Catalytic system which can be used in processes for the hydroconversion of heavy oils by means of hydrotreatment in slurry phase, characterized in that it comprises: a catalyst, having the function of hydrogenating agent, containing MoS.sub.2 or WS.sub.2 or mixtures thereof in lamellar form or an oil-soluble precursor thereof; a co-catalyst, having nanometric or micronic particle-sizes, selected from cracking and/or denitrogenation catalysts. The co-catalyst preferably consists of zeolites having small-sized crystals and with a low aggregation degree between the primary particles, and/or oxides or sulfides or precursors of sulfides of Ni and/or Co in a mixture with Mo and/or W.

Systems and methods are provided for catalytic hydroprocessing to form lubricant base oils. The methods can include performing high pressure hydrofinishing after fractionating the hydrotreated and/or hydrocracked and/or dewaxed effluent. Performing hydrofinishing after fractionation can allow the high hydrogen pressure for hydrofinishing to be used on one or more lubricant base oil fractions that are desirable for high pressure hydrofinishing. This can allow for improved aromatic saturation of a lubricant base oil product while reducing or minimizing the hydrogen consumption. The high pressure hydrofinishing can be performed at a hydrogen partial pressure of at least about 2500 psig (˜17.2 Mpa), or at least about 2600 psig (˜18.0 Mpa), or at least about 3000 psig (˜20.6 MPa). The high pressure hydrofinishing can allow for formation of a lubricant base oil product with a reduced or minimized aromatics content, a reduced or minimized 3-ring aromatics content, or a combination thereof.

Systems and methods are provided for catalytic hydroprocessing to form lubricant base oils. The methods can include performing high pressure hydrofinishing after fractionating the hydrotreated and/or hydrocracked and/or dewaxed effluent. Performing hydrofinishing after fractionation can allow the high hydrogen pressure for hydrofinishing to be used on one or more lubricant base oil fractions that are desirable for high pressure hydrofinishing. This can allow for improved aromatic saturation of a lubricant base oil product while reducing or minimizing the hydrogen consumption. The high pressure hydrofinishing can be performed at a hydrogen partial pressure of at least about 2500 psig (˜17.2 Mpa), or at least about 2600 psig (˜18.0 Mpa), or at least about 3000 psig (˜20.6 MPa). The high pressure hydrofinishing can allow for formation of a lubricant base oil product with a reduced or minimized aromatics content, a reduced or minimized 3-ring aromatics content, or a combination thereof.

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to improve the quality of vacuum residue. The improved quality of vacuum residue can be provided by one or more of reduced viscosity, reduced density (increased API gravity), reduced asphaltene content, reduced carbon residue content, reduced sulfur content, and reduced sediment. Vacuum residue of improved quality can be produced while operating the upgraded ebullated bed reactor at the same or higher severity, temperature, throughput and/or conversion. Similarly, vacuum residue of same or higher quality can be produced while operating the upgraded ebullated bed reactor at higher severity, temperature, throughput and/or conversion.

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to improve the quality of vacuum residue. The improved quality of vacuum residue can be provided by one or more of reduced viscosity, reduced density (increased API gravity), reduced asphaltene content, reduced carbon residue content, reduced sulfur content, and reduced sediment. Vacuum residue of improved quality can be produced while operating the upgraded ebullated bed reactor at the same or higher severity, temperature, throughput and/or conversion. Similarly, vacuum residue of same or higher quality can be produced while operating the upgraded ebullated bed reactor at higher severity, temperature, throughput and/or conversion.

A system for upgrading pyrolysis oil may include a pyrolysis upgrading unit having a mixed metal oxide catalyst and a separation unit operable to separate used mixed metal oxide catalyst from a reaction effluent. A method for upgrading pyrolysis oil may include contacting the pyrolysis oil with hydrogen in the presence of the mixed metal oxide catalyst at reaction conditions to produce a reaction effluent. The pyrolysis oil may include multi-ring aromatic compounds. The mixed metal oxide catalyst may include a plurality of catalyst particles and each of the plurality of catalyst particles having a plurality of metal oxides. Contacting the pyrolysis oil with hydrogen in the presence of the mixed metal oxide catalyst at the reaction conditions may convert at least a portion of the multi-ring aromatic compounds in the pyrolysis oil to the light aromatic compounds.

A system for upgrading pyrolysis oil may include a pyrolysis upgrading unit having a mixed metal oxide catalyst and a separation unit operable to separate used mixed metal oxide catalyst from a reaction effluent. A method for upgrading pyrolysis oil may include contacting the pyrolysis oil with hydrogen in the presence of the mixed metal oxide catalyst at reaction conditions to produce a reaction effluent. The pyrolysis oil may include multi-ring aromatic compounds. The mixed metal oxide catalyst may include a plurality of catalyst particles and each of the plurality of catalyst particles having a plurality of metal oxides. Contacting the pyrolysis oil with hydrogen in the presence of the mixed metal oxide catalyst at the reaction conditions may convert at least a portion of the multi-ring aromatic compounds in the pyrolysis oil to the light aromatic compounds.

A method for upgrading pyrolysis oil includes contacting a pyrolysis oil feed with hydrogen in the presence of a mixed metal oxide catalyst in a slurry reactor to produce an intermediate stream comprising light aromatic compounds comprising mono-aromatic compounds, di-aromatic compounds, or both, passing the intermediate stream to a hydrocracking reactor, contacting the intermediate stream with hydrogen in the presence of a hydrocracking catalyst in a hydrocracking reactor to produce a hydrocracking effluent comprising aromatic compounds having six to nine carbon atoms, passing the hydrocracking effluent to a transalkylation reactor, and contacting the hydrocracking effluent with hydrogen in the presence of a transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent comprising xylenes.

A process and a system are used for production of multiple grades of ultralow aromatic solvents/chemicals having preferred boiling range, flash point and viscosity from different hydrocarbon streams. A plurality of hydrotreating steps are used to hydrotreat a plurality of hydrocarbon feedstocks in the presence of a hydrogen gas stream and a catalyst system. Further, at least one dissolved gas stripping step, at least one adsorption step, and a distillation step are included in the process. Desired iso-paraffin molecules are thereby preserved, and the undesired aromatic molecules are converted into desired naphthene molecules.

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).