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332 Y. Xie et al. / Applied Energy 136 (2014) 325–335 Fig. 9. The amount of ILs and energy consumption for a pressure swing CO2 separation process. Table 5 Coefficients in Eq. (16) for calculating the heat capacity of imidazolium-based ILs [71–78]. ILs, such as gas solubility, density, viscosity and surface tension. The heat capacity of BF4-, FP6-, and Tf2N-based ILs were collected and studied in this work, which are illustrated in Fig. 10. The values of Cp change from 250 to 700 J/mol/K and increase with increasing temperature. It can be seen that the magnitude of Cp of ILs increases in the order of [emim][PF6] < [emim][BF4] < [bmim] [BF4] < [bmim][PF6] < [hmim][PF6] < [hmim][BF4] < [omim][BF4] < [emim][Tf2N] < [bmim][Tf2N] < [hmim][Tf2N] < [omim][Tf2N]. The values of Cp increase with increasing chain-length, and the Cp of [Tf2N]-based ILs is higher than those of [BF4]-based and [PF6]- based ILs. The energy consumption for a temperature swing process to separate 1 mol of CO2 was calculated. It was assumed that CO2 was absorbed at 298 K and desorbed at 323 K and 0.1 MPa. The CO2 desorption enthalpy, the difference of excess enthalpy and sensible enthalpy are all included in the total energy consumption according to Eq. (14). Due to the available heat capacities of ILs, only 10 ILs were studied in this section. The calculated energy consumptions together with the contri- butions from each part are listed in Table 6. It can be seen that due to the high heat capacity of ILs, the sensible enthalpy has a significant influence on the total energy consumption for the CO2 separation process. Therefore, it is expected that the IL with low ILs C5 C6 Ref. [emim][BF4] [bmim][BF4] [hmim][BF4] [omim][BF4] [emim][PF6] [bmim][PF6] [hmim][PF6] [emim][Tf2N] [bmim][Tf2N] [hmim][Tf2N] [omim][Tf2N] 203.66 0.34 225.68 0.47 277.26 0.51 316.06 0.61 [71] 84.93 0.58 [72] 243.16 0.56 [73] 169.78 0.84 [74] 364.59 0.47 [75] 400.92 0.55 [76] 418.24 0.76 [77] 437.43 0.74 [78] For pressure swing process, if the gas is compressed before entering the column, the compression work needs to be considered [70]. Assuming 1 mol of CO2 is compressed from atmospheric pres- sure to 1 MPa at 298 K, the compression work is 6.8 kJ. If CO2 is separated from the flue gas (CO2 + N2) and the concentration of CO2 is around 0.15 (mole fraction), the compression work will reach up to 45.3 kJ. If CO2 is separated from the biogas (CO2 + CH4) and the concentration of CO2 is around 0.3, the compression work will be 22.7 kJ. For the CO2 in the synthesis gas generated from bio- mass gasification, the partial pressure of CO2 can be up to 1 MPa, and no compression work is needed in the CO2 separation process. Therefore, the energy demand for compression work depends on the sources of CO2. 3.3.2. Temperature swing process If the solvent is regenerated by increasing temperature, sensible enthalpy needs to be accounted. The sensible enthalpy relates to the heat capacities of ILs and CO2. The temperature-dependent heat capacities of imidazolium-based ILs were surveyed, and the available ones were fitted to the following equation: CP 1⁄4C5 þC6T ð16Þ where Cp is the heat capacity of pure ILs, C5 and C6 are parameters as listed in Table 5. The literature survey reveals that the study on the heat capacity of ILs is much less compared to the studies of other properties of Fig. 10. Heat capacity of imidazolium-based ILs at different temperatures. -j- [emim][BF4], -h- [bmim][BF4], -d- [hmim][BF4], -s- [omim][BF4], -N- [emim][PF6], -4- [bmim][PF6], -.- [hmim][PF6], -r- [emim][Tf2N], -- [bmim][Tf2N], -}- [hmim][Tf2N], -H- [omim][Tf2N].PDF Image | CO2 Separation with Ionic Liquids
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