A regeneration method for catalytic cracking reaction, the method is applied in a catalytic reaction process of petroleum hydrocarbon materials, and the method comprises: feeding the regenerated and semi-regenerated catalyst from a regenerator separately into different positions of a reactor for reaction. A part of the semi-regenerated catalyst is firstly processed in a purification cooler for removing carried nitrogen, oxygen, carbon dioxide and impurity gases before being fed into the reactor. Spent catalyst or the purified and cooled semi-regenerated catalyst is fed into a catalyst mixing section of the reactor for controlling the temperature of the catalyst being contact with the oil material to be gasified, thereby achieving a three stage cycle of the catalyst in the reactor and a three stage control for the reaction outlets of the oil material gasification zone and the cracking reaction zone and the catalyst taking part in the reaction.

The present invention relates to a method for improving the cooling capacity of a gas solids olefin polymerization reactor by splitting the fluidization gas and returning part of the fluidization gas to the reactor into the bottom zone of the reactor and another part of the fluidization gas directly into the dense phase formed by particles of a polymer of the at least one olefin suspended in an upwards flowing stream of the fluidization gas in the middle zone of the reactor.

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.

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.

The present disclosure provides a method and an apparatus for integrating pressurized hydrocracking of heavy oil and coke gasification. A coupled reactor having a cracking section and a gasification section is used in the method: a heavy oil feedstock and a hydrogenation catalyst are fed into a cracking section, to generate light oil-gas and coke; the coke is carried by the coke powder into the gasification section, to generate syngas; a regenerated coke powder is returned to the cracking section; the syngas enters the cracking section and merges with light oil-gas, and enters a gas-solid separator, to separate out first-stage solid particles and second-stage particles in sequence, and a purified oil-gas product is collected; oil-gas fractionation of the purified oil-gas product is performed, and a light oil product and a syngas product are collected. Yield and quality of the light oil can be improved by the method.

A process for recovering catalyst from a fluidized catalytic reactor effluent is disclosed comprising reacting a reactant stream by contact with a stream of fluidized catalyst to provide a vaporous reactor effluent stream comprising catalyst and products. The vaporous reactor effluent stream is contacted with a liquid coolant stream to cool it and transfer the catalyst into the liquid coolant stream. A catalyst lean vaporous reactor effluent stream is separated from a catalyst rich liquid coolant stream. A return catalyst stream is separated from the catalyst rich liquid coolant stream to provide a catalyst lean liquid coolant stream, and the return catalyst stream is transported back to said reacting step.

The present disclosure includes a system for producing low carbon olefins and/or aromatics from raw material comprising naphtha. The system can include a reaction unit that includes a fast fluidized bed reactor, a stripping unit that includes a stripper, and a regeneration unit. The reactor unit is adapted to allow the catalytic cracking of naphtha and to output reaction unit effluent material (spent catalyst and product gas) into the stripping unit, which is adapted to output product gas. The stripping unit is connected to and in fluid communication with the regeneration unit such that the stripping unit supplies the spent catalyst from the reaction unit to regeneration unit. The regeneration unit is adapted to regenerate the spent catalyst to form regenerated catalyst. The regeneration unit is connected to and in fluid communication with the fast fluidized bed reactor such that, in operation, regenerated catalyst can be sent to the fast fluidized bed reactor of the reaction unit.

A coupling reaction apparatus for heavy oil cracking-gasification, including a cracking section and a gasification section communicated with each other, and the cracking section is located above the gasification section; the cracking section is provided with a heavy oil raw material inlet and a fluidizing gas inlet, and an upper part of the cracking section is provided with an oil-gas outlet; and the gasification section is provided with a gasification agent inlet.

The present invention relates to a process for removing polymer material from a gas-solids olefin polymerization reactor wherein the gas-solids olefin polymerization reactor is connected to the top part of an outlet vessel via a feed pipe wherein the powder surface of discharged polymer material and the barrier gas injection point are situated in the outlet vessel as such to fulfill the following criteria: R′=X/Y≤2.0; and R″=X/D≥1.0; wherein X=Distance between the powder surface and the barrier gas injection point; Y=Distance between the barrier gas injection point and the vessel outlet; and D=Equivalent outlet vessel diameter, an apparatus for continuously removing polymer material comprising a gas-solids olefin polymerization reactor, an outlet vessel and a feed pipe connecting the gas-solids olefin polymerization reactor with the top part of the outlet vessel and the use of said apparatus for polymerizing alpha-olefin homo- or copolymers having alpha-olefin monomer units of from 2 to 12 carbon atoms and for increasing the barrier gas efficiency of the gas-solids olefin reactor to at least 75%.

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.