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strong chemical affinities for acid gases (Yang et al., 2008). Absorption-based systems are widely employed for not only natural gas purification, but also for CO2 separation from flue gas (Aaron and Tsouris, 2005). The dynamics of an absorption-based purification system are well understood, and operation and product collection in an absorption process is continuous. However, implementation of absorption-based systems requires large capital costs. As a result of bulk liquid circulation, which is the primary process in the system, the system size is large; therefore, absorption-based systems seldom find applications in off-shore platforms or smaller plants. Continuous operation of the system deteriorates the solvent gradually over time due to irreversible reactions of more strongly reacting impurities with the solvent, and replacement of the solvent is expensive. The reversible energy requirement reported in the literature for absorption- based systems is 0.34 kWh kg-1 CO2, while the same for the adsorption-based processes can be as low as 0.16 kWh kg-1 CO2 (Göttlicher and Pruschek, 1997) for a feed gas mixture with 28% CO2 by volume. The actual operating costs for the MEA absorption systems (Bounaceur et al., 2006), however, can be up to 1.67 kWh kg-CO2-1. The second commonly used separation method – membrane gas separation – relies on preferential sieving of the components in the feed gas mixture based on a combination of gas molecule size, selectivity of membrane material, and membrane sizes (Koros and Mahajan, 2000). Membrane separation processes are gaining importance in small-scale (< 6000 m3 hr-1) and medium-scale applications (6000 - 50000 m3 hr-1) applications, at off-shore locations, and in remote locations where energy availability is an issue, because of advantages such as small footprint, simplicity in design, low 12PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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