In a method for producing hydrogen and carboxylic acid, a primary alcohol of 1 to 7 carbon atoms and water are reacted by being continuously introduced into a flow reactor packed with a solid catalyst consisting of an alloy of ruthenium and tin on a support and passed through the reactor under temperature and pressure conditions at which the water assumes a gaseous state. This method enables hydrogen and carboxylic acid to be produced in a high yield or at a high purity from a primary alcohol and water in a short time and by simple operations.

Electrochemical cells for the production of hydrogen from liquid fuels and methods of operating the cells to produce hydrogen and electricity are provided. The electrochemical cells are solid state cells that incorporate a thermochemical conversion catalyst and a hydrogen oxidation catalyst into the anode and utilize solid acid electrolytes. This cell design integrates thermally driven chemical conversion of a starting fuel with electrochemical removal of hydrogen from the conversion reaction zone.

A dehydrogenation method is provided that includes subjecting a first hydrogen storage body including compound including two or more N-heterocycloalkyl groups, and second hydrogen storage body including a compound including a substituted or unsubstituted cycloalkyl group and an N-heterocycloalkyl group, to a dehydrogenation reaction in the presence of a catalyst to produce hydrogen.

H2 production, sulfuric acid and SO2 production process refers to an innovative process VIA the phenomena of the Sulfur-Iodine (S-I) thermochemical cycle. The process consist of the acid gas burner to burn all the acid gases with air, enriched air or oxygen and without using any fuel gas to produce SO2. The acid gases are normally processed in the prior arts of the sulfur recovery units. Iodine is used to produce the hydrogen.

A portion or all of the acid gases are sent to the acid gas burner in accordance with the present invention.

The present innovation not only produces hydrogen but also reduces the SO2 and CO2 emissions.

The produced SO2 is sent to other units to produce other fertilizer products and the produced CO2 is sent to CO2 removal or CO2 Liquefaction process.

The hydrogen is produced is used to supply the needs within the facility like hydrotreaters to reduce external import and to reduce the operating costs.

Provided is a catalyst structure for a liquid organic hydrogen carrier (LOHC) dehydrogenation reactor, including a support, a plurality of channels formed on the support in such a manner that the LOHC may flow therethrough, and an LOHC dehydrogenation catalyst that is coated on the inner surfaces of the channels and is in contact with the LOHC to carry out LOHC dehydrogenation, wherein the hydrogen gas generated from the dehydrogenation is discharged along the channels so that the contact area between the LOHC and the LOHC dehydrogenation catalyst may be increased.

It is provided solid, heterogeneous catalysts and a method for producing H.sub.2 by steam reforming. More particularly, the catalyst comprises at least one metal element of Cu, Ni, Fe, Co, Mo, Mn, Mg, Zr, La, Ce, Ti, Zn and W, having a formula Cu.sub.aNi.sub.bFe.sub.c-Co.sub.dMO.sub.eMn.sub.fMg.sub.gZr.sub.hLa.sub.iCe.sub.jTi.sub.kZn.sub.lW.sub.mO.sub.x, wherein a, b, c, d, e, f, g, h, i, j, k, I and m are molar ratios for the respective elements, wherein a, b, c, d, e, f, g and m are >0, h, I, j, k and I are >0 or a, b, c, d, e, f, g, i, and j are ≥0, h, k, I and m are >0 and x is such that the catalyst is electrically neutral. The produced H.sub.2 can be used to powered vehicle as described herein.

A catalytic method for producing gaseous products from a fuel and a gaseous reagent having the steps of: providing a catalyst and the fuel to a reactor vessel such that the catalyst and the fuel are in fluid communication with each other within the reactor vessel, where the catalyst is a mixture of reduced metal oxides; and contacting the fuel and catalyst with the gaseous reagent within the reactor vessel at a reaction temperature to produce gaseous products, where the gaseous reagent contains at least CO.sub.2 or H.sub.2O, where the fuel comprises a carbonaceous source, and wherein the gaseous products are CO or syngas.

A bimetallic catalyst composition containing a mesh substrate having supported thereon an alumina washcoat on which are impregnated bimetallic particles of rhodium and ruthenium in specified amounts. A process for the catalytic partial oxidation of a hydrocarbon, such as methane or natural gas, involving contacting the hydrocarbon with an oxidant in the presence of the aforementioned bimetallic catalyst under reaction conditions sufficient to produce synthesis gas, that is, to a mixture of hydrogen and carbon monoxide.

A nanocomposite catalyst includes a support, a multiplicity of nanoscale metal oxide clusters coupled to the support, and one or more metal atoms coupled to each of the nanoscale metal oxide clusters. Fabricating a nanocomposite catalyst includes forming nanoscale metal oxide clusters including a first metal on a support, and depositing one or more metal atoms including a second metal on the nanoscale metal oxide clusters. The nanocomposite catalyst is suitable for catalyzing reactions such as CO oxidation, water-gas-shift, reforming of CO.sub.2 and methanol, and oxidation of natural gas.

A metal/α-MoC.sub.1-x load-type single-atomic dispersion catalyst, a synthesis method therefor, and applications thereof. The catalyst uses α-MoC.sub.1-x as carrier, and has metal that has the mass fraction ranging from 1-100% and that is dispersed on carrier α-MoC.sub.1-x in the single atom form. The catalyst provided in the present application can be adapted to a wide alcohol/water proportion in hydrogen production based on aqueous-phase reforming of alcohols, outstanding hydrogen production performance can be obtained at a variety of proportions, and catalysis performance of the catalyst is much higher than that of metal loaded with an oxide carrier. Especially when the metal is Pt, catalysis performance of the catalyst provided in the present application in the hydrogen production based on aqueous-phase reforming of alcohols is much higher than that of a Pt/α-MoC.sub.1-x load-type catalyst on the α-MoC.sub.1-x carrier on which Pt is disposed on a layer form in the prior art. The hydrogen production performance of the catalyst provided in the present application can be higher than 20,000 h.sup.−1 at the temperature of 190° C.