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on local adsorbent layer packing properties. Therefore, the average ΔT value can be different for a different choice of thermocouple locations. The present work investigated the optimum geometry, materials, and operating conditions for a TSA-based process by developing a full process model. While each of the stages, adsorption, desorption, cooling and purge, are analyzed computationally to predict the process performance, only the adsorption stage was considered in detail by conducting 2-D axisymmetric modeling, alternative process modeling, and experiments to understand factors affecting the adsorption of CO2 in microchannels. It is recommended that gas-liquid-adsorbent interactions should also be studied experimentally for the desorption stage. In particular, the convective-diffusive flow early in the desorption stage and diffusive flow late in desorption stage can be studied by means of visual inspection and mass spectrometry. The selection of adsorbent and HTF materials for the experiments are critical due to measurability concerns. Silicalite, which can use water as the HTF, has moderate CO2 selectivity and very low adsorption capacity at near-ambient pressures. This adsorbent is shown to offer excellent adsorption swing capacities at high pressures as seen in Chapters 2 and 3. Zeolite 5A and its variants have excellent CO2 adsorption capacity at ambient pressure as discussed in Chapter 4; however, the design of the desorption stage experiments would be difficult if water were used as the HTF. The heavy lubricant oil, PAO, which does not interfere with CO2 adsorption, has already been shown to be impractical for microchannel flows. Furthermore, the flammability of PAO poses additional constraints on the design of desorption stage experiments. Designing high pressure flow-visualization desorption experiments with silicalite-water pair is one of the feasible options. A 2-D axisymmetric 162PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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