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energy requirement amounted to 1.6 kWh kg-CH4-1, which is competitive with the reversible electrical input for the cryogenic separation process. Two avenues to reduce the energy requirement – reduction of desorption temperature and reduction of pressure drop across the microchannel – were considered. Desorption temperature reduction resulted in reduction of the adsorption capacity, thereby reducing the purity of the product and deterioration of overall performance of the process. However, reduction in the pressure drop across the microchannel reduced the total energy requirement by 53%, without any significant change in the cycle time. Additionally, about 97% of the total energy could be supplied as low-grade heat, making the present concept environmentally friendly and energy efficient. The improved energy requirement value, 0.725 kWh kg- CH4-1, is competitive with those for MEA absorption-based systems most commonly used for natural gas purification (Göttlicher and Pruschek, 1997). Furthermore, the maintenance costs associated with the present concept are expected to be smaller as solid adsorbent would require replacement less frequently. The use of microchannels with a small amount of adsorbent per microchannel in addition to convective transport within the microchannel increases the compactness and scalability of the system for a given adsorbent mass drastically over the conventional PSA-based systems. The process therefore yields very high process capacity, moderate CH4 recovery, high product purities and moderate energy utilization. Gas separation was studied by designing and constructing a test facility with a mass spectrometer and conducting batch adsorption tests on adsorbent-coated microchannels. The first phase of the experiments was conducted on PLOT columns, for which precise information on adsorbent mass and packing fraction was absent. 160PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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