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adsorbable components, O2 and N2. The oxygen component (22%) was actually a mixture of O2 and Ar which have very similar adsorption isotherms for the sorbents of interest. The product of each cycle was comprised of a volumetric mixture of the output stream of the feed step and the cocurrent depressurization step. A portion of this product stream was used to purge the bed countercurrently in step V. In order to compare the performance of the Li94.5Na1.5-X-1.0 and the Li94.2Na0.7Ag1.1-X-1.0 sorbent developed in this work, the product throughputs of the two sorbents were studied under two different cycle conditions using computer simulations. In order to facilitate a fair comparison of the sorbent performance, the cycle conditions were optimized such that the product purity and product recovery obtained were the same for both the sorbents in each respective simulation run. In this work, the product purity, product recovery and product throughput are defined as follows : product purity = (amount of O 2 from steps II and III) (6) (amount of N 2 and O2 from steps II and III) product recovery = (O 2 from steps II and III) - (O 2 used in step V) (7) (O2 fed in step I and step II) product throughput = (amount of O 2 produced per hour (kg/hr)) (8) (amount of adsorbent used in the bed (kg)) The mathematical model and the numerical method used for the PSA simulations in this study has been explained in detail in an earlier work.2 Hence, only the basic assumptions will be listed here. The model used assumes the flow of a gaseous mixture 65PDF Image | PSA USING SUPERIOR ADSORBENTS
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