A reactor includes: a main reactor core including main reaction flow channels through which the raw material fluid flows, and main temperature control flow channels through which the heat medium flows along a flow direction of the raw material fluid flowing in the main reaction flow channel; and a pre-reactor core including pre-reaction flow channels of which an outlet side connects with an inlet side of the main reaction flow channels and through which the raw material fluid flows, and pre-temperature control flow channels of which an inlet side connects with an outlet side of the main reaction flow channels and through which the product serving as the heat medium flows along a flow direction of the raw material fluid flowing in the pre-reaction flow channel.

A reactor includes: a main reactor core including main reaction flow channels through which the raw material fluid flows, and main temperature control flow channels through which the heat medium flows along a flow direction of the raw material fluid flowing in the main reaction flow channel; and a pre-reactor core including pre-reaction flow channels of which an outlet side connects with an inlet side of the main reaction flow channels and through which the raw material fluid flows, and pre-temperature control flow channels of which an inlet side connects with an outlet side of the main reaction flow channels and through which the product serving as the heat medium flows along a flow direction of the raw material fluid flowing in the pre-reaction flow channel.

A system is described for providing a hydrocarbon product stream. An electrolysis section provides a syngas stream from a first feed comprising CO.sub.2 and a second feed comprising H.sub.2O, which is then passed to an F-T section where it is converted to a hydrocarbon product stream and a tail gas stream. An electrical steam reformer section said tail gas stream and convert it to a second syngas stream, which is then recycled upstream the FT section. A process is also provided for converting a first feed comprising CO.sub.2 and a second feed comprising H.sub.2O to a first hydrocarbon product stream in a system according to the invention. The system of the invention can be combined with an upgrading section, in a gas-to-liquid plant.

A renewable fuel production system includes a carbon dioxide capture unit for extracting carbon dioxide from atmospheric air, a carbon dioxide electrolyzer for converting carbon dioxide to carbon monoxide, a water electrolyzer for converting water to hydrogen, a synfuels generator for converting carbon monoxide produced by the carbon dioxide electrolyzer and hydrogen produced by the water electrolyzer to a fuel. The fuel produced can be synthetic gasoline and/or synthetic diesel. A renewable fuel production process includes the steps of extracting carbon dioxide from atmospheric air via a carbon dioxide capture unit, converting carbon dioxide to carbon monoxide via a carbon dioxide electrolyzer, converting water to hydrogen via a water electrolyzer, and converting carbon monoxide produced via the carbon dioxide electrolyzer and H.sub.2 produced via the water electrolyzer to a fuel. The system is also capable of simultaneously or alternatively producing a separate industrial chemical.

Fuel cell arrangement having an improved efficiency. The arrangement comprises one or more fuel cell units 110 and a methanation unit 200 and a control unit 300. The fuel cell unit comprises a water inlet 111, a hydrogen outlet 112 and an oxygen outlet 113. The methanation unit comprises a catalyst 222, a hydrogen inlet 213, a carbon oxide inlet 214 having a first controllable valve 215 and a methane outlet 216, wherein the hydrogen outlet of the first fuel cell unit is coupled to the hydrogen inlet of the methanation unit, and the methanation unit is adapted to convert hydrogen and carbon oxide into methane, wherein the control unit is adapted to control the first controllable valve so as to obtain an optimum converting process to convert hydrogen and carbon oxide into methane.

The invention relates to Fischer-Tropsch synthesis in a compact version. A compact reactor comprises a housing, rectangular reaction channels inside the housing, which are filled with a cobalt catalyst, synthesis gas injection nozzles in the number determined by the ratio of the number of channels to the number of synthesis gas injection nozzles, an input and output nozzle for heat transfer medium on which a pressure controller installed, and an assembly for withdrawing synthetic hydrocarbons. The cobalt catalyst is activated by passing hydrogen through it. Synthetic hydrocarbons are produced by passing synthesis gas through the reaction channels filled with the activated cobalt catalyst. The space velocity of synthesis gas is increased every 300-500 h, followed by returning to the initial process conditions. This provides a high-molecular-weight hydrocarbon output per unit mass of the reactor.

An apparatus for producing a natural gas using carbon dioxide and water in air that includes an air-compressing member, a water collecting member, a water storing member, a carbon dioxide collecting member, a water electrolysis member, and a methanation reaction member. The water electrolysis member electrolyzes water separated from compressed air. The methanation reaction member generates a natural gas by reacting hydrogen from the electrolysis and carbon dioxide from the carbon dioxide collecting member. A method of producing a natural gas using carbon dioxide and water in air includes supplying hydrogen electrolyzed from water separated from air and carbon dioxide collected from the dry air to a methanation reaction member to generate a natural gas. A natural gas-synthesizing equipment system includes an apparatus for producing a natural gas using carbon dioxide and water in air.

A system includes an oxidative combustion reactor configured to receive solid organic waste and O2, and to output a combined stream of H2O and CO2. A separator is configured to receive the combined stream of H2O and CO2 from the combustion reactor and to separately output a stream of CO2 and a stream of H2O. A Sabatier reactor is operatively connected to receive CO2 from the separator and to receive H2 from an H2 source, and to output gaseous CH4.

The present technology is directed to processes for conversion of synthesis gas in a tubular reactor to produce a synthetic product that utilizes high activity carbon monoxide hydrogenation catalysts and a heat transfer structure that surprisingly provides for higher per pass conversion with high selectivity for the desired synthetic product without thermal runaway.

A reverse water-gas shift catalyst that can be used at high temperatures is obtained. A reverse water-gas shift catalyst (cat1) is produced by executing an impregnation-supporting step of impregnating a carrier (cb1) containing alumina as a main component with nickel as a catalytically active component (ca1) to be supported on the carrier, and calcinating a precursor obtained in the impregnation-supporting step at a temperature of 500? C. or higher.