A process for the production of formaldehyde-stabilised urea is described comprising the steps of: (a) generating a synthesis gas comprising hydrogen, nitrogen, carbon monoxide, carbon dioxide and steam in a synthesis gas generation unit; (b) recovering carbon dioxide from the synthesis gas to form a carbon dioxide-depleted synthesis gas; (c) synthesising methanol from the carbon dioxide-depleted synthesis gas in a methanol synthesis unit and recovering the methanol and a methanol synthesis off-gas comprising nitrogen, hydrogen and residual carbon monoxide; (d) subjecting at least a portion of the recovered methanol to oxidation with air in a formaldehyde production unit; (e) subjecting the methanol synthesis off-gas to methanation in a methanation reactor containing a methanation catalyst to form an ammonia synthesis gas; (f) synthesising ammonia from the ammonia synthesis gas in an ammonia production unit and recovering the ammonia; (g) reacting a portion of the ammonia and at least a portion of the recovered carbon dioxide stream in a urea production unit to form a urea stream; and (h) stabilising the urea by mixing the urea stream and a stabiliser prepared using formaldehyde recovered from the formaldehyde production unit, wherein a source of air is compressed and divided into first and second portions, the first portion is provided to the formaldehyde production unit for the oxidation of methanol and the second portion is further compressed and provided to the synthesis gas generation unit.

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 discloses a dehydrogenation reaction system for a liquid hydrogen source material, comprising a storage device used for storing a liquid hydrogen source material and a liquid hydrogen storage carrier, a reaction still used for dehydrogenation of the liquid hydrogen source material, a gas-liquid separator used 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. The normal-pressure and temperature dehydrogenation system for the liquid hydrogen source material is used for dehydrogenation reaction of the liquid hydrogen source material, and generated hydrogen can be supplied to fuel cells or internal combustion engines to be converted into electric energy or mechanical energy so as to be applied to automobiles, emergency power supplies, large-scale energy storage, smart power grids, chemical engineering, pharmacy and other industrial and civil fields.

A hydrogen storage material in liquid form is provided. The liquid hydrogen storage comprises at least two different hydrogen storage components, each one of the components is selected from an unsaturated aromatic hydrocarbon or a heterocyclic unsaturated compound, and at least one of the hydrogen storage components is a low-melting-point compound whose melting point is lower than 80 DEG C.

The present disclosure refers to systems and methods for the production, storage, and transportation of hydrogen. In a representative embodiment a reactor system comprises a fluidized bed combustor configured for reduced metal oxide oxidation and heat generation without significant greenhouse gas emission and/or with readily capturable emissions. The reactor system also comprises a liquid organic hydrogen carrier dehydrogenation reactor. The fluidized bed combustor is operatively coupled to the liquid organic hydrogen carrier dehydrogenation reactor. Advantageously, at least a portion of heat generated by the fluidized bed combustor may be transferred to the liquid organic hydrogen carrier dehydrogenation reactor. In this manner hydrogen production and transportation is both energy efficient, low carbon intensity and cost-effective.

The invention relates to a four-component catalyst and a seven-component catalyst and refractory supports for use in the thermoneutral reforming of petroleum-based liquid hydrocarbon fuels.

According to an embodiment there is provided a method of developing catalysts that are able to reduce the levels of tars in the syngas by reforming. One embodiment develops a co-catalyst, char supported nickel catalyst, for syngas conditioning. Biomass-derived char does not only serve as a support, but also plays a role in catalyzing the reactions. Biomass-derived char is a byproduct of biomass thermo-conversion process. In one variation, hydrazine was used to reduce supported Ni.sup.2 into Ni.sup.0. Compared with the traditional method of reducing nickel with hydrogen flow, this reduction method increases nickel dispersion rate and reduces nickel particle size.

Provided is a power conversion system having a solid-oxide fuel cell capable of stably generating electricity from hydrogen generated by an organic hydride. The power conversion system includes a solid-oxide fuel cell, a reactor for producing hydrogen and a dehydrogenation product from an organic hydride by dehydrogenation reaction, and a heat engine for generating motive power. The power conversion system separates the hydrogen produced by the reactor, and supplies the hydrogen as fuel to the solid-oxide fuel cell. Exhaust heat of the heat engine is supplied to both the solid-oxide fuel cell and the reactor.

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.

An interconnected set of two or more stages of reactors to form a bio-reforming reactor that generates syngas for a number of different liquid fuel or chemical processes is discussed. A first stage includes a circulating fluidized bed reactor that is configured to cause a chemical devolatilization of the biomass into its reaction products of constituent gases, tars, chars, and other components, which exit through a reactor output from the first stage. A second stage of the bio-reforming reactor has an input configured to receive a stream of some of the reaction products that includes the constituent gases and at least some of the tars as raw syngas, and then chemically reacts the raw syngas within a vessel of the second stage to make the raw syngas from the first stage into a chemical grade syngas by further cracking the tars, excess methane, or both.