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proportionally. Therefore, the normalized product collected during the adsorption stage decreases as th increases. From a process standpoint, choosing a greater Dh and a thinner adsorbent layer results in shorter cycle times. For example, with a Dh of 200 m and th of 100 m, the total cycle time is estimated to be 2225 s, compared to 203 s with a Dh of 530 m and th of 30 m, as illustrated later. This enhanced performance is attributed to large mass flow rates through a large microchannel, and to reduced mass transfer resistances through a thin adsorbent layer. It must be noted that this optimization is based on the mass of purified product, whereas the optimization for energy requirement is addressed in a later section. Table 2.6.Effect of adsorbent layer thickness on adsorption stage performance Dh [μm] 530 th Vw×10-8 [μm] [m3] 15 2.43 30 4.71 60 8.86 120 1.55 Mads×10-6 Mprod ×10-6 [kg] [kg] 6.83 10.3 13.3 11.7 24.9 12.3 43.5 12.3 Mprod [kg kg-1] 1.51 0.88 0.49 0.28 2.3.2 Adsorbent and HTF material selection The appropriate adsorbent material and HTF are selected based on another parametric study to assess the feasibility of adsorbent-HTF pairs. The full process performance observed with the use of silicalite – water is compared against that of the zeolite 5A – polyalphaolefin (PAO) pair. Zeolite 5A has a higher selectivity for CO2 compared to silicalite as shown in Figure 2.9, which shows the competitive adsorption isotherms for zeolite 5A and silicalite for a CH4-CO2 mixture (70/30). The dual-site Langmuir equation (DSL) for modeling the 49PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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