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• • • • membrane permeation gaseous diffusion electrochemical separation of chlorine hydrate formation forpartial separation of chlorine It is emphasized that evaluations are preliminary for the purpose of determining general limits in the possible applications. Two or more methods conceivably could be used in a final device if a simpler device resulted. No attempt has been made to finalize possible combinations of devices or to consider design for imple mentation . Separation by Membrane Permeation Membrane permeation techniques utilizing permselectivity, which is the tendency for certain materials to pass one gas more readily than others, were considered briefly as a basis for a separation of CO^ in a battery system. This process differs from ordinary diffusional processes in that the gases dissolve to a greater or lesser extent in the membrane material, diffuse through, and are released on the outlet side. Membrane permeability separation processes have been used industrially for a variety of gaseous separation processes. Membrane materials used (36-1) include polymers, glass, and metal. The theory for this type of device is well developed. The principle limitation for application of this type of device to the zinc- chlorine battery system is the need to compress the gas mixture prior to separation to achieve useful separations even in a perfect multi-stage device. This arises because the partial pressure or chemical potential, of the gas on the upstream side of each stage must be at least slightly higher than the gas partial pressure on the downstream side. The maximum pressures expected in the zinc-chlorine battery will be in the hydrate store where pressures of 1.6 atm conceivably would be available. Even with CO^ concentrations in the store as high as 5%, the CO^ partial pressure would be only 0.08 atm. At 1% inerts concentration in the store, the partial pressure would be 0.016 atm. Discharging to 1 atm would, therefore, require that the CO^ partial pressure be increased to 1 atm. Ignoring pressure losses in a membrane separation device, increasing the CO^ partial pressures to 1 atm would require gas compression from the store pressure to approximately 13 atm when CO^ concentration is 5% in the store, and 62.5 atm when it is 1%. These compression ratios are not excessively energy consumptive. However, they require the design of a low-volume, high-pressure gas pump compatible with the corrosive chlorine atmosphere. Solution of the attendant materials problems would be required. 36-4PDF Image | Development of the Zinc-Chlorine Battery for Utility
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