The present invention is related to a method of coupling methane dry-reforming and composite catalyst regeneration. A composite catalyst is filled into a reactor, and methane or a methane mixture gas is introduced therein. CaCO.sub.3 in the composite catalyst is decomposed under 600-850 C. CO.sub.2 obtained by the decomposition reacts with methane to perform methane dry-reforming reaction and produce synthesis gas containing CO and hydrogen. The composite catalyst contains CaCO.sub.3 , active nickel and alumina support. This method couples the CaCO.sub.3 decomposition reaction in calcium looping and methane dry-reforming reaction to solve the technical problem of limiting CaCO.sub.3 decomposition by high-temperature equilibrium. The decomposition of CaCO.sub.3 is enhanced, and the CO.sub.2 produced by decomposing CaCO.sub.3 is dry-reformed to produce synthesis gas to be utilized.

A reactor system comprising a first reactor assembly, a first pressure transition assembly, a second reactor assembly and a second pressure transition assembly.

Process to conduct a steam cracking reaction in a fluidized bed reactor The disclosure relates to a process to perform a steam cracking reaction, said process comprising the steps of providing a fluidized bed reactor comprising at least two electrodes; and a bed comprising particles, wherein the particles are put in a fluidized state by passing upwardly through the said bed a fluid stream, to obtain a fluidized bed; heating the fluidized bed to a temperature ranging from 500? C. to 1200? C. to conduct the endothermic chemical reaction; wherein at least 10 wt. % of the particles based on the total weight of the particles of the bed are electrically conductive particles and have a resistivity ranging from 0.001 Ohm.Math.cm to 500 Ohm.Math.cm at 800? C. and in that the step of heating the fluidized bed is performed by passing an electric current through the fluidized bed.

In one embodiment described herein, fuel may be converted into syngas by a method comprising feeding the fuel and composite metal oxides into a reduction reactor in a co-current flow pattern relative to one another, reducing the composite metal oxides with the fuel to form syngas and reduced composite metal oxides, transporting the reduced composite metal oxides to an oxidation reactor, regenerating the composite metal oxides by oxidizing the reduced composite metal oxides with an oxidizing reactant in the oxidation reactor, and recycling the regenerated composite metal oxides to the reduction reactor for subsequent reduction reactions to produce syngas. The composite metal oxides may be solid particles comprising a primary metal oxide and a secondary metal oxide.

Method and device for biogas upgrading and hydrogen production from anaerobic fermentation of biological material under production of energy rich gases selected among methane and hydrogen or a combination thereof. The method comprises addition of hydrogen gas to a fermentation step to enhance the methane: CO.sub.2 ratio in the raw biogas produced. At least part of the raw biogas is subjected to a step of sorption enhanced reforming without prior separation of CO.sub.2, using CaO as an absorbent to capture CO.sub.2 from the raw biogas as well as CO.sub.2 released in the reforming reaction. CaO is regenerated in an endothermic reaction using heat at least partially provided, directly or indirectly, by the bio-gas to be upgraded, thereby producing substantially pure hydrogen and substantially pure CO.sub.2.

The process for obtaining M.sup.1BH.sub.4, the process comprising contacting M.sup.1-B0.sub.2 with a metal M.sup.2 in the presence of molecular hydrogen (H.sub.2) under conditions permitting the formation of M.sup.1-BH.sub.4 and M.sup.2-oxide, wherein the M.sup.1 is a metal selected from column I of the periodic table of elements or alloys of metals selected from column I of the periodic table of elements and M.sup.2 is a metal or an alloy of metals selected from column II of the periodic table of elements, provided that M.sup.2 is not Mg and M.sup.1 is different from M.sup.2.

Novel redox based systems for fuel and chemical production with in-situ CO.sub.2 capture are provided. A redox system using one or more chemical intermediates is utilized in conjunction with liquid fuel generation via indirect Fischer-Tropsch synthesis, direct hydrogenation, or pyrolysis. The redox system is used to generate a hydrogen rich stream and/or CO.sub.2 and/or heat for liquid fuel and chemical production. A portion of the byproduct fuels and/or steam from liquid fuel and chemical synthesis is used as part of the feedstock for the redox system.

A method of producing hydrogen gas is provided. The method can include the steps of providing a reaction vessel containing aluminum, delivering a stream of natural gas to the reaction vessel, in which the natural gas includes methane, and heating the reaction vessel at a temperature in a range of 300 to 800? C., in which the heating causes a chemical reaction between the methane and the aluminum to provide hydrogen gas and aluminum carbide. The method can include delivering steam to the reaction vessel and heating the reaction vessel at a temperature in a range of 300 to 800? C., in which the heating causes a chemical reaction between the methane, steam, and the aluminum to provide hydrogen gas, aluminum carbide, and aluminum oxycarbide.

A reactor configuration is proposed for selectively converting gaseous, liquid or solid fuels to a syngas specification which is flexible in terms of H.sub.2/CO ratio. This reactor and system configuration can be used with a specific oxygen carrier to hydro-carbon fuel molar ratio, a specific range of operating temperatures and pressures, and a co-current downward moving bed system. The concept of a CO.sub.2 stream injected in-conjunction with the specified operating parameters for a moving bed reducer is claimed, wherein the injection location in the reactor system is flexible for both steam and CO.sub.2 such that, carbon efficiency of the system is maximized.

Novel redox based systems for fuel and chemical production with in-situ CO.sub.2 capture are provided. A redox system using one or more chemical intermediates is utilized in conjunction with liquid fuel generation via indirect Fischer-Tropsch synthesis, direct hydro genation, or pyrolysis. The redox system is used to generate a hydrogen rich stream and/or CO.sub.2 and/or heat for liquid fuel and chemical production. A portion of the byproduct fuels and/or steam from liquid fuel and chemical synthesis is used as part of the feedstock for the redox system.