A method for producing an oligosilane including a reaction step of introducing a fluid containing a hydrosilane into a continuous reactor provided with a catalyst layer inside to produce an oligosilane from the hydrosilane and discharging a fluid containing the oligosilane from the reactor. The reaction step satisfies all of the following conditions (i) to (iii): (i) a temperature of the hydrosilane-containing fluid at an inlet of the catalyst layer is higher than a temperature of the oligosilane-containing fluid at an outlet of the catalyst layer; (ii) the temperature of the hydrosilane-containing fluid at the inlet of the catalyst layer is from 200 to 400 C.; and (iii) the temperature of the oligosilane-containing fluid at the outlet of the catalyst layer is from 50 to 300 C.

A catalyst filter basket for containing catalyst material within a catalytic chemical reactor. The catalyst filter basket includes a central frame having a base ring and a generally cylindrical inner screen portion which extends upwardly from the base ring. A generally cylindrical outer screen assembly is releasably secured to the central frame by a quick release mechanism.

Non-oxidative direct methane conversion (NDMC) to value-added products, such as H.sub.2, C.sub.2 hydrocarbons, and aromatics, occurs within a reactor heated to an elevated temperature. The reactor can have a first volume, where a feed gas including methane is provided, separated from a second volume, where a sweep gas is provided, by a dense thin film membrane supported on a porous wall. The thin film membrane is a mixed ionic-electronic permeable membrane that allows H2 generated in the first volume to be transported to the second volume for removal by (or reaction with) the sweep gas. A catalyst can be provided in or adjacent to the first volume. For example, the catalyst can be a metal doped quartz material (e.g., Fe(c)SiO.sub.2) or a metal/zeolite material (e.g., Mo/ZSM5). Methane conversion and/or product selectivity in the reactor can be manipulated by control of gas flow rates, reaction temperatures, and/or feed and sweep gas compositions.

An apparatus (10) and the use thereof for preheating at least one fluid are proposed. The apparatus (10) has a solid heating body (12). Channels (16) for passage of the fluid are formed in the heating body (12). The heating body (12) is heatable. The heating body (12) is designed to heat the fluid to a target temperature within a target time, wherein the target temperature is at least a temperature at which a predetermined chemical reaction of the fluid takes place with a predetermined conversion within a predetermined time. The target time is shorter than the predetermined time. The heating body (12), for preheating of the fluid, is heated to the target temperature and the fluid is passed through the channels (16) within the target time.

Various embodiments may include a reactor for carrying out equilibrium-limited reactions comprising: a reaction chamber for receiving a catalyst; a sorption chamber for receiving a sorption agent; a feedstock feeding device; a sorption agent feeding device; and a gas-permeable element separating the reaction chamber from the sorption chamber, wherein the gas-permeable element repels particles of the sorption agent.

A system for continuously treating recycled polymeric material includes a hopper configured to feed the recycled polymeric material into the system. An extruder can turn the recycled polymeric material in a molten material. In some embodiments, the extruder uses thermal fluids, electric heaters, and/or a separate heater. The molten material is depolymerized in a reactor. In some embodiments, a catalyst is used to aid in depolymerizing the material. In certain embodiments, the catalyst is contained in a permeable container. The depolymerized molten material can then be cooled via a heat exchanger. In some embodiments, multiple reactors are used. In certain embodiments, these reactors are connected in series. In some embodiments, the reactor(s) contain removable static mixer(s) and/or removable annular inserts.

A carbon monoxide oxidation device for oxidizing carbon monoxide contained in a hydrogen rich reformat gas includes a gas stream perturbation device designed as at least one propeller-shaped plate with a plate portion having a surface facing the gas stream and at least one blade which is connected to the plate portion and has a leading edge and an effluent edge, wherein a surface defined between leading edge and effluent edge is inclined in relation to the surface of the plate portion with a predetermined blade inclination angle, thereby defining at least one opening in the plate.

Reforming alcohol is disclosed. Alcohol is introduced into a conduit of an alcohol reformer so that the alcohol flows through a catalyst stage within the conduit. The catalyst stage includes an alcohol reforming catalyst, and a heat transfer member comprising thermally conductive material. The heat transfer member is in thermal contact with the conduit and the alcohol reforming catalyst. Simultaneously, exhaust gas is introduced from an internal combustion engine into an exhaust channel. The exhaust gas in the exhaust channel contacts fins extending outward from the conduit so that heat from the exhaust gas is transferred through the fins, the conduit, and the heat transfer member to the alcohol reforming catalyst.

Reaction methods are disclosed including induction catalysts. Such reactions may involve heating a catalyst by inductive heating; contacting the catalyst with a composition such that a reaction occurs and removing a reaction product. Example reactions include catalysts with ferrimagnetic metal oxide material and reactions involving organic reactants.

A reactor (1) delimited by a shell (2) extending along a vertical axis: a vessel provided with a reaction zone (10) containing a bed of catalyst; at least one inlet (3) for a gaseous feed; at least one outlet (4) for a gaseous effluent produced in the reaction zone (10),
inside the reaction zone (10), at least two tubes extending substantially vertically over the height of the reaction zone, the tubes being permeable to a gas phase and impermeable to catalyst, each tube (9) having an upper end (11) in communication with the inlet for the feed or with the outlet means for an effluent and an opposed second end (12), the tubes (9, 24) supported at their upper end by a first plate (14) which is secured to the shell (2), via a connection assembly providing a pivot and slide type connection.