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while selectivity for CO2-over-N2 for binary 85%N2/15%CO2 and ternary 15%CO2/84.9%N2/0.1%H2O mixtures as function of pressure are shown in Figure S10 of the Supplementary Material. Results for the simulated adsorption isotherms of ternary mixtures at different conditions for the three materials can also be found in the Supplementary Material, Figures S11-S17. 3.3. Implications for the application in PSA, VSA and TSA processes. Swing adsorption cycles can be manipulated to meet a variety of demanding requirements. For instance, same working capacities can be obtained by changing the adsorption/desorption conditions. Nevertheless, the most cost-effective material will lead the best selection for the CO2 capture process.85,109,110,111 The aim of this section is to test different conditions in order to be able to select, for each structure, those conditions that minimize the energy requirements for CO2 capture. The chosen model has some idealized conditions that it is relevant to highlight: experimentally, there are changes in temperature during the adsorption/desorption steps, and also along the column. Besides, the maximum removal is achieved with no determined desorption time, and crystal activation of structures may not be always the same. These features are not considered in the simplified modeling used here hence, the results presented are for an ideal system, with higher purity and lower specific energy consumption values predicted than in the real case. However, the general trends obtained in this work should be maintained for practical implementations, as inferred from the agreement with parametric studies in the literature with similar adsorption/desorption conditions (see Figure S18 in the Supplementary Material). Figure 5 summarizes different values for carbon dioxide working capacity in VSA, PSA and TSA processes, including all the mixtures evaluated in the previous section. 28PDF Image | swing adsorption processes for CO2 capture in selected MOFs and zeolites
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