A dehydrogenation reaction system for a liquid hydrogen source material includes a storage device used for storing a liquid hydrogen source material and a liquid hydrogen storage carrier, a reaction still for dehydrogenation of the liquid hydrogen source material, a gas-liquid separator for separating the products, hydrogen and liquid hydrogen storage carrier which are generated after dehydrogenation of the liquid hydrogen source material, a buffer tank used for storing hydrogen, and a heating device used for heating the reaction still. The liquid hydrogen source material is input into the reaction still by means of a pump through an input pipe, dehydrogenation reaction of the liquid hydrogen source material is conducted in the reaction still, generated hydrogen is conveyed to the buffer tank, and the liquid hydrogen storage carrier generated after dehydrogenation is conveyed back to the storage device.

Chemical looping reform methods comprising heating an oxygen carrier in the presence of a catalyst and plasma radicals to react the oxygen carrier with a fuel to provide a reduced oxygen carrier; and contacting the reduced oxygen carrier with water or carbon dioxide to produce hydrogen or carbon monoxide, respectively, and regenerate the oxygen carrier. The chemical looping reform methods are carried out at low temperatures such as from 150 C. to 1000 C., preferably from 150 C. to 500 C. Catalyst used in the chemical looping reform methods include a sintered rare earth metal oxide oxygen carrier and perovskite. Methods of preparing the catalyst are also provided.

A process is described for the production of formaldehyde, comprising (a) subjecting methanol to oxidation with air in a formaldehyde production unit thereby producing a formaldehyde-containing stream; (b) separating said formaldehyde-containing stream into a formaldehyde product stream and a formaldehyde vent gas stream; wherein the vent gas stream, optionally after treatment in a vent gas treatment unit, is passed to one or more stages of: (i) synthesis gas generation, (ii) carbon dioxide removal, (iii) methanol synthesis or (iv) urea synthesis.

The present invention relates to the use of a formulation which is liquid at ambient temperature comprising at least a mixture of benzene, toluene and xylene for the fixing and the release of hydrogen in at least one hydrogenation/dehydrogenation cycle of said formulation.

The invention also relates to the use of said formulation for the transportation and the handling of hydrogen resulting from the steam cracking of petroleum products, of inevitable hydrogen resulting from chemical reactions, such as the electrolysis of salt, or of hydrogen resulting from the electrolysis of water.

A process for hydrogen production, the process comprising the steps of mixing hot water and hot oil to produce a mixed stream; increasing a temperature of the mixed stream to produce a reactor feed; upgrading the reactor feed in the non-catalytic reactor to produce a non-catalytic effluent, wherein a temperature in non-catalytic reactor is between 375? C. and 500? C., wherein the non-catalytic reactor is in the absence of catalyst; upgrading the catalytic feed in the catalytic reactor to produce a reactor effluent, wherein a temperature in catalytic reactor is between 550? C. and 700? C., wherein the catalyst is selected from the group consisting of transition metal oxides, lanthanide oxides, and combinations of the same, separating the reactor effluent in the high pressure separator to produce a gases stream; and separating the gases stream in the gases separator to produce a gas product and a light hydrocarbon stream.

An easily transportable micro-scale process is described for the direct production of liquid fuels from flare gas, biogas, stranded natural gas, natural gas emissions from methane hydrate dissociation, and other low-volume, gas-phase hydrocarbon resources. The process involves the design of an integrated series of tubular catalytic reactors in which each consecutive catalytic reactor in the series has been designed with larger volumes of catalyst so that a single pass efficiency of about 90% or greater is achieved while keeping the temperatures and pressures of each reactor similar and without requiring tailgas recycling to the reactors. Typically, the process employs a direct fuel production catalyst that produces undetectable, detrimental carboxylic acids in the fuel and catalyst reaction water. As a result, the directly produced, premium fuels are non-corrosive and do not degrade during long-term storage.

A method for providing hydrogen gas comprises a release of hydrogen gas in a dehydrogenation reactor by catalytic dehydrogenation of an at least partially charged hydrogen carrier medium to form an at least partially discharged hydrogen carrier medium, a catalytic oxidation of the at least partially discharged hydrogen carrier medium means of an oxidizing agent to form an at least partially oxidized hydrogen carrier medium in an oxidation reactor, a reduction of the at least partially oxidized hydrogen carrier medium to form the at least partially charged hydrogen carrier medium by catalytic hydrogenation in a hydrogenation reactor and a removal of at least one oxygen-containing impurity from the at least partially charged hydrogen carrier medium and/or from the at least partially oxidized hydrogen carrier medium.

The present disclosure is directed to methods using durable functional materials for processes that include an oxidation step. The durable functional materials are redox active oxygen carrier materials that include a zirconia or yttria-stabilized-zirconia (YSZ) matrix containing a redox-active metal ion(s), such as, but not limited to Fe, Mn, Cu, Co and Cr. In an embodiment, these materials are used in chemical looping processes.

Provided is a system and a method which allow hydrogen to be produced both efficiently and in a stable manner when using exhaust gas produced by power generation as a heat source for the dehydrogenation reaction, controlling the temperature of the dehydrogenation reaction within an appropriate range. The system (1) for producing hydrogen comprises a dehydrogenation reaction unit (51) for producing hydrogen from an organic hydride by a dehydrogenation reaction in presence of a dehydrogenation catalyst; a first power generation unit (2) for generating electric power from energy of combustion gas produced by combustion of fuel; a waste heat recovery unit (3) for receiving heat from exhaust gas expelled from the first power generation unit; a heat exchanger (21) provided in the waste heat recovery unit for exchanging heat between the exhaust gas and a heat medium; and a circulation line (L1-L3) for introducing the heat medium heated in the heat exchanger to the dehydrogenation reaction unit in liquid form, and returning the heat medium expelled from the dehydrogenation reaction unit to the heat exchanger; wherein the heat medium is introduced into the dehydrogenation reaction unit at an introduction temperature ranging between 352 C. and 392 C., the heat medium is expelled from the dehydrogenation reaction unit at an expulsion temperature ranging between 337 C. and 367 C., and a difference between the introduction temperature and the expulsion temperature ranges between 10 C. and 50 C.

A process is described for the production of formaldehyde, comprising (a) subjecting methanol to oxidation with air in a formaldehyde production unit thereby producing a formaldehyde-containing stream; (b) separating said formaldehyde-containing stream into a formaldehyde product stream and a formaldehyde vent gas stream; wherein the vent gas stream, optionally after treatment in a vent gas treatment unit, is passed to one or more stages of: (i) synthesis gas generation, (ii) carbon dioxide removal, (iii) methanol synthesis or (iv) urea synthesis.