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mixture, is shown in Figure 8. The presence of H2O, SO2 and NO2 as impurities with a percentage between 0.001% and 1% were considered, while the increase of the impurity is in detriment of the same N2 percentage. Notice that, in order to compare TSA with pressure processes, an exergetic comparison was used, and further compression of the rich-CO2 stream to supercritical fluid for transportation was not included in the calculations. With these assumptions, TSA specific energy consumptions are the lowest in Mg-MOF-74 and zeolite 13X for impurities content lower than 0.5% and 0.02% respectively. Notice that although one of the best options for all three adsorbent materials is VSA with regeneration at 0.05bar, it is really difficult to expand in practice at so low pressure values, and therefore it may not be viable in certain plants. As inferred from Figure 8, it is clear that zeolite 13X is more appropriate for VSA and TSA processes. However, the energy requirements increase as impurities are explicitly considered in the mixture, the change being sharper for impurities with higher isosteric heat, (i.e., higher affinity); in this case, the increase in the slope follows the tendency H2O > SO2 > NO2, (marked by the arrows in Figure 8). Although it was expected that H2O and SO2 carry out a negative influence in the total CO2 recovery cost, at so low percentages, SO2 does not exert a decisive influence in the process, since the quantity of adsorbed CO2 is not drastically reduced below 0.1%. It is remarkable that, in some cases, the addition of impurities reduces the energetic requirement per tonne of CO2 captured. For instance, the requirements for VSA 1→0.1bar with Mg-MOF-74 shows a reduction from 4 GJ/tonne-CO2 in the binary mixture to 2.7 GJ/tonne-CO2 including 0.1% H2O. SO2 also shows this reduction, but is lesser than the one obtained for a more affinity species, while the minimum value is 40PDF Image | swing adsorption processes for CO2 capture in selected MOFs and zeolites
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