Supplemental heat required to raise the temperature of a regenerated catalyst to the minimum required to promote the catalyzed reaction in an FCC unit is provided by introducing adsorbent material containing HPNA compounds and HPNA precursors with the coked catalyst into the FCC catalyst regeneration unit for combustion. The HPNA compounds and HPNA precursors can be adsorbed on either a carbonaceous adsorbent, such as activated carbon, that is completely combustible and generates no ash, or on fresh or coked FCC catalyst that is recovered from an HPNA adsorption column that has treated the bottoms from a hydrocracking unit to remove the HPNA compounds and their precursors.

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.

The present disclosure provides a method of treating waste plastic pyrolysis oil. The method includes a first step of washing waste plastic pyrolysis oil with water and then removing moisture; a second step of mixing the waste plastic pyrolysis oil from which the moisture is removed and a sulfur source to prepare a mixed oil; a third step of hydrotreating the mixed oil with hydrogen gas in the presence of a hydrotreating catalyst; a fourth step of separating the hydrotreated mixed oil into a liquid stream and a gas stream to obtain liquid pyrolysis oil; and a fifth step of recovering hydrogen gas from the separated gas stream and recycling the recovered hydrogen gas to the third step.

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.

Systems and methods are disclosed for enhancing the processing of hydrocarbons in a FCC unit by introduction of fluidized plastic at one or more locations of the FCC unit. In an embodiment, the method may include passing a coked FCC catalyst from a cyclone of the FCC unit to a regenerator. The method may include introducing at least oxygen and a fluidized plastic into the regenerator. The method may include combusting a combination of the fluidized plastic and a coke from the coked FCC catalyst in the regenerator, thereby to oxidize via the oxygen and produce a regenerated FCC catalyst and a flue gas. The method may include supplying the regenerated FCC catalyst from the regenerator to a riser of the FCC unit to crack the gas oil supplied to the riser of the FCC unit.

A catalytic cracking additive, its preparation and application thereof are provided. The catalytic cracking additive contains 10-50 wt % of a modified β zeolite, 20-85 wt % of a clay and 5-35 wt % of a boron-containing binder, based on the total weight of the catalytic cracking additive. The modified β zeolite comprises 0.1-1 wt % of CuO and 1-15 wt % of P.sub.2O.sub.5, and has a micro-activity index of at least 58; the boron-containing binder comprises 70-97 wt % of Al.sub.2O.sub.3 and 3-30 wt % of B.sub.2O.sub.3, and has a pH value of 1.0-3.5. The catalytic cracking additive can significantly improve the yield of C4 olefins and the concentration of C4 olefins in liquefied gas.

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 process for producing olefins from methanol with an MTO catalyst and oligomerizing a resulting olefin stream with an oligomerization catalyst to produce an oligomerized olefin stream. Oligomerization may comprise a first stage ethylene and/or propylene oligomerization step followed by a second stage oligomerization step of the first stage oligomerized olefin stream to higher olefins. The oligomerized olefin stream can be separated into jet and diesel fuel streams.

A method for producing renewable diesel includes introducing a primary feedstock comprising biologically-derived triglycerides with catalyst poisons into a first reaction chamber and hydrolyzing the primary feedstock within the first reaction and liquid-liquid extraction chamber for at least an hour such that the reacted triglycerides are separated into an aqueous solution comprising glycerol and catalyst poisons, and an intermediate feedstock comprising free fatty acids and catalyst poisons. The method also includes distilling the intermediate feedstock to separate the intermediate feedstock into a purified intermediate stream and a lower volume bottom stream containing unreacted triglyceride, diglyceride, monoglyceride, FFA and catalyst poisons. The method also includes combining the purified intermediate feedstock with a hydrogen stream and converting, in a second reaction chamber comprising a metallic catalyst bed, the purified intermediate feedstock into a product comprising long-chain alkanes. The method also includes hydrotreating the purified intermediate feedstock into a renewable diesel product.

According to embodiments described herein, a method of processing a whole crude oil feed stream may include passing a whole crude oil feed stream into a fluid catalytic cracking unit and contacting the whole crude oil feed stream with an adsorbent material and a cracking catalyst. The adsorbent material may adsorb at least a portion of the sulfur of the whole crude oil feed stream and at least a portion of the whole crude oil feed stream may be catalytically cracked to produce coke disposed on the cracking catalyst. The method may further include passing the adsorbent material and the cracking catalyst to a regenerator, wherein the adsorbent material and the cracking catalyst contact an oxygen-containing gas at a temperature sufficient to remove at least a portion of the sulfur on the adsorbent material and combust at least a portion of the coke on the catalyst.