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The specific energy utilization predicted for the present work is 0.68 kWh kg-product-1 and is found to be lower than the actual energy requirement for MEA absorption systems and the reversible electrical input for cryogenic distillation installations (Göttlicher and Pruschek, 1997). The CO2-specific energy requirement is also found competitive with the existing adsorption- and MEA absorption-based systems. The TSA-based process in the present study is assessed to be suitable for large-scale industrial applications and can be powered primarily with low-grade heat. The use of microchannels utilizing a small amount of adsorbent per microchannel in addition to convection based fluid dynamics within the microchannel increase the compactness and scalability of the system drastically over existing PSA-based systems. For a single stage purification process, a favorable process performance region is predicted, which yields very high process capacity, moderate CH4 recovery, high product purities, and moderate energy utilization. Product purity enhancement by staged purification is also possible with the present concept without affecting cycle design and scalability. Product purities up to 99.9% are possible through appropriate timing of the process stages and by maintaining the necessary thermodynamic equilibrium between the stages. Such an implementation, however, would require a comparative feasibility assessment of utilizing a second stage TSA-based monolith over other processes like cryogenic separation, which also produce high product purity at an increased operating cost. 97PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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