Compositions based on effluents and/or products from FCC processing of a high saturate content, low heteroatom content feedstock are provided. By processing a high saturate content, low heteroatom content feed under various types of FCC conditions, a variety of compositions with unexpected compositional features and/or unexpected properties can be formed. The unexpected compositional features and/or unexpected properties can correspond to features and/or properties associated with one or more of the total effluent, a naphtha boiling range portion of effluent, a distillate or light cycle oil boiling range portion of the effluent, and/or a bottoms portion of the effluent.

Provided is a continuous process for converting waste plastic into recycle for polypropylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or polypropylene, and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. Pyrolysis oil and wax, comprising naphtha/diesel and heavy fractions, is passed to a refinery FCC unit. A liquid petroleum gas C.sub.3 olefin/paraffin mixture is recovered from the FCC unit. The C.sub.3 paraffins and C.sub.3 olefins are separated into different fractions with the C.sub.3 olefin fraction passed to a propylene polymerization reactor, and the C.sub.3 paraffin fraction passed optionally to a dehydrogenation unit to produce additional propylene.

This application relates to renewable diesel production and to production of renewable naphtha in a renewable diesel unit. Disclosed herein is an example of a method of renewable diesel production. Examples embodiments of the method may include hydrotreating the biofeedstock by reaction with hydrogen to form a hydrotreated biofeedstock; contacting at least a portion of the hydrotreated biofeedstock with a dewaxing catalyst to produce a renewable diesel product and a renewable naphtha product; separating the renewable diesel product and the renewable naphtha product in a product splitter; and monitoring an octane number of the renewable naphtha product with an analyzer.

Provided herein are methods for hydroisomerization of a hydrocarbon feedstock comprising contacting the hydrocarbon feedstock with hydrogen and a catalyst to yield a hydrocarbon product having an increase in branched hydrocarbons relative to the hydrocarbon feedstock. The present catalysts comprise a heteroatom-doped Beta zeolite having a trivalent cation as a framework metal oxide, an extra-framework species comprised of cerium and/or cobalt, and from 0.01 to 1.5 wt. % of a group VIII or VIB metal, or a combination thereof.

Provided in one embodiment is a continuous process for converting waste plastic into recycle for polyethylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or polypropylene, and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a pyrolysis oil and optionally wax comprising a naphtha/diesel and heavy fraction, and char. The pyrolysis oil and wax is passed to a refinery FCC unit from which a liquid petroleum gas C.sub.3-C.sub.5 olefin/paraffin mixture fraction is recovered. The liquid petroleum gas C.sub.3-C.sub.5 olefin/paraffin mixture fraction is passed to a refinery alkylation unit, with a propane and butane fraction recovered from the alkylation unit. The propane and butane fraction is then passed to a steam cracker for ethylene production. In another embodiment, a naphtha fraction (C.sub.5-C.sub.8) is recovered from the alkylation unit and passed to the steam cracker. In another embodiment, a propane/propylene fraction (C.sub.3-C.sub.3) is recovered from the FCC and passed to the steam cracker.

A continuous process for converting waste plastic into recycle for polypropylene polymerization is provided. The process integrates refinery operations to provide an effective and efficient recycle process. The process comprises selecting waste plastics containing polyethylene and polypropylene and then passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. The naphtha/diesel fraction is passed to a refinery FCC unit, from which is recovered a liquid petroleum gas C.sub.3 olefin/paraffin mixture. The C.sub.3 paraffins and C.sub.3 olefins are separated into different fractions with a propane/propylene splitter. The C.sub.3 olefin fraction is passed to a propylene polymerization reactor. The C.sub.3 paraffin fraction is optionally passed to a dehydrogenation unit to produce additional propylene and then the resulting C.sub.3 olefin is passed to a propylene polymerization reactor. The heavy fraction of pyrolyzed oil is passed to an isomerization dewaxing unit to produce a lubricating base oil.

A process is provided for producing a liquid hydrocarbon material suitable for use as a fuel or as a blending component in a fuel. The process includes co-processing a pyrolysis oil derived from a waste plastic raw material and a biorenewable feedstock comprising triglycerides in a catalytic cracking process in a presence of a solid catalyst at catalytic cracking conditions to provide a cracking product. The cracking product may be fractionated to provide at least one of a gasoline fraction and a middle distillate fraction.

A process for sulfuric acid catalyzed alkylation involving the use of surfactants which form bi-continuous micro-emulsions with the sulfuric acid and the hydrocarbon is described. The bi-continuous phase facilitates and improves the sulfuric acid catalyzed alkylation reactions. The concentration of the surfactant is selected based on the type of olefin feed. Easy to alkylate feeds, such as 2-butene, use lower concentrations of surfactant, while feeds which are harder to alkylate, such as propene or isobutene, use higher concentrations of the surfactant. In addition, increasing the concentration of sulfuric acid when a surfactant is included resulted in higher calculated RON. The use of a surfactant and a high concentration of sulfuric acid can provide a calculated RON over 100 and close to theoretical yields.

A process for converting light paraffins and/or light hydrocarbons to a high octane gasoline composition is disclosed. The process involves: (1) oxidation of iso-paraffins to alkyl hydroperoxides and alcohol; (2) conversion of the alkyl hydroperoxides and alcohol to dialkyl peroxides; and (3) radical coupling of one or more iso-paraffins and/or iso-hydrocarbons using the dialkyl peroxides as radical initiators, thereby forming a gasoline composition comprising gasoline-range molecules including a C7 enriched gasoline composition having a road octane number (RON) greater than 100.

Provided is a continuous process for converting waste plastic into recycle for polyethylene polymerization. In one embodiment, the process comprises selecting waste plastics containing polyethylene and/or polypropylene and passing the waste plastics through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into offgas, a naphtha/diesel fraction, a heavy fraction, and char. The naphtha/diesel fraction is passed to a crude unit distillation column in a refinery where a straight run naphtha (C.sub.5-C.sub.8) fraction or a propane/butane (C.sub.3-C.sub.4) fraction is recovered. The straight run naphtha fraction (C.sub.5-C.sub.8) or the propane/butane (C.sub.3-C.sub.4) fraction is passed to a steam cracker for ethylene production. The heavy fraction from the pyrolysis unit can also be passed to an isomerization dewaxing unit to produce a base oil.