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compared with the increased bed capacity of a slightly larger bed, meaning that it is preferable to use the volume required by the air plenums to increase heat transfer for more adsorbent. Figures 2.7 and 2.8 show an ideal TSA path and the path computed by our model for each stage in the adsorption cycle. From these work cycles it can be seen that the second stage resembles the ideal path more so than the first stage, indicating that stage 2 operates more efficiently. By not cooling the adsorbent bed and initiating an adsorption half-cycle immediately after a desorption half-cycle any CO2 remaining in the fluid phase is blown out which reduces the effectiveness of the adsorbent bed. 2.4 Conclusions General algebraic relationships were developed to determine optimum stage sizes for a coupled 2 stage TSA compressor, and modeled using material and energy balances to describe breakthrough behavior. The models were solved for both a desorption and adsorption-half cycle of CO2 on 5A zeolite. We determined that an optimum combined volume for the first and second stages occurs at a specific equilibration pressure between the two stages, and is de- pendent on the properties of the adsorbent used as well as the operating procedure of the TSA beds. Next finite element models were developed simulating the TSA beds using material and energy balances and solved in order to model the breakthrough behav- ior of CO2 for both adsorption and desorption half-cycles. Using these solutions it was determined that following a desorption half-cycle with an adsorption half-cycle without allowing the bed to cool decreases the performance of the TSA bed as the accumulated fluid phase adsorbate is blown out of the adsorption bed in the initial period of the half-cycle. We also discovered that any extra cooling afforded by the addition of air plenums did not affect the adsorption of CO2 significantly. 19PDF Image | TEMPERATURE SWING ADSORPTION COMPRESSION AND MEMBRANE SEPARATIONS
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