A methanation reaction catalyst is for subjecting CO and/or CO.sub.2 to methanation reaction with hydrogen, and is a calcined product of a wet mixture of zirconia and/or a salt of Zr, a salt of a stabilizing element, a salt of Ni, and an inorganic oxide. The stabilizing element is at least one of element selected from the group consisting of Y, La, Ce, Pr, Nd, Sm, Gd, Dy, Ca, Mg, Mn, Fe, and Co, and the inorganic oxide is at least one of inorganic oxide selected from the group consisting of silica, alumina, titania, and ceria. When the inorganic oxide contains the silica, the mole ratio of the Ni atom with respect to the Si atom is 0.20 or more and 10.0 or less. When the inorganic oxide contains the alumina, the mole ratio of the Ni atom with respect to the Al atom is 0.20 or more and 7.0 or less. When the inorganic oxide contains the titania, the mole ratio of the Ni atom with respect to the Ti atom is 0.30 or more and 10.5 or less. When the inorganic oxide contains the ceria, the mole ratio of the Ni atom with respect to the Ce atom is 0.70 or more and 25.0 or less.

The present invention relates to a thermochemical reactor system for a temperature swing cyclic process with integrated heat recovery comprising at least two modules, wherein each module comprises at least one chemical reaction zone (CRZ) and at least one thermal energy storage unit (TES), wherein the at least two modules are operationally connected for at least one heat transfer fluid (HTF) for transporting heat between the two modules, wherein each chemical reaction zone (CRZ) comprises at least one reacting material that undergoes in a reversible manner an endothermic reaction at temperature T.sub.endo and an exothermic reaction at temperature T.sub.exo, wherein T.sub.endo and T.sub.exo differ from each other, wherein the at least one reacting material is provided in at least one encapsulation within each of the chemical reaction zones (CRZ) such that a contact of the reacting material and the at least one heat transfer fluid is avoided. The present invention relates further to a method for operating such a reactor system.

The present invention relates to a thermochemical reactor system for a temperature swing cyclic process with integrated heat recovery comprising at least two modules, wherein each module comprises at least one chemical reaction zone (CRZ) and at least one thermal energy storage unit (TES), wherein the at least two modules are operationally connected for at least one heat transfer fluid (HTF) for transporting heat between the two modules, wherein each chemical reaction zone (CRZ) comprises at least one reacting material that undergoes in a reversible manner an endothermic reaction at temperature T.sub.endo and an exothermic reaction at temperature T.sub.exo, wherein T.sub.endo and T.sub.exo differ from each other, wherein the at least one reacting material is provided in at least one encapsulation within each of the chemical reaction zones (CRZ) such that a contact of the reacting material and the at least one heat transfer fluid is avoided. The present invention relates further to a method for operating such a reactor system.

A hydrocarbon is produced by applying mechanical energy to a metal body containing stainless steel by solid-solid contact so that a contact pressure per unit area is 30 kPa or more, in the presence of a gas containing carbon dioxide and a hydrogen source, thereby adding hydrogen to carbon dioxide. Further, a hydrocarbon is produced by providing a reaction vessel for applying mechanical energy to a metal body by solid-solid contact in the presence of a gas containing carbon dioxide and a hydrogen source, a gas introduction unit for introducing the gas containing carbon dioxide to the reaction vessel, a hydrogen source introduction unit for introducing the hydrogen source to the reaction vessel, and a gas discharge unit for discharging a gas containing the hydrocarbon produced in the reaction vessel, and adding hydrogen to the carbon dioxide in the reaction vessel.

A hydrocarbon is produced by applying mechanical energy to a metal body containing stainless steel by solid-solid contact so that a contact pressure per unit area is 30 kPa or more, in the presence of a gas containing carbon dioxide and a hydrogen source, thereby adding hydrogen to carbon dioxide. Further, a hydrocarbon is produced by providing a reaction vessel for applying mechanical energy to a metal body by solid-solid contact in the presence of a gas containing carbon dioxide and a hydrogen source, a gas introduction unit for introducing the gas containing carbon dioxide to the reaction vessel, a hydrogen source introduction unit for introducing the hydrogen source to the reaction vessel, and a gas discharge unit for discharging a gas containing the hydrocarbon produced in the reaction vessel, and adding hydrogen to the carbon dioxide in the reaction vessel.

A hydrocarbon is produced by applying mechanical energy to a metal body containing stainless steel by solid-solid contact so that a contact pressure per unit area is 30 kPa or more, in the presence of a gas containing carbon dioxide and a hydrogen source, thereby adding hydrogen to carbon dioxide. Further, a hydrocarbon is produced by providing a reaction vessel for applying mechanical energy to a metal body by solid-solid contact in the presence of a gas containing carbon dioxide and a hydrogen source, a gas introduction unit for introducing the gas containing carbon dioxide to the reaction vessel, a hydrogen source introduction unit for introducing the hydrogen source to the reaction vessel, and a gas discharge unit for discharging a gas containing the hydrocarbon produced in the reaction vessel, and adding hydrogen to the carbon dioxide in the reaction vessel.

Disclosed herein is a method comprising the steps of: a) producing a hydrocarbon stream from syngas via a Fischer-Tropsch reaction, wherein the hydrocarbon stream comprises a first C2 hydrocarbon stream comprising ethane and a first ethylene product; b) separating at least a portion of the first C2 hydrocarbon stream from the hydrocarbon stream; c) separating at least a portion of the first ethylene product from the first C2 hydrocarbon stream, thereby producing a second C2 hydrocarbon stream; d) converting at least a portion of the ethane in the second C2 hydrocarbon stream to a second ethylene product; and e) producing polyethylene from at least a portion of the second ethylene product.

Disclosed herein is a method comprising the steps of: a) producing a hydrocarbon stream from syngas via a Fischer-Tropsch reaction, wherein the hydrocarbon stream comprises a first C2 hydrocarbon stream comprising ethane and a first ethylene product; b) separating at least a portion of the first C2 hydrocarbon stream from the hydrocarbon stream; c) separating at least a portion of the first ethylene product from the first C2 hydrocarbon stream, thereby producing a second C2 hydrocarbon stream; d) converting at least a portion of the ethane in the second C2 hydrocarbon stream to a second ethylene product; and e) producing polyethylene from at least a portion of the second ethylene product.

A reforming device (10) according to the present invention has a compressor (11), a first heat exchanger (12), a desulfurization device (13), a reformer (14), a raw material gas branching line (L11) that extracts a compressed natural gas (21) from a downstream side of the desulfurization device (13) with respect to the flow direction of the natural gas (21) and supplies the natural gas (21) to the reformer (14), and a flue gas discharging line (L12) that discharges a flue gas (22) generated in the reformer (14), wherein the first heat exchanger (12) is provided in the flue gas discharging line (L12), and the flue gas (22) is used as a heating medium of the compressed natural gas (21).

Included are an ammonia synthesis column that synthesizes ammonia from a raw material gas, a discharge line that discharges a synthetic gas, a water-cooled cooler that cools the synthetic gas with a coolant, disposed in the discharge line, an ammonia separator into which a synthetic gas after cooling is introduced and which separates the ammonia gas and a liquid ammonia from each other, a raw material return line that returns a raw material gas containing the separated ammonia gas to the ammonia synthesis column side as a return raw material gas, and a compressor that compresses the return raw material gas, disposed in the raw material return line. An ammonia concentration in the return raw material gas is 5 mol % or more, and an ammonia synthesis catalyst that synthesizes the ammonia gas in the ammonia synthesis column is a ruthenium catalyst.