Provided is a process capable of converting the cokes on spent catalysts in a fluid catalytic cracking (FCC) process into synthesis gas. The produced synthesis gas contains high concentrations of CO and H.sub.2 and may be utilized in many downstream applications such as syngas fermentation for alcohol production, hydrogen production and synthesis of chemical intermediates. A reducer/regenerator reactor for a fluid catalytic process comprising a chemical looping system to produce synthesis gas is also described.

Disclosed herein is an apparatus and a method for catalytic conversion of chemical substances in the presence of pulverulent catalysts in a trickle bed reactor with residence times in the range of 0.1-10 seconds, wherein the apparatus includes a trickle bed reactor (2), the inlet side of which is functionally connected to a catalyst reservoir vessel (1) and a reactant feed, and the outlet side of which is functionally connected to a separator (3). The separator (3) has an exit conduit for leading off product stream, wherein the apparatus has the characteristic feature that the exit conduit disposed on the separator (3) for leading off product stream has a continuously acting valve connected via a controller to a pressure measurement sensor, wherein the continuously acting valve and the pressure measurement sensor form a pressure control circuit with a controller.

An apparatus for continuous preparation of carbon nanotubes, based on a fluidized bed reactor. The fluidized bed reactor comprises an annular varying diameter zone, a raw material gas inlet, a catalyst feeding port, a protective gas inlet, and a pulse gas controller. The annular varying diameter zone is located at a zone from a ¼ position starting from the bottom to the top. The pulse gas controller is disposed at the arc-shaped top portion of the annular varying diameter zone. The catalyst feeding port is located at the top of the fluidized bed reactor. The raw material gas inlet and the protective gas inlet are located at the bottom of the fluidized bed reactor. The device is also provided with a product outlet and a tail gas outlet. The device has a simple structure and low cost, is easy to operate, has a high raw material utilization rate, can effectively control the problem of carbon deposition on the inner wall of a primary reactor, can manufacture high-purity carbon nanotubes, and is suitable for large-scale industrial production.

A regenerator vessel for adsorbing halogen-containing material from a regenerator vent gas stream has a plurality of catalyst nozzles disposed at a top portion of the regenerator vessel. A first gas outlet is associated with a chlorination zone, and a second gas outlet associated with a combustion zone. A drying zone is in fluid communication with an air heater and the drying zone located in a bottom portion of the regenerator vessel. The first gas outlet is configured to withdraw a first gas stream from the chlorination zone and the second gas outlet is configured to withdraw a second gas stream from the combustion zone. The top portion of the regenerator vessel has an adsorption zone having a vent gas inlet port, a vent gas outlet port, and a portion of an annular catalyst bed.

A steam-assisted catalytic cracking process for a hydrocarbon feed is provided. The process includes: introducing the hydrocarbon feed, a fluid catalytic cracking (FCC) catalyst, and steam to a FCC reactor with a mass ratio of steam to hydrocarbon feed between 0.05 and 1.0; cracking the hydrocarbon feed in the presence of the FCC catalyst and steam to produce a cracked hydrocarbon feed and spent FCC catalyst, the spent FCC catalyst comprising coke deposits and hydrocarbon deposits; stripping the hydrocarbon deposits from the spent FCC catalyst with steam in a stripper to obtain a hydrocarbon-stripped spent FCC catalyst; regenerating the hydrocarbon-stripped spent FCC catalyst in a regenerator by subjecting the stripped spent FCC catalyst to heat in the presence of oxygen to combust the coke deposits on the stripped spent FCC catalyst and produce a regenerated FCC catalyst; recycling the regenerated FCC catalyst.

The present disclosure discloses a fluidized bed cooler with regional coordination enhancement, comprising a shell, a catalyst inlet, an interior of the shell is divided into a catalyst inlet influence region, a dilute phase region, a dense phase region and a gas distributor influence region; a catalyst inlet inclined tube is provided obliquely upward at the catalyst inlet, and a regional particle distributor is provided at the catalyst inlet; the dense phase region is provided with a plurality of dense phase baffle plates, and the dilute phase region is provided with a plurality of dilute phase baffle plates; and the gas distributor influence region is provided with double gas distributors. The fluidized bed cooler simultaneously well solves the low internal stability and the low heat exchange efficiency of the fluidized bed cooler, thereby realizing the stable and efficient operation of the fluidized bed cooler.

A regenerator vessel for adsorbing halogen-containing material from a regenerator vent gas stream has a plurality of catalyst nozzles disposed at a top portion of the regenerator vessel. A first gas outlet is associated with a chlorination zone, and a second gas outlet associated with a combustion zone. A drying zone is in fluid communication with an air heater and the drying zone located in a bottom portion of the regenerator vessel. The first gas outlet is configured to withdraw a first gas stream from the chlorination zone and the second gas outlet is configured to withdraw a second gas stream from the combustion zone. The top portion of the regenerator vessel has an adsorption zone having a vent gas inlet port, a vent gas outlet port, and a portion of an annular catalyst bed.

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

Methods and systems for producing pyrolysis products from a mixed plastics stream are described herein. The method may include conducting pyrolysis of a plastic feedstock to produce a stream of plastic pyrolysis oil; feeding a catalytic cracking feed stream and a catalyst from a catalyst regenerator into a fluidized bed reactor, where the catalytic cracking feed stream comprises the plastic pyrolysis oil; cracking the catalytic cracking feed stream in the fluidized bed reactor to produce a product stream and a spent catalyst; and transporting the spent catalyst to the catalyst regenerator and regenerating the catalyst in the catalyst regenerator. The product stream comprises olefins having a carbon number of C.sub.2-C.sub.4 and distillate fuel.

A downflow reactor, e.g. a downer reactor or system, includes an outer wall defining an interior reactor space. An elongated plug is within the outer wall having a first end and a second end, defining a longitudinal axis between the first and second ends. A distribution baffle positioned at a vertical position between the first end and the second end of the elongated plug configured and adapted to direct hot down flowing catalyst towards a feedstock spray.