Systems and methods are provided for increasing the yield of products generated during co-processing of biomass oil in a fluid catalytic cracking (FCC) system. The systems and methods can allow for increased yield by reducing or minimizing formation of carbon oxides, gas phase products, and/or coke yields during the co-processing. This can be achieved by adding a hydrogen-rich co-feed to the co-processing environment. Examples of hydrogen-rich co-feeds include high hydrogen content vacuum gas oil co-feed, high hydrogen content distillate co-feed, and/or high hydrogen content naphtha co-feed. Additionally or alternately, various types of fractions that contain a sufficient amount of hydrogen donor compounds can be used to reduce or minimize carbon oxide formation.

A method for converting an olefin or an alcohol has a pretreatment step of obtaining a conductive catalyst by a pretreatment for suppressing electrostatic charging of a non-conductive catalyst and a step of converting an olefin or an alcohol by a fluidized bed reaction using the conductive catalyst.

A fluidized bed reactor, a device, and a method for producing low-carbon olefins from oxygen-containing compound are provided. The fluidized bed reactor includes a reactor shell, a reaction zone, a coke control zone and a delivery pipe, where there are n baffles arranged in the coke control zone, and the n baffles divide the coke control zone into n sub-coke control zones which include a first sub-coke control zone, a second sub-coke control zone, and an nth sub-coke control zone; at least one catalyst circulation hole is provided on each of the n-1 baffles, so that the catalyst flows in an annular shape in the coke control zone, where n is an integer. The device and method can be adapted to a new generation of DMTO catalyst, and the unit consumption of production ranges from 2.50 to 2.58 tons of methanol/ton of low-carbon olefins.

A method for producing a stabilized biomass oil, which can be used as it stands or separated into streams that can be used for preparing fuels and combustibles and/or for preparing lubricants, or be used in a hydroconversion cracking method, in particular for manufacturing fuels.

Disclosed is a process for producing a jet fuel, comprising a step of converting an alcohol stream in a fluidized bed, a jet fuel and a plant associated with said process. The process involves the following steps: (a) converting a C1 to C6 alcohol stream to produce a mixture containing paraffins, olefins, aromatics, and water; (b) separating water from the mixture; (c) oligomerizing olefins; and (d) alkylating aromatics from the mixture; (e) forming a stream of hydrocarbons to be hydrogenated; (f) hydrogenating the stream of hydrocarbons to be hydrogenated; (g) recovering at least one jet fuel fraction from the hydrogenated hydrocarbon stream.

Conversion step (a) is carried out in a reaction zone comprising at least one fluidized catalytic bed.

In the mixture of paraffins, olefins, aromatics and water produced in conversion step (a), the ratio of the mass of C3+ olefins to the total mass of olefins is greater than or equal to 0.8.

A catalyst regeneration method is suitable for use in a fluidized catalytic cracking unit that includes a catalytic cracking reactor and a catalyst regenerator. The regeneration method includes the steps of: 1) providing a bio-based liquid phase fuel; 2) introducing the bio-based liquid phase fuel into a catalyst regenerator or a stripping section of the catalytic cracking reactor; 3) introducing an oxygen-containing gas into the catalyst regenerator; and 4) sending the spent catalyst from the catalytic cracking reactor to the catalyst regenerator, where the spent catalyst is contacted with the bio-based liquid phase fuel or the residue thereof and oxygen-containing gas to carry out coke burning regeneration. This method can greatly reduce the carbon emission of the catalytic cracking unit and can also provide energy for other process units and also converts part of the bio-based liquid phase fuel into chemicals.

A slurry reactor system including a slurry reactor configured to convert, under slurry hydroconversion conditions, a slurry reactor content flowing upwards and containing a feedstock including one or more of fats, oils and greases, a slurry hydroconversion catalyst and a hydrogen stream to a slurry hydroconversion effluent containing a slurry phase effluent including catalyst particles and a liquid product and a vapor phase effluent including a hydroconversion product, and one or more separation units in fluid communication with the slurry reactor to receive the slurry hydroconversion effluent. A given one of the one or more separation units is configured to separate the slurry phase effluent from the vapor phase effluent.

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.