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Figure 12. Effect of AFR/G on (a) YCH4,PG and YCH4,SG; (b) Energy utilization and ηCO2 using 50 wt. % ChCl/Urea (1:2) as absorbent Table 6. Operational conditions and simulation results based on plant capacity of 242.3 m3/h (STP). Parameter L/G Mass flow rate of absorbent Nab pflash AFR/G ηCO2 YCH4, PG YCH4, SG Loss ratio of CH4 RECO2 Units H2O m3∙m-3 0.195 30 wt. % ChCl/Urea (1:2) 0.0999 50 wt. % ChCl/Urea (1:2) 0.0545 70 wt. % ChCl/Urea (1:2) 0.0285 kg∙h-1 47179.6 11 8 7 6 MPa 0.3 m3∙m-3 2.1 % 99.54 % 96.70 % 0.0633 % 0.311 % 99.56 0.3 2.1 99.45 96.66 0.0846 0.414 99.04 0.3 2.1 99.20 96.66 0.103 0.502 98.81 25506.3 14472.7 7894.5 0.3 2.1 97.54 96.66 0.173 0.837 98.65 Based on the simulation results summarized in Table 6, the L/G ratio and mass flow rate of absorbent decreased 87 % when the content of ChCl/Urea (1:2) increased to 70 wt. %. This means that the absorption capacity of the solvent increased 7 times. Meanwhile, the number of theoretical stages reduced from 11 to 6, which directly affected the height of absorber. Besides, the L/G ratio, AFR/G ratio, Nab and pflash listed in Table 6 can be used as a reference in process design even the plant capacity is different from 242.3 m3/h (STP). 3.3.2. Energy utilization. Based on the optimal Nab, L/G ratio, AFR/G ratio and pflash for each solvent listed in Table 6, the energy utilization including power, heating and cooling in biogas upgrading system was studied. For the biogas upgrading process illustrated in Table 7, the total electrical power included the power for operating the solvent pump (WP), compressor (WC) and blower (WB). In addition, the heat duty for cooling the compressed biogas (QC), the heat duty of the flash tank (QF) and the energy used for transferring the solution from the flash tank (QH) to the desorber were also considered in estimating the overall energy utilization. Isentropic efficiency of 75 % was assumed for the gas compression52, while the mechanical efficiency due to the losses from the seals and valves in the compressor was assumed to be 85 %. The efficiency of the pump was assumed to be 80 % 4, while the driver efficiency was assumed 18PDF Image | CO2 Separation with Ionic Liquids
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