SYSTEM FOR ENERGY STORAGE, HYDROGEN PRODUCTION AND THE MANUFACTURE OF METHANOL FOR ABATING OF GREENHOUSE GASES

Abstract: An apparatus and method for the thermal and photolytic production of oxygen. Chlorine from acid and chlorine storage vessel (10) and liquid water are conveyed to heat exchange apparatus (05) for preheating. The gaseous chlorine and water are then further heated in reformer cell (25) by means of both thermal and photolytic energy, where they react to produce hydrogen chloride and oxygen, with equilibrium amounts of steam and chlorine. The aforementioned hydrogen chloride, oxygen, steam and chlorine are then cooled in heat exchange apparatus (05), where the condensed water acts to solvate the hydrogen chloride to dilute hydrochloric acid. Gaseous oxygen and chlorine are vented and conveyed to gas clean-up unit (100). Another embodiment of this invention is a method for the joint i) abatement of emission of a "greenhouse" gas by removing carbon dioxide from an effluent and ii) manufacture of methanol by reaction of hydrogen with carbon dioxide.

Description: SYSTEM FOR ENERGY STORAGE. HYDROGEN PRODUCTION AND THE MANUFACTURE OF METHANOL FOR ABATING OF GREENHOUSE GASES Field of the Invention The present invention relates generally to an apparatus and method for the manufacture of methanol and the simultaneous abatement of the emission of greenhouse gases. Description of the Related Art It has been known for many years that the reaction of hydrogen with carbon monoxide over an appropriate catalyst surface leads to the formation of numerous organic compounds: hydrocarbons, alcohols and the like. More recently, it has been found that H 2 + CO, react to produce methanol (purity of 80-90%) with yields of about 1.3% per pass over the catalyst. Much of this work has been performed since 1980. SUMMARY OF THE INVENTION It is an object of this invention to provide an improved apparatus and method for generating hydrogen and oxygen from water. It is an additional object of the present invention to provide an apparatus and method for the solar-augmented electrolytic and thermal production of hydrogen and oxygen. It is another object of the present invention to provide an apparatus and method for the solar-augmented electrolysis of hydrohalic acid to produce a halogen gas. It is another object of the present invention to provide an apparatus and method for an integrated, continuously- or intermittently-operable system providing both hydrogen and oxygen generation, and utility load leveling capabilities. It is another object of the present invention to provide an apparatus and method for both the formation of hydrogen halide, and reformation of hydrohalic acid employed in the electrolysis cell. It is still another object of the present invention to provide an apparatus and method for the production of potable water from a contaminated water feedstream. Accordingly, the present invention provides both an apparatus and method for the electrolytic production of hydrogen, and the thermal and photolytic production of oxygen. In the first step of the cycle a concentrated hydrohalic acid solution is electrolyzed to produce hydrogen, halogen, and dilute hydrohalic acid solution. The source of hydrohalic acid can be any source available, hydrogen chloride is preferred. The source of hydrogen chloride (HC1) can be any source available. However, a preferred source would be from a municipal solid waste to energy facility which burns solid waste and produces 3-8 tons of hydrochloric acid (HC1) per 1,000 tons of solid waste from typical municipal waste. Note that the method of this embodiment produces hydrogen and chlorine. Typical municipal solid waste burning can also be a source of carbon dioxide for another embodiment of this invention, described more fully below, namely the method for abatement of emission of "greenhouse" gas to manufacture methanol by reaction with hydrogen. Thus, two of the embodiments of this invention could be symbiotic with a municipal solid waste to energy facility, using the HC1 and the C0 2 from the solid waste to produce methanol for fuel and/or electricity which could be chemically stored during off peak hours for discharge during peak hours. In the second, or hydrogen halide formation and electrolyte reformation step, the halogen is reacted with steam in a gas phase thermal and photolytic process to reform the hydrogen halide and produce oxygen. An advantage of the novel reformation step is the ability to utilize a contaminated water feedstream for the production of the reusable hydrogen halide. The present invention also provides both an apparatus and method for the radiation-augmented electrolytic production of hydrogen and oxygen. Reduction of electrical and thermal energy reguirements is achieved by using radiation to: (i) activate photo-sensitive metallic hexahalide ions, which reduces the electrolysis electrode potential; and (ii) energize the hydrogen halide formation reaction. By utilizing radiation- augmented electrolysis, the conventional halogen oxidation reaction is replaced by oxidation of a metallic hexahalide, which occurs at a lower overvoltage and smaller reversible cell potential. Radiant energy thus both replaces electrical energy for the production of hydrogen, and increases the efficiency of electrical energy storage. Another embodiment of this invention is a method for the joint i) abatement of emission of a "greenhouse" gas, by removing carbon dioxide from an effluent from burning fossil fuel or other source of carbon dioxide and ii) manufacture of methanol by reaction of hydrogen with carbon dioxide. The fossil fuel could be coal or any petroleum product, typically fuel oil. The method comprises a) reacting carbon dioxide in the effluent of the burning of fossil fuel or other source of carbon dioxide such as from fermentation, from a municipal waste treatment facility or from a lime kiln, by flowing contact of the effluent with a bed of basic metal oxide at a temperature suitable to form a metal carbonate, b) then stopping the effluent flow after the bed is substantially converted to the carbonate, and c) heating the carbonate to a temperature suitable to release carbon dioxide, then d) mixing the released carbon dioxide with the hydrogen, e) while passing the mixture over the catalyst of another metal oxide at a suitable temperature and pressure for a reaction, thereby f) forming methanol. Preferably the method temperature of step a) is from about 330 to about 380°C and the pressure is atmospheric. Preferably the temperature of step c) is from about 475 to about 550°C and the pressure is atmospheric. Preferably the temperature of step e) is from about 140 to about 310°C and the pressure is from about 5 to about 55 atmospheres. Although any source can be used, the preferred source of hydrogen in step d) is from a radiation augmented electrolytic production process. Also, preferably there are a plurality of beds of metal oxide of step a) and at least one of the beds is used to react with carbon dioxide as in step a) to form carbonate while the other bed is being heated as in step c) to release carbon dioxide. In a more preferred embodiment, the temperature of step a) is from about 350°C to about 375°C and the pressure of step a) is atmospheric, the temperature of step c) is from about 500 to about 540°C, the pressure of step c) is atmospheric, the temperature of step e) is from about 150 to about 300°C and the pressure of step e) is from about 10 to about 50 atmospheres. The preferred metal oxide for step a) is selected from the group consisting of magnesium oxide, calcium oxide, zinc oxide and mixtures thereof. The preferred metal oxide catalyst of step c) is selected from the group consisting of ZnO on Zr0 2 , CuO on ZnO, Cuθ/ZnO/Al,0 3 and mixtures thereof. Another embodiment of this invention is the apparatus for the joint i) abatement of emission of a "greenhouse" gas carbon dioxide from burning fossil fuel or other source of carbon dioxide such as from fermentation, from a municipal waste treatment facility or from a lime kiln and ii) manufacture of methanol by reaction of hydrogen and carbon dioxide. The apparatus comprises a) means for reacting carbon dioxide in the effluent of a burning fossil fuel or other source of carbon dioxide such as from fermentation, from a municipal waste treatment facility or from a lime kiln by flowing contact of effluent with a bed of basic metal oxide to form a metal carbonate, b) means for stopping effluent flow after the bed is substantially converted to the carbonate, c) means for heating carbonate to a temperature suitable to release carbon dioxide, d) means for mixing the released carbon dioxide with the hydrogen, e) means for passing the mixture over a catalyst of another metal oxide to thereby form methanol. The preferred means for reacting in means a) is a bed of metal oxide mounted in the effluent conduit from a burning fossil fuel. The preferred means for stopping the effluent in means b) is a damper in the conduit. It is also preferred that there be a plurality of the beds mounted in a plurality of conduits. Then these beds are alternately i) used to react carbon dioxide with the metal oxide then ii) heated to release carbon dioxide by means of alternately opening and closing a damper system in the conduit. The preferred means of heating c) is a system to pass heated inert gas across the carbonate. The preferred means of passing the mixture over a catalyst is a reactor system, which can be a fixed bed, a mixed bed, or a fluidized bed. BRIEF DESCRIPTION OF THE DRAWINGS Other objects, features, and advantages of the present invention will become more fully apparent from the following detailed description of the preferred embodiments, the appended claims, and the accompanying drawings. As depicted in the attached drawings: FIG. 1 is a schematic block diagram of the apparatus and method embodied by a conventional hydrogen-halogen load leveling battery. FIG. 2 is a schematic block diagram of the apparatus and method embodied by the hydrogen halide formation, and electrolyte reformation, modes of operation of the present invention. FIG. 3 is a schematic block diagram of the apparatus and method preferably embodied by the radiation-augmented, hydrogen-halogen battery for the production of hydrogen and oxygen. FIG. 4 is a schematic block diagram of the apparatus and method preferably embodied by the electrolyte-conditioning and -storage mode of operation of the present invention. FIG. 5 is a schematic block diagram of the apparatus and method preferably embodied by the charging of the radiation-augmented battery mode of operation of the present invention. FIG. 6 is a schematic block diagram of the apparatus and method preferably embodied by the potable water production mode of the present invention. FIGURE 7 and 7A are schematic diagrams of the apparatus and method embodied by the C0 2 deposition mode followed by the C0 2 release mode of the present invention, using two bed of metal oxide, alternately. FIGURE 8 is a schematic diagram of the apparatus and method embodied by a methanol manufacture embodiment of operation of the present invention. FIGURE 9 is a schematic diagram of a fired heater apparatus associated with the generation of C0 2 in an effluent for this invention. FIGURE 10 is a schematic diagram of a fired heater apparatus showing another emobiment useful to heat the N 2 or H 2 purge gas for use in the apparatus to produce methanol, such as in Figure 8. DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention will be disclosed in terms of the currently perceived preferred embodiments thereof. By way of example, the present invention will be disclosed in connection with Group VIII transition metals, halogens, and halide ions. For illustrative purposes, iridium is disclosed as the transition metal, and chlorine as the halogen component. The radiation flux employed may generally be described as electromagnetic radiation. Preferably, solar rays are the source of that radiation. It should be readily apparent to those skilled in the art, however, that other sources of radiation energy might be suitably employed. Exemplary alternative sources include photons generated from nuclear-excited flash lamps, alpha particles, beta particles, gamma rays, x-rays, protons, or fission fragments. The present invention facilitates use of different combinations of solar, thermal, and electrical power in an integrated system for hydrogen production and/or utility load leveling. A fundamental basis of the first embodiment of the present invention lies in the fact that the voltage required to electrolyze a hydrochloric acid solution is less than that required to electrolyze water. In the electrolysis of hydrochloric acid, hydrogen is liberated at the cathode and chlorine is liberated at the anode, whereas in the electrolysis of water, hydrogen is liberated at the cathode and oxygen is liberated at the anode. Furthermore, both the E° value for the chlorine half cell and the overpotential of chlorine are lower than that for oxygen. Additionally, as a result of the temperature dependence of the E° value, increased ion mobility at high temperature leading to decreased IR drop, and diminished overvoltage, the voltage required to electrolyze HCl decreases with an increase in temperature. The water-chlorine cycle employed in the first illustrative embodiment uses electrical, thermal, and photolytic energy to convert water to hydrogen and oxygen as marketable products. The process reverses the hydrogen combustion reaction (1) in two steps, using chlorine as an intermediate which is not consumed. The reactions and their enthalpies at 298 K are: H,-0- reaction H 2 + i;0 2 H 2 0 -15 . 11 kw-hr/ lb H 2 ( 1 ) H,-C1, reaction H, + Cl_ → 2HC1 -11.54 kw-hr/lb H 2 (2) Electrolyte reformation reaction H 2 0 + Cl 2 → 2HC1 + h _ 3.57 kw-hr/lb H 2 (3) HCl electrolysis 2HC1 → H 2 + Cl 2 11.54 kw-hr/lb H 2 (4) Reaction (4) , the major energy-consuming step, uses electrical power to electrolyze the HCl formed by Reaction (3) . The cost of producing hydrogen by electrolysis is proportional to the voltage of the electrolysis cell. In the first step of the hydrogen production (or battery charging) cycle, a concentrated hydrochloric acid solution is electrolyzed to produce hydrogen, chlorine, and dilute hydrochloric acid solution. In the second, or hydrogen halide formation and electrolyte reformation step, the chlorine is reacted with steam in a gas phase thermal process to form hydrogen chloride and oxygen, and then solvated. The apparatus and method of an illustrative embodiment of the invention will now be described with reference to FIG. 2. In the hydrogen halide formation mode of operation, chlorine from acid and chlorine storage vessel 10 and liquid water are conveyed to heat exchange apparatus 05 for preheating. The gaseous chlorine and water are then further heated in reformer cell 25 by means of both thermal and photolytic energy, where they react to produce hydrogen chloride and oxygen, with equilibrium amounts of steam and chlorine. In the electrolyte reformation mode of operation, the aforementioned hydrogen chloride, oxygen, steam, and chlorine are then cooled in heat exchange apparatus 05, where the condensed water acts to solvate the hydrogen chloride to dilute hydrochloric acid. Gaseous oxygen and chlorine are vented and conveyed to gas clean-up unit 100. The hydrogen halide formation process has been examined in detail and found to be feasible at 600°C, and to occur with good yields and without undesired by-products. At 600°C, an HCl yield of 79.9% and an 0 2 yield of 79.3% were achieved. The oxygen produced during the formation step can be separated from the chlorine using any suitable conventional separation technique. Exemplary techniques include separation based on boiling points, in which the mixture is cooled to - 40°C to liquefy the chlorine while oxygen remains in the gaseous phase; membrane separation; differential adsorption; and flow separation, based on the solubility of chlorine in a solution of hydrochloric acid. In the flow technique, a mixture of chlorine and oxygen is passed through a solution of hydrochloric acid flowing downward. The solubility of Cl 2 increases in an HCl solution, due to the formation of Cl 3 " : Cl 2 + Cl " → Cl 3 ' Oxygenwillmove intheupwarddirection, thus separatingthe twogases. Inthe reformation of HCl fromchlorine and steam, if chlorine is used as a limitingreactant, only a small amount of unreacted chlorinewill bepresentwith a largequantity of oxygen. In a variation of the first illustrative embodiment, the inventionproduceshydrogenwhile operating as a load leveling battery by charging and discharging atdifferent currentdensities. By maintaining thevoltage at a nearly constant value, but increasingthe current density substantially on charging, the rate andamount of hydrogenproduced increases. Thoughthepower consumed during chargingwill increase as a result of the increased current density, it is lower-cost, off-peakpower. Optionally, the same effect couldbe attained by charging for a longerperiod of time thanthe time ofdischarge. Of the increased amount of hydrogen producedduringthe chargingcycle, aportion is utilized inthe fuel cell dischargemode, andthe balance is available for export as aproduct. The additional hydrochloric acidrequired for the surplus hydrogenproduction is attainedthrough electrolyte reformation fromthe chlorine produced duringthe battery charging cycle. In an additional illustrative embodiment of the present invention, an apparatus and method for the solar-augmented electrolytic and thermal production of hydrogen and oxygen are provided. Reduction of electrical and thermal energy requirements is achieved by using solar energy to: (i) activate photo-sensitive metallic hexahalide ions, which reduces the electrolysis electrode potential; and (ii) energize a portion of the hydrogen halide reformation reaction. By utilizing solar-augmented electrolysis, the conventional halogen oxidation reaction is replaced by oxidation of the metallic hexahalide, which occurs at a lower overvoltage and smaller reversible cell potential. Solar energy thus replaces both electrical power and thermal energy to eliminate a significant portion of the cost of either hydrogen production or electrical energy storage. The present invention describes a method for both hydrogen production and electrical energy storage by utilizing a combination of electrolysis, photolysis, and electrolyte reformation. The electrolysis process is based on the electrochemistry of a hydrohalic acid electrolyte. The photolytic process is based on the photochemistry of transition metal complex ions. The aqueous hydrohalic electrolyte contains another electrolyte, consisting of a metallic element of the type known as a Group VIII transition or post-transition element, along with a suitable counter-ion of opposite charge. The metallic element will be in a positive oxidation state. The overall charge of the complex ion, e.g., a metallic hexahalide ZX 5 , where Z is the transition metal and X 6 is the hexahalide, could be minus three (-3), or ZX Under the influence of an electric field, the negative ion ZX 6 "3 migrates toward the anode, where it is oxidized, leading to an ion of minus two (-2) charge: ZX 6 ZJL + e-. The species ZX 6 is then exposed to visible light, whereby it is promoted to an excited electronic state: ZX 6 ~2 + hv -* (ZX 6 "2 )*. The (ZX 6 "2 )* is then able to oxidize the halide ion in a hydrohalic acid, for example, which has a minus one (-1) oxidation state, to the elemental halogen, which has a zero oxidation state: (ZX 6 - 2 )* + X " → ZX 6 "3 + \ 2 To ensure that the process proceeds as desired, it is required that the ZX 6 "2 absorb visible light more strongly than the ZX 6 *3 . This condition can be achieved by providing these species in the form of the indicated complex ions. These species consist of a central Group VIII metallic ion in the positive oxidation state, surrounded and bound to one or more charged or neutral ions or molecules referred to as ligands. Exemplary metallic ion species include Fe, Co, Ni, Ru, Rh, Pd, Os, Ir, and Pt. Typical oxidation states of these ions may range from +1 to +8. Typical ligands include molecules such as H 2 0, NH 3 , and CO, as well as ions such as CN " , N0 2 " , Cl " , Br " , and I " . An example of the photochemical effect of transition metal complex ions is the charge transfer transition in IrCl 6 ~3 when subjected to radiation at visible wavelengths. This reaction is described by H.B. Gray, Science. Vol. 214 (1981) , 1201: IrCV 2 + Cl " + hv → IrCl 6 "3 + %C1 2 (5) In principle, a related charge transfer transition in IrCl 6 ~3 could facilitate the reduction of protons, completing a cycle that produces hydrogen and chlorine from HCl and water: IrCl 6 ~3 + H * + hv → IrCV 2 + i,H 2 (6) Since the absorption coefficient of IrCl 6 "3 is more than an order of magnitude smaller than that of IrCl β "2 at solar wavelengths, however, the quantum yield for the formation of H 2 is small. Reaction (6) is therefore not feasibly integrated in a practical cycle. A high quality aspect of solar radiation is the short average wavelength of solar photons of approximately 500 nm. The energy of an average solar photon is sufficient to cause selected photochemical reactions which can produce energy which may then be stored for subsequent use. Photochemical research has demonstrated that when HCl solutions containing IrCl 6 ~2 ions are irradiated, IrCl β "3 and chlorine gas are produced. The lower overvoltage and smaller reversible cell potential associated with the anodoic oxidation of IrCl 6 "3 is the basis for employing solar energy to reduce the cost of producing electrolytic hydrogen and oxygen. Solar-augmented -electrolysis thus comprises supplying an aqueous solution of HCl and IrCl 6 "2 to a photolysis cell, which is irradiated to reduce the IrCl 6 "2 to IrCl 6 "3 and produce gaseous Cl 2 , which is continuously swept from the cell. The aqueous solution of HCl and IrCl 6 "2 is then introduced into an anode half cell which is separated from the cathode half cell by a semipermeable membrane. An electrical potential is applied across the anode and the cathode, whereby IrCl 6 ~3 is oxidized to IrCl 6 "2 at the anode, and H 2 is evolved at the cathode. Of the two redox reactions (5) and (6) , reaction (5) is spontaneous in the presence of sunlight and reaction (6) is not. In an embodiment of the present invention, the redox reactions are therefor organized such that the photolysis reaction in a separate photocell may be combined with conventional electrolysis. Conventional electrolysis of HCl(aq) consists of the following half reactions: 2H * + 2e " → H 2 (gas) Cathode (7) 2C1 " → Cl 2 (gas) + 2e " Anode (8) In the process according to the present invention, reaction (7) is unchanged. The anode reaction is replaced with a cycle including the photochemical redox reaction (5) and an electrolysis half-cell reaction. The mechanism of the solar- augmented anode reaction is as follows: IrCl 6 "2 + hv → IrCV 2- (9) IrCV 2' + cl " → IrCl 6 "3 + J;C1 2 (10) IrCl 6 "3 → IrCl 6 "2 + e- (11) Reaction (9) is the photo excitation step; reaction (10) represents the electron transfer from the chloride ion to the excited iridium chloride; and, reaction (11) represents the donation of an electron by IrCl 6 "3 . The overall reaction may thus be generically represented as: aq H * + Cl " + hv + e " cat ^H 2 + JjCl . (12) Reaction (12) thus illustrates the overall photolysis and electrolysis of hydrochloric acid in an aqueous solution seeded with iridium hexachloride. The catalyst is aqueous IrCl 6 "2 /IrCl 6 "3 . Though the photolysis step has been described in terms of the use of a single species of metallic hexahalide, other embodiments thereof are possible. To supplement the individual absorption spectrum and thereby provide a broader band and more continuous absorption of photolytic energy, more than one type of metallic hexahalide may be used simultaneously. Thus, exemplary multi-metallic hexahalide solutions could include RuCl 6 /RhCl 6 /IrCl 6 , or any suitable combination of the Group VIII metals in conjunction with a single halogen species. The metallic hexahalides selected are those with a half-cell potential for oxidation which is lower than that of the halogen gas alone, to ensure that the gas is not evolved at the anode. The apparatus and method of an additional illustrative embodiment will now be described with reference to FIG. 3. In the solar-augmented mode of operation, a concentrated aqueous solution of HCl and IrCl 6 "2 is conveyed from acid and chlorine storage vessel 10 to photolysis cell 40. Solar radiation is introduced into the photolysis cell by means of solar concentrator 30. To ensure that the photolytic reaction proceeds, the chlorine evolved must be swept from the photolytic solution and conducted away from the cell. Exemplary methods of effecting the chlorine sweep are based on partial pressure reduction, and include steam stripping or boiling with an inert gas. The chlorine conducted from the photolysis cell is utilized to produce HCl by means of the electrolyte reformation process. The IrCl 6 "3 produced in the photolysis step is conducted to the anode chamber of electrolysis cell 70. Since the operating temperature of the photolysis cell is preferably above 100°C and that of the electrolysis cell is below 90°C, means are provided for further enhancing the thermal efficiency of the process by recovering heat from the IrCl 6 "3 /HCl stream through a conventional heat exchange apparatus 50. The anode chamber of the electrolysis cell is separated from the cathode chamber by a semipermeable membrane. Means are provided for applying an electrical potential across the anode and cathode cells. Gaseous hydrogen evolved in the cathode cell is conveyed to hydrogen clean-up unit 80 for the removal of impurities, and introduced to hydrogen storage vessel 90. IrCl 6 "2 evolved in the anode cell and the dilute aqueous solution of HCl are conveyed to acid and chlorine storage vessel 10. Oxygen gas produced during the hydrogen halide formation process is withdrawn and delivered to foreign gas clean-up unit 100 for removal of impurities. The apparatus and method of another illustrative embodiment will now be described with reference to FIG. 4, which depicts the electrolyte- conditioning and -storage mode of operation of the present invention. During the solar day, a hydrochloric acid solution seeded with IrCl b "2 at the start of the cycle is photolyzed to establish an inventory of IrCl 6 "3 The IrCl 6 "3 is then stored for subsequent electrolysis during periods of off-peak power. In the electrolyte-conditioning mode of operation, an aqueous solution of HCl and IrCl 6 "2 is conveyed from acid and chlorine storage vessel 10 to photolysis cell 40. Solar radiation is introduced into the photolysis cell by means of solar concentrator 30. Chlorine evolved in the photolysis step is conducted away from the photolysis cell, and is reformed to HCl by means of the electrolyte reformation process. The IrCl 6 "3 produced in the photolysis step is then cooled in heat exchanger 50 and returned to acid and chlorine storage vessel 10. The apparatus and method of another illustrative embodiment will now be described with reference to FIG. 5, which depicts the charging of the radiation-augmented battery mode of operation of the present invention. This embodiment utilizes the pre-conditioned inventory of IrCl 6 "3 generated during the solar day for the electrolytic production of hydrogen during periods of off-peak power. In the radiation-augmented battery mode of operation, an aqueous solution of HCl and IrCl 6 "3 is conveyed from acid and chlorine storage vessel 10 to electrolysis cell 70. Gaseous hydrogen evolved in the cathode cell is conveyed to hydrogen clean-up unit 80 for the removal of impurities, and introduced to hydrogen storage vessel 90. IrCl 6 "2 evolved in the anode cell and the aqueous solution of HCl are conveyed to acid and chlorine storage vessel 10. The apparatus and method of another illustrative embodiment will now be described with reference to FIG. 6, which depicts the potable water production mode of the present invention. This embodiment represents an integrated system for the production of potable water from the hydrogen and oxygen generated during solar-augmented electrolysis. A contaminated water feedstream may be utilized in the process for reformation of the hydrogen chloride. Hydrogen produced during solar- augmented electrolysis, and oxygen produced during the reformation step, are combined in fuel cell 110 to generate electrical power and potable water. The electrical power is conducted to power conditioning unit 120 for subsequent use in electrolysis cell 70. In another embodiment, this invention simultaneously addresses two problems. (1) The United States, and other countries as well, seem to be approaching an era when energy sources in general, and liquid fuels in particular, will be in short supply. (2) The unabated release of greenhouse gases, especially C0 2 , into the atmosphere is attributed to a warming of the climate of the Earth. This invention is a method and apparatus which attacks both of the above problems simultaneously. The essence of the approach is to regard the C0 2 content of smokestack effluent from fossil fuel burning power plants, or from other industrial facilities burning large amounts of coal, oil, natural gas, etc., not as an obvious and necessary potential environmental disaster, but rather as a source of recoverable energy via capture and recycling of the C0 2 content. It is proposed to capture the C0 2 contents from any source such as a power plant, municipal waste treatment or other stack gas trains, fermentation or lime kiln effluent using basic metal oxides such an MgO, CdO, CaO, ZnO or possibly others such as Sc 2 0 3 , BeO, La 2 0 3 , Co 2 0 3 or NiO. These oxides will react with C0 2 to form carbonates such as ZnC0 3 , CdCo 3 , CaC0 3 , MgC0 3 , etc. Hydroxides such as Mg(0H) 2 , Zn(0H) 2 , Cd(0H) 2 , Ca(OH) 2 , etc. can also form, and account must be taken of this possibility. Fortuitously, in several cases the temperature at which H 2 0 is released from the hydroxide is lower than the temperature at which C0 2 is released from the carbonate. For example, in the case of MgO, magnesium hydroxide decomposes (at one atmosphere) at 268°C, whereas, MgC0 3 decomposes at 402°C. (Lange's Handbook, 13th Ed.) Accordingly, by maintaining a bed of MgO at approximately 350 to 375 °C it is possible to selectively remove C0 2 from a flow gas containing both H 2 0 and C0 2 admixed with about 80% N 2 at a total pressure of 1 at , forming MgC0 3 and leaving water vapor in the flowing gas train. Other references give different and somewhat conflicting data on the temperatures of melting and decomposition of Mg(OH) 2 and MgC0 3 , but in all cases it is reported that the vapor of H 2 0 over Mg(OH) 2 reaches a given pressure (for example, 1 atm) at a temperature almost 200 degrees centigrade below that at which the vapor of C0 2 over MgC0 3 reaches that pressure. It is proposed to operate an apparatus as described above for a period of time until nearly the entire bed of metal oxide has been converted to carbonate. Then, for example by opening and closing appropriate dampers, flues or valves, the temperature of the bed can be increased to near 540°C, and all of the C0 2 driven out essentially as one slug. This gas is then admixed with hydrogen, and flowed over an appropriate catalytic substrate to form CH 3 OH. In practical application, it would be desirable to have two metal oxide beds such that one is absorbing C0 2 while the second bed is eluting previously trapped C0 2 . As another embodiment, it is useful to use solar energy as the heat energy source for the steps involving the release of C0 2 from the solid carbonate, and/or for the solar augmented reaction converting C0 2 plus H 2 into CH 3 OH. The process may be operated with or without the solar aspect. Profitable operation of a system as described may depend on the following factors: (1) In principle, a large amount of methanol could be produced - the carbon content of the input fuel could be converted almost stoichiometrically into methanol. Therefore, the entire facility would best be designed as a "co- generation facility", optimized simultaneously the generation of energy and production of methyl alcohol. (2) If the whole procedure is to be feasible, a ready source of non-fossil H 2 is required. This could be obtained, for instance, by electrolysis of water produced using solar or nuclear energy. In particular, it would be advantageous to use hydrogen gas produced by the process disclosed in parent application Ser. No. 07/526,435, now U.S. , and described above at pages 1 to 15. (3) It is entirely possible that in the near future, power plants or other large users of fossil fuel will be charged an "environmental impact" fee depending on the mass of C0 2 released to the atmosphere. Since no C0 2 would be released at the site of the co-generation facility, the net saving on the impact fee would in effect be a credit towards the plant operation. (4) It will be seen that, overall, a given quantity of carbon (say one mole) would be burned twice -once in the form of coal, fuel oil, etc. , at the power plant site, releasing energy and forming the by-product methanol, CH 3 OH. The same mass of carbon would be burned again, typically in a vehicle as an automobile or aircraft, which would presumable release C0 2 to the atmosphere. Overall, however, the net release of C0 2 into the atmosphere would in effect be halved. (5) Since methanol is a clean burning fuel, having no disadvantageous environmental aspects other than the release of C0 2 , it is entirely possible that a facility could be operated with production of methanol as the primary purpose; in that case, electrical energy (or in some circumstances process steam) is regarded as a by¬ product. (6) It is clear that other gases such as S0 2 , H 2 S, and NO. would exist in a power plant stack gas along with the relatively benign water and the desirable C0 2 . It is expected that corresponding useful materials could ultimately be produced as by¬ products, including elemental sulfur, sulfuric acid, nitric acid, etc. Sale of such products would justify the added expense of separating and processing such materials. (7) In many existing facilities, the final temperature of the stack gas prior to release to the atmosphere might be too low to operate the metal oxide, (e.g., MgO, CaO, etc.) absorption beds. A proposed solution is to locate the adsorption bed intermediate between the furnace and the steam boiler. It should be possible to design an apparatus in such a way that the heat is primarily directed to the boiler as desired, while simultaneously producing the metal carbonate. (8) It will be noted that the two stages of the C0 2 entrapment process involve reactions which are the reverse of each other. MgO + C0 2 → MgC0 3 (Absorption of C0 2 ) MgC0 3 → MgO + C0 2 (Release of C0 2 ) The two values of the enthalpy change would be exactly equal in magnitude but opposite in sign at a fixed temperature, and should differ only moderately ' over, say, 200°C temperature differential. (The Gibbs free energy changes sign due to the favorable entropy change of releasing C0 2 gas.) Thus, if heat energy from absorption of C0 2 by the metal oxide M0 2 is retained for use in other parts of the process (desorbing the C0 2 from the second absorber bed, providing process steam, pre-warming the combustion air stream, etc.) the net energy requirement of trapping C0 2 should be small. Conservation of the heat released could be accomplished by use of known technology such as countercurrent heat flow or heat pipes. The implementation of the C0 2 desorption cycle described above uses hot stack gas from the furnace for elution of trapped C0 2 from the exhausted metal oxide bed. This gas is expected to consist mainly of N 2 , C0 2 , and water vapor, since most of the oxygen will have been consumed to support combustion of the fuel. An alternate design of the C0 2 desorption apparatus and operating method is proposed, in which an inert gas such as N 2 is heated by a heat exchanger placed in contact with the hot furnace gases, either before or after the main boiler tubes. The flow of the two gas streams, that is either the hot N 2 or the C0 2 - rich furnace gas, is diverted as desired between the two metal oxide C0 2 - entrapment beds by dampers or valving as in Figures 7 and 7A. In Figure 7 bed A is reacting with carbon dioxide to form magnesium carbonate in bed A by effluent gas coming in as the cooler gas through line 1 which after having carbon dioxide removed passes to vent to line 2. Simultaneously, bed B is being heated by hot gas coming through line 3 to drive off carbon dioxide through line 4. The reverse arrangement is shown in Figure 7A wherein bed B is receiving the cooler gas containing carbon dioxide to line 3 to form the carbonate and the gas is removed to vent through line 4 while simultaneously the hotter gas is introduced to bed A through line 1 and carbon dioxide is driven off through line 2. This is achieved by simply switching the dampers or valves 5 and 6 as shown in the two alternative positions in Figures 7 and 7A. The source of the carbon dioxide fossil fuel can be as shown in Figure 9 wherein a fossil fuel is burned in firebox 100 and the effluent gases pass through main boiler tubes 101 to stack 102 which has conduits 104 and 104a splitting therefrom. Dampers 103, 103a and 103b are used to control the flow of gases. Secondary heat recovery 105 is used in conduit 104 to form cooler gas 106 whereas no heat recovery is used in conduit 104a and warmer gas 107 results. PRODUCTION OF METHANOL Carbon dioxide separated from furnace gas as described above can be hydrogenated over one of several catalysts to produce methanol plus water, using one of several known procedures. The hydrogen and carbon dioxide are delivered separately to the reactor system via valving and flow control apparatus. Since water is a product of the reaction, it is desired to have the feed mixture as water-free as possible, to avoid a le Chatelier shift back towards reactants. The reactor system can be fabricated according to any of several standard designs, including fixed-bed, mixed-bed, or fluidized bed designs. Several catalyst systems are known for efficient conversion of carbon dioxide and hydrogen into methanol plus water, according to the reaction: C0 2 + 3 H ► CH 3 OH + H 2 0 Systems which have been described include ZnO on ZrO, CuO on ZnO, and CuO/ZnO/A10 3 , also generally described as a Cu-Zn-Al catalyst. For use the catalysts are typically exposed to the H 2 and C0 2 mixture at 300-500 degrees C, and moderate pressures of one to several atmospheres. This treatment tends to reduce metal oxides to metals, which are present during actual use of the catalysts. The synthesis reaction itself is appropriately carried on at temperatures in the range of 150°C to 250°-300°C. Higher temperatures are neither appropriate nor required, since the equilibrium in the reaction of CO, and H, to make methanol and water becomes increasingly unfavorable as temperature increases above ambient. Since in the reaction four moles of gas yields two moles, a moderate increase in pressure can be advantageous. Moderate pressures in the range of 10 to 50 atmospheres are adequate for the process. Hydrogen can readily be recovered and recycled; it is advantageous to use an excess of hydrogen compared to C0 2 pressure, greater than the 3:1 value based on reaction stoichiometry. A preferred embodiment and best mode of this part of the overall process consists of 10 weight % of ZnO on ZrO support; temperature 360°C; C0 2 /H 2 ratio 1:3; total pressure of 10 atm; and a gas flow rate of 6.5 millimole per hour per gram of catalyst. This procedure converts the reactants to methanol of more than 99 % purity with an efficiency of approximately 1.3% per pass over the catalyst. Admixture of CuO with the ZnO, and use of A10 3 support in lieu of ZrO have also been described but it is not obvious that better results were obtained. For the primary purpose of the manufacture of methyl alcohol, set forth in this disclosure, catalysts as described above, consisting generally of moderatley active metals such as copper, zinc, and aluminum, are effective. However, it is known that mixtures of C0 2 plus H 2 can be catalytically reacted to give hydrocarbon gases, in preference to methanol, over somewhat more active catalyst such as those including the metals cobalt, palladium, and platinum. Under some commercial circumstances, it is possible that coproduction of hydrogen gases plus processes steam (or other forms of available energy) might have more value than production of methanol. It is accordingly possible to suggest an alternate embodiment in which hydrocarbon gases are produced rather than methanol. The effluent from the reactor bed, consisting of a mixture of water and methanol in the gas phase, with residues of C0 2 and/or H 2 , is cooled in order to condense out the liquid water and methanol as a homogeneous mixture. Residual H 2 and C0 2 is recirculated for use in the process. Methanol (b.p. 65°C) and water (b.p. 100°C) are separated by distillation. An advantage of the overall system as described is the availability of inexpensive or waste heat from the system consisting of the furnace/boilers/flues and heat exchange units. This heat can be advantageously used to provide the reaction temperature for the methanol synthesis and to provide the heat required for the distillation of water-methyl alcohol mixture. In practice, the apparatus shown in the figure for condensation of the methanol-water mixture can be designed so as to constitute both condensation and distillation in one unit, so that water is withdrawn as a liquid at temperature below 100°C, and methanol is obtained as a vapor which is condensed at temperatures below 65°C, and the H 2 -C0 2 excess gas returned to the reactor bed as described previously. A typical apparatus to prepare methanol is shown in Figure 8. The carbon dioxide which may contain inert nitrogen is received from source 110 which may be, for example, the C0 2 recovery lines 2 or 4 in Figures 7 and 7A. Gas flows through line 111 and joins fresh hydrogen make up gas from source 113 through line 112 along with carbon dioxide hydrogen and nitrogen recycle coming from line 115 as shown. These three effluents join in line 114 to flow across catalyst bed 130. This catalyst is a zinc oxide, zirconium oxide catalyst operating at about 360°C. The effluent from catalyst bed 130 exits through line 131 and contains water, methanol, carbon dioxide, hydrogen and nitrogen which then enters separator/condenser 150 which is held at 80°C at the bottom and 50°C at the top, thereby separating out the water through line 151 into container 140 where water is removed through line 141. Gases from separator 150 flow overhead through line 152 and contain carbon dioxide, hydrogen and methanol. Then the methanol is separated out with condenser 160 containing inert packing maintained at about 30°C. The methanol exits through line 161 into container 120 and is removed through methanol removal line 121. The overhead gas goes through line 161 and contains carbon dioxide, hydrogen and nitrogen for recycle which is fed to recirculating pump 130 which has for its outlet line 115. In order to prevent accumulation of excess N 2 in the system, a membrane gas separator (known in the art and commercially available) is installed in line 115, following recirculating pump 130. Nitrogen (along with some C0 2 as a result of imperfect separation) is vented to atmosphere, while nearly all of the H 2 and much of the C0 2 is recycled. (Loss of some C0 2 us tolerated to facilitate operation of the membrane separator. H 2 /N 2 separation is fast and efficient but good C0 2 /N 2 separation is more difficult; loss of some C0 2 is not a problem.) Pump 130 is required to maintain at least a 3:1 pressure drop across the membrane separator in order to drive the separation process. A further embodiment of the invention uses hot hydrogen gas to elute C0 2 from the metal oxide beds shown in Figure 7. This embodiment requires a different version of the furnace/boiler arrangement, as shown in Figure 10. In this case, the flue above the primary boiler tubes 17 includes a heat exchange coil 14 which is used to heat gases for desorbing C0 2 from the trapping beds. Using valve 13, either an inert gas (preferably N 2 ) introduced from pipe 11, or H 2 introduced from pipe 12, is heated with coil 14 and then directed the switching valve 15 of Figure 17. This gas flow (either N 2 or H 2 ) is adjusted to be approximately 200°C hotter than the flue gas from which C0 2 is recovered. Combusion gases flow through stack 16 across coil 14 and secondary heat recovery unit 18 and through pipe 19 for C0 2 recovery. As valves 5 and 6 of Figure 7B are switched to begin eluting C0 2 from MgO bed B, the gas flow line 5 from the apparatus in Figure 10 at first contains inert N 2 gas, which flows over bed B of Figure 7, warming it. During this stage, the output gas from bed B of Fig. 7, carried via line 4 through valve 6, is harmlessly vented to air, since it contains nearly pure nitrogen gas. During this same time, the gases contained in the methanol producing apparatus of Figure 8 continue to recycle under influence of pump 130, with no input through line 110 fro that period. Since the gas mixture on average needs to flow across the catalyst bed about 75 times for complete conversion to methanol, temporary intermittent interruption of input of fresh C0 2 into the apparatus of Figure 8 is acceptable. When the MgO bed B of Figure 7B is almost hot enough to start releasing C0 2 , the gas carried by tube 15 of Figure 10 is switched over to pure H 2 , using valve 3 of Figure 10. Also at that time, the output gas in pipe 4 of Figure 7B is directed input line 110 of Figure 8. In this embodiment, input line 110 of Figure 8 conveys a mixture of C0 2 and H 2 gases; no nitrogen is present. This embodiment has an important advantage, since the membrane separator 130 of Figure 8 is not required, and is eliminated. As a result, pump 130 operates with a lower power requirement, since the pressure differential needed for membrane separation is avoided. For the primary purpose of the manufacture of methyl alcohol (methanol) , set forth in this embodiment, catalysts as described above, consisting generally of moderately active metals such as copper, zinc, and aluminum, are effective. However, it is known that mixtures of C0 2 plus H 2 can be catalytically reacted to give hydrocarbon gases, in preference to methanol, over somewhat more active catalyst such as those including the metals cobalt, palladium, and platinum. Under some commercial circumstances, it is possible that coproduction of hydrogen gases plus processes steam (or other forms of available energy) might have more value than production of methanol. It is accordingly possible to suggest an alternate embodiment in which hydrocarbon gases are produced, rather than methanol. The effluent from the reactor bed, consisting of a mixture of water and methanol in the gas phase, with residues of C0 2 and/or H 2 , is cooled in order to condense out the liquid water and methanol as a homogeneous mixture. Residual H 2 and C0 2 are recirculated for use in the process. Methanol (b.p. 65°C) and water (b.p. 100°C) are separated by distillation. An advantage of the overall system as described is the availability of inexpensive or waste heat from the system consisting of the furnace/boilers/flues and heat exchange units. This heat can be advantageously used to provide the reaction temperature for the methanol synthesis and to provide the heat required for the distillation of the water-methyl alcohol mixture. In practice, the apparatus shown in the figure for condensation of the methanol-water mixture can be designed so as to constitute both condensation and distillation in one unit, so that water is withdrawn as a liquid at temperature below 100°C, and methanol is obtained as a vapor which is condensed at temperatures below 65°C, and the H 2 and C0 2 excess gas returned to the reactor bed as described previously. While the invention has been described in connection with what is presently considered to be the most practical and preferred embodiments, the invention is not limited to the disclosed embodiment but, on the contrary, is intended to cover various modifications and equivalents included within the spirit and scope of the following claims.

Claims: CLAIMS : 1. In a hydrogen/halogen electrolytic cell as an efficient battery for electrical load leveling and load shifting, a method comprising the steps of: storing off-peak electricity through electrolyzing concentrated hydrohalic acid into hydrogen, halogen, and dilute hydrohalic acid; and providing peaking electricity by recombining said hydrogen and halogen, producing concentrated hydrohalic acid for subsequent cycles. 2. A method of producing a hydrogen halide and oxygen, comprising the steps of: photochemically and thermally reacting water with a single halogen gas to produce hydrogen halide and oxygen; and separating said oxygen from said hydrogen halide. 3. A method of electrolyte reformation, comprising the steps of: photochemically and thermally reacting water with a single halogen gas to produce hydrogen halide and oxygen; separating said oxygen from said hydrogen halide; and producing a hydrohalic acid by solvating said hydrogen halide with water. 4. The method of claim 3, wherein concentrated hydrohalic acid is produced by solvating said hydrogen halide with dilute hydrohalic acid. 5. A continuous method of providing load leveling and hydrogen and oxygen production from one system, comprising the steps of: electrolyzing concentrated hydrohalic acid into hydrogen, halogen, and dilute hydrohalic acid; photochemically and thermally reacting water with said halogen to produce hydrogen halide and oxygen; separating said oxygen from said hydrogen halide; and producing concentrated hydrohalic acid by solvating said hydrogen halide with dilute hydrohalic acid, wherein said system utilizes a cell having a charging current density and a discharging current density, said charging and discharging having a period of time. 6. The method of claim 5, further comprising the step of providing electrical power storage concurrently with hydrogen and oxygen production by utilizing a cell charging current density greater than a cell discharge current density, to produce more molecular hydrogen and halogen on charging than that which is consumed on discharging. 7. The method of claim 5, further comprising the step of providing electrical power storage concurrently with hydrogen and oxygen production by charging for a longer period of time than a time of discharge. 8. A method of photolysis, comprising the steps of: using photolytic energy to excite a transition metal halide complex in solution with a hydrohalic acid, causing a metal ion-ligand to be photochemically reduced to a lower oxidation state, and halide ions to be oxidized to molecular halogen; and continuously removing said molecular halogen from the presence of the photolytic reaction. 9. The method of claim 8, further comprising the use of two or more transition metal halide complexes in solution with said hydrohalic acid simultaneously. 10. The method of claim 8 or claim 9, further comprising the use of electrical energy to electrolyze said photochemically reduced, transition metal halide complexes in solution with a hydrohalic acid, causing said metal ion-ligand to be electrolytically oxidized to a higher oxidation state of that species, and hydrogen ions to be reduced to molecular hydrogen. 11. A method of producing molecular hydrogen and halogens from hydrohalic acid in solution with transition metal halide complexes comprising: using photolytic energy to excite a transition metal halide complex in solution with a hydrohalic acid, causing a metal ion-ligand to be photochemically reduced to a lower oxidation state, and halide ions to be oxidized to molecular halogen; continuously removing said molecular halogen from the presence of the photolytic reaction; and using electrical energy to electrolyze said photochemically reduced, transition metal halide complexes in solution with said hydrohalic acid, causing said metal ion-ligand to be electrolytically oxidized to a higher oxidation state of that species, and hydrogen ions to be reduced to molecular hydrogen. 12. A continuous method of providing load leveling and hydrogen and oxygen production from one system, comprising the steps of: using photolytic energy to excite a transition metal halide complex in solution with a hydrohalic acid, causing a metal ion-ligand to be photochemically reduced to a lower oxidation state, and halide ions to be oxidized to molecular halogen; continuously removing said molecular halogen from the presence of the photolytic reaction; using electrical energy to electrolyze said photochemically reduced, transition metal halide complexes in solution with said hydrohalic acid, causing said metal ion-ligand to be electrolytically oxidized to a higher oxidation state of that species, and hydrogen ions to be reduced to molecular hydrogen; photochemically and thermally reacting water with said molecular halogen to produce hydrogen halide and oxygen; separating said oxygen from said hydrogen halide; and producing concentrated hydrohalic acid by solvating said hydrogen halide with dilute hydrohalic acid. 13. The method of claim 12, further comprising the step of providing electrical power storage concurrently with hydrogen and oxygen production by utilizing a cell charging current density greater than a cell discharge current density, to produce more molecular hydrogen and halogen on charging than that which is consumed on discharging. 14. The method of claim 12, further comprising the step of providing electrical power storage concurrently with hydrogen and oxygen production by charging for a longer period of time than a time of discharge. 15. The method of claim 8, 9, 11, or 12, wherein said photolysis occurs during the solar day, with said photochemically reduced metal ion-ligand stored for subsequent electrolysis. 16. The method of claim 10, 11, 12, or 13, wherein said electrolysis occurs during the night with off-peak electrical energy. 17. The method of claim 12, 13, or 14, further comprising the production of potable water and electrical power from a contaminated water feedstream by combining said hydrogen and said oxygen in a fuel cell. 18. The method of claim 8, 9, 11, or 12, further comprising the addition of an excess of halide ions to said hydrohalic acid. 19. The method of claim 5, 11, or 12 further comprising the recovery of excess thermal energy. 20. A hydrogen/halogen electrolytic cell as an efficient battery for electrical load leveling and load shifting comprising: means for storing off-peak electricity through electrolyzing concentrated hydrohalic acid into hydrogen, halogen, and dilute hydrohalic acid; and means for providing peaking electricity by recombining said hydrogen and halogen producing concentrated hydrohalic acid for subsequent cycles 21. A hydrogen halide and oxygen production system comprising: means for photochemically and thermally reacting water with a single halogen gas to produce hydrogen halide and oxygen; and means for separating said oxygen from said hydrogen halide. 22. An electrolyte reformation system comprising: means for photochemically and thermally reacting water with a single halogen gas to produce hydrogen halide and oxygen; means for separating said oxygen from said hydrogen halide; and means for producing a hydrohalic acid by solvating said hydrogen halide with water. 23. A continuous load leveling and hydrogen and oxygen production system comprising: means for electrolyzing concentrated hydrohalic acid into hydrogen, halogen, and dilute hydrohalic acid; means for photochemically and thermally reacting water with said halogen to produce hydrogen halide and oxygen; means for separating said oxygen from said hydrogen halide; means for producing concentrated hydrohalic acid by solvating said hydrogen halide with dilute hydrohalic acid; and means for providing electrical power storage concurrently with hydrogen and oxygen production by utilizing a cell charging current density greater than a cell discharge current density, to produce more molecular hydrogen and halogen on charging than that which is consumed on discharging. 24. The system of claim 23, further comprising means for providing electrical power storage concurrently with hydrogen and oxygen production by utilizing a cell charging current density greater than a cell discharge current density, to produce more molecular hydrogen and halogen on charging than that which is consumed on discharging. 25. The system of claim 24, further comprising means for providing electrical power storage concurrently with hydrogen and oxygen production by charging for a longer period of time than a time of discharge. 26. A photolysis system comprising: means for using photolytic energy to excite a transition metal halide complex in solution with a hydrohalic acid, causing a metal ion-ligand to be photochemically reduced to a lower oxidation state, and halide ions to be oxidized to molecular halogen; and means for continuously removing said molecular halogen from the presence of the photolytic reaction. 27. The system of claim 26, further comprising means for the use of electrical energy to electrolyze said photochemically reduced, transition metal halide complexes in solution with a hydrohalic acid, causing said metal ion-ligand to be electrolytically oxidized to a higher oxidation state of that species, and hydrogen ions to be reduced to molecular hydrogen. 28. A system for producing molecular hydrogen and halogens from hydrohalic acid in solution with transition metal halide complexes comprising: means for using photolytic energy to excite a transition metal halide complex in solution with a hydrohalic acid, causing a metal ion-ligand to be photochemically reduced to a lower oxidation state, and halide ions to be oxidized to molecular halogen; means for continuously removing said molecular halogen from the presence of the photolytic reaction; and means for using electrical energy to electrolyze said photochemically reduced, transition metal halide complexes in solution with said hydrohalic acid, causing said metal ion-ligand to be electrolytically oxidized to a higher oxidation state of that species, and hydrogen ions to be reduced to molecular hydrogen. 29. A continuous load leveling and hydrogen and oxygen production system comprising: means for using photolytic energy to excite a transition metal halide complex in solution with a hydrohalic acid, causing a metal ion-ligand to be photochemically reduced to a lower oxidation state, and halide ions to be oxidized to molecular halogen; means for continuously removing said molecular halogen from the presence of the photolytic reaction; means for using electrical energy to electrolyze said photochemically reduced, transition metal halide complexes in solution with said hydrohalic acid, causing said metal ion-ligand to be electrolytically oxidized to a higher oxidation state of that species, and hydrogen ions to be reduced to molecular hydrogen; means for photochemically and thermally reacting water with said molecular halogen to produce hydrogen halide and oxygen; means for separating said oxygen from said hydrogen halide; and means for producing concentrated hydrohalic acid by solvating said hydrogen halide with dilute hydrohalic acid, wherein said system utilizes a cell having a current discharge density and a current charging density and said charging an discharging having a period of time. 30. The system of claim 29, further comprising means for providing electrical power storage concurrently with hydrogen and oxygen production by utilizing a cell charging current density greater than a cell discharge current density, to produce more molecular hydrogen and halogen on charging than that which is consumed on discharging. 31. The system of claim 30, further comprising means for providing electrical power storage concurrently with hydrogen and oxygen production by charging for a longer period of time than a time of discharge. 32. The system of claim 29, 30, or 31, further comprising means for the production of potable water and electrical power from a contaminated water feedstream by combining said hydrogen and said oxygen in a fuel cell. 33. A molecular halogen production system comprising: means for electrolyzing concentrated hydrohalic acid into hydrogen, halogen, and dilute hydrohalic acid; means for photochemically and thermally reacting water with said halogen to produce hydrogen halide and oxygen; means for separating said oxygen from said hydrogen halide; and means for producing a concentrated hydrohalic acid by solvating said hydrogen halide with dilute hydrohalic acid. 34. The system of claim 25, 30, or 31, further comprising means for the recovery of excess thermal energy. 35. A method for the joint i) abatement of emission of a "greenhouse" gas by removing carbon dioxide from an effluent and ii) manufacture of methanol by reaction of hydrogen with carbon dioxide comprising: a) reacting carbon dioxide in the effluent by flowing contact of the effluent with a bed of basic metal oxide at a temperature suitable to form a metal carbonate, b) then stopping said effluent flow after said bed is substantially converted to said carbonate c) and heating said carbonate to a temperature suitable to release carbon dioxide, d) then mixing said released carbon dioxide with said hydrogen e) while passing said mixture over a catalyst of another metal oxide at a suitable temperature and pressure for a reaction, and f) forming methanol. 36. The method of claim 35 wherein the temperature of step a) is from about 330°C to about 380°C. 37. The method of claim 35 wherein the pressure of step a) is atmospheric. 38. The method of claim 35 wherein the temperature of step c) is from about 475°C to about 550°C. 39. The method of claim 35 wherein the pressure of step c) is atmospheric. 40. The method of claim 35 wherein the temperature of step e) is from about 140°c to about 310°C. 41. The method of claim 35 wherein the pressure of step e) is from about 5 to about 55 atmospheres. 42. The method of claim 35 wherein said effluent is from burning of fossil fuel. 43. The method of claim 35 wherein said effluent is from a fermentation process. 44. The method of claim 35 wherein said effluent is from a lime kiln. 45. The method of claim 35 where the source of hydrogen in step d) is from a radiation augmented electrolytic production process. 46. The method of claim 35 wherein there is a plurality of beds of metal oxide in step a) and at least one of said beds is used to react with carbon dioxide as in step a) to form carbonate while the other said bed is being heated as in step c) to release carbon dioxide. 47. The method of claim 35 wherein the temperature of step a) is from about 350°C to about 375°C, the pressure of step a) is atmospheric, the temperature of step c) is from about 500°C to about 540°C, the pressure of step c) is atmospheric, the temperature of step e) is from about 150°C to about 300°C, and the pressure of step e) is from about 20 to about 50 atmospheres. 48. The method of claim 35 wherein the metal oxide in step a) is selected from the group consisting of magnesium oxide, zinc oxide, cadmium oxide, and mixtures thereof. 49. The method of claim 35 wherein the metal oxide of step c) is a catalyst selected from the group consisting of ZnO on Zr0 2 , CuO on ZnO, CuO/ZnO/Al 2 0 3 and mixtures thereof. 50. The method of claim 35 wherein the process of step e) is adjusted to also produce hydrocarbons. 51. Apparatus for the joint i) abatement of emission of a "greenhouse" gas, carbon dioxide from burning fossil fuel and ii) manufacture of methanol by reaction of hydrogen with carbon dioxide comprising a) means for reacting carbon dioxide in the effluent of the burning of a fossil fuel in flowing contact of the effluent with a bed of basic metal oxide, b) means for stopping said effluent flow after the bed is substantially converted to the metal carbonate, c) means for heating the carbonate to a temperature suitable to release carbon dioxide, d) means for mixing the released carbon dioxide with hydrogen, e) means for passing the mixture of hydrogen and carbon dioxide over a catalyst of another metal oxide, and f) means for collecting the methanol formed. 52. The apparatus of claim 51 wherein the means for reacting in means a) is a bed of the metal oxide mounted in the effluent conduit from burning of a fossil fuel. 53. The apparatus of claim 52 wherein the means for stopping said effluent in means b) is a damper in said conduit. 54. The apparatus of claim 52 wherein there are a plurality of said beds mounted in a plurality of said conduits. 55. The apparatus of claim 54 wherein said beds are alternately i) used to react carbon dioxide with said metal oxide then ii) heated to release carbon dioxide by means of alternately opening and closing a damper system in said conduits. 56. The apparatus of claim 51 wherein said means of heating c) is a system to pass heated inert gas across said carbonate. 57. The apparatus of claim 51 wherein said means of passing the mixture over a catalyst is a reactor system. 58. The apparatus of claim 57 wherein said reactor system is a fixed bed. 59. The apparatus of claim 57 wherein said reactor system is a mixed bed. 60. The apparatus of claim 57 wherein said reactor system is a fluidized bed. 61. A continuous method of providing load leveling and hydrogen and oxygen production from one system comprising: storing electrical energy by electrolyzing concentrated hydrochloric acid to produce dilute hydrochloric acid and hydrogen and chlorine, producing electrical energy by electrochemically reacting the hydrogen and chlorine and reforming concentrated hydrochloric acid, photochemically and thermally enacting a water feedstream with available chlorine to produce hydrogen chloride and oxygen, separating said oxygen as product from said hydrogen chloride, producing supplemental concentrated hydrochloric acid by solvating said hydrogen chloride with a solvent selected from the group consisting of water and available dilute hydrochloric acid, electrolyzing the supplemental concentrated hydrochloric acid to produce hydrogen as product and recycle chlorine and dilute hydrochloric acid, wherein said system utilizes hydrochloric acid electricity produced by a municipal solid waste-to-energy facility.

Inventors: HANRAHAN ROBERT J, PARKER ROBIN Z, HANRAHAN, ROBERT, J., PARKER, ROBIN, Z.
Applicants: SOLAR REACTOR TECH, SOLAR REACTOR TECHNOLOGIES, INC.
Application year: 1992
Main classification: C01B7
IPC codes: C01B3, C01B7, C01B13, C02F1, C07C29, C07C31, C25B1, H01M8