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and 2.7 (900 cpsi) at 1 l/min. These indicate laminar flow and thus we expect Taylor dispersion to intrude on the breakthrough curve. An estimation of extent of Taylor and axial dispersion on the total dispersion has been done in our previous study2 in which we concluded that the influence of these factors on overall dispersion is negligible. The dispersion observed for the 900 cpsi structured adsorbent can therefore be attributed to mass transfer resistance or perhaps maldistribution of the gas into the channels. If a 900 cpsi structured adsorbent with mass transfer resistance and flow distribution similar to the 400 cpsi structured adsorbent could be prepared, it would represent a better or “ideal” monolithic adsorbent. This “ideal” 900 cpsi adsorbent was simulated in the study described below. 4.2 Process simulation Results In order to ensure that the simulation parameters were chosen correctly and the simulations mimic the real system, benchmarking against the experimental breakthrough curves for sample C5400 was first performed. The overall mass transfer coefficient, k400 for the C5400 adsorbent was first determined by fitting the breakthrough data, see Figure 10 (a). This figure illustrates that the model can describe experimental data adequately. Since the breakthrough data of the C5900 adsorbent were not indicative of an “ideal” adsorbent (as discussed above), we have chosen to simulate the “ideal” 900 cpsi adsorbent. The overall mass transfer coefficient k900 for the ideal 900 cpsi adsorbent was estimated using our expression for monoliths developed earlier 2: Wd 1 1 d W 1 d d W 3 6 k900 4kf 8De Eq.(3) where W and d are wall thickness and channel width of monolith (as depicted in Figure 1 (b)), kf is external gas film mass transfer coefficient calculated from correlations presented 124PDF Image | Structured Zeolite Adsorbents for PSA Applications
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