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 fixed bed arrangement formed as an insert for a reactor for catalytic conversion of reaction media, in particular for catalytic methanation of a gas mixture including hydrogen and carbon dioxide, having a receiving chamber, which extends axially within an outer sleeve, and through which reaction media flows during the reactor operation for receiving a catalyst material, and a heat exchanger arrangement having a fluid flow path for a temperature control fluid, which fluid flow path is spatially separated from the receiving chamber, for removing and supplying heat from/to the process. The outer sleeve is formed by the heat exchanger arrangement, at least in regions. The fixed bed arrangement includes a reactor for the catalytic reaction of reaction media having a pressure chamber for receiving reaction media, and such a fixed bed arrangement inserted into the pressure chamber.

A fluidized apparatus contains a double-trapezoid structural member. These fluidized apparatuses are used in the nitro compound hydrogenation reaction process. The fluidized apparatus includes a shell, a gas distributor, and an inner chamber defined by an inner wall of said shell and an upper surface of said gas distributor, in the middle region of said inner chamber is disposed a perforated plate, the perforated plate comprise an outer edge region and a center region, assuming the opening rate of the outer edge region is A1 (the unit is %), assuming the opening rate of the center region is A2 (the unit is %), then A1/A2=0-0.95.

The present invention relates to a nitro compound hydrogenation reaction process and hydrogenation reaction apparatus, which can achieve the objects of the continuous reaction of the nitro compound and the long-period run of regeneration and activation. The nitro compound hydrogenation reaction process comprises a hydrogenation step, a regeneration step, an optional activation step and a recycling step. There exists at least one step of degassing the spent catalyst between the hydrogenation step and the regeneration step. According to circumstances, there exists at least one step of degassing the regenerated catalyst between the regeneration step and the activation step.

A load-following reactor system and associated facilities for improved control of a reactor under varying loads. The load-following reactor may be a tube-cooled reactor for methanol synthesis. A reactant may be controlled by at least one valve element such that a portion of the reactant is fed to the reactor through the reactor tubes, and a portion of the reactant is fed to the reactor after being heated in a heat exchanger. The heated portion of the reactant may be fed to the reactor after the tubes. The valve element may be controlled based on a temperature of the reactor and/or a flowrate of reactant feed to adapt the temperature of the reactor to the changing reactant flowrate.

The present disclosure discloses a fluidized bed cooler with regional coordination enhancement, comprising a shell, a catalyst inlet, an interior of the shell is divided into a catalyst inlet influence region, a dilute phase region, a dense phase region and a gas distributor influence region; a catalyst inlet inclined tube is provided obliquely upward at the catalyst inlet, and a regional particle distributor is provided at the catalyst inlet; the dense phase region is provided with a plurality of dense phase baffle plates, and the dilute phase region is provided with a plurality of dilute phase baffle plates; and the gas distributor influence region is provided with double gas distributors. The fluidized bed cooler simultaneously well solves the low internal stability and the low heat exchange efficiency of the fluidized bed cooler, thereby realizing the stable and efficient operation of the fluidized bed cooler.

A multi-stage product gas generation system converts a carbonaceous material, such as municipal solid waste, into a product gas which may subsequently be converted into a liquid fuel or other material. One or more reactors containing bed material may be used to conduct reactions to effect the conversions. Unreacted inert feedstock contaminants present in the carbonaceous material may be separated from bed material using a portion of the product gas. A heat transfer medium collecting heat from a reaction in one stage may be applied as a reactant input in another, earlier stage.

Electrically heated reforming reactors and associated reforming processes are disclosed, which benefit from a number of advantages in terms of attaining and controlling the input of heat to catalytic conversion processes such as in the reforming of hydrocarbons (e.g., methane) using H.sub.2O and/or CO.sub.2 as an oxidant. The disclosed reactors provide the ability to target the input of heat to specific regions within a catalyst bed volume. This allows for the control of the temperature profile in one or more dimensions (e.g., axially and/or radially) and/or otherwise tailoring heat input for processing specific reformer feeds, achieving specific reformer products, effectively utilizing the catalyst, and/or compensating for a number of operating parameters (e.g., flow distribution). Dynamic control of the heat input may be used in response to changes in feed or product composition and/or catalyst activity.

A reformer tube for producing synthesis gas by steam reforming of hydrocarbon-containing input gases is proposed where an outer shell tube is divided by means of a separating tray into a reaction chamber and an exit chamber, a dumped bed of a steam-reforming-active solid catalyst is arranged in the reaction chamber, at least one heat exchanger tube is arranged inside the reaction chamber and inside the dumped catalyst bed, whose entry end is in fluid connection with the dumped catalyst bed and whose exit end is in fluid connection with the exit chamber, the exit end of the heat exchanger tube is fed through the separating tray and opens out into a corrosion-protected inner tube which is disposed in the interior of the shell tube and is in fluid connection with a collection conduit for the synthesis gas product, and a gas-permeable thermal insulation layer is arranged between the inner wall of the shell tube and the outer wall of the inner tube.

The present invention relates generally to an apparatus for housing a chemical looping process comprising of at least one fluidized-bed combustor reactor, at least one entrained riser, at least one particle separator, optionally at least one particle holding reactor, at least one moving-bed reactor, at least one standpipe, at least one L-valve system for solid flow control and interconnecting sections.