The hydrogenation capacity of an upflow hydrocarbon hydrotreatment reactor is increased by expanding the gas-liquid contact surface.

A petroleum hydrocarbon multi-stage fluid catalytic reaction method and reactor are described. The method implements a sectional multi-stage reaction in one reactor and comprises primary-stage and secondary-stage catalytic cracking reactions of feedstock oil and primary-stage and secondary-stage catalytic cracking reactions of light hydrocarbons and/or cycle oil, which occur in different reaction regions of the reactor. The primary-stage reaction of the light hydrocarbon and/or circulation oil is carried out in an independent reaction region. The reactor comprises a first reaction section, a catalyst splitter, a third reaction section, a second reaction section and a settler.

The present disclosure relates to an apparatus for preparing an oligomer, including: a reactor receiving a monomer stream and performing an oligomerization reaction to prepare a reaction product; a product discharge line for transferring a reaction product stream discharged from the reactor; and a bubble catcher provided in any area of the product discharge line to remove bubbles contained in the reaction product stream.

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.

A method for facilitating the distribution of the flow of one or more streams within a bed vessel is provided. Disposed within the bed vessel are internal materials and structures including multiple operating zones. One type of operating zone can be a processing zone composed of one or more beds of solid processing material. Another type of operating zone can be a treating zone. Treating zones can facilitate the distribution of the one or more streams fed to processing zones. The distribution can facilitate contact between the feed streams and the processing materials contained in the processing zones.

The present invention relates to a fluidized bed gas distribution nozzle with the following features in its functional position: a gas inlet pipe (10), having: an inner surface (10i), an outer surface (10o), a lower end section (10l) adapted to receive gas from an associated gas source, an upper end section (10u), a plurality of openings (12) formed in the upper end section (10u), each opening (12) extending form the inner surface (10i) of the gas inlet pipe (10) to the outer surface (10o) of the gas inlet pipe (10), a gas distribution cap (20) connected or connectable to the gas inlet pipe (10), having: an upper top (20u), a lower bottom (20l) arranged at a vertical distance below said upper top (20u) and surrounding the gas inlet pipe (10), a peripheral wall (20w) having an inner surface (20i) and an outer surface (20o) and extending between said upper top (20u) and said lower bottom (20l), outlets (22) within the peripheral wall (20w) extending from the inner surface (20i) of the peripheral wall (20w) to the outer surface (20o) of the peripheral wall (20w).

A fluidized bed reactor, a device, and a method for producing low-carbon olefins from oxygen-containing compound are provided. The fluidized bed reactor includes a reactor shell, a reaction zone, a coke control zone and a delivery pipe, where there are n baffles arranged in the coke control zone, and the n baffles divide the coke control zone into n sub-coke control zones which include a first sub-coke control zone, a second sub-coke control zone, and an nth sub-coke control zone; at least one catalyst circulation hole is provided on each of the n-1 baffles, so that the catalyst flows in an annular shape in the coke control zone, where n is an integer. The device and method can be adapted to a new generation of DMTO catalyst, and the unit consumption of production ranges from 2.50 to 2.58 tons of methanol/ton of low-carbon olefins.

A fluidized bed reactor includes a main shell and a coke control zone shell; the main shell includes an upper shell and a lower shell; the upper shell encloses a gas-solid separation zone, and the lower shell encloses a reaction zone; the reaction zone axially communicates with the gas-solid separation zone; the coke control zone shell is circumferentially arranged on an outer wall of the main shell; the coke control zone shell and the main shell enclose an annular cavity, and the annular cavity is a coke control zone; n baffles are radially arranged in the coke control zone, and the n baffles divide the coke control zone into n coke control zone subzones, where n is an integer; the coke control zone subzones are provided with a coke control raw material inlet; and a catalyst circulation hole is formed in each of n-1 of the baffles.

A coke control reactor, and a device and method for preparing low-carbon olefins from an oxygen-containing compound are provided. The coke control reactor includes a coke control reactor shell, a reaction zone I, and a coke controlled catalyst settling zone; a cross-sectional area at any position of the reaction zone I is less than that of the coke controlled catalyst settling zone; n baffles are arranged in a vertical direction in the reaction zone I; the n baffles divide the reaction zone I into m reaction zone I subzones; and a catalyst circulation hole is formed in each of the baffles, such that a catalyst flows in the reaction zone I in a preset manner. A catalyst charge in the present coke control reactor can be automatically adjusted, and an average residence time of a catalyst in the coke control reactor can be controlled by changing process operating conditions.

A continuous acoustic chemical microreactor system is disclosed. The system includes a continuous process vessel (CPV) and an acoustic agitator coupled to the CPV and configured to agitate the CPV along an oscillation axis. The CPV includes a reactant inlet configured to receive one or more reactants into the CPV, an elongated tube coupled at a first end to the reactant inlet and configured to receive the reactants from the reactant inlet, and a product outlet coupled to a second end of the elongated tube and configured to discharge a product of a chemical reaction among the reactants from the CPV. The acoustic agitator is configured to agitate the CPV along the oscillation axis such that the inner surface of the elongated tube accelerates the one or more reactants in alternating upward and downward directions along the oscillation axis.