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to be 85 %. The “kWth” and “kWe” are the units of heat duty and electricity power, respectively. When calculating the total energy utilization, the heat duty required in the process was converted to electricity for comparing, where the conversion efficiency of heat to electricity was assumed to be 0.3. 53 The results showed that for the biogas plant with a capacity of 242.3 Nm3/h, the total energy utilization for biogas upgrading with water was 58.11 kW. The addition of ChCl/Urea (1:2) into water decreased the energy utilization. For example, with 50 wt. % ChCl/Urea (1:2), the energy utilization decreased down to 45.93 kW, that is, the total energy utilization decreased dramatically by 21 % compared to water. Further increase of the content of ChCl/Urea (1:2) led to a further decrease of energy utilization but with a low rate, for example, when the content of ChCl/Urea (1:2) increased from 50 to 70 wt. %, energy utilization only decreased by 4 %. The electrical power includes the power for operating the pump, compressor and blower. As we can see from Table 7, it decreased down to 35.13 kW from 48.1 kW. This corresponds to a dramatic decrease by 27 % with the increasing content of ChCl/Urea (1:2). To compare with other biogas plant with different capacity, the specific energy utilizations per Nm3 raw biogas (SERG) and per Nm3 upgraded biogas (SEPG) were calculated, and the corresponding results are listed in Table 7. According to the report of Bauer at al. 4, for a practical HPWS process with the plant capacity of 250 Nm3/h, the value of SERG was around 0.3 kWh/Nm3. Patterson et al. 5 gathered SEPG from a range of industrial and academic literatures for relatively well-established technologies including water scrubbing. The gathered SEPG were relatively consistent with a range of 0.20-0.43 kWh/Nm3. In this work, the calculated values of SERG and SEPG were 0.24 and 0.43 kWh/Nm3, respectively. These values are consistent with the values reported by others, and thus further confirmed that the simulation results obtained in this work are reliable. Compared with other CO2 capture process such as amine scrubbing (0.56-0.646 kWh/Nm3) 5, the energy utilization of HPWS process and the process using aqueous ChCl/Urea (1:2) was lower because of no thermal energy demand for solvent regeneration. Table 7. Summary of energy requirements for biogas upgrading using different absorbents Energy Units Water utilization WC kWe 30.02 WP kWe 13.51 WB kWe 4.57 QC kWth 26.17 QF kWth 5.31 QH kWth 1.89 Total kWe 58.11 SERG kWh/Nm3 0.24 SEPG kWh/Nm3 0.43 30 wt. % ChCl/Urea (1:2) 29.53 6.92 4.57 25.73 2.26 1.02 49.72 0.21 0.37 50 wt. % ChCl/Urea (1:2) 29.13 3.77 4.57 25.37 2.25 0.58 45.93 0.19 0.34 70 wt. % ChCl/Urea (1:2) 28.59 1.97 4.57 24.89 4.79 0.32 44.13 0.18 0.33 3.3.3. Diameters and pressure drop of the absorber and desorber. In this work, the packing material was a plastic pall ring with the diameter of 25 mm, and 62 % of the flooding velocity (maximum capacity) as recommended in Aspen Plus was used when calculating the diameters. As listed Table 8, the diameters for both absorber and desorber decreased with increasing ChCl/Urea (1:2) content. When the content of ChCl/Urea (1:2) increased from 0 to 70 wt. %, the diameter of the absorber decreased from 0.59 to 0.33 19PDF Image | CO2 Separation with Ionic Liquids
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