A feedstock is processed in an FCC unit to produce at least light olefins, FCC naphtha, light cycle oil and heavy cycle oil. Light cycle oil, and in certain embodiments hydrotreated light cycle oil, is subjected to deep hydrogenation to produce a deeply hydrogenated middle distillate fraction. All or a portion of the deeply hydrogenated middle distillate fraction is used as feed to the stream cracking zone to produce light olefins.

A feedstock is processed in an FCC unit to produce at least light olefins, FCC naphtha, light cycle oil and heavy cycle oil. Light cycle oil, and in certain embodiments hydrotreated light cycle oil, is subjected to hydrogenation to produce a deeply hydrogenated middle distillate fraction. All or a portion of the deeply hydrogenated middle distillate fraction is used as feed to a petrochemicals production complex to produce light olefins.

A feedstock is processed in an FCC unit to produce at least light olefins, FCC naphtha, light cycle oil and heavy cycle oil. Light cycle oil, and in certain embodiments hydrotreated light cycle oil, is subjected to hydrogenation to produce a deeply hydrogenated middle distillate fraction. All or a portion of the deeply hydrogenated middle distillate fraction is used as feed to a petrochemicals production complex to produce light olefins.

Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a petrochemicals production complex for conversion into light olefins and other hydrocarbon products. Feeds to the deep hydrogenation zone include middle distillate range streams from a distillate hydrotreating zone, a vacuum gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a middle distillate range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a petrochemicals production complex for conversion into light olefins and other hydrocarbon products. Feeds to the deep hydrogenation zone include middle distillate range streams from a distillate hydrotreating zone, a vacuum gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a middle distillate range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

A method for preparing hexadecahydropyrene includes the step of carrying out the hydrogenation reaction to hydrocarbon oil containing pyrene compounds in the presence of a hydrogenation catalyst. The pyrene compounds are selected from at least one of pyrene and unsaturated hydrogenation products thereof. The hydrogenation catalyst contains a carrier and an active metal component loaded on the carrier. The active metal component is Pt and/or Pd and the carrier contains a small crystal size Y zeolite, alumina and amorphous silica-alumina. The small crystal size Y zeolite has an average grain diameter of 200-700 nm, a molar ratio of SiO.sub.2 to Al.sub.2O.sub.3 of 40-120, a relative crystallinity of ≥95%, and a specific surface area of 900-1,200 m.sup.2/g. The pore volume of secondary pores in 1.7-10 nm diameter is more than 50% of the total pore volume.

A method of making a multifunctional catalyst for upgrading pyrolysis oil includes contacting a zeolite support with a solution including at least a first metal catalyst precursor and a second metal catalyst precursor, the first metal catalyst precursor, the second metal catalyst precursor, or both, including a heteropolyacid. Contacting the zeolite support with the solution deposits or adsorbs the first metal catalyst precursor and the second catalyst precursor onto outer surfaces and pore surfaces of the zeolite support to produce a multifunctional catalyst precursor. The method further includes removing excess solution from the multifunctional catalyst precursor and calcining the multifunctional catalyst precursor to produce the multifunctional catalyst comprising at least a first metal catalyst and a second metal catalyst deposited on the outer surfaces and pore surfaces of the zeolite support.

The invention relates to a method for hydroprocessing a hydrocarbon feed, operated at a temperature of between 180° C. and 450° C., in the presence of a catalyst comprising i) a composite material comprising a compound based on at least one crystalline aluminium solid and carbon, the deposited carbon content being between 1 and 25 wt. % of the total mass of the composite material, and ii) at least one element of group VIB and at least one element of group VIII, in the sulfide form thereof, said catalyst being produced by a method comprising at least: a) a step of bringing a carbon precursor into contact with a compound based on at least one crystalline aluminium solid, b) a step of thermally treating the solid produced by step a), c) repeating steps a) and b) until the desired deposited carbon content is reached, d) depositing at least one element of group VIB and at least one element of group VIII on the surface of the solid produced by step c), and e) a step of sulfidisation of the solid produced in step d).

The invention relates to a method for hydroprocessing a hydrocarbon feed, operated at a temperature of between 180° C. and 450° C., in the presence of a catalyst comprising i) a composite material comprising a compound based on at least one crystalline aluminium solid and carbon, the deposited carbon content being between 1 and 25 wt. % of the total mass of the composite material, and ii) at least one element of group VIB and at least one element of group VIII, in the sulfide form thereof, said catalyst being produced by a method comprising at least: a) a step of bringing a carbon precursor into contact with a compound based on at least one crystalline aluminium solid, b) a step of thermally treating the solid produced by step a), c) repeating steps a) and b) until the desired deposited carbon content is reached, d) depositing at least one element of group VIB and at least one element of group VIII on the surface of the solid produced by step c), and e) a step of sulfidisation of the solid produced in step d).

An integrated process is provided herein having a first reaction zone to lower sulfur and nitrogen content of the initial feedstock to a target level to facilitate processing in a second reaction zone for deep hydrogenation. With the very low heteroatom content, noble metal catalyst materials used in the second reaction zone are protected and maximum saturation of aromatics is achieved. The processes and systems herein are suitable for converting certain heavy fractions, typically considered “low value” feedstocks, into higher value products including gasoline and diesel, and a hydrogen-rich, aromatic-lean heavy fraction suitable as feed for olefin production processes, or as a lubricant base oil.