A process for upgrading plastics to olefins, paraffins, and aromatics with a core-shell catalyst in a fluidized bed reactor is described.

A process for catalytically cracking hydrocarbons is disclosed. The process comprises contacting a hydrocarbon feed stream with a catalyst to catalytically crack the hydrocarbon feed stream to provide a cracked stream and spent catalyst. The spent catalyst is disengaged from the cracked stream in a reactor vessel. Hydrocarbons are stripped from the spent catalyst. The cracked stream is fractionated in a main fractionation column into products comprising a slurry oil stream from a bottom of the main fractionation column. The slurry oil stream is filtered in a filter vessel through a filter to provide a filtered slurry oil stream. Thereafter, the filter is backflushed with a hydrocarbon stream to produce a backflushed hydrocarbon stream comprising catalyst fines. The backflushed hydrocarbon stream is recycled to the reactor vessel. An apparatus for catalytically cracking hydrocarbons is also disclosed.

In various aspects, systems and methods are provided for operating an oxygen-fired catalyst regenerator with flue gas recycle and CO.sub.2 capture. An oxygen-fired catalyst regenerator contrasts with an air-fired regenerator. The oxygen-fired catalyst regenerator substantially reduces nitrogen within the system, which facilitates CO.sub.2 capture by reducing the energy required to capture CO.sub.2. In various aspects, a first portion of the regenerator flue gas is passed to a CO.sub.2 capture system and a second portion is recycled to the regenerator. Before the flue gas is recycled or diverted to the CO.sub.2 capture, it is passed to various processes that remove and/or reduce SO.sub.x, NO.sub.x, particulate, and water content. In various aspects, a portion of the treated flue gas may be combined with substantially pure O.sub.2 and recycled to the regenerator.

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.

A naphtha-to-aromatics fluidized bed device and a method thereof are provided. The device at least includes: a light hydrocarbon aromatization reactor; and a naphtha-to-aromatics reactor; the high-temperature regenerated catalyst is first directed into the light hydrocarbon aromatization reactor, and after cooling, subsequently introduced into the naphtha-to-aromatics reactor. The method includes using the above-mentioned device and a metal molecular sieve bifunctional catalyst. Under the action of the catalyst in the naphtha to aromatics reactor, naphtha is converted into a product gas containing aromatics, light alkanes, and other components. Light alkanes and the like separated from the product gas are further converted into aromatics and other components in the light hydrocarbon aromatization reactor. The method enables efficient and highly selective conversion of linear and branched aliphatic hydrocarbons into aromatics, with para-xylene content in the xylene mixture exceeding >50 wt %.

A process for regeneration of a process enclosure and a catalyst comprising precipitated ammonium salts, and a process and a process plant for continuous hydrotreating a feedstock comprising nitrogen and halides.

A process for upgrading a bio-oil stream is disclosed. The process comprises reacting a bio-oil stream with hydrogen in the presence of a catalyst in a reactor to produce an upgraded bio-oil stream. The upgraded bio-oil stream is charged to an FCC unit, a hydroprocessing unit, or a reforming unit to produce an intermediate blend or a fuel stream. A fuel oil stream can be taken from the upgraded bio-oil stream. The catalyst may be separated and recycled to the reactor. The upgraded bio-oil stream can be used directly to produce an intermediate blend or fuel. A fuel oil stream may be taken from the upgraded bio-oil stream.