of Thol et al. (2013).
! 04-06-13 EWL, Add dipole moment.
! 09-21-15 MLH, Add viscosity correlation of Avgeri et al. (2014).
________________________________________________________________________________
#EOS !---Equation of state---
FEQ !Helmholtz equation of state for benzene of Thol et al. (2015).
:TRUECRITICALPOINT: 562.02 3.901 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
:DOI:
?
?```````````````````````````````````````````````````````````````````````````````
?Thol, M., Lemmon, E.W., and Span, R.,
? Unpublished equation of state, but similar to the one published in:
? "Equation of State for Benzene for Temperatures from the Melting Line up to
? 725 K with Pressures up to 500 MPa,"
? High Temp.-High Press., 41:81-97, 2012.
?
?The estimated uncertainties of properties calculated with the equation
? for benzene are 0.1% below 350 K and 0.2% above 350 K for saturated vapor
? pressures and liquid densities, 1% for saturated vapor densities, 0.1% for
? densities up to 350 K and 100 MPa, 0.1 - 0.5% in density above 350 K, 1% for
? the isobaric heat capacities and saturated heat capacities, and 0.5% for
? sound speeds. Deviations in the critical region are higher for all
? properties except saturated vapor pressures.
?
!```````````````````````````````````````````````````````````````````````````````
278.674 !Lower temperature limit [K]
725.0 !Upper temperature limit [K]
500000.0 !Upper pressure limit [kPa]
11.45 !Maximum density [mol/L]
CPP !Pointer to Cp0 model
78.11184 !Molar mass [g/mol]
278.674 !Triple point temperature [K]
4.785 !Pressure at triple point [kPa]
11.44 !Density at triple point [mol/L]
353.219 !Normal boiling point temperature [K]
0.211 !Acentric factor
562.02 4907.277 3.901 !Tc [K], pc [kPa], rhoc [mol/L]
562.02 3.901 !Reducing parameters [K, mol/L]
8.314472 !Gas constant [J/mol-K]
10 4 4 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
0.03512459 1.0 4. 0. !a(i),t(i),d(i),l(i)
2.2338 0.29 1. 0.
-3.10542612 0.696 1. 0.
-0.577233 1.212 2. 0.
0.25101 0.595 3. 0.
-0.705518 2.51 1. 2.
-0.139648 3.96 3. 2.
0.83494 1.24 2. 1.
-0.331456 1.83 2. 2.
-0.0279953 0.82 7. 1.
0.7099766 0.57 1. 2. 2. -1.032 -1.864 1.118 0.729 0. 0. 0.
-0.3732185 2.04 1. 2. 2. -1.423 -1.766 0.639 0.907 0. 0. 0.
-0.0629985 3.2 3. 2. 2. -1.071 -1.825 0.654 0.765 0. 0. 0.
-0.803041 0.78 3. 2. 2. -14.2 -297.9 1.164 0.870 0. 0. 0.
eta beta gamma epsilon
EXP[eta*(delta-epsilon)^2+beta*(tau-gamma)^2]
#AUX !---Auxiliary function for Cp0
CPP !Ideal gas heat capacity function for benzene of Thol et al. (2015).
?
?```````````````````````````````````````````````````````````````````````````````
?Thol, M., Lemmon, E.W., and Span, R., 2015.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
1.0 8.314472 !Reducing parameters for T, Cp0
1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
3.94645 0.0
7.36374 4116.0
18.649 1511.0
4.01834 630.0
#AUX !---Auxiliary function for PX0
PX0 !Helmholtz energy ideal-gas function for benzene of Thol et al. (2015).
?
?```````````````````````````````````````````````````````````````````````````````
?Thol, M., Lemmon, E.W., and Span, R., 2015.
?
!```````````````````````````````````````````````````````````````````````````````
1 2 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
2.94645 1.0 !ai, ti for [ai*log(tau**ti)] terms
-0.673584364528315 0.0 !aj, ti for [ai*tau**ti] terms
2.5555552197611604 1.0 !aj, ti for [ai*tau**ti] terms
7.36374 4116.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms
18.649 1511.0
4.01834 630.0
#AUX !---Auxiliary function for PH0
PH0 !Ideal gas Helmholtz form for benzene of Thol et al. (2015)
?
?```````````````````````````````````````````````````````````````````````````````
?Thol, M., Lemmon, E.W., and Span, R., 2015.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
1 2 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)); cosh; sinh
2.94645 1.0 !ai, ti for [ai*log(tau**ti)] terms
-0.6740687105 0.0 !aj, ti for [ai*tau**ti] terms
2.5560188958 1.0
7.36374 -7.3235827906 !aj, ti for [ai*log(1-exp(ti*tau)] terms
18.649 -2.6885164229
4.01834 -1.1209565496
--------------------------------------------------------------------------------
@EOS !---Equation of state---
FE1 !Helmholtz equation of state for benzene of Thol et al. (2012).
?
?```````````````````````````````````````````````````````````````````````````````
?Thol, M., Lemmon, E.W., Span, R.
? "Equation of state for benzene for temperatures from the melting line up to
? 725 K with pressures up to 500 MPa,"
? High Temperatures-High Pressures, 41(2):81-97, 2012.
?
?The approximate uncertainties of properties calculated with the equation
? for benzene are 0.1% below 350 K and 0.2% above 350 K for saturated vapor
? pressures and liquid densities, 1% for saturated vapor densities, 0.1% for
? densities up to 350 K and 100 MPa, 0.1 - 0.5% in density above 350 K, 1% for
? the isobaric heat capacities and saturated heat capacities, and 0.5% for
? sound speeds. Deviations in the critical region are higher for all
? properties except saturated vapor pressures.
?
!```````````````````````````````````````````````````````````````````````````````
278.674 !Lower temperature limit [K]
725.0 !Upper temperature limit [K]
500000.0 !Upper pressure limit [kPa]
11.45 !Maximum density [mol/L]
CPP !Pointer to Cp0 model
78.11184 !Molar mass [g/mol]
278.674 !Triple point temperature [K]
4.783 !Pressure at triple point [kPa]
11.45 !Density at triple point [mol/L]
353.22 !Normal boiling point temperature [K]
0.211 !Acentric factor
562.02 4906.3 3.902 !Tc [K], pc [kPa], rhoc [mol/L]
562.02 3.902 !Reducing parameters [K, mol/L]
8.314472 !Gas constant [J/mol-K]
10 4 4 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
0.03513062 1.0 4. 0. !a(i),t(i),d(i),l(i)
2.229707 0.3 1. 0.
-3.100459 0.744 1. 0.
-0.5763224 1.174 2. 0.
0.2504179 0.68 3. 0.
-0.7049091 2.5 1. 2.
-0.1393433 3.67 3. 2.
0.8319673 1.26 2. 1.
-0.3310741 2.6 2. 2.
-0.02793578 0.95 7. 1.
0.7087408 1.0 1. 2. 2. -1.032 -1.867 1.1180 0.7289 0. 0. 0.
-0.3723906 2.47 1. 2. 2. -1.423 -1.766 0.6392 0.9074 0. 0. 0.
-0.06267414 3.35 3. 2. 2. -1.071 -1.824 0.6536 0.7655 0. 0. 0.
-0.86295 0.75 3. 2. 2. -14.35 -297.5 1.1640 0.8711 0. 0. 0.
@EOS !---Equation of state---
FE2 !Helmholtz equation of state for benzene 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.
?
?The uncertainties in density for benzene are 1% in the vapor phase, 0.3% in
? the liquid phase up to 400 K (with lower uncertainties at lower temperatures),
? 1% in the liquid phase between 400 and 500 K, and 2% and rising at
? temperatures above 500 K. Near the saturation line at temperatures below 350
? K, the liquid phase uncertainty decreases to 0.05%. The uncertainties in
? vapor pressures are 0.15% at temperatures below 380 K, and 0.5% at higher
? temperatures. The uncertainties in heat capacities and sound speeds are 2%
? in the vapor phase and 5% in the liquid phase.
?
!```````````````````````````````````````````````````````````````````````````````
278.7 !Lower temperature limit [K]
635.0 !Upper temperature limit [K]
78000.0 !Upper pressure limit [kPa]
11.45 !Maximum density [mol/L]
CP2 !Pointer to Cp0 model
78.108 !Molar mass [g/mol]
278.7 !Triple point temperature [K]
6.0329 !Pressure at triple point [kPa]
11.385 !Density at triple point [mol/L]
353.234 !Normal boiling point temperature [K]
0.2092 !Acentric factor
562.05 4894.0 3.9560608 !Tc [K], pc [kPa], rhoc [mol/L]
562.05 3.9560608 !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
-0.918572178424 3. 0. 0. 0. !a(i),t(i),d(i),l(i)
1.55357491575 4. 0. 0. 0.
-0.356149241161 5. 0. 0. 0.
0.817273664265 0. 1. 0. 0.
-3.31303917534 1. 1. 0. 0.
3.35336626528 2. 1. 0. 0.
-2.56976312022 3. 1. 0. 0.
0.427304812515 4. 1. 0. 0.
0.406483484297 0. 2. 0. 0.
-0.329744378187 1. 2. 0. 0.
0.208907540720 2. 2. 0. 0.
0.0777471199254 0. 3. 0. 0.
-0.202621443063 1. 3. 0. 0.
-0.01485803507 0. 4. 0. 0.
0.0503167715817 1. 4. 0. 0.
0.00293012717053 1. 5. 0. 0.
0.918572178424 3. 0. 2. 0.95481
-1.55357491575 4. 0. 2. 0.95481
0.356149241161 5. 0. 2. 0.95481
-0.0447029533153 3. 2. 2. 0.95481
0.957712367542 4. 2. 2. 0.95481
-1.14688433057 5. 2. 2. 0.95481
@AUX !---Auxiliary function for Cp0
CP2 !Ideal gas heat capacity function for benzene.
?
?```````````````````````````````````````````````````````````````````````````````
?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.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
1.0 78.108 !Reducing parameters for T, Cp0
5 0 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
-0.478176 0.0
0.00618649 1.0
-0.00000380363 2.0
0.699648e-9 3.0
0.42661e-13 4.0
^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^^
#ETA !---Viscosity---
VS1 !Pure fluid viscosity model for benzene of Avgeri et al. (2014).
:DOI: 10.1063/1.4892935
?
?```````````````````````````````````````````````````````````````````````````````
?Avgeri, S., Assael, M.J., Huber, M.L., and Perkins, R.A.,
? "Reference Correlation of the Viscosity of Benzene from the Triple Point to 675 K and up to 300 MPa,"
? J. Phys. Chem. Ref. Data, 43(3), 033103, 2014. doi: 10.1063/1.4892935
?
?The correlation is valid from the triple point to 675 K, and at pressures up to 300 MPa, with the exception of
? the temperature range lower than 350 K where the pressure is restricted to 200 MPa. For the liquid phase,
? at temperatures from 288 K to 373 K and pressures up to 80 MPa, uncertainty is estimated (at a 95% confidence level)
? to be 1.8%, increasing to 3.4% at 200 MPa, and 5% at pressures up to the correlation maximum.
? For the liquid at temperatures from 373 K to 523 K, the uncertainty is 2.7% at pressures from saturation to 50 MPa,
? rising to 3.6% at 300 MPa. For temperatures above 523 K, uncertainty in the liquid phase is estimated to be 5%.
? The uncertainty for the low-density fluid phase at temperatures from 305 K to 640 K and pressures to 0.3 MPa is estimated to be 0.2%.
?
!```````````````````````````````````````````````````````````````````````````````
278.674 !Lower temperature limit [K]
725.0 !Upper temperature limit [K]
500000.0 !Upper pressure limit [kPa]
11.45 !Maximum density [mol/L]
1 !Number of terms associated with dilute-gas function
CI1 !Pointer to reduced effective collision cross-section model
0.540 !Lennard-Jones coefficient sigma [nm]
412.0 !Lennard-Jones coefficient epsilon/kappa [K]
1.0 1.0 !Reducing parameters for T, eta
0.18875509 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term]
9 !Number of terms for initial density dependence
412. 0.094826978 !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
0 0 8 6 0 0 !# resid terms: close-packed density; simple poly; numerator of rational poly; denominator of rat. poly; numerator of exponential; denominator of exponential
562.02 3.902 1.0 !Reducing parameters for T, rho, eta (correlation in terms of uPa-s)
-2.263924 0.5 1.6666666667 0. 0 ! n1
11.493352 0.5 2.6666666667 0. 0 ! n2
-90.79586 0.5 3.6666666667 0. 0 ! n3
27.4582 0.5 4.6666666667 0. 0 ! n4
-9.98945 0.5 5.6666666667 0. 0 ! n5
1.68589 1.5 1.6666666667 0. 0 ! n6
5.260067 1.5 2.6666666667 0. 0 ! n7
11.101276 1.5 4.6666666667 0. 0 ! n8
-0.205488251 0.0 0. 0. 0 ! d1
0.074757797 0.0 1. 0. 0 ! d2
-2.74872 0.0 2. 0. 0 ! d3
1.0 0.0 3. 0. 0 ! d4
-0.083078339 1.0 0. 0. 0 ! d5
-1.1113 1.0 2. 0. 0 ! d6
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 benzene.
?
?```````````````````````````````````````````````````````````````````````````````
?Avgeri, S., Assael, M.J., Huber, M.L., and Perkins, R.A., 2014.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
4 !Number of terms
0.234018 0 !Coefficient, power of Tstar
-0.476136 1
0.0 2
-0.015269 3
================================================================================
#TCX !---Thermal conductivity---
TC1 !Pure fluid thermal conductivity model for benzene of Assael et al. (2012).
:DOI: 10.1063/1.4755781
?
?```````````````````````````````````````````````````````````````````````````````
?Assael, M.J., Mihailidou, E., Huber, M.L., and Perkins, R.A.,
? "Reference Correlation of the Thermal Conductivity of Benzene from the Triple Point to 725 K and up to 500 MPa,"
? J. Phys. Chem. Ref. Data, 41(4), 043102, 2012. doi: 10.1063/1.4755781
?
?Uncertainty in thermal conductivity is estimated to be less than 4.4%, for temperatures up to 725 K and pressures
? less than 350 MPa, except in the critical region where uncertainties are much larger.
?
!```````````````````````````````````````````````````````````````````````````````
278.674 !Lower temperature limit [K]
725.0 !Upper temperature limit [K]
500000.0 !Upper pressure limit [kPa]
11.45 !Maximum density [mol/L]
3 3 !# terms for dilute gas function: numerator, denominator
1.0 0.001 !Reducing parameters for T, tcx
56991.07 0.
-521.44 1.
1.5449 2.
562.02 0.
9.714 1.
0.0026102 2.
10 0 !# terms for background gas function: numerator, denominator
562.02 3.9019 1. !Reducing parameters for T, rho, tcx
0.0282489 0. 1. 0.
-0.0773415 0. 2. 0.
0.0714001 0. 3. 0.
-0.0236798 0. 4. 0.
0.00300875 0. 5. 0.
-0.0119268 1. 1. 0.
0.0833389 1. 2. 0.
-0.0898176 1. 3. 0.
0.0363025 1. 4. 0.
-0.00490052 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 benzene of Assael et al. (2012).
?
?```````````````````````````````````````````````````````````````````````````````
?Assael, M.J., Mihailidou, E., Huber, M.L., and Perkins, R.A., 2012.
?
!```````````````````````````````````````````````````````````````````````````````
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)
1.02 !R0 (universal amplitude)
0.065 !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)
0.216e-9 !Xi0 (amplitude) [m]
0.0569 !Gam0 (amplitude) [-]
0.62e-9 !Qd_inverse (modified effective cutoff parameter) [m]
843.0 !Tref (reference temperature) [K]
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
@TRN !---ECS Transport---
ECS !Extended Corresponding States model (C12 reference); predictive mode for benzene.
?
?```````````````````````````````````````````````````````````````````````````````
?*** ESTIMATION METHOD *** NOT STANDARD REFERENCE QUALITY ***
?Unpublished; uses method described in the following reference:
?Huber, M.L., Laesecke, A., and Perkins, R.A.
? "Model for the Viscosity and Thermal Conductivity of Refrigerants, Including
? a New Correlation for the Viscosity of R134a,"
? Ind. Eng. Chem. Res., 42(13):3163-3178, 2003. doi: 10.1021/ie0300880
?
?Estimated uncertainty 3% for liquid in range 293 K to 350 K at pressures <180 MPa
?
?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.
?
!```````````````````````````````````````````````````````````````````````````````
278.674 !Lower temperature limit [K]
725.0 !Upper temperature limit [K]
500000.0 !Upper pressure limit [kPa]
11.45 !Maximum density [mol/L]
FEQ C12.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)
0.5349 !Lennard-Jones coefficient sigma [nm]
412.3 !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
3 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2
1.09271 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
-0.161324 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
0.0486596 0. 2. 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
********************************************************************************
@ETA !---Viscosity---
VS5 !Pure fluid viscosity model for benzene of Chung et al. (1988).
?
?```````````````````````````````````````````````````````````````````````````````
?Uses functional form in
? Chung, T-H., Ajlan, M., Lee, L.L. and Starling, K.E.
? "Generalized Multiparameter Correlation for Nonpolar and Polar Fluid Transport Properties"
? Ind. Eng. Chem. Res. 1988, 27, 671-679. doi: 10.1021/ie00076a024
? Parameters sigma, epsilon and w, mur, kappa fit to data.
?
?*** ESTIMATION METHOD *** NOT STANDARD REFERENCE QUALITY *** **
?
?Estimated uncertainty for liquid at 298 < T < 348 K, for p < 60 MPa is ~ 3%, larger at
? higher temps and pressures. Estimated uncertainty of dilute gas at 300 < t < 620 is ~ 2%
?
!```````````````````````````````````````````````````````````````````````````````
278.674 !Lower temperature limit [K]
725.0 !Upper temperature limit [K]
500000.0 !Upper pressure limit [kPa]
11.45 !Maximum density [mol/L]
1 !Number of terms associated with dilute-gas function
NUL !Pointer to reduced effective collision cross-section model; not used
0.5023 !Lennard-Jones coefficient sigma [nm] =0.809vc*(1/3)A, fit
444.37 !Lennard-Jones coefficient epsilon/kappa [K] =Tc/1.2593, fit
1.0 1.0 !Reducing parameters for T, eta
0.18875509 0.5 !=0.021357*SQRT(MW) [Chapman-Enskog term]
0 !Number of terms for initial density dependence
0.5693 0.3209 0.0642 0. 0 !w, mur, kappa for Chung, fit
0 !Additional parameters for Chung
NUL !Pointer to the viscosity critical enhancement auxiliary function (none used)
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
#STN !---Surface tension---
ST1 !Surface tension model for benzene of Mulero et al. (2012).
:DOI: 10.1063/1.4768782
?
?```````````````````````````````````````````````````````````````````````````````
?Mulero, A., Cachadiña, I., and Parra, M.I.,
? "Recommended Correlations for the Surface Tension of Common Fluids,"
? J. Phys. Chem. Ref. Data, 41(4), 043105, 2012. doi: 10.1063/1.4768782
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
3 !Number of terms in surface tension model
562.02 !Critical temperature used in fit (dummy)
0.07298 1.232 !Sigma0 and n
-0.0007802 0.8635
-0.0001756 0.3065
#PS !---Vapor pressure---
PS5 !Vapor pressure equation for benzene of Cullimore (2010).
?
?```````````````````````````````````````````````````````````````````````````````
?Cullimore, I.D., 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. !
562.02 4906.3 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
-7.1661 1.0
2.1551 1.5
-2.0297 2.2
-4.0668 4.8
0.38092 6.2
#DL !---Saturated liquid density---
DL1 !Saturated liquid density equation for benzene of Cullimore (2010).
?
?```````````````````````````````````````````````````````````````````````````````
?Cullimore, I.D., 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. !
562.02 3.902 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
18.160 0.534
-56.879 0.686
87.478 0.84
-64.365 1.0
18.5 1.2
#DV !---Saturated vapor density---
DV3 !Saturated vapor density equation for benzene of Cullimore (2010).
?
?```````````````````````````````````````````````````````````````````````````````
?Cullimore, I.D., 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. !
562.02 3.902 !Reducing parameters
6 0 0 0 0 0 !Number of terms in equation
-3.1147 0.419
-4.6689 1.12
-16.161 2.8
-146.50 7.3
518.87 10.0
-827.72 12.0
@END
c 1 2 3 4 5 6 7 8
c2345678901234567890123456789012345678901234567890123456789012345678901234567890
0.5349 !Lennard-Jones coefficient sigma [nm] for ECS method
412.3 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method