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Y. Xie et al. / Applied Energy 175 (2016) 69–81 75 Table 6 The parameters of process simulation. Parameter CH4/CO2 Pbiogas Tbiogas Pabsorber/Pflash1/Pflash2 Tabsorber/Tdesorber Plant capacity Nstage Purity of CH4 CH4 loss Table 7 Units vol% bar K bar K N m3/h % % Values 55/45 1 293 8/3/0.2 293/293 224 11 97 <1 Fig. 8. Comparison of the calculated and experimental solubility of CO2/CH4 mixture in [bmim][Tf2N] at 303 K, 313 K and 323 K when the mole ratios of CO2 to CH4 are 1/3, 1 and 3. Calculated diameters, solvents and gas compositions from the processes. 3. Process simulation 3.1. Process description A conceptual process for biogas upgrading using ILs was simu- lated and the schematic is illustrated in Fig. 9. The biogas is pres- surized to 8 bar in the compressors and injected into the bottom of an absorber while the solvent is sprayed from the top of the absorber. The absorber is operated at 293.15 K and 8 bar based on the operational conditions for water-scrubbing. CH4 is obtained on the top of the absorber, while the CO2-enriched solvent enters the first flash tank (Flash-1). The gas released from Flash-1 (3 bar) is recirculated to the second compressor and mixed with the raw biogas. The CO2-enriched solvent is sent to the second flash tank (Flash-2) and regenerated by decreasing the pressure. The solvent leaving from the bottom of Flash-2 is recirculated and mixed with pure IL solvent. 3.2. Comparison of imidazolium-based ILs Based on the literature survey, the capacity of a biogas plant is in a range of 150–2000 N m3/h. Götz et al. [72] reported the details of a high pressure water-scrubbing, and the plant capacity was set to be 242.3 N m3/h. Cozma et al. [8] performed modeling and sim- ulation of biogas upgrading with high pressure water-scrubbing where the plant capacity was set to be 10.854kmol/h Unit Diameter of absorber, m Make-up solvent, t/h Recirculated solvent, t/h CH4-OFFG, mol% CO2-OFFG, mol% CH4-LIQCIR, mol% CO2-LIQCIR, mol% CH4-GASCIR, mol% CO2-GASCIR, mol% [hmim][Tf2N] [bmim][Tf2N] 0.53 0.46 0.372 0.360 24.45 23.64 0.023 0.025 0.977 0.975 0.000012 0.0000051 0.0072 0.0038 0.181 0.215 0.819 0.785 [bmim][PF6] 0.66 0.365 23.97 0.005 0.995 0.00000079 0.0045 0.119 0.881 (243.14 N m3/h). Therefore, in this work, the capacity of the biogas plant was set to be 10 kmol/h (224 N m3/h). In simulation, the biogas was assumed to be a mixture of 55% CH4 and 45% CO2. The simulation was based on the equilibrium approach. The purity of CH4 in the product gas (PG) was set to be 0.97 by varying the amount of ILs. The regeneration degree of ILs was set to be 98.5%. The process parameters are listed in Table 6. The biogas upgrading using [hmim][Tf2N], [bmim][Tf2N] and [bmim][PF6] as solvents were investigated, respectively. The simulation results are listed in Table 7. The amounts of recirculated solvents follow: [bmim][Tf2N] < [bmim][PF6] < [hmim][Tf2N]. The gas loading in ILs is the key factor influencing the amount of solvent, and Fig. 10 shows the calculated CO2 and CH4 loadings in [hmim][Tf2N], [bmim][Tf2N] and [bmim][PF6] at 293K. The CO2 loading in [bmim][Tf2N] is high, and this observation is consis- tent with the low amount of recirculated [bmim][Tf2N]. For [hmim][Tf2N], the high CH4 loading leads to a high amount of recir- culated solvent. Therefore, both the CO2 and CH4 loadings are importance for evaluating the performance of biogas-upgrading Fig. 9. Schematic of biogas upgrading using ILs.PDF Image | CO2 Separation with Ionic Liquids
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