Ethylene glycol !Short name 107-21-1 !CAS number 1,2-Ethandiol !Full name OH(CH2CH2)OH !Chemical formula {C2H6O2} Glycol alcohol !Synonym 62.06784 !Molar mass [g/mol] 260.6 !Triple point temperature [K] 470.313 !Normal boiling point [K] 719.0 !Critical temperature [K] 10508.7 !Critical pressure [kPa] 5.88 !Critical density [mol/L] 0.619 !Acentric factor 2.41 !Dipole moment [Debye] McClellan, A.L., "Tables of Experimental Dipole Moments, " Rahara Enterprises, El Cerrito, CA, Vol. 3 (1989) NBP !Default reference state 10.0 !Version number 3082 !UN Number :UN: other !Family :Family: ???? !Heating value (upper) [kJ/mol] :Heat: 1S/C2H6O2/c3-1-2-4/h3-4H,1-2H2 !Standard InChI String :InChi: LYCAIKOWRPUZTN-UHFFFAOYSA-N !Standard InChI Key :InChiKey: ???? !Alternative fluid for mixing rules :AltID: 7d1768e0 !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 ! 11-27-06 EWL, Original version. ! 03-11-09 EWL, Add transport routines. ! 08-20-10 IDC, Add ancillary equations. ! 03-25-14 MLH, Add surface tension. ! 12-31-14 EWL, Refit equation of state. ! 05-04-17 MLH, Prelim vis and therm con ecs fits added with revised EOS, revised surft with revised Tc. ! 04-23-18 EWL, Add final equation of state of Zhou and Lemmon (2018). ! 04-24-18 MLH, Revised transport and surface tension with final EOS. ________________________________________________________________________________ #EOS !---Equation of state--- FEQ !Helmholtz equation of state for ethylene glycol of Zhou and Lemmon (2018). :TRUECRITICALPOINT: 719.0 5.88 !True EOS critical point [K, mol/L] (where dP/dD=0 and d^2P/dD^2=0 at constant T) :DOI: ? ?``````````````````````````````````````````````````````````````````````````````` ?Zhou, Y. and Lemmon, E.W., ? unpublished equation, 2018. ? !``````````````````````````````````````````````````````````````````````````````` 260.6 !Lower temperature limit [K] 750.0 !Upper temperature limit [K] 100000.0 !Upper pressure limit [kPa] 18.31 !Maximum density [mol/L] CPP !Pointer to Cp0 model 62.06784 !Molar mass [g/mol] 260.6 !Triple point temperature [K] (NIST Chemistry Webbook) 0.0002366 !Pressure at triple point [kPa] 18.30 !Density at triple point [mol/L] 470.313 !Normal boiling point temperature [K] 0.619 !Acentric factor 719.0 10508.7 5.88 !Tc [K], pc [kPa], rhoc [mol/L] 719.0 5.88 !Reducing parameters [K, mol/L] 8.3144598 !Gas constant [J/mol-K] 14 4 7 12 0 0 0 0 0 0 0 0 !# terms and # coefs/term for normal terms, Gaussian terms, and Gao terms 0.019393376 1.0 5. 0. !a(i),t(i),d(i),l(i) 1.2215576 0.1 1. 0. 1.2751617 1.27 1. 0. -3.6681302 1.244 1. 0. -1.4660821 1.1 2. 0. 0.24628603 0.32 3. 0. -0.063217756 1.0 4. 0. 1.4131488 0.89 2. 1. 3.5245547 1.2 3. 1. -2.2658015 1.34 3. 1. 0.94972119 1.3 4. 1. -0.13037392 1.49 5. 1. 0.19881857 1.23 6. 1. -0.022141839 0.18 7. 1. 1.1273408 1.1 1. 2. 2. -0.9 -0.91 1.17 1.37 0. 0. 0. -0.12188623 0.75 1. 2. 2. -1.35 -1.25 1.49 0.4 0. 0. 0. -0.79487875 0.79 2. 2. 2. -0.8 -0.97 1.3 1. 0. 0. 0. -0.024231918 0.77 3. 2. 2. -1.9 -0.5 1.5 2.45 0. 0. 0. -0.00574040155 0.6 4. 2. 2. -2.0 -1.0 1.2 1.9 0. 0. 0. 0.0083087704 1.0 5. 2. 2. -1.3 -0.42 1.2 2. 0. 0. 0. -0.041852456 1.0 3. 2. 2. -20.0 -1000.0 1.07 0.9 0. 0. 0. #AUX !---Auxiliary function for Cp0 CPP !Ideal gas heat capacity function for ethylene glycol of Zhou and Lemmon (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Zhou, Y. and Lemmon, E.W., 2018. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1.0 8.3144598 !Reducing parameters for T, Cp0 1 1 0 0 0 0 0 !Nterms: polynomial, exponential, cosh, sinh 4.0 0.0 20.86 1260.0 #AUX !---Auxiliary function for PX0 PX0 !Helmholtz energy ideal-gas function for ethylene glycol of Zhou and Lemmon (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Zhou, Y. and Lemmon, E.W., 2018. ? !``````````````````````````````````````````````````````````````````````````````` 1 2 1 0 0 0 0 0 !Nterms: ai*log(tau**ti); ai*tau**ti; ai*log(1-exp(bi*tau)) 3.0 1.0 !ai, ti for [ai*log(tau**ti)] terms -1.2230958209345886 0.0 !aj, ti for [ai*tau**ti] terms 3.8389800933704281 1.0 !aj, ti for [ai*tau**ti] terms 20.86 1260.0 !aj, ti for [ai*log(1-exp(-ti/T)] terms ++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++ #TRN !---ECS Transport--- ECS !Extended Corresponding States model (Propane reference) :DOI: 10.6028/NIST.IR.8209 ? ?``````````````````````````````````````````````````````````````````````````````` ? *** ESTIMATION METHOD--- NOT STANDARD REFERENCE QUALITY--- ? ?Based on comparisons to limited liquid-phase thermal conductivity data, uncertainty of the thermal conductivity ? is estimated to be 2% for the liquid phase at atmospheric pressure between 298 K and 452 K. ? Gas-phase thermal conductivity data are unavailable, and uncertainty is estimated to be 20%. ? ?Based on comparisons to limited liquid-phase viscosity data, uncertainty I estimated to ? be 4% for the liquid phase between 288 K and 373 K at atmospheric pressure. ? At pressures up to 10 MPa the uncertainty rises to 20%. ? Gas-phase viscosity data is unavailable, uncertainty is estimated to be 20%. ? ?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 ? ?The Lennard-Jones parameters were estimated with the method of Chung. ? !``````````````````````````````````````````````````````````````````````````````` 260.0 !Lower temperature limit [K] 750.0 !Upper temperature limit [K] 10000.0 !Upper pressure limit [kPa] 18.31 !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) 0.4482 !Lennard-Jones coefficient sigma [nm] for ECS method 570.95 !Lennard-Jones coefficient epsilon/kappa [K] for ECS method 1 0 0 !Number of terms in f_int term in Eucken correlation, spare1, spare2 1.32e-3 0. 0. 0. !Coefficient, power of T, spare1, spare2 4 0 0 !Number of terms in psi (visc shape factor): poly,spare1,spare2 0.864168 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -2.30208e-3 0. 1. 0. !Coefficient, power of Tr, power of Dr, spare -1.83225e-3 0. 2. 0. !Coefficient, power of Tr, power of Dr, spare 9.04878e-3 0. 3. 0. !Coefficient, power of Tr, power of Dr, spare 2 0 0 !Number of terms in chi (t.c. shape factor): poly,spare1,spare2 1.79177 0. 0. 0. !Coefficient, power of Tr, power of Dr, spare -0.275354 0. 1. 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 ethylene glycol of Perkins et al. (2013). ? ?``````````````````````````````````````````````````````````````````````````````` ?Perkins, R.A., Sengers, J.V., Abdulagatov, I.M., and Huber, M.L., ? "Simplified Model for the Critical Thermal-Conductivity Enhancement in Molecular Fluids," ? Int. J. Thermophys., 34(2):191-212, 2013. doi: 10.1007/s10765-013-1409-z ? !``````````````````````````````````````````````````````````````````````````````` 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) 1.02 !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) 0.166e-9 !Xi0 (amplitude) [m] 0.073 !Gam0 (amplitude) [-] 5.42e-10 !Qd_inverse (modified effective cutoff parameter) [m]; arbitrary guess 1078.5 !Tref (reference temperature)=1.5*Tc [K] ~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~~ #STN !---Surface tension--- ST1 !Surface tension model for ethylene glycol of Huber (2018). :DOI: 10.6028/NIST.IR.8209 ? ?``````````````````````````````````````````````````````````````````````````````` ?Fit to the data of: ? Azizian, S. and Hemmati, M., "Surface Tension of Binary Mixtures of Ethanol + Ethylene Glycol from 20 to 50 °C," J. Chem. Eng. Data, 48:662-663, 2003. doi: 10.1021/je025639s ? Azizian, S. and Bashavard, N., "Surface Tensions of Dilute Solutions of Cycloheptanol in Ethylene Glycol," J. Chem. Eng. Data, 50:1091-1094, 2005. doi: 10.1021/je050055m ? Rafati, A.A., Bagheri, A., and Najafi, M., "Surface Tension of Non-Ideal Binary and Ternary Liquid Mixtures at Various Temperatures and p = 81.5 kPa," J. Chem. Thermodyn., 43:248-254, 2011. doi: 10.1016/j.jct.2010.09.003 ? Estimated uncertainty for 283-323 K is 2%. ? !``````````````````````````````````````````````````````````````````````````````` 0. ! 10000. ! 0. ! 0. ! 1 !Number of terms in surface tension model 719.0 !Critical temperature used in fit (dummy) 0.0731084 0.776849 !sigma0 and n #PS !---Vapor pressure--- PS5 !Vapor pressure equation for ethylene glycol of Zhou and Lemmon (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Zhou and Lemmon, 2018. ? ?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. ! 719.0 10508.7 !Reducing parameters 5 0 0 0 0 0 !Number of terms in equation -10.193 1.0 6.7548 1.5 -6.0404 1.9 -3.869 3.64 -8.4146 18.0 #DL !---Saturated liquid density--- DL1 !Saturated liquid density equation for ethylene glycol of Zhou and Lemmon (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Zhou and Lemmon, 2018. ? ?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. ! 719.0 5.88 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation 1.3902 0.29 -7.6323 1.25 3.5326 0.75 10.85 1.8 -8.7298 2.5 3.3638 3.4 #DV !---Saturated vapor density--- DV3 !Saturated vapor density equation for ethylene glycol of Zhou and Lemmon (2018). ? ?``````````````````````````````````````````````````````````````````````````````` ?Zhou and Lemmon, 2018. ? ?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. ! 719.0 5.88 !Reducing parameters 6 0 0 0 0 0 !Number of terms in equation -0.47502 0.173 -5.5419 0.6 -16.175 2.08 -50.153 4.8 -86.316 10.0 -169.85 18.0 @END c 1 2 3 4 5 6 7 8 c23456/8901234567890123456789012345678901234567890123456789012345678901234567890