A method and a system for hydrocracking an oil feedstock to produce a light oil stream without build-up of heavy polynuclear aromatic (HPNA) hydrocarbons in the recycle stream. The method may include hydrocracking an oil feedstock, separating the produced effluent into a first, second, and third product stream, and hydrogenating the third product stream in a third reactor over a noble metal hydrogenation catalyst at an operational pressure equal to or less than the second reactor.

A method of upgrading refining streams with high polynucleararomatic hydrocarbon (PNA) concentrations can include: hydrocracking a PNA feed in the presence of a catalyst and hydrogen at 380° C. to 430° C., 2500 psig or greater, and 0.1 hr.sup.−1 to 5 hr.sup.−1 liquid hourly space velocity (LSHV), wherein the weight ratio of PNA feed to hydrogen is 30:1 to 10:1, wherein the PNA feed comprises 25 wt % or less of hydrocarbons having a boiling point of 700° F. (371° C.) or less and having an aromatic content of 50 wt % or greater to form a product comprising 50 wt % or greater of the hydrocarbons having a boiling point of 700° F. (371° C.) or less and having an aromatic content of 20 wt % or less.

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.

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.

Provided is a continuous process for converting waste plastic into a feedstock for polyethylene polymerization. The process comprises selecting waste plastics containing polyethylene and/or 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 then separated into offgas, a pyrolysis oil comprising a naphtha/diesel/heavy fraction, and char. The pyrolysis oil is passed to a crude unit in a refinery from which a naphtha fraction (C.sub.5-C.sub.8), or a propane and butane (C.sub.3-C.sub.4) fraction, is recovered. The naphtha fraction, or propane and butane (C.sub.3-C.sub.4) fraction, is then passed to a steam cracker for ethylene production.

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 the naphtha/diesel fraction and heavy fraction, is sent to a refinery FCC unit. A liquid petroleum gas C.sub.3-C.sub.5 olefin/paraffin mixture is recovered from the FCC unit and passed to a refinery alkylation unit. A propane fraction is recovered from the alkylation unit and passed to a dehydrogenation unit to produce propylene. The propylene is passed to a propylene polymerization reactor.

The invention relates to various nonlimiting embodiments that include methods, apparatuses or systems for processing natural gas comprising a heavies removal column processing natural gas and light oil reflux. The overhead stream goes to heavies treated natural gas storage. The heavies removal column reboiler bottoms stream product is input to a debutanizer column. The debutanizer column overhead lights are input to a flash drum where the bottoms is pumped through a heat exchanger as a light oil reflux input to the heavies removal column, while the debutanizer reboiler bottoms product is stored as stabilized condensate. Alternatively, debutanizer column overhead lights are sent to heavies treated gas storage and the bottoms stream product goes to a depentanizer column, the overhead lights are pumped through a heat exchanger as a light oil reflux input to the heavies removal column, while the depentanizer reboiler bottoms product is stabilized condensate.

The present invention relates to an apparatus for the hydroconversion of heavy oil products (the fresh load). Said apparatus comprises: a slurry bubble column hydroconversion reactor, which comprises a feed line in which the fresh load and the recirculated slurry phase are conveyed, an inlet line for a hydrogenating stream and an outlet for a reaction effluent through an outlet nozzle; a stripping column at high pressure and high temperature placed downstream of the reactor and directly connected to the reactor head through a pipeline in which the reaction effluent flows; said column having an inlet line for a stripping gas, an inlet for the reactor effluent, a head outlet for steam and an outlet for the slurry phase; lines and means for recirculating the slurry leaving the stripping column; lines and means for taking a drain stream, which has the function of preventing the accumulation of solids in the reactor. The stripping column is characterized in that it contains one or more contact devices that allow physical contact to be created between different phases.

This disclosure relates to the production of chemicals and plastics using pyrolysis oil from the pyrolysis of plastic waste as a co-feedstock along with a petroleum-based, fossil fuel-based, or bio-based feedstock. In an aspect, the polymers and chemicals produced according to this disclosure can be certified under International Sustainability and Carbon Certification (ISCC) provisions as circular polymers and chemicals at any point along complex chemical reaction pathways. The use of a mass balance approach which attributes the pounds of pyrolyzed plastic products derived from pyrolysis oil to any output stream of a given unit has been developed, which permits ISCC certification agency approval.

The use of bio oil from at least one renewable source in a hydrotreatment process, in which process hydrocarbons are formed from said glyceride oil in a catalytic reaction, and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron. A bio oil intermediate including bio oil from at least one renewable source and the iron content of said bio oil is less than 1 w-ppm calculated as elemental iron.