A method for circulating a cooled regenerated catalyst comprises the following steps: a regenerated catalyst derived from a regenerator is cooled to 200-720° C. by a catalyst cooler, which either directly enters into a riser reactor 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; the reaction product is introduced into a settling vessel to separate the catalyst and oil gas; the separated catalyst ready for regeneration is stream-stripped in a stream stripping phase and enters the regenerator for regeneration through charring; after cooling, the regenerated catalyst returns to the riser reactor for recycling.

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.

Provided are a method for the catalytic conversion of hydrocarbons with a downer reactor and a device thereof. The specific process of the method is as follows: a raw material of hydrocarbons after being pre-heated (or not) and a low-temperature regenerant from a regenerant cooler entering an entry end of a downer reactor, flowing down along the reactor for reactions such as catalytic cracking, and a mixture of a reactive oil and gas and a catalyst descending to the end of the reactor for rapid separation, thereby achieving the rapid separation of the catalyst and the oil and gas. The main operation conditions thereof are as follows: the reaction temperature is 460 to 680° C., the reaction pressure is 0.11 to 0.4 MPa, the contact time is 0.05 to 2 seconds, and the weight ratio of the catalyst to the raw material (a catalyst-to-oil ratio) is 6 to 50. The separated catalyst to be regenerated (abbreviated as a spent agent) is stripped by means of a stripper, and enters a regenerator and is burned for regeneration, wherein the regeneration temperature is controlled at 630-730° C. The regenerant from the regenerator enters the regenerant cooler to be cooled to 200-720° C., and then enters the downer reactor 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.

Compositions and methods for restoring catalytic activity by dissolving soft coke with a solvent, one method including detecting soft coke deposition on a catalyst composition; preparing an aromatic bottoms composition with a Hildebrand solubility parameter of at least about 20 SI to remove the soft coke from the catalyst composition; and washing the catalyst composition with the aromatic bottoms composition until at least a portion of the soft coke deposition is removed.

Methods and systems for enhancing hydrocarbon processing in a fluid catalytic cracking (FCC) unit by introducing a renewable feedstock into the FCC unit at alternative locations of the FCC unit to increase residence time and promote a higher degree of FCC feedstock cracking. The renewable feedstock may include one or more of plastic-derived pyrolysis oil or plastic-derived hydrocarbons, biomass-derived pyrolysis oil, municipal waste-derived pyrolysis oil, vegetable based feedstock, animal fat feedstock, algae oil, sugar-derived hydrocarbons, or carbohydrate-derived hydrocarbons. The alternative locations of the FCC unit may include one or more of FCC reactor catalyst bed, an FCC catalyst stripper, at a nozzle located downstream of a gas oil injection point, or at a nozzle located upstream of the gas oil injection point.

The present invention addresses to a process for the production of aromatic compounds from streams containing linear chains with 5 to 18 carbon atoms, of fossil or renewable origin, and application in the field of catalytic cracking aiming at a regenerator operation at much lower temperature, between 480° C. and 620° C., preferably the temperature should be between 500° C. and 600° C. The coked catalyst generated by the cracking of light streams with low potential for delta coke generation can have the combustion effected at a lower temperature. The regeneration temperature must be at least 40° C. and at most 100° C. higher than the reaction temperature, keeping the catalyst circulation high to maintain the energy balance in the reaction section. The minimum regeneration temperature can be ensured by installing an air preheating furnace before entering the regenerator and passing through the air distributor inside the regenerator. The used catalyst must contain zeolite with pores of intermediate size. Such conditions greatly favor the production of aromatics and the octane rating of the produced naphtha.

Systems and methods for the catalytic cracking of light hydrocarbons, such as naphtha, to form light olefins and aromatics is disclosed. The systems and methods may include a catalytic cracking process that involves mixing catalyst with a gas and then this mixture is used to contact a hydrocarbon feed, e.g., light straight run naphtha or heavy straight run naphtha. The hydrocarbon feed may be mixed with dry gas such as methane and/or hydrogen to dilute the hydrocarbon feed, before the hydrocarbon feed is contacted with the catalyst/gas mixture.

A FCC process including the steps of (a) adding a crude lignin oil (CLO) to a FCC unit, wherein the FCC unit has a FCC riser, a catalyst regenerator and a reactor/stripper, wherein CLO is a crude lignin oil composition including lignin and a polar organic solvent in 1:10 to 1:0.3 w/v ratio, (b) optionally adding a second feed including a conventional FCC feedstock to the FCC unit, (c) adding a regenerated catalyst from the regenerator to the FCC riser for catalytic cracking and upgrading the CLO and second feedstock to produce upgraded products and deactivated catalyst, (d) adding the upgraded products and deactivated catalyst from the FCC riser to the reactor/stripper and separating upgraded products from deactivated catalyst in the reactor/stripper, (e) adding the deactivated catalyst from (d) to the regenerator to regenerate the deactivated catalyst to provide regenerated catalyst; and
collecting the upgraded products.

Disclosed is a method of catalytically cracking naphtha in a fluidized bed. Effluent from the fluidized bed is separated into catalyst particles and gas product by a cyclone having a loop seal connected to the cyclone's dipleg.