The invention relates to a process for utilizing a hydrocarbon-comprising and/or carbon dioxide-comprising coproduct gas, accompanying gas and/or biogas, wherein hydrocarbon-comprising and/or carbon dioxide-comprising coproduct gas, accompanying gas and/or biogas is introduced into a reaction space and the multicomponent mixture comprised in the coproduct gas, accompanying gas and/or biogas is converted in a high-temperature zone at temperatures of more than 1000? C. and in the presence of a carrier into a product gas mixture which comprises more than 95% by volume of CO, CO.sub.2, H.sub.2, H.sub.2O, CH.sub.4 and N.sub.2 and optionally into a carbon-comprising solid which is deposited to an extent of at least 75% by weight, based on the total mass of the carbon-comprising solid, on the carrier where the flow velocity of the gas mixture of coproduct gas, accompanying gas and/or biogas in the reaction zone is less than 20 m/s.

A heat generating device includes a container, a heat generating element, and a heater. A hydrogen-based gas contributing to heat generation is introduced into the container. The heat generating element is provided inside the container. The heater is configured to heat the heat generating element. The heat generating element includes a base made of a hydrogen storage metal, a hydrogen storage alloy, or a proton conductor, and a multilayer film provided on a surface of the base. The multilayer film having a stacking configuration of: a first layer that is made of a hydrogen storage metal or a hydrogen storage alloy, and a second layer that is made of a hydrogen storage metal, a hydrogen storage alloy, or ceramics different from that of the first layer. The first layer and the second layer have a layer shape with a thickness of less than 1000 nm.

A hydrogen production device is provided. The device comprises: a dry reforming reaction unit for directly reacting methane and carbon dioxide in biogas to produce a synthesis gas containing hydrogen; and a gas shift unit for reacting carbon monoxide in the synthesis gas produced in the dry reforming reaction unit with water vapor to produce carbon dioxide and hydrogen, and for capturing the produced carbon dioxide.

A method of operating an oxygen transport membrane based reforming system employing one or more packs of thermally coupled panels of reformer tubes and oxygen transport membrane (OTM) reactors close to thermo-neutral point is provided. The method produces syngas by converting a hydrocarbon-containing feed, such as natural gas in the reformer tubes of a pack by endothermic steam reforming reactions. The heat required for endothermic reforming reactions is provided by exothermic oxidizing reactions occurring inside the OTM reactors of the pack. At a thermo-neutral point the heat released by exothermic reactions matches the heat required to support endothermic reactions and heat losses in the pack. The method modulates the flow rate of hydrocarbon-containing feed and/or steam-to-carbon ratio of the combined feed to the pack to maintain the surface temperature of oxygen transport membrane reactors below a target maximum temperature. The syngas product oxygen-to-carbon ratio is maintained within a desired target range such that the OTM based reforming system is operated close to thermo-neutral point.

A chemical reactor (e.g. reformer reactor) system includes a manifold (126) for management of a flow of gaseous reaction medium thereto. Manifold (126) includes manifold housing (128) defining manifold chamber (129) and having at least one additional component selected from: a gas distributor (127); a heater; and a cavity having a seal within or adjacent to it.

A method for producing synthesis gas may involve introducing a hydrocarbon-containing coke-oven gas and a carbon dioxide-containing converter gas into a first reaction zone where hydrogen present in the hydrocarbon-containing coke-oven gas reacts at least partly with carbon dioxide to form water, which reacts thermally with hydrocarbon to form synthesis gas containing carbon monoxide and hydrogen. The method may further involve introducing an oxygen-containing gas in a second reaction zone, and using the oxygen-containing gas and some hydrogen from the first reaction zone to produce thermal energy. Still further, the method may involve supplying the thermal energy produced in the second reaction zone to the first reaction zone.

A combined reformer and purifier for converting a hydrogen-rich feedstock into purified hydrogen is described. The combined reformer and purifier can include at least one compression plate as an assembly comprising at least one first cavity comprising a catalyst effective to liberate hydrogen from said hydrogen-rich feedstock and forming a hydrogen-rich mixed gas. The compression plate assembly can also include at least one second cavity enclosing a burner or oxidative catalytic reactor to oxidize said hydrogen-depleted raffinate or said hydrogen-rich feedstock to supply heat to the at least one first cavity containing said catalyst. The compression plate assembly can also include an interior surface proximal to said membrane and an exterior surface distal to said membrane. The compression plate assembly can also include a third cavity effective to preheat said hydrogen-rich feedstock prior to being delivered to said catalyst.

The invention relates to the production of synthesis gas by means of particularly a series arrangement of heat exchange reforming and autothermal reforming stages, in which the heat required for the reforming reactions in the heat exchange reforming stage is provided by hot effluent synthesis gas from the autothermal reforming stage. More particularly, the invention relates to optimisation of the operation and control of an arrangement of heat exchange reforming and autothermal reforming stages and introduction of an additional waste heat boiler.

A process for the synthesis of ammonia from a hydrocarbon feedstock, wherein the process includes reforming the hydrocarbon feedstock to produce a make-up gas and converting said make-up gas into ammonia, the process is performed in an ammonia synthesis plant requiring an electric power for operation and also requiring a start-up power (Ps) for start-up, wherein a first electric power (P1) is internally produced in the ammonia plant, and a second electric power (P2) is imported, wherein said second electric power is equal to or greater than said start-up power (Ps).

A method for producing -rich synthesis gas comprises the following steps: decomposing a hydrocarbon-containing fluid into an H.sub.2/C-aerosol in a first hydrocarbon converter by supplying energy which is at least partly provided in the form of heat; introducing at least a first stream of the H.sub.2/C-aerosol into a first sub-process which comprises the following steps: directing at least a part of the H.sub.2/C-aerosol from the first hydrocarbon converter into a first C-converter; introducing CO.sub.2 into the first C-converter and mixing the CO.sub.2 with the H.sub.2/C-aerosol introduced into the first C-converter; converting the mixture of H.sub.2/C-aerosol and CO.sub.2 into a synthesis gas at a temperature of 800 to 1700 C.; mixing additional H.sub.2 with the synthesis gas for the production of H.sub.2-rich synthesis gas. In a second sub-process running in parallel with the first sub-process, hydrogen H.sub.2 and carbon dioxide CO.sub.2 are produced from a hydrocarbon-containing fluid, wherein at least a portion of the CO.sub.2 produced in the second sub-process is introduced into the first C-converter; and wherein at least a portion of the H.sub.2 produced in the second sub-process is mixed with the synthesis gas from the first C-converter. The CO.sub.2 which is needed for the conversion of C in the first C-converter can thereby be provided independently of an external source, and the entire operational sequence is easily controllable.