Bubble column reactor assemblies are provided, an assembly (100) comprising: a reactor vessel (102) comprising a bottom end and a top end. A pre-distributor plate (114) having a bottom surface and a top surface, disposed in the 5 reactor vessel (102) such that the bottom surface faces the bottom end of the reactor vessel (102). A gas distributor (106) is disposed below the pre-distributor plate (114) to receive and inject gas into a liquid prior to distribution of gas and liquid by the pre-distributor plate (114). The gas distributor (106) comprises: a common manifold (108) and a plurality of ring-shaped pipes disposed along a length of the 10 common manifold (108); and a plurality of nozzles disposed along an outer circumference of each ring-shaped pipe of the plurality of ring-shaped pipes to inject gas and create vortexes for uniform distribution of the gas in the liquid.

According to one or more embodiments, a chemical feed distributor may include a chemical feed inlet, a body, a plurality of primary chemical feed outlets, and a secondary chemical feed outlet. The chemical feed inlet may pass a chemical feed stream into the chemical feed distributor. One or more walls of the body may define an elongated chemical feed stream flow path. The plurality of primary chemical feed outlets may be spaced along at least a portion of the length of the elongated chemical feed stream flow path and may be operable to pass a first portion of the chemical feed stream out of the feed distributor and into a vessel. The secondary chemical feed outlet may be downstream of the plurality of primary chemical feed outlets and may be operable to pass a second portion of the chemical feed stream out of the chemical feed distributor.

A fluidized bed processing system include a vessel having a vessel wall and a plurality of chemical feed distributors coupled to the vessel wall and extending into an internal volume of the vessel. Each of the chemical feed distributors includes a distributor body forming a chemical feed flow path and a plurality of chemical feed outlets. The fluidized bed processing system further includes at least one intermediate beam having at plurality of slots spaced apart along a beam length. That intermediate beam is coupled to the vessel wall at both ends, each chemical feed distributor passes through one slot of the intermediate beam, and the intermediate beam provides vertical support for each of the plurality of chemical feed distributors. The fluidized bed processing system can include lateral guides. The intermediate beams and lateral guides support the chemical feed distributors vertically and laterally.

Disclosed are a reaction tower, a production system, and a production method for producing potassium manganate. The reaction tower includes a reaction tower body and a bubble generator. The reaction tower body has a reaction chamber. The bubble generator includes an outer housing. The outer housing is disposed in the reaction chamber and has a gas flow channel therein. The outer housing is configured to direct an external reactant gas into the gas flow channel. The outer housing is provided with multiple first pores each having a diameter less than 10 mm, via which the gas flow channel communicates with the reaction chamber. The reaction tower is used in the production system. The reactant gas is introduced into the reaction chamber in the form of small bubbles by the action of the bubble generator, to increase the area of contact of the reactant gas with manganese ore powder and lye.

In a process as disclosed according to the present invention, gases or gas mixtures used to form a reactant mixture in an at least temporarily ignitable composition are fed into a mixing chamber (11) through the passages (131) in a boundary wall (13) of the mixing chamber (11) and by means of one or more feed conduits (14) which have feed orifices (141) and extend into the mixing chamber (11), respectively. The present invention likewise provides a corresponding reactor (1).

A fluidized bed reactor for producing para-xylene and co-producing light olefins from benzene and methanol and/or dimethyl ether, including a first distributor and a second distributor. The first distributor is located at the bottom of the fluidized bed, and the second distributor is located at the downstream of the first distributor along a gas flow direction. Also, a method for producing para-xylene and co-producing light olefins, including the following steps: a material stream A enters a reaction zone of the fluidized bed reactor from the first gas distributor; a material stream B enters the reaction zone of the fluidized bed reactor from the second gas distributor; a reactant contacts a catalyst in the reaction zone to generate a gas phase stream comprising para-xylene and light olefins.

A fast fluidized bed reactor, device and method for preparing para-xylene and co-producing light olefins from methanol and/or dimethyl ether and benzene, 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 benzene, 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 benzene, the yield of para-xylene, and the selectivity of light olefins are increased.

Provided are a method for producing hydrocyanic acid and a device for producing hydrocyanic acid, which can improve a yield of the hydrocyanic acid in a vapor phase contact ammoxidation reaction of methanol. The method for producing hydrocyanic acid includes a step of obtaining hydrocyanic acid by a vapor phase contact ammoxidation reaction by supplying a raw material gas including methanol in a fluidized bed reactor (1) through a raw material gas disperser (7) disposed in the fluidized bed reactor (1) and bringing the methanol into contact with ammonia and oxygen in the presence of a metal oxide catalyst, in which the raw material gas disperser (7) has one or more pores for releasing the raw material gas into the fluidized bed reactor (1), and the number of pores per unit cross-sectional area of the fluidized bed reactor (1) is 10 to 45 pieces/m.sup.2.

Disclosed are a reaction tower, a production system, and a production method for producing potassium manganate. The reaction tower includes a reaction tower body and a bubble generator. The reaction tower body has a reaction chamber. The bubble generator includes an outer housing. The outer housing is disposed in the reaction chamber and has a gas flow channel therein. The outer housing is configured to direct an external reactant gas into the gas flow channel. The outer housing is provided with multiple first pores each having a diameter less than 10 mm, via which the gas flow channel communicates with the reaction chamber. The reaction tower is used in the production system. The reactant gas is introduced into the reaction chamber in the form of small bubbles by the action of the bubble generator, to increase the area of contact of the reactant gas with manganese ore powder and lye.

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in.sup.−1 to 5 in.sup.−1, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr.sup.−1)(gal.sup.−1) to 6.0 (lb)(hr.sup.−1)(gal.sup.−1).