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CH4 Mi Ag uCg,i zL t adsVw Purity Mi kg,i Mi i Puritykg ,i (3.6) (3.7) (3.8) (3.9) MW ii MCH4,product MCH4,purge MCH ,feed Puritymole,i i kg,i MW Figure 3.4 shows the variation of product purity with process capacity evaluated for different feed and collection times. As feed time is increased, more CO2 enters the microchannel, reducing product purity as seen in Figure 3.4. Additionally, as the collection time is increased, process capacity increases at the cost of purity. Nevertheless, the purity values do not fall below 87% for the operating conditions considered here. More importantly, process capacity with the use of adsorbent-coated microchannels is found to be up to 100-fold greater than that for the bed-based PSA processes at similar product purities. The reasons for such very high predicted process capacities are: (a) extremely small requirement of adsorbent mass per microchannel, (b) higher intra- crystalline diffusivity values as a result of smaller adsorbent particles (~1 μm) and (c) high heat and mass transfer coefficients as a result of a convection-based design, unlike the diffusion-based designs of bed-based PSA systems. For the void fraction and adsorbent loading considered here, the adsorbent mass per microchannel is only 1.325×10-5 kg, whereas for example, the adsorbent mass required for construction of the bed studied by Olajossy et al. (2003) is 3.9 kg. Purity 76 4PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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