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Specially developed porous metal hydrides (PMH) or Misch metal (Mm) matrix alloys, containing Ni, Fe, La, Al, H, have very high rates of sorption and heat of adsorption with hydrogen as adsorbates and have promising uses in development of metal hydride refrigeration and heat pump systems (Nagel et al, 1984; Ron, 1984; Yanoma et al, 1988; Charters et al, 1996; De Beijers and Horsman, 1993). 4.3.3 Storage for heat upgrade A less conventional form of chemical bond storage dehydrogenation of alcohols and hydrogenation of aldehydes or ketone can be illustrated by: Alcohol ↔ Aldehyde (or ketone) + Hydrogen This reaction sequence can upgrade thermal energy with no consumption or production of other chemicals (Lauerhass and Rudd, 1983). The process comprises two main units: an endothermic reactor (low-temperature heat is supplied to a distillation column for separation products and residual reactants) and an exothermic reactor (high-temperature heat is released) (Mooksuwan and Kumar, 2000). The feasibility is based on dehydrogenation of i-propanol and hydrogenation of acetone has been proven experimentally (Taneda et al, 1995). The dehydrogenation can be of methanol, ethanol or n-butanol and hydrogenation of formaldehyde, acetaldehyde or butyraldehyde, respectively. The dehydrogenation reaction takes place in liquid phase with catalysts in liquid-film state (Saito, 1995) at low- temperature (70–100oC) and requires thermal energy; while the hydrogenation reaction is carried out in gas-phase at a higher temperature (150–200oC) as an exothermic reaction. Dehydrogenation reaction occurs at the boiling point of liquid phase and its temperature level is fixed by the equilibrium conditions at reaction pressure. The alcohol produced by hydrogenation reaction of aldehyde or ketone and hydrogen is recycled for dehydrogenation reaction (KlinSoda and Piumsomboon, 2007). Since two reverse reactions running at different temperature levels are involved, at least two reactors and one heat exchanger are used in the system cycle (Gastauer and Kameyama, 1995). Part of low-level thermal energy supplied is upgraded to high- level energy and the rest is removed by condenser at ambient temperature (Karaca et al, 2002) The rate of dehydrogenation reaction depends on the aldehyde (or ketone) concentration in the liquid reaction mixture, the products (aldehyde or ketone and hydrogen) are to be continuously removed (aldehyde or ketone by vaporisation) from the endothermic reactor. Reaction and vaporisation take place simultaneously. To efficiently convert thermal energy into chemical energy a high aldehyde (or ketone) concentration in liquid mixture is required. However, since the reaction rate rapidly decreases as the content of aldehyde (or ketone) in the reaction mixture increases the operation of dehydrogenation reactor is limited to low aldehyde (or ketone) concentrations (Gastauer and Kameyama, 1995). Typical hydrogenation and dehydrogenation reactions: • At80–90oC (CH3)2CHOH(l) →(CH3)2CO(g) +H2(g) 41PDF Image | EPSRC Thermal Management of Industrial Processes
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