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It is also important to note that a higher process capacity results in a lower energy ratio, enhancing the economic viability. The lowest energy ratio calculated for the baseline case is 14%. An increase in the adsorption stage duration beyond 0.22 s may result in lower values of energy ratios, but at the cost of significant drop in product purity. This value of energy ratio is equivalent to 1.6 kWh kg-product-1 absolute operating power input and is higher than the reversible electrical energy requirement predicted for chemical absorption (0.34 kWh kg-1) and that for cryogenic distillation (1.0 kWh kg-1) (Göttlicher and Pruschek, 1997). However, the actual operating energy requirement for the MEA absorption system is reported (Bounaceur et al., 2006) to be up to 1.67 kWh kg-product-1, making the process analyzed in the present study comparable to absorption systems in terms of energy consumption. Avenues for energy reduction are discussed in the next section. 3.5 Reduction in operating energy requirement As shown in Figure 3.6, energy utilization is dominated by the sensible heat required to raise the temperature of the monolith and power input to the purge gas compressor, requiring 42% and 53% of the total energy input, respectively. The sensible heat required can be reduced by decreasing the desorption temperature, thereby reducing the temperature swing available for the process. Simulations are conducted with three desorption temperatures (200°C, 100°C, 50°C), while keeping the rest of the parameters the same as the baseline case described in Chapter 2. Figure 3.8(a) shows variation of cyclic CO2 adsorbed concentrations as a function of temperature. As expected, the operating adsorption capacity drops significantly with temperature swing, affecting the product purity accordingly. For a 82PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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