An apparatus includes an integrated heat exchanger and reactor module. The integrated heat exchanger and reactor module includes a heat exchanger channel, and a reactor channel which is thermally coupled to the heat exchanger channel. The reactor channel includes a layer of catalyst material that is configured to produce hydrogen by endothermic catalytic decomposition of ammonia, which flows through the reactor channel, using thermal energy that is absorbed by the reactor channel from the heat exchanger channel.

A flow reactor can promote a reaction under appropriate temperature management, can precent reaction fluid or generated gas from being trapped in a heat transmission part, can be disassembled for easy cleaning, and to which a coating or lining can be applied. This flow reactor is provided with two flow paths, a reaction flow path and a second flow path, in a space formed between an inner cylinder and an outer cylinder that are concentric. A spiral heat transmission body is disposed between the inner cylinder and the outer cylinder, and the spiral heat transmission body has a substantially triangular cross-sectional shape in an axial cross-sectional view. The spiral heat transmission body partitions the space into the reaction flow path and the second flow path, and heat is exchanged via the spiral heat transmission body between a reaction fluid F1 flowing through the reaction flow path and a heat medium F2 flowing through the second flow path.

A flow reactor is structured to increase the overall heat transfer coefficient, which represents the efficiency of heat exchange with respect to a reactive fluid to be treated. This flow reactor is provided with three flow passages, which are a first flow passage, a second flow passage, and a third flow passage which spirally circulate within a space formed between an inner tube and an outer tube. The flow passages are compartmented by an inner heat transfer body and an outer heat transfer bodies. The heat transfer bodies spirally circulate, have a screw-like cross-sectional shape in an axial cross-sectional view, and are assembled in a screw-like configuration. By changing the shapes of a male-thread portion and a female-thread portion, the flow passage area of the first flow passage is changed, the second flow passage and the third flow passage are spirally formed, and heat exchange and reaction take place through the heat transfer bodies.

A reactor for performing a reaction between two immiscible fluids of different density, comprising an interior formed by a cylindrical, vertically oriented elongate shell, a bottom and a cap, wherein the interior is divided by internals into a backmixed zone, a zone of limited backmixing preferably arranged below the backmixed zone and a plug-flow zone which are at least consecutively traversable by one of the fluids, wherein the backmixed zone comprises at least one inlet and the plug-flow zone comprises an outlet and the backmixed zone comprises at least one mixing apparatus selected from a stirrer, a jet nozzle and means for injecting the fluid of lower density, a first cylindrical internal element which in the interior extends in the longitudinal direction of the reactor, which delimits the zone of limited backmixing from the plug-flow zone and which comprises a first passage to the backmixed zone and a second passage to the plug-flow zone, a second internal element which delimits the backmixed zone from the plug-flow zone such that there is no direct fluid connection between the backmixed zone and the plug-flow zone, and backmixing-preventing third internal elements in the form of random packings, structured packings or liquid-permeable trays arranged in the zone of limited backmixing. The reactor allows an optimal residence time distribution in the reaction of the two immiscible fluids of different density. The invention further relates to a process for performing a continuous reaction in the reactor.

A strengthening oxidation system of the external micro-interfacial unit for producing PTA with PX is provided, including: a reactor, a circulating heat exchange device and a micro-interfacial unit. The reactor includes an outer casing and an inner cylinder disposed concentrically inside the outer casing. The circulating heat exchange device is disposed at an exterior of the reactor, and is connected with the outer casing and the inner cylinder respectively, for regulating reaction temperatures of the first reaction zone, the second reaction zone and the third reaction zone inside the reactor in a reaction process of producing PTA with PX. the micro-interfacial unit is connected between the reactor and the circulating heat exchange device, and connected with an external feed pipe of the reactor, for crushing a gas phase material into micro bubbles with a diameter greater than or equal to 1 μm and less than 1 mm and for mixing the micro bubbles with a liquid phase material to form an emulsion at the exterior of the reactor before a reaction material enters each of the reaction zones inside the reactor.

In a first stage of a methane conversion system, at least some methane (CH.sub.4) in an input gas flow stream can be converted into C.sub.2 hydrocarbons, hydrogen gas (H.sub.2), and aromatics to provide a first processed stream. The conversion can be direct non-oxidative methane conversion (DNMC). At least some of the aromatics can be removed from the first processed stream to provide a second processed stream. In a second stage of the methane conversion system, at least some of the H.sub.2 can be removed from the second processed stream to provide a recycle stream. The recycle stream can be returned to the first stage of the methane conversion system for further conversion of methane and removal of aromatics and H.sub.2 products.

The present disclosure relates to a device for directing a coking-prone liquid to a high temperature environment, where the device includes an inner tube positioned concentrically within an outer tube, creating a first annular space between an outer wall of the inner tube and an inner wall of the outer tube and a first intermediate tube positioned concentrically around the outer tube, creating a second annular space.

The disclosure provides for a process for a non-catalytic oxidative coupling of methane reaction remarkable in that the process comprises a step of providing a counter-current shell-tube reactor comprising at least two tubes defining a tubular part and a shell part surrounding the tubular part and at least one inlet to feed a gaseous feed stream and at least one outlet to discharge a product stream; a step of providing a gaseous feed stream comprising a gas mixture of methane and oxygen in a defined molar ratio and preheated to a defined operating inlet temperature; a step of feeding the gaseous feed stream at least in the tubular part of the counter-current shell-tube reactor and a step of recovering a product stream.

A strengthening oxidation system of the external micro-interfacial unit for producing PTA with PX is provided, including: a reactor, a circulating heat exchange device and a micro-interfacial unit. The reactor includes an outer casing and an inner cylinder disposed concentrically inside the outer casing. The circulating heat exchange device is disposed at an exterior of the reactor, and is connected with the outer casing and the inner cylinder respectively, for regulating reaction temperatures of the first reaction zone, the second reaction zone and the third reaction zone inside the reactor in a reaction process of producing PTA with PX. the micro-interfacial unit is connected between the reactor and the circulating heat exchange device, and connected with an external feed pipe of the reactor, for crushing a gas phase material into micro bubbles with a diameter greater than or equal to 1 μm and less than 1 mm and for mixing the micro bubbles with a liquid phase material to form an emulsion at the exterior of the reactor before a reaction material enters each of the reaction zones inside the reactor.

An apparatus for the production of hydrogen from a fuel source includes a combustor configured to receive a combustor fuel and convert the combustor fuel into a combustor heat; a reformer disposed annularly about the combustor, a removable structured catalyst support disposed within the gap and coated with a catalyst to induce combustor fuel combustion reactions that convert the combustor fuel to the combustor heat, and a combustor fuel injection aperture configured for mixing combustion fuel into the combustion catalyst. The combustor fuel injection aperture being disposed along a length of the combustion zone. The reformer and the combustor define a gap therebetween and the reformer is configured to receive the combustor heat.