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adsorbent layer and make it ready for the next purification cycle. The performance of the silicalite-water pair was compared against that of the other adsorbent-HTF pair, zeolite 5A - PAO. Although zeolite 5A is a strong CO2 adsorbent, the use of PAO as an HTF resulted in severe performance deterioration as a result of the high viscosity of the lubricant oil. Furthermore, once PAO enters the adsorbent layer, it cannot be removed in a practicable manner as a result of its low volatility. Therefore, silicalite, which has moderate affinity for CO2, was deemed suitable as an adsorbent with water as the HTF, which offers excellent heat and mass transfer characteristics. By simulating the full process model for a range of feed and product collection times and plotting the performance indicators against those of the existing processes, the present concept was predicted to yield up to 55 times greater process capacity as compared to bed-based PSA processes (Kapoor and Yang, 1989; Olajossy et al., 2003) and up to four times greater capacity than a microchannel-based design with separate, parallel adsorbent-coated and HTF channels (Pahinkar et al., 2016). A first stage product purity range of 87% - 99% predicted for the present concept is competitive with the bed- based processes. The CH4 recovery from the present concept used in a single stage is up to 84% as a result of loss of the rest of the gas to the liquid water. By designing a two- stage purification system, the product purity could be enhanced to 99.9%. The multistage design could purify the product stream by subjecting it to successive purification stages; additionally, it also recovers gases from the desorption stream and separates impurities from it to create a CO2 rich stream to be used for sequestration. The operating energy requirement for the present concept was found to be 14% of the combustion potential of the product for the baseline case. The equivalent absolute 159PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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