A turbulent fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, resolving or improving the competition problem between an MTO reaction and an alkylation reaction during the process of producing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and toluene, and achieving a synergistic effect between the MTO reaction and the alkylation reaction. By controlling the mass transfer and reaction, competition between the MTO reaction and the alkylation reaction is coordinated and optimized to facilitate a synergistic effect of the two reactions, so that the conversion rate of toluene, the yield of para-xylene, and the selectivity of light olefins are increased. The turbulent fluidized bed reactor includes a first reactor feed distributor and a number of second reactor feed distributors and are arranged sequentially along the gas flow direction.

A process comprising polymerizing olefin monomers and optionally comonomers in a first reactor vessel, thereby forming a raw product stream comprising polymerized solids, unreacted monomer and optionally comonomer, the polymerized solids comprising olefin polymer, volatile organic compounds (VOC) and catalyst system. Then the polymerized solids are contacted with a catalyst poison selected from carbon monoxide, carbon dioxide, oxygen, water, alcohols, amines, or mixtures thereof, thereby forming a passivated stream. The passivated stream is maintained in an agitated state within a second reactor. The passivated stream within the second reactor is then contacted with a circulating gas comprising unreacted monomer for a residence time, thereby reducing the concentration of VOC in the polymerized solids by at least 10 wt % compared to the level before entering the second reactor, thereby forming a purified olefin polymer solids stream.

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.

In an FCC apparatus and process structured packing should be located at the very top of the stripping section in an upper region. The lower region below the structural packing may be equipped with fluidization equipment such as stripping media distributors and one or more gratings. This arrangement enables stripping of entrained hydrocarbons off the incoming catalyst immediately upon entry into the stripping section allowing the entrained hydrocarbon to exit the stripping section with minimized residence time to minimize post-riser cracking. Revamp of stripping sections with tall stripping sections should conducted in this way to improve performance and reduce down-time for equipment installation.

A reactor for producing a synthesis gas from a fuel, with a housing (2) with a combustion part accommodating a first fluidized bed in operation, a riser (3) extending along a longitudinal direction of the reactor (1) and accommodating a second fluidized bed in operation, a down-comer (4) positioned parallel to the riser and extending into the first fluidized bed, and one or more feed channels (33) for providing the fuel to the reactor (1). The reactor (1) further has a riser air chamber section (B) connected to a lower part of the riser (3), the riser air chamber section (B) comprising a cylindrical wall (28) with a plurality of circumferentially located holes (24, 25).

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 the 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 catalyst bed and whose exit end is in fluid connection with the exit chamber, wherein gas-contacted parts of the reformer tube, in particular the at least one heat exchanger tube, are fabricated from a nickel-based alloy and coated on their inside with an aluminum diffusion layer.

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include, in some embodiments, feeding a hydrocarbon, a first catalyst and a second catalyst to a reactor, wherein the first catalyst has a smaller average particle size and is less dense than the second catalyst. A first portion of the second catalyst may be recovered as a bottoms product from the reactor, and a cracked hydrocarbon effluent, a second portion of the second catalyst, and the first catalyst may be recovered as an overhead product from the reactor. The second portion of the second catalyst may be separated from the overhead product, providing a first stream comprising the first catalyst and the hydrocarbon effluent and a second stream comprising the separated second catalyst, allowing return of the separated second catalyst in the second stream to the reactor.

A reactor for producing a synthesis gas from a fuel, with a housing (2) with a combustion part accommodating a first fluidized bed in operation, a riser (3) extending along a longitudinal direction of the reactor (1) and accommodating a second fluidized bed in operation, a down-comer (4) positioned parallel to the riser and extending into the first fluidized bed, and one or more feed channels (33) for providing the fuel to the reactor (1). The reactor (1) further has a riser air chamber section (B) connected to a lower part of the riser (3), the riser air chamber section (B) comprising a cylindrical wall (28) with a plurality of circumferentially located holes (24, 25).

An apparatus includes a riser reactor within the reaction vessel. The riser reactor defines a longitudinal axis and including a riser reactor inlet at one end and at least one riser reactor outlet at an opposite end. The apparatus includes a separation vessel including at least one separation chamber and at least one collection chamber distributed in an alternating manner about the longitudinal axis. Each separation chamber comprises two vertical lateral walls which also comprise a wall of an adjacent one of the at least one collection chamber. A lateral separation chamber outlet is defined in at least one of the vertical lateral walls to provide fluid and particle communication from the lateral separation chamber to the adjacent one of the at least one collection chamber. The separation vessel includes at least one collection chamber deflector positioned in the at least one collection chamber.

A multi-zoned fluidized bed reactor system may include a multi-zoned fluidized bed reactor and at least one catalyst regeneration loop. The multi-zoned fluidized bed reactor comprising a housing, a fluid bed distributor plate positioned at the bottom of the housing, a fluidized catalyst bed disposed vertically above the fluid bed distributor plate and a condensation zone disposed vertically above the fluidized catalyst bed. The at least one catalyst regeneration loop may be fluidly coupled to the stripping zone and a reaction zone. The at least one catalyst regeneration loop may be operable to withdraw a portion of spent catalyst from the stripping zone, regenerate the portion of spent catalyst to produce regenerated catalyst, and return the regenerated catalyst to the reaction zone. A method of regenerating catalyst in a multi-zoned fluidized bed reactor may include passing a portion of spent catalyst from a stripping zone to a catalyst regeneration loop.