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bottom as the module was mounted in a horizontal orientation. This temperature gradient led us to conclude that the flow of the shell-side purge gas was not evenly distributed through all sections of tubes across the cross section of the membrane module, meaning that the surface area utilized for the mass and energy transport was being limited by channeling effects on the shell side. This has a large impact on our model, in which it is assumed that the purge gas is distributed across the surface area of the tubes evenly. The calculated values for the surface area utilization efficiencies for water per- meation, i.e., ηM , are plotted for varying feed relative humidities against the ratio of purge to feed gas, Vs/Vt, in Figure 6.11. It can be seen that as the Vs/Vt ratio de- creases, ηM decreases, suggesting that the flow distribution on the shell side becomes less ideal as the purge gas flow rate is reduced. Alternatively, as the feed relative hu- midity increases, ηM decreases implying that the membrane’s performance should be improving as the membrane is hydrated but the transport due to forced convection on the shell side is not as effective as theory predicts. These are good indicators of flow maldistribution occurring on the shell side and that the membrane is not dehydrating the feed stream as predicted. 6.5 Conclusions Mathematical models were developed and solved in conjunction with experi- ments for the dehydration of a feed stream using a multi-tube shell and tube mem- brane under counter-current operation in order to determine the effects of scale. The models accounted for two interfacial resistances and resistance in the membrane for both heat and mass transport. Several cases were examined in which the relative humidity of the feed stream varied from 33% to 60% as well as the Vs/Vt ratio varied from 0.7 to 1.1. We determined that a lack of uniform flow pattern on the shell-side created by 123PDF Image | TEMPERATURE SWING ADSORPTION COMPRESSION AND MEMBRANE SEPARATIONS
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