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一些优化：CAN和PLC地址的优化

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Methyl stearate !Short name
112-61-8 !CAS number
Methyl octadecanoate !Full name
C19H38O2 !Chemical formula {C19H38O2}
Methyl ester stearic acid !Synonym
298.50382 !Molar mass [g/mol]
311.84 !Triple point temperature [K] TDE, Jan 2010
629.56 !Normal boiling point [K]
775.0 !Critical temperature [K]
1239.0 !Critical pressure [kPa]
0.7943 !Critical density [mol/L]
1.02 !Acentric factor
1.54 !Dipole moment [Debye]
NBP !Default reference state
10.0 !Version number
???? !UN Number :UN:
FAME !Family :Family:
???? !Heating value (upper) [kJ/mol] :Heat:
1S/C19H38O2/c1-3-4-5-6-7-8-9-10-11-12-13-14-15-16-17-18-19(20)21-2/h3-18H2,1-2H3 :InChi: !Standard InChI String
HPEUJPJOZXNMSJ-UHFFFAOYSA-N !Standard InChI Key :InChiKey:
111888d0 (decane) !Alternative fluid for mixing rules :AltID:
81403130 !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 M.L. Huber, NIST Physical and Chemical Properties Division, Boulder, Colorado
! 03-25-08 MLH, Original version.
! 08-27-08 EWL, Add equation of state.
! 11-21-08 MLH, Add preliminary predictive transport.
! 08-20-10 IDC, Add ancillary equations.
! 10-25-10 MLH, Revise thermal conductivity estimation based on methyl oleate.
! 11-06-10 MLH, Revise ECS viscosity with data of pratas 2010.
! 04-17-14 EWL, Add surface tension coefficients of Mulero et al. (2014).
________________________________________________________________________________
#EOS !---Equation of state---
FEQ !Helmholtz equation of state for methyl stearate of Huber et al. (2009).
:TRUECRITICALPOINT: 775.0 0.7943 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T)
:DOI: 10.1021/ef900159g
?
?```````````````````````````````````````````````````````````````````````````````
?Huber, M.L., Lemmon, E.W., Kazakov, A., Ott, L.S., and Bruno, T.J.,
? "Model for the Thermodynamic Properties of a Biodiesel Fuel,"
? Energy & Fuels, 23:3790-3797, 2009.
?
?The uncertainties in the liquid phase between 270 K and 350 K are 0.6% for
? density, 0.4% for speed of sound, and 5% for heat capacity. The uncertainty
? in vapor pressure between 350 K and 500 K is 5%, and increases at lower
? temperatures due to the limited data and very low pressures. Uncertainties in
? the critical region and the vapor phase are unknown due to the lack of data.
?
!```````````````````````````````````````````````````````````````````````````````
311.84 !Lower temperature limit [K]
1000.0 !Upper temperature limit [K]
50000.0 !Upper pressure limit [kPa]
2.86 !Maximum density [mol/L]
CPP !Pointer to Cp0 model
298.50382 !Molar mass [g/mol]
311.84 !Triple point temperature [K]
0.000006011 !Pressure at triple point [kPa]
2.85 !Density at triple point [mol/L]
629.56 !Normal boiling point temperature [K]
1.02 !Acentric factor
775.0 1239.0 0.7943 !Tc [K], pc [kPa], rhoc [mol/L]
775.0 0.7943 !Reducing parameters [K, mol/L]
8.314472 !Gas constant [J/mol-K]
10 4 3 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms
0.03959635 1.0 4. 0. !a(i),t(i),d(i),l(i)
2.466654 0.3 1. 0.
-3.89595 1.25 1. 0.
-0.1167375 1.65 2. 0.
0.04127229 0.8 3. 0.
-1.403734 3.1 1. 2.
-0.6465264 3.4 3. 2.
1.934675 2.3 2. 1.
-1.608124 3.8 2. 2.
-0.01113813 1.2 7. 1.
2.125325 3.2 1. 2. 2. -1.1 -0.9 1.14 0.79 0. 0. 0.
-0.7772671 3.8 1. 2. 2. -1.6 -0.65 0.65 0.90 0. 0. 0.
-0.4183684 3.8 3. 2. 2. -1.1 -0.75 0.77 0.76 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 methyl stearate of Huber et al. (2009).
?
?```````````````````````````````````````````````````````````````````````````````
?TDE 3.0 internal version, March 2008, Planck-Einstein form
? based on estimation from Joback method, uncertainty 10%.
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
1.0 1.0 !Reducing parameters for T, Cp0
1 3 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh
247.115 -0.0916606
276.94 556.17
408.997 1311.85
472.702 2825.71
#AUX !---Auxiliary function for PX0
PX0 !Helmholtz energy ideal-gas function for methyl stearate of Huber et al. (2009).
?
?```````````````````````````````````````````````````````````````````````````````
?TDE 3.0 internal version, March 2008, Planck-Einstein form
? based on estimation from Joback method, uncertainty 10%.
?
!```````````````````````````````````````````````````````````````````````````````
1 3 3 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau))
-1.0 1.0 !ai, ti for [ai*log(tau**ti)] terms
-125.3828887023318 0.0 !aj, ti for [ai*tau**ti] terms
-36.0623931346332256 1.0 !aj, ti for [ai*tau**ti] terms
29.7211130902334766 0.0916606
33.3082372952239183 556.17
49.1910490685155537 1311.85
56.8530020435001688 2825.71
================================================================================
#TCX !---Thermal conductivity---
TC1 !Pure fluid thermal conductivity model for methyl stearate of Huber (2018).
:DOI: 10.6028/NIST.IR.8209
?
?```````````````````````````````````````````````````````````````````````````````
?Huber, M.L., "Models for the Viscosity, Thermal Conductivity, and Surface Tension
? of Selected Pure Fluids as Implemented in REFPROP v10.0," NISTIR 8209, 2018.
? doi: 10.6028/NIST.IR.8209
?
?The correlation below is an estimation, based on results for methyl oleate, adjusted for
? application to methyl stearate.
?
?The estimated uncertainty of the correlation for the liquid phase is 5%. The dilute gas is
? based on predicted values and uncertainties are larger, on the order of 10-30%.
?
!```````````````````````````````````````````````````````````````````````````````
311.84 !Lower temperature limit [K]
1000.0 !Upper temperature limit [K]
50000.0 !Upper pressure limit [kPa]
2.86 !Maximum density [mol/L]
4 0 !# terms for dilute gas function: numerator, denominator
775.0 1.0 !Reducing parameters for T, tcx
-0.00027125 0.
0.00259365 1.
0.0350241 2.
-0.00902273 3.
10 0 !# terms for background gas function: numerator, denominator
775.0 0.7943 1. !Reducing parameters for T, rho, tcx
-0.0410106 0. 1. 0.
0.0328443 0. 2. 0.
-0.00418506 0. 3. 0.
0.0 0. 4. 0.
0.0 0. 5. 0.
0.0606657 1. 1. 0.
-0.0498407 1. 2. 0.
0.0121752 1. 3. 0.
0.0 1. 4. 0.
0.0 1. 5. 0.
TK3 !Pointer to critical enhancement auxiliary function
++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
@TRN !---ECS Transport---
ECS !Extended Corresponding States model (Propane reference) for methyl stearate.
:DOI: 10.6028/NIST.IR.8209
?
?```````````````````````````````````````````````````````````````````````````````
?Huber, M.L., "Models for the Viscosity, Thermal Conductivity, and
? Surface Tension of Selected Pure Fluids as Implemented in REFPROP v10.0",
? NISTIR 8209; doi: 10.6028/NIST.IR.8209
?
?VISCOSITY
? Estimated uncertainty approximately 5% for liquid at atmospheric pressure,
? Estimated uncertainty otherwise approximately 10-50%
? Values based on estimation method of extended corresponding states.
?
?THERMAL CONDUCTIVITY
? Values based on estimation method of
? extended corresponding states; Estimated uncertainty approximately 10-50%
?
?The Lennard-Jones parameters were estimated with the method of Chung.
?
!```````````````````````````````````````````````````````````````````````````````
311.84 !Lower temperature limit [K]
1000.0 !Upper temperature limit [K]
50000.0 !Upper pressure limit [kPa]
2.86 !Maximum density [mol/L]
FEQ PROPANE.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)
0.8735 !Lennard-Jones coefficient sigma [nm] from method Chung=0.809vc*(1/3)A
615.42 !Lennard-Jones coefficient epsilon/kappa [K] from Chung=Tc/1.2593
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
1.466540 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
-0.260069 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare
0.0354629 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
1.20 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare
TK3 !Pointer to critical enhancement auxiliary function
#AUX !---Auxiliary function for the thermal conductivity critical enhancement
TK3 !Simplified thermal conductivity critical enhancement for methyl stearate 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) [-]
0.875e-9 !Qd_inverse (modified effective cutoff parameter) [m] value for butane
1162.5 !Tref (reference temperature)=1.5*Tc [K]
~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~
#STN !---Surface tension---
ST1 !Surface tension model for methyl stearate of Mulero et al. (2014).
:DOI: 10.1063/1.4878755
?
?```````````````````````````````````````````````````````````````````````````````
?Mulero, A. and Cachadiña, I.,
? "Recommended Correlations for the Surface Tension of Several Fluids
? Included in the REFPROP Program,"
? J. Phys. Chem. Ref. Data, 43, 023104, 2014.
? doi: 10.1063/1.4878755
?
!```````````````````````````````````````````````````````````````````````````````
0. !
10000. !
0. !
0. !
2 !Number of terms in surface tension model
775. !Critical temperature used in fit (dummy)
0.02313 3.242 !Sigma0 and n
0.04567 1.163
#PS !---Vapor pressure---
PS5 !Vapor pressure equation for methyl stearate 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. !
775.0 1239.0 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
-14.597 1.0
13.836 1.5
-14.484 2.12
-5.1856 4.7
-2.7076 8.0
#DL !---Saturated liquid density---
DL1 !Saturated liquid density equation for methyl stearate 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. !
775.0 0.7943 !Reducing parameters
5 0 0 0 0 0 !Number of terms in equation
-11.202 0.439
78.636 0.59
-125.54 0.73
72.942 0.9
-11.524 1.2
#DV !---Saturated vapor density---
DV3 !Saturated vapor density equation for methyl stearate 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. !
775.0 0.7943 !Reducing parameters
6 0 0 0 0 0 !Number of terms in equation
-18.187 0.71
81.619 1.3
-90.210 1.5
-528.88 6.0
1127.0 7.0
-844.53 8.0
@END
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