The present invention relates to the technical field of petroleum hydrocarbon catalytic conversion, referring to a multi-stage fluidized catalytic reaction process of petroleum hydrocarbon. In the present reaction process, multi-stage reaction takes place in the same reactor, including first order reaction and the second order reaction of FCC feedstock oil, cracking reaction process of light hydrocarbons and/or cycle oil. In the present process, catalyst replacement and two-stage relayed reaction takes place between the first and second order reaction of feedstock oil. Two-stage reaction of light hydrocarbons and/or cycle oil takes place too. These reactions take place in different region in the same one reactor. The first order reaction of light hydrocarbons and/or cycle oil takes place in independent region. In the present invention, catalytic cracking conversion of catalytic feedstock oil, light hydrocarbon and cycle oil takes place in respective reaction region and reaction condition. Multi-stage and stepped selectivity control of catalyst and reaction temperature is realized. Multi-stage reaction and stepped arrangement of temperature is realized in the same reactor. It could improve the yield and selectivity of olefin, and decrease the yield of by-products such as coke obviously.

A method for circulating a cooled regenerated catalyst comprises the following steps: a regenerated catalyst derived from a regenerator (5) is cooled to 200-720 C. by a catalyst cooler (8A), which either directly enters into a riser reactor (2) without mixing with hot regenerated catalyst, or enters the same after mixing with another portion of uncooled hot regenerated catalyst and thereby obtaining a hybrid regenerated catalyst with its temperature lower than that of the regenerator; a contact reaction between a hydrocarbon raw materials and the catalyst is performed in the riser reactor (2); the reaction product is introduced into a settling vessel (1) to separated the catalyst and oil gas; the separated catalyst ready for regeneration is stream-stripped in a stream stripping phase (1A) and enters the regenerator (5) for regeneration through charring; after cooling, the regenerated catalyst returns to the riser reactor (2) for recycling.

An integrated hydrotreating and hydrocracking process includes contacting a hydrocarbon oil stream with a hydrogen stream and a hydrotreating catalyst in a moving-bed hydrotreating reactor, thereby producing a hydrocarbon product stream and a spent hydrotreating catalyst; contacting the hydrocarbon product stream with a second hydrogen stream and a hydrocracking catalyst in a hydrocracking reactor, thereby producing a hydrocracked hydrocarbon product stream; processing the spent hydrotreating catalyst to produce regenerated hydrotreating catalyst; and recycling the regenerated hydrotreating catalyst to the moving-bed hydrotreating reactor.

Apparatus and processes herein provide for converting hydrocarbon feeds to light olefins and other hydrocarbons. The processes and apparatus include a conventional riser reactor in combination with a mixed flow (e.g., including both counter-current and co-current catalyst flows) fluidized bed reactor designed for maximizing light olefins production. The effluents from the riser reactor and mixed flow reactor are processed in a catalyst disengagement vessel, and the catalysts used in each reactor may be regenerated in a common catalyst regeneration vessel. Further, integration of the two-reactor scheme with a catalyst cooler provides a refinery the flexibility of switching the operation between the two-reactor flow scheme, a catalyst cooler only flow scheme, or using both simultaneously.

The present invention relates to a gas-solid separation device specially adapted to the external risers of catalytic cracking units. The device comprises a pipe (19) forming substantially an angle of 90 with respect to a riser (2), said pipe (19) dividing into two tubular sections (4) forming between them an angle 2*, being between 5 and 85. This device simultaneously makes it possible to channel the stripping gases and improves the overall efficiency of the separation by virtue of better control of the contact time. The present invention also relates to a catalytic cracking process using said gas-solid separation device.

A catalytic reactor comprises a filter unit which extracts and collects particles from the fluid flow stream above the reactor internals, the filter unit comprises elements which are safely, easily and quickly handled without the need for tools.

A process is presented for the management of sulfur on a catalyst. The catalyst is a dehydrogenation catalyst, and sulfur accumulates during the dehydrogenation process. Sulfur compounds are stripped from the spent catalyst and the catalyst is cooled before the regeneration process. The process includes controlling the amount of sulfur that needs to be removed from the catalyst before regeneration.

A process is presented for the management of sulfur on a catalyst. The catalyst is a dehydrogenation catalyst, and sulfur accumulates during the dehydrogenation process. Sulfur compounds are stripped from the spent catalyst and the catalyst is cooled before the regeneration process. The process includes controlling the amount of sulfur that needs to be removed from the catalyst before regeneration.

A process and apparatus for catalytically cracking fresh heavy hydrocarbon feed to produce cracked products is disclosed. A fraction of the cracked products can be obtained to re-crack it in a downer reactor. The downer reactor may produce high selectivity to light olefins. Spent catalyst from both reactors can be regenerated in the same regenerator.

Systems and methods are provided for selective oxidation of CO and/or C.sub.3 hydrocarbonaceous compounds in a reaction environment including hydrocarbons and/or hydrocarbonaceous components. The selective oxidation can be performed by exposing the CO and/or C.sub.3 hydrocarbonaceous compounds to a catalytic metal that is encapsulated in a small pore zeolite. The small pore zeolite containing the encapsulated metal can have a sufficiently small pore size to reduce or minimize the types of hydrocarbons or hydrocarbonaceous compounds that can interact with the encapsulated metal.