A catalytic burner arrangement is provided including at least a catalytic burner unit with a housing having a reaction chamber in which a catalyst is arranged, wherein the catalyst is adapted to react a fuel, particularly a hydrogen containing fluid, with an oxidant, particularly air, for producing heat, the housing having a fluid inlet for supplying a fluid stream into the housing and a find outlet for exiting a fluid stream from the housing, and the catalytic burner arrangement further includes a mixing unit forming a mixing chamber in which fuel and oxidant are mixed, wherein the mixing device includes a fuel inlet, an oxidant inlet and an fuel-oxidant-mixture outlet, and wherein the fluid inlet of the catalytic burner unit merges with the fuel-oxidant-outlet of the mixing unit for transferring the fuel-oxidant-mixture from the mixing chamber to the reaction chamber of the catalytic burner unit wherein the fuel-oxidant-outlet of the mixing chamber is pipe-shaped and extents into the mixing chamber of the mixing unit, and wherein a length of the pipe-shaped fuel-oxidant-outlet extents over the oxidant inlet and/or the fuel inlet.

Process for manufacturing a hydrogen-containing synthesis gas from a natural gas feedstock, comprising the conversion of said natural gas into a raw product gas and purification of said product gas, the process having a heat input provided by combustion of a fuel; said process comprises a step of conversion of a carbonaceous feedstock, and at least a portion of said fuel is a gaseous fuel obtained by said step of conversion of said carbonaceous feedstock.

A process synthesizes C.sub.5 and higher hydrocarbons from natural gas through intermediate conversion of natural gas to synthesis gas and subsequent conversion of CO and H.sub.2 by Fischer-Tropsch synthesis. The process includes steam reforming of natural gas in a steam reforming reactor to form synthesis gas, separating carbon dioxide from the synthesis gas by a liquid absorption method to a residual carbon dioxide content in the synthesis gas no more than 5 vol. %, separating an excess of hydrogen from the synthesis gas by a hydrogen-permeable membrane apparatus to a H.sub.2:CO molar ratio in the range of 1.9 to 2.3 and synthesizing liquid hydrocarbon from the synthesis gas by Fischer-Tropsch synthesis.

Systems and methods are provided for performing hydrocarbon reforming within a reverse flow reactor environment (or another reactor environment with flows in opposing directions) while improving management of CO.sub.2 generated during operation of the reactor. The improved management of CO.sub.2 is achieved by making one or more changes to the operation of the reverse flow reactor. The changes can include using an air separation unit to provide an oxygen source with a reduced or minimized content of nitrogen and/or operating the reactor at elevated pressure during the regeneration stage. By operating the regeneration at elevated pressure, a regeneration flue gas can be generated that is enriched in CO.sub.2 at elevated pressure. The CO.sub.2-enriched stream can include primarily water as a contaminant, which can be removed by cooling while substantially maintaining the pressure of the stream. This can facilitate subsequent recovery and use of the CO.sub.2.

The present invention relates to a process for converting carbon dioxide and hydrogen by performing a reverse water gas shift reaction at elevated temperature, the process comprising introducing carbon dioxide, hydrogen and oxygen into a reaction vessel having an inlet and an outlet, and, wherein the reverse water gas shift reaction takes place in two different zones of the reaction vessel, being a top zone (z1) adjacent to a bottom zone (z2). The process produces a product stream comprising mainly carbon monoxide, hydrogen and water. The process is useful in reducing the carbon footprint of certain industrial technologies, and in addition, the process is useful in the production of synthesis gas.

According to one embodiment of the present invention, there is provided a hydrogen extraction reactor, comprising a chamber including an inner space; a reaction unit which is provided to pass through the inside of the chamber and where an endothermic reaction for hydrogen extraction occurs; a heating unit which is provided to be spaced apart from the reaction unit inside the chamber and transfers heat to the inside of the chamber; and a heat transfer material which is provided between the reaction unit and the heating unit in the chamber, wherein the heat transfer material undergoes a phase transition between a gas phase and a liquid phase according to the entry and exit of heat from the heating unit or the reaction unit.

A process of hydrogen production comprising the steps of: subjecting a gaseous mixture comprising a hydrocarbon and steam, and having a steam to carbon ratio of at least 0.9:1, to adiabatic pre-reforming in a pre-reformer followed by autothermal reforming with an oxygen-rich gas in an autothermal reformer to generate a reformed gas mixture, optionally adding steam to the reformed gas mixture, increasing the hydrogen content of the reformed gas mixture by subjecting it to one or more water-gas shift stages in a water-gas shift unit to provide a hydrogen-enriched reformed gas, cooling the hydrogen-enriched reformed gas and separating condensed water therefrom, passing the resulting de-watered hydrogen-enriched reformed gas to a carbon dioxide separation unit to provide a carbon dioxide gas stream and a crude hydrogen gas stream, passing the crude hydrogen gas stream to a purification unit to provide a purified hydrogen gas and a fuel gas.

The invention relates to a plant for production of hydrogen, and to a method for operating this plant, comprising a steam reforming reactor having a furnace, in which reactor water and at least one carbonaceous energy carrier are reacted to form a hydrogen-containing crude synthesis gas, and at least one cleaning device for purifying the crude synthesis gas, to which the crude synthesis gas is fed from the steam reforming via at least one feed line. According to the invention, upstream of one of the at least one cleaning devices at least one return line branches off from the feed line, through which the crude synthesis gas is at least in part recirculated into the furnace of the steam reforming reactor.

Methods for producing hydrogen from ammonia are described. The methods involve the use of a two-stage hydrogen PSA configuration. The effluent stream from the ammonia cracking reaction zone is sent to the first hydrogen PSA unit where it is separated into a high purity, high-pressure hydrogen stream and a low-pressure tail gas stream. The high-pressure hydrogen stream can be recovered. The low-pressure tail gas stream is compressed and sent to the second hydrogen PSA unit where it is separated into a second high-pressure stream and a second low-pressure tail gas stream. The second high-pressure hydrogen stream can be recycled to the first hydrogen PSA unit for further separation.

A power generation system includes: a combustor operative to combust a fuel; a power generator operative to utilize energy obtained from the combustor when generating electric power; a fuel supplier operative to supply the fuel to the combustor; an air supplier operative to supply combustion air to the combustor; a discharged gas passage through which a discharged gas from the combustor flows; a CO detector operative to detect CO in the discharged gas; a temperature detector operative to detect a temperature of the discharged gas; and control circuitry operative to, when the discharged gas is flowing through the discharged gas passage, perform at least one of an operation of detecting a structural abnormality of the discharged gas passage based on a difference between detected temperatures of the temperature detector relative to a difference between heated amounts of the discharged gas heated by a heater and an operation of detecting the structural abnormality of the discharged gas passage based on the difference between the detected temperatures of the temperature detector relative to a difference between outputs of at least one of the fuel supplier and the air supplier.