A synthesis device may include a pressure vessel with an inlet and an outlet for fluid, a catalyst bed that is disposed within the pressure vessel, a plate heat exchanger that is disposed in a flow path of fluid between the inlet of the pressure vessel and the catalyst bed such that fluid flowing into the catalyst bed is heated by fluid flowing out of the catalyst bed. The plate heat exchanger may be disposed outside a reactor volume occupied by the catalyst bed in the pressure vessel. The catalyst bed may be one of a plurality of catalyst beds disposed axially over one another in the pressure vessel.

A method for producing polyphenylene ether amine includes following steps. In step (a), a hydrogenation reaction tank is provided; a guided gas stirrer is disposed in the hydrogenation reaction tank. In step (b), a reaction solution is placed in the hydrogenation reaction tank, and the reaction solution is nitro polyphenylene ether dissolved in a solvent. In step (c), a hydrogenation catalyst is added to the reaction solution. In step (d), a hydrogen gas is introduced into the hydrogenation reaction tank. In step (e), the guided gas stirrer is activated. In step (f), a hydrogenation reaction is carried out on the conditions that a reaction temperature is 50-200 degrees Celsius and a reaction time is 1-20 hours, so as to hydrogenate the nitro polyphenylene ether in the reaction solution to polyphenylene ether amine. In step (g), the reaction solution is cooled down to a room temperature; the hydrogenation catalyst is removed.

A reactor for hydrocarbon production that separates wax reaction products from lightweight gaseous reaction products. The reactor has a housing, a catalyst bed, a product recovery zone, and a stripping zone. The catalyst bed can be provided in multi-tubular and other fixed bed configurations. The stripping zone receives light-weight gas reaction products from the product recovery zone, while a gas outlet of the housing receives non-lightweight gaseous hydrocarbon reaction products from the product recovery zone. A wax outlet of the housing receives wax products from the product recovery zone.

Horizontal reactor (1) for catalytic reactions, comprising an outer cylindrical shell (2), a catalytic bed (5) and heat exchange plates (6) immersed in said catalytic bed, parallel to each other and supplied with a heat exchange fluid; said reactor comprises a container (7) for said catalytic bed (5) and said plates (6), said container is extractable slidably from said shell, by means of at least one linear guide (31, 32, 45) extended longitudinally with respect to said shell (2).

Method for revamping a multi-bed ammonia converter, wherein said converter comprises a plurality of adiabatic catalytic beds including a first catalytic bed and one or more further catalytic bed(s), said catalytic beds being arranged in series so that the effluent of a bed is further reacted in the subsequent bed; at least a first inter-bed heat exchanger arranged between said first catalytic bed and a second catalytic bed to cool the effluent of said first bed before admission into said second bed, and optionally further inter-bed heat exchanger(s) arranged between consecutive beds; said method involves the conversion of said first catalytic bed into an isothermal catalytic bed.

The invention relates to a catalytic reactor suited for exothermal reactions with a radial process fluid flow and process fluid flow guides which ensures an extended fluid flow path and higher flow velocity and thereby enhanced cooling of the catalyst bed in the reactor.

Plate heat exchanger for internals of isothermal chemical reactors, said plate heat exchanger comprising a plurality of heat exchange plates (1) having an essentially rectangular shape, wherein each plate comprises two walls (2, 3) which are joined together along their perimeter, and wherein each plate comprises a respective first collector for feeding a heat exchange medium to the plate and a respective second collector for receiving said medium form the plate, said first collector and second collector being fixed to opposite sides of said plate, and at least one (10, 30) of said first collector and second collector comprises edge surfaces which are planar and parallel to respective planar end portions (12, 13) of said plate, to provide plane and parallel surfaces for automated welding.

A reaction device for preparing light olefins from methanol and/or dimethyl ether, and more specifically relates to a reaction device for preparing light olefins from methanol and/or dimethyl ether, which mainly comprises a dense phase fluidized bed reactor (2), a cyclone separator (3), a stripper (5), a lift pipe (7), a dense phase fluidized bed regenerator (10), a cyclone separator (11), a stripper (13), and a lift pipe (15), wherein the dense phase fluidized bed reactor (2) is separated into n (n2) secondary reaction zones by a material flow controller (17), and the dense phase fluidized bed regenerator (10) is separated into m (m2) secondary regeneration zones by the material flow controller (17).

Horizontal reactor (1) for catalytic reactions, comprising an outer cylindrical shell (2), a catalytic bed (5) and heat exchange plates (6) immersed in said catalytic bed, parallel to each other and supplied with a heat exchange fluid; said reactor comprises a container (7) for said catalytic bed (5) and said plates (6), said container is extractable slidably from said shell, by means of at least one linear guide (31, 32, 45) extended longitudinally with respect to said shell (2).

A reaction device for preparing light olefins from methanol and/or dimethyl ether, and more specifically relates to a reaction device for preparing light olefins from methanol and/or dimethyl ether, which mainly comprises a dense phase fluidized bed reactor (2), a cyclone separator (3), a stripper (5), a lift pipe (7), a dense phase fluidized bed regenerator (10), a cyclone separator (11), a stripper (13), and a lift pipe (15), wherein the dense phase fluidized bed reactor (2) is separated into n (n2) secondary reaction zones by a material flow controller (17), and the dense phase fluidized bed regenerator (10) is separated into m (m2) secondary regeneration zones by the material flow controller (17).