In accordance with the present invention, there is provided a process for producing hydrogen and graphitic carbon from a hydrocarbon gas comprising: contacting at a temperature between 600° C. and 1000° C. the catalyst with the hydrocarbon gas to catalytically convert at least a portion of the hydrocarbon gas to hydrogen and graphitic carbon, wherein the catalyst is a low grade iron oxide.

A fluidizing nozzle for introducing fluid into a fluidized bed reactor and a fluidized bed reactor. The fluidizing nozzle includes a nozzle tube limiting at least a part of a feed channel in which fluid is configured to flow, at least one fluid discharge opening arranged near a downstream end of the nozzle tube, and a pot-like hood, which sealingly closes the nozzle tube with a hood cover of the pot-like hood at the downstream end of the nozzle tube at which said at least one fluid discharge opening is provided. The feed channel is provided with a flow restriction element defining at least one flow restriction feed channel upstream of said at least one fluid discharge opening.

An actuator is provided that includes a housing, a linear actuating shaft disposed within the housing, a piston coupled with the shaft, and a fluid barrier disposed on an end of the shaft and encircled by the piston. The piston is movable longitudinally between an extended configuration and a retracted configuration upon rotation of the shaft. The fluid barrier engages an inner surface of the piston preventing fluid communication across the fluid barrier. The fluid barrier has a shaft engaging side which receives the shaft and a fluid facing side. A cavity is formed between the piston and the fluid facing side and expands when the piston moves to the extended configuration and contracts when the piston moves to the retracted configuration. A port is disposed in the piston and extends from the cavity to external the piston thereby permitting fluid communication between the cavity and external the piston.

A combustor air bar grid for use within a fluidized bed reactor includes at least two main air collector bars in fluid communication with a source of fluidizing gas, a plurality of primary air bars that are transversal to the main air collector bars and arranged on the at least two main air collector bars such that the main air collector bars support them, and in fluid communication to at least two of the main air collector bars. The main air collector bars and the primary air bars define ash removal openings in the air bar grid and a plurality of fluidized nozzles are arranged to each of the primary air bars for fluidizing the bed reactor. A fluidized bed reactor includes such a combustor air bar grid.

A process for adjusting filling level in a gasifier for carbonaceous material in the form of a floating bed reactor in which biomass and/or coke (K) is transformed into a product gas includes providing a substantially conical, downwardly tapering floating bed reactor comprising an upper reactor ceiling a lower inlet opening into which biomass and/or coke (K) are introduced into the floating bed reactor from below and a gaseous gasification agent (V) is introduced upwardly, so that a fixed bed, which is elevated from the location of the inlet opening and held in suspension, forms within the conical reactor, wherein the flow rate of the gaseous gasification agent (V) together with the biomass and/or the coke (K) is adapted in such a way that a stable bed forms in the reactor.

A method of producing aluminum chlorohydrate comprises adding small form aluminum metal pellets to a reactant receiving space of a reactor tank to form a pellet bed; adding aqueous hydrochloric acid to the reactant receiving space of the reactor tank; and continuously circulating the aqueous hydrochloric acid through the pellet bed. In some embodiments, the continuously circulating aqueous hydrochloric acid dispels reaction gases from the pellet bed. Methods described herein can, in some cases, further comprise consecutively adding additional small form aluminum metal pellets to the reactant receiving space of the reactor tank as the small form aluminum metal pellets are consumed in the pellet bed.

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different.

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different.

The present invention pertains to improved processes and catalysts for aromatization. The processes generally contacting a feed stream comprising a naphtha fraction having a C.sub.6 to C.sub.8 content with a catalyst pellet composition to form aromatic hydrocarbons. The catalyst pellet composition generally comprises a plurality of cylindrical pellets each pellet comprising a Group VIII metal on a zeolite. The pellets may have (a) a plurality of holes passing through the length of the cylindrical pellets, (b) a dome-shaped top and bottom, and (c) a plurality of semi-circular grooves along the length of the exterior of the cylinder.

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different.