A hybrid dehydrogenation reaction system includes: an acid aqueous solution tank having an acid aqueous solution; an exothermic dehydrogenation reactor including a chemical hydride of a solid state and receiving the acid aqueous solution from the acid aqueous solution tank for an exothermic dehydrogenation reaction of the chemical hydride and the acid aqueous solution to generate hydrogen; an LOHC tank including a liquid organic hydrogen carrier (LOHC); and an endothermic dehydrogenation reactor receiving the liquid organic hydrogen carrier from the LOHC tank and generating hydrogen through an endothermic dehydrogenation reaction of the liquid organic hydrogen carrier by using heat generated from the exothermic dehydrogenation reactor.

The present invention discloses a catalytic process for the manufacture of hydrogen and hydrocarbons simultaneously in the same reactor from renewable source, i.e. lipids, glycerides and fatty acids from plant, animal or algae oil, where in the multiple unstaurations in the renewable feedstock and the catalytic intermediates produced in the process from renewable feedstock is converted catalytically using simultaneous combination of in-situ occurring reactions. These in-situ occurring reactions are simultaneous combination of hydroconversion, reforming and water gas shift reactions wherein the reaction is performed in the presence of one or more metal sulfides form of metals of Group VI and/or Group IX and/or Group X elements, specifically comprises of one or more active metal combinations such as Co, W, Mo, Ni, P, with Pt, Pd encapsulated inside sodalite cages for prevention against poisoning from sulfur based compounds. The hydroconversion comprises of reactions in presence of hydrogen such as hydrocracking, dehydrogenation, dehydrocyclization, hydrodeoxygenation, hydrodesulfurization, hydrodenitrogenation, decarboxylation, decarbonylation, cyclization and aromatization reactions. The catalyst along with the active metals also includes porous silica-alumina, zeolite, silica, alumina, silicoaluminophosphates or a combination of two or more thereof used as support for the above said process. These catalysts are loaded in a graded beds (two or more beds of different catalyst mixtures) or simultaneously (mixture of different catalyst systems) and reacted specifically at lower temperatures than the steam reforming conditions i.e. at pressure from 10 to 150 atmosphere, average temperature of the catalytic bed from 250° C. to 500° C., space-velocity of from 0.5 h.sup.−1 to 8 h.sup.−1, and hydrogen to feed ratio of from 300 NL of hydrogen/L of feed to 3500 NL hydrogen/L of feed., Initially hydrogen gas is supplied for conversion of the renewable feed stocks, as the reaction process the hydrogen consumed during the conversion of plant, animal or algae oil into hydrocarbons is balanced from the in-situ reactions such as reforming, dehydrogenation, water gas shift etc occurring during the same process. This production of hydrogen makes the entire process refinery independent and more economical and sustainable. Along with hydrogen the renewable feed stock is also converted into hydrocarbons ranging between C1-C24 carbon number, comprising of n-paraffins, isoparaffins, cyclo paraffins, naphthenes, and aromatics and polynuclear aromatics.

The present invention discloses a catalytic process for the manufacture of hydrogen and hydrocarbons simultaneously in the same reactor from renewable source, i.e. lipids, glycerides and fatty acids from plant, animal or algae oil, where in the multiple unstaurations in the renewable feedstock and the catalytic intermediates produced in the process from renewable feedstock is converted catalytically using simultaneous combination of in-situ occurring reactions. These in-situ occurring reactions are simultaneous combination of hydroconversion, reforming and water gas shift reactions wherein the reaction is performed in the presence of one or more metal sulfides form of metals of Group VI and/or Group IX and/or Group X elements, specifically comprises of one or more active metal combinations such as Co, W, Mo, Ni, P, with Pt, Pd encapsulated inside sodalite cages for prevention against poisoning from sulfur based compounds. The hydroconversion comprises of reactions in presence of hydrogen such as hydrocracking, dehydrogenation, dehydrocyclization, hydrodeoxygenation, hydrodesulfurization, hydrodenitrogenation, decarboxylation, decarbonylation, cyclization and aromatization reactions. The catalyst along with the active metals also includes porous silica-alumina, zeolite, silica, alumina, silicoaluminophosphates or a combination of two or more thereof used as support for the above said process. These catalysts are loaded in a graded beds (two or more beds of different catalyst mixtures) or simultaneously (mixture of different catalyst systems) and reacted specifically at lower temperatures than the steam reforming conditions i.e. at pressure from 10 to 150 atmosphere, average temperature of the catalytic bed from 250° C. to 500° C., space-velocity of from 0.5 h.sup.−1 to 8 h.sup.−1, and hydrogen to feed ratio of from 300 NL of hydrogen/L of feed to 3500 NL hydrogen/L of feed., Initially hydrogen gas is supplied for conversion of the renewable feed stocks, as the reaction process the hydrogen consumed during the conversion of plant, animal or algae oil into hydrocarbons is balanced from the in-situ reactions such as reforming, dehydrogenation, water gas shift etc occurring during the same process. This production of hydrogen makes the entire process refinery independent and more economical and sustainable. Along with hydrogen the renewable feed stock is also converted into hydrocarbons ranging between C1-C24 carbon number, comprising of n-paraffins, isoparaffins, cyclo paraffins, naphthenes, and aromatics and polynuclear aromatics.

The present invention relates to a hydrogen gas production method, which includes: a first step of concentrating an aqueous solution containing an alkali metal formate; a second step of protonating at least a part of the alkali metal formate by electrodialysis to produce a formic acid; and a third step of decomposing the formic acid to produce a hydrogen gas.

The present invention relates to a hydrogen gas production method, which includes: a first step of concentrating an aqueous solution containing an alkali metal formate; a second step of protonating at least a part of the alkali metal formate by electrodialysis to produce a formic acid; and a third step of decomposing the formic acid to produce a hydrogen gas.

A hydrogen storage device 200 comprises: a first vessel 230, having a first fluid inlet 210 and/or a first fluid outlet 220, having therein a thermally conducting network 240 thermally coupled to a first heater (not shown); wherein the first vessel 230 is arranged to receive therein a hydrogen storage material in thermal contact, at least in part, with the thermally conducting network 240; wherein the thermally conducting network 240 has a lattice geometry, a gyroidal geometry and/or a fractal geometry in two and/or three dimensions, comprising a plurality of nodes, having thermally conducting arms therebetween, with voids between the arms; and wherein the hydrogen storage material comprises and/or is a liquid organic hydrogen carrier, LOHC.

The system includes a reactor vessel having a reactor space bound by a reactor wall. The reactor vessel is arranged for holding a mixture of a catalyst and formic acid in the reactor space. The reactor vessel includes a mixture inflow opening for allowing the mixture to enter the reactor space and a mixture outflow opening for allowing said mixture to exit the reactor space, and a gas outflow opening for allowing hydrogen originating from the mixture to exit the reactor space. A method for hydrogen production includes: providing the formic acid and the catalyst into the reactor space; withdrawing the mixture from the reactor space; heating and/or cooling the mixture to a predetermined temperature range outside the reactor space; and introducing the heated and/or cooled mixture into the reactor space in a predetermined direction having a tangential component arranged for stirring said mixture in the reactor space.

The system includes a reactor vessel having a reactor space bound by a reactor wall. The reactor vessel is arranged for holding a mixture of a catalyst and formic acid in the reactor space. The reactor vessel includes a mixture inflow opening for allowing the mixture to enter the reactor space and a mixture outflow opening for allowing said mixture to exit the reactor space, and a gas outflow opening for allowing hydrogen originating from the mixture to exit the reactor space. A method for hydrogen production includes: providing the formic acid and the catalyst into the reactor space; withdrawing the mixture from the reactor space; heating and/or cooling the mixture to a predetermined temperature range outside the reactor space; and introducing the heated and/or cooled mixture into the reactor space in a predetermined direction having a tangential component arranged for stirring said mixture in the reactor space.

A catalyst composition for manufacturing a catalyst for hydrogen production based on thermochemical reaction of methanol is disclosed. The catalyst composition includes a support component and an active component. The support component includes cement and clay, wherein a weight ratio of the cement to the clay is 3/7 to 9/1. The active component includes copper oxide or a precursor of copper oxide. Based on 100 parts by weight of the support component, a content of the active component is 5 to 10 parts by weight.

A reactor system and a process for carrying out the methanol cracking reaction of a feedstock comprising methanol to hydrogen are provided, where the heat for the endothermic methanol cracking reaction is provided by resistance heating.