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structured monolith contactor. Krishnamurthy et al. (2014) reported a wide range of energy utilization as a function of process capacity for a bed-based vacuum-pressure swing adsorption (VPSA). CO2 separation costs for MEA absorption-based systems are reported by Luis (2016), Pirngruber et al. (2013) and Bounaceur et al. (2006). To enable a comparison of the energy requirement of the present concept with these studies, the energy requirement estimated for the present concept for removal for CH4 is recalculated as energy requirement for separating CO2 from the feed mixture. The mass of CO2 removed during the adsorption stage is used to normalize the actual energy requirement per cycle, and the energy requirement values are plotted against the mass of CO2 removed per unit adsorbent mass per hour in Figure 3.11(c). From Figure 3.11(a), it is clear that process performance remains superior to that of the bed-based PSA processes, and also of the TSA-process that uses separate alternating microchannels for the flow of working fluids and HTFs (Kapoor and Yang, 1989; Olajossy et al., 2003; Pahinkar et al., 2016). A marginal reduction in product output with a reduction in pressure drop across the microchannel is seen; however, this change is insignificant compared to the gains predicted over the systems discussed in the literature. As seen in Figure 3.4, process capacity remains up to two orders of magnitude greater than that of the bed-based systems and up to 4 times greater than the capacity of the TSA-process with separate alternating microchannels. From the product purity–CH4 recovery graph shown in Figure 3.11(b), CH4 recovery is observed to improve from a maximum of 82.8% to 87.9% and 88.05% without compromising product purity as the pressure drop across the microchannel decreases from 100 kPa to 25 kPa and 10 kPa, respectively. This improvement is attributed to the sharper adsorption wave at lower fluid 90PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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