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Viscosity Surface tension Heat capacity η/Pa·s, T/K σ/ N·m-1, T/K Cp/J·mol-1·K-1, T/K [hmim][Tf2N] [bmim][Tf2N] [bmim][PF6] ChCl/Urea [Amim][HCOO] [hmim][Tf2N] [bmim][Tf2N] [bmim][PF6] ChCl/Urea [hmim][Tf2N] [bmim][Tf2N] [bmim][PF6] ChCl/Urea -223.1 13542.1 -57.55 5330.4 -304.4 18135.4 -443.7 26670.2 -523.5 28491.3 0.0131 -8.617 0.0127 -8.639 0.0111 -6.073 0.0924 0.6043 472.1 0.3581 499.1 -0.0549 -464.0 4.780 117.3 0.2085 30.71 6.433 42.51 62.14 75.91 22.69 21.53 8.531 0 0.00060 0.00093 -0.0063 1.679E-12 NRTL-RK model was used to describe the vapor-liquid equilibria. The parameters for Henry’s constants (h1-h4, υ1 and υ2 in eqs. 3.22 and 3.23) and the activity coefficient in the liquid phase for NRTL model (mij, mji , nij and nji in eq.3.26) were determined from the fitting of experimental data. For CO2-H2O and CH4-H2O systems, the model parameters were taken from Aspen databank. For CO2-IL and CH4-IL systems, the parameters were fitted to the experimental solubility data. Firstly, the coefficients for calculating the Henry’s constants were extrapolated from the measured gas solubility. Secondly, the parameters (υ1 and υ2) for infinite dilution partial volume were fitted by setting NRTL parameters to be zero using the solubility data at low pressures. Thirdly, the NRTL parameters were further fitted with the fixed υ1 and υ2 using the gas solubility in the whole investigated pressure range. 39PDF Image | CO2 Separation with Ionic Liquids
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