Methyl oleate !Short name 112-62-9 !CAS number Methyl cis-9-octadecenoate !Full name C19H36O2 !Chemical formula {C19H36O2} Methyl ester oleic acid !Synonym 296.48794 !Molar mass [g/mol] 253.47 !Triple point temperature [K] 627.18 !Normal boiling point [K] 782.0 !Critical temperature [K] 1246.0 !Critical pressure [kPa] 0.81285 !Critical density [mol/L] 0.906 !Acentric factor 1.63 !Dipole moment [Debye] NBP !Default reference state 10.0 !Version number ???? !UN Number :UN: FAME !Family :Family: ???? !Heating value (upper) [kJ/mol] :Heat: 1S/C19H36O2/c1-3-4-5-6-7-8-9-10-11-12-13-14-15-16-17-18-19(20)21-2/h10-11H,3-9,12-18H2,1-2H3/b11-10- :InChi: !Standard InChI String QYDYPVFESGNLHU-KHPPLWFESA-N !Standard InChI Key :InChiKey: 111888d0 (decane) !Alternative fluid for mixing rules :AltID: f300b9e0 !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. ! 11-20-08 MLH, Add preliminary predictive transport. ! 08-20-10 IDC, Add ancillary equations. ! 10-25-10 MLH, Add correlation for therm. cond. based on R. Perkins data. ! 11-6-10 MLH, Revise ECS viscosity based on fortin 2010 data. ! 04-17-14 EWL, Add surface tension coefficients of Mulero et al. (2014). ! 02-16-17 KG, Add ancillary equations. ! 11-17-17 MLH, Revise viscosity. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for methyl oleate of Huber et al. (2009). :TRUECRITICALPOINT: 782.0 0.81285 !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. ? !``````````````````````````````````````````````````````````````````````````````` 253.47 !Lower temperature limit [K] 1000.0 !Upper temperature limit [K] 50000.0 !Upper pressure limit [kPa] 3.05 !Maximum density [mol/L] CPP !Pointer to Cp0 model 296.48794 !Molar mass [g/mol] 253.47 !Triple point temperature [K] 0.0000000003781 !Pressure at triple point [kPa] 3.05 !Density at triple point [mol/L] 627.18 !Normal boiling point temperature [K] 0.906 !Acentric factor 782.0 1246.0 0.81285 !Tc [K], pc [kPa], rhoc [mol/L] 782.0 0.81285 !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 0.04596121 1.0 4. 0. !a(i),t(i),d(i),l(i) 2.2954 0.34 1. 0. -3.554366 1.14 1. 0. -0.2291674 1.4 2. 0. 0.06854534 0.6 3. 0. -1.535778 3.3 1. 2. -0.7334697 4.1 3. 2. 1.7127 1.9 2. 1. -1.471394 3.8 2. 2. -0.01724678 1.3 7. 1. 2.11547 3.4 1. 2. 2. -1.1 -0.9 1.14 0.79 0. 0. 0. -0.7555374 3.8 1. 2. 2. -1.6 -0.65 0.65 0.90 0. 0. 0. -0.4134269 4.0 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 oleate 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 90.2385 0.146118 234.797 613.529 335.768 1405.31 431.66 2867.76 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for methyl oleate 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 230.1791429440617662 0.0 !aj, ti for [ai*tau**ti] terms -34.1983488947336269 1.0 !aj, ti for [ai*tau**ti] terms 10.853200589171168 -0.146118 28.2395977186635747 613.529 40.3836217958501607 1405.31 51.9167823747250523 2867.76 ================================================================================ #TCX !---Thermal conductivity--- TC1 !Pure fluid thermal conductivity model for methyl oleate of Perkins and Huber (2011). :DOI: 10.1021/ef200417x ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A. and Huber, M.L., ? "Measurement and Correlation of the Thermal Conductivities of Biodiesel Constituent Fluids: ? Methyl Oleate and Methyl Linoleate," ? Energy & Fuels, 25:2383-2388, 2011. ? ?The estimated uncertainty of the correlation for the liquid phase is 2.5%. The dilute gas is ? based on predicted values and uncertainties are larger, on the order of 10-30%. ? !``````````````````````````````````````````````````````````````````````````````` 253.47 !Lower temperature limit [K] 1000.0 !Upper temperature limit [K] 50000.0 !Upper pressure limit [kPa] 3.05 !Maximum density [mol/L] 4 0 !# terms for dilute gas function: numerator, denominator 782.0 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 782.0 0.81285 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 oleate. :DOI: 10.6028/NIST.IR.8209 ? ?``````````````````````````````````````````````````````````````````````````````` ?Huber, M.L., (2018) "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 2 % for atm pressure liquid ? 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. ? !``````````````````````````````````````````````````````````````````````````````` 253.47 !Lower temperature limit [K] 1000.0 !Upper temperature limit [K] 10000.0 !Upper pressure limit [kPa] limited pressure range 3.05 !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) 0.8668 !Lennard-Jones coefficient sigma [nm] from method Chung=0.809vc*(1/3)A 620.98 !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 1.92477 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.515884 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare 7.03972e-2 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 1.190 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 oleate 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]; based on butane 1173.0 !Tref (reference temperature)=1.5*Tc [K] ******************************************************************************** @TCX !---Thermal conductivity--- TC5 !Pure fluid thermal conductivity model for methyl oleate of Chung et al. (1988). ? ?``````````````````````````````````````````````````````````````````````````````` ?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. 1998, 27, 671-679. ? !``````````````````````````````````````````````````````````````````````````````` 225.68 !Lower temperature limit [K] 1000. !Upper temperature limit [K] 50000. !Upper pressure limit [kPa] 10. !Maximum density [mol/L] 0.87 !Lennard-Jones coefficient sigma [nm] =0.809vc*(1/3)A 621.0 !Lennard-Jones coefficient epsilon/kappa [K] =Tc/1.2593 0.91 0. 0. !w, mur, kappa for Chung 0 !Additional parameters for Chung TK3 !Pointer to critical enhancement auxiliary function ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for methyl oleate of Mulero et al. (2014). :DOI: 10.1063/1.4878755 ? ?``````````````````````````````````````````````````````````````````````````````` ?Mulero, A. and Cachadiņa, 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. ! 1 !Number of terms in surface tension model 782. !Critical temperature used in fit (dummy) 0.0565 1.31 !Sigma0 and n #PS !---Vapor pressure--- PS5 !Vapor pressure equation for methyl oleate of Gao (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Gao, K., 2017. ? ?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. ! 782.0 1246.0 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -13.663 1.0 13.240 1.5 -14.122 2.1 -7.8690 4.9 -14.347 12.5 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for methyl oleate of Gao (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Gao, K., 2017. ? ?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. ! 782.0 0.81285 !Reducing parameters 7 0 0 0 0 0 !Number of terms in equation 8.8882 0.6 -82.732 1.4 279.40 1.9 -505.98 2.5 642.01 3.2 -454.98 3.8 117.86 4.5 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for methyl oleate of Gao (2017). ? ?``````````````````````````````````````````````````````````````````````````````` ?Gao, K., 2017. ? ?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. ! 782.0 0.81285 !Reducing parameters 7 0 0 0 0 0 !Number of terms in equation -13.220 0.664 170.88 1.7 -531.07 2.1 700.70 2.6 -410.61 3.1 -207.26 9.8 -660.64 21.5 @END c 1 2 3 4 5 6 7 8 c2345678901234567890123456789012345678901234567890123456789012345678901234567890