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desorber and heat exchanger. To conduct energy demand analysis, it was assumed that 1 mol of CO2 was separated and out of the desorber at temperature of T2 and pressure of P2, and n mol of CO2 was released from the solvent (ILs). In the absorber, it was assumed that (1+n) mol of CO2 was absorbed by m mol of ILs at temperature of T1 and pressure of P1. Figure 3.1. The schematic of CO2 separation process with ILs. The energy demand for solvent regeneration can be calculated with the following equations: Q Qdes Qex Qsen Qdes H (T,P) Hg (3.34) Haq (3.35) d i s 2 2 C O2 Qex Hex (n m)Hex(T,P) (1 n m)Hex(T,P) (3.36) C O2 222 111 Qsen mC (T T) nC (T T) (3.37) p,IL 2 1 p,CO2 2 1 where Qdes is the energy demand in order to vaporize CO2 from liquid to gas phase, which is termed as the desorption enthalpy. H g and H aq are the enthalpies of CO2 in the gas CO2 CO2 and liquid phase. H ex (T , P ) is the excess 111 11 enthalpy of the solution at T and P , H ex (T , P ) is the excess enthalpy of the solution at T and P , Qex is the energy demand 222 22 due to the difference of excess enthalpy between the streams, Qsen is the sensible heat due to the increase of temperature in the desorber, and Cp,IL and Cp,CO2 are the heat capacities of IL and CO2, respectively. 17PDF Image | CO2 Separation with Ionic Liquids
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