Liu et al. measured the co-solubility of CO2 and N2 in water and aqueous solutions with a 5 wt.% salt mixture containing an equal mass of NaCl, KCl, and CaCl2 up to 160 bar and 50⁰C. The total amount of N2 and CO2 in the liquid sample was calculated from the measured temperature, pressure, and volume using the Peng-Robinson equation of state, whereas the composition of the gas phase was determined using a gas chromatogram. Figure shows the experimental and modelled solubility of CO2 (panels a, c, and e) and N2 (panels b, d, f) against the equilibrium gas partial pressures at three different total pressures. Both the experimental and calculated molar fractions of CO2 and N2 in the gas phase (e.g., yCO2 and yN2) are expressed on a "water-free" basis, i.e., the water content in the gas phase is considered negligible. Hassanpour et al. measured the co-solubility of CO2 and N2 in water and brines at different pressures and temperatures. The experiments were performed with three gas phase systems simulating the composition of typical flue gas streams containing different CO2/N2 ratios. For each gas system, N2 and CO2 were injected into a cell containing water/brines at a specific molar ratio and were left to mix until the pressure and the temperature within the cell stabilized. Gas samples were also taken and analyzed by GC to confirm the desired gas composition. The CO2/N2 aqueous molar fraction was calculated from the material balance, i.e., by considering the initial gas composition and the final gas composition upon equilibration. The moles in the gas phase upon equilibration were calculated using pressure, temperature, and volume measurements and the compressibility factor using CPA-SRK72 EOS. Figure shows the CO2 (panels a, c, e) and N2 (panels b, d, f) solubility in water at total gas pressures up to 250 bar and 30⁰C. For each equilibrated system, Hassanpour and coauthors reported also the composition of the gas phase upon equilibration. Both in the experiments and models, the water content of the gas phase was considered negligible. Figure shows the consistency between the experimental and modelled composition of CO2 (panels a, c, e) and N2 (panels b, d, f) in the gas phase for systems containing three different CO2/N2 mixtures. Besides the solubility measurements in water, the co-solubility of CO2 and N2 was measured also in three different NaCl solutions (i.e., 5, 10, and 15% wt.). Before equilibration, the gas phase contained 14.6% (mol) CO2 and 85.4% N2. Figure shows the measured and predicted CO2 (panels a, c, e) and N2 (panels b, d, f) solubility in the three brines at different pressures and temperatures. The composition of the gas phase upon equilibration with the NaCl solutions predicted with both PHREEQC and Reaktoro is also compared with the experimentally inferred values. The performance of the models is displayed in Figure .