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of the microchannel geometry, the cooling stage is also rapid, lasting only 3 s. One of the areas of further improvement is the purge stage, where the microchannel configuration with a prescribed constant pressure drop results in small rate of liquid water removal from the adsorbent layer. The options of mechanisms by which water can be removed from the adsorbent layer are limited. However, the overall cycle time for the TSA process proposed is smaller than the PSA processes documented in the literature (600 - 1200 s) (Kapoor and Yang, 1989; Olajossy et al., 2003). Parametric studies on microchannel geometry are conducted, which show that a larger diameter channel with a thinner adsorbent layer results in short and efficient purification cycles. In particular, the cycle time is estimated to be 203 s for a Dh of 530 mandthof30m,whichincreasesto2225sforaDh of200mandthof100m. Large mass flow rates as a result of the large microchannel diameter, and reduction in mass transfer resistances within the adsorbent layer as a result of the thinner adsorbent layer result in fast execution of each of the stages. The full process model is simulated with two adsorbent-HTF pairs, silicalite–water and zeolite 5A–PAO. Although zeolite 5A is an excellent CO2 adsorbent, it cannot be used with water, because of its greater affinity for water. The use of PAO, which does not interfere with CO2 adsorption in zeolite 5A, results in a very slow process due to its high viscosity. Additionally, because of its low volatility, it cannot be evaporated out of the adsorbent layer. The silicalite–water pair, however, yields excellent process performance, due to higher temperature sensitivity of silicalite and excellent heat and mass transfer characteristics offered by water. Therefore, silicalite–water is the preferred adsorbent–HTF pair for this system. 66PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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