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Figure 4.3. CO2 loading (a) and absorption enthalpy (b) at 298 K in [bmim][BF4], [hmim][BF4] , [omim][BF4]. Figure 4.4. CO2 loading (a) and absorption enthalpy (b) 298 K in [bmim]-based ILs. [bmim][BF4], [bmim][PF6], [bmim][Tf2N], [bmim][NO3], [bmim][DCA], [bmim][TfO]. 4.1.3 Energy demand for solvent regeneration Based on the available properties of imidazolium-based ILs as well as the CO2 solubility, the energy demand on CO2 separation with imidazolium-based ILs was estimated. The analysis was based on the CO2 separation process illustrated in Figure 3.1. The total energy demand (Qtotal) consists three parts, the energy demand to vaporize CO2 from liquid to gas phase (Qdes), the energy demand due to the difference of excess enthalpy between the streams (Qex), and the sensible heat used to the increase the solution temperature in the desorber (Qsen). Depending on the method for solvent regeneration, three options (pressure swing, temperature swing, pressure and temperature swing (i.e. solvent is regenerated by both 24PDF Image | CO2 Separation with Ionic Liquids
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