A method for carrying out catalytic gas phase reactions including providing a tube bundle reactor which has a bundle of reaction tubes that are filled with a catalyst charge and are cooled by a heat transfer medium, conveying a reaction gas through the catalyst charge, the reaction gas flowing into each reaction tube divided into two part flows introduced in the axial direction of the reaction tube at different points in the catalyst charge the catalyst charge has at least two catalyst layers of different activity, wherein the activity of the first catalyst layer, in the flow direction of the reaction gas, is lower than the activity of the at least one other catalyst layer and in step a first part flow is introduced into the first catalyst layer and each further part flow is introduced past the first catalyst layer into the at least one further catalyst layer.

Disclosed herein is a method of producing a product comprising C2-C5 hydrocarbons and C6-C18 hydrocarbons comprising the steps of: a) converting synthesis gas to the product comprising C2-C5 hydrocarbons and C6-C18 hydrocarbons in a first reactor; b) removing the product comprising C2-C5 hydrocarbons and C6-C18 hydrocarbons from the first reactor; c) reintroducing the C6-C18 hydrocarbons into the first reactor and/or introducing the C6-C18 hydrocarbons into a cooling jacket of the first reactor; and d) performing an exothermic reaction in the first reactor, thereby transferring heat from the exothermic reaction to the C6-C18 hydrocarbons, thereby storing heat in the C6-C18 hydrocarbons.

Disclosed herein is a method of producing a product comprising C2-C5 hydrocarbons and C6-C18 hydrocarbons comprising the steps of: a) converting synthesis gas to the product comprising C2-C5 hydrocarbons and C6-C18 hydrocarbons in a first reactor; b) removing the product comprising C2-C5 hydrocarbons and C6-C18 hydrocarbons from the first reactor; c) reintroducing the C6-C18 hydrocarbons into the first reactor and/or introducing the C6-C18 hydrocarbons into a cooling jacket of the first reactor; and d) performing an exothermic reaction in the first reactor, thereby transferring heat from the exothermic reaction to the C6-C18 hydrocarbons, thereby storing heat in the C6-C18 hydrocarbons.

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.

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.

The invention relates to a method for converting a gas into methane (CH.sub.4) which includes: a step of activating a catalytic material including praseodymium oxide (Pr.sub.6O.sub.11) associated with nickel oxide (NiO) and alumina (Al.sub.2O.sub.3), the respective proportions of which are, relative to the total mass of these three compounds: Pr.sub.6O.sub.11: 1 wt % to 20 wt %, NiO: 1 wt % to 20 wt %, and Al.sub.2O.sub.3: 60 to 98 wt %; and a step of passing a gas including at least one carbon monoxide (CO) over the activated catalytic material.

A system for preventing a catalyst from overheating is provided. The system includes: a first reactor filled with a catalyst at least in part and configured to receive reaction gas and produce product gas; and a second reactor configured to cool a catalyst discharged from the first reactor. The catalyst is circulated between the first reactor and the second reactor by injecting the catalyst cooled in the second reactor into the first rector.

A methanation reactor for reacting dihydrogen with a carbon-based compound and producing methane. The reactor has a hollow body configured to receive a fluidized bed of catalytic particles, an inlet for each carbon-based compound and dihydrogen, and an outlet for methane and water. A water inlet is provided to inject liquid-phase cooling water into the fluidized bed. When each carbon-based compound is a gas, the reactor has at least one water-injection nozzle and at least one gas injection nozzle for a gas consisting of the carbon-based gas and dihydrogen, and at least one water-injection nozzle positioned below the gas-injection nozzle. The flow rate of water introduced into the hollow body can depend on the temperature measured in the reactor.

An integrated microchannel reactor and heat exchanger comprising: (a) a waveform sandwiched between opposing shim sheets and mounted to the shim sheets to form a series of microchannels, where each microchannel includes a pair of substantially straight side walls, and a top wall formed by at least one of the opposing shim sheets, and (b) a first set of microchannels in thermal communication with the waveform, where the waveform has an aspect ratio greater than two.

A system and method for utilizing renewable electricity by methanol synthesis via plasma-catalysis CO.sub.2 hydrogenation. Hydrogen produced via water electrolysis and CO.sub.2 captured from industrial processes undergo a reverse water-gas shift reaction, driven efficiently by an atmospheric-pressure plasma jet, yielding a CO/CO.sub.2/H.sub.2 mixed product. This mixture is subsequently pressurized in multi-stage pressurization after passing a buffer storage tank to further efficiently synthesize green methanol in the plasma jet reactor. The present disclosure employs a two-stage methanol synthesis process that powered by renewable electricity: plasma-based CO.sub.2 pre-conversion followed by CO/CO.sub.2 catalytic hydrogenation. This approach addresses the issues of catalyst deactivation and high reaction temperatures associated with traditional thermocatalytic reverse water-gas shift reactions, while overcoming the thermodynamic limitations of direct CO.sub.2 hydrogenation. The plasma jet reactor exhibits high energy efficiency, with rapid start-up and shutdown capabilities, and can operate directly using fluctuating renewable energy.