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16 Chapter 2 CO2 removal process evaluation Por the experimental work liquid nitrogen (LN2) has been used to provide the amount of cooling which would be available from hydrogen. The air exiting the warm side of the CO2 subliming heat exchanger passes into a coiled tube immersed in a LN2 bath. A bypass around the LN2 bath and two valves allow control of the proportion of air passing through the LN2 bath. This allows control of the cold end temperature. The pressure drop between the air inlet and outlet, in addition to that due to the valves and core, may be increased to aid the re-vaporisation of water and the degree of CO2 removal. This may be done using the bypass valves which also control the cold end temperature. In practice, initial cool-down is envisaged being achieved by using the boil-off vapour, resulting from initial filling ofthe liquid hydrogen vessel. Subsequent re-cooling of the CO2 subliming heat exchangers is done using a bypass from the hydrogen-air heat exchanger. This schematic represents the general layout for a fully instrumented research apparatus used for this experimental project, not a prototype. The eventual layout may, for example, consist of only two 3 fluid (or 3 stream) heat exchangers with cross-over valves. Por this project the CO2 removal apparatus was sized based on a 1-1.2kW alkaline fuel cell. 2.4 Criteria for efficiency The minimum work requirement (W) for separation of CO2 from air may be calculated for a thermodynamically ideal separation system as -Win =RT ~ y.ln(lIy.) J 11l 11lL...J J J j (2.4) where Yj=n/~=mole fraction of the lh component, and the subscript m refers to the mixture. This equation, shown by Barron[58-p151], can be used to calculate for CO2 the minimum work input which equates to 293 J/kg of air. It is difficult to establish an equitable criteria for efficiency, or rather, Figure of Merit (POM), of a CO2 removal system. The use of expendable absorbers poses no immediate energy penalty other than that due to the pressure drop through the material. On this basis, it is difficult for any regenerable system to have a comparable POM. Por this work, the POM of the refrigeration purification method proposed may be calculated in several ways. The actual work input may be taken as: • work for gas compression to overcome the pressure drop in the CO2 removal device, and the work input for hydrogen liquefaction; • the work input for gas compression only, since the hydrogen has already been liquified for storage; orPDF Image | CO2 removal from air for alkaline fuel cells operating with liquid H2
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