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.

Compositions can include mixtures having from about 2 wt % to about 40 wt % of C.sub.10-C.sub.20 linear paraffins based on the weight of the mixture, from about 60 wt % to about 98 wt % of C.sub.10-C.sub.20 branched saturated hydrocarbons based on the weight of the mixture, and less than or equal to about 30 wt % of C.sub.20+ saturated hydrocarbons based on the weight of the mixture. Methods to obtain these compositions can include the isomerization of one or more C.sub.10-C.sub.20 alpha olefins under skeletal isomerization conditions to obtain an isomerization mixture and the hydrotreating of the isomerization mixture.

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 process for treatment of PFO from a steam cracking zone includes selectively hydrogenating PFO or a portion thereof for conversion of polyaromatics compounds contained in the PFO into aromatic compounds with one benzene ring to produce a selectively hydrogenated stream. The selectively hydrogenated stream is selectively hydrocracked for selective ring opening and dealkylation to produce a selectively hydrocracked BTX+ stream. The selectively hydrocracked BTX+ stream is separated into BTX compounds. Optionally the PFO is separated into a first stream containing C9+ aromatics compounds with one benzene ring, and a second stream containing C10+ aromatic compounds, whereby the first stream containing C9+ aromatics compounds with one benzene ring is passed to the selective hydrocracking step, and the feed to the selective hydrogenation step comprises all or a portion of the second stream containing C10+ aromatic compounds.

The present invention is based on the use of a two-step hydrocracking process comprising a step of hydrogenation placed upstream of the second hydrocracking step, the hydrogenation step treating the unconverted liquid fraction separated in the distillation step in the presence of a specific hydrogenation catalyst. Furthermore, the hydrogenation step and second hydrocracking step are carried out under specific operating conditions and in particular under very specific temperature conditions.

A process for preparing hydrocarbons from an oxygenated hydrocarbon feedstock, such as animal fat, having a high nitrogen impurity is described. The process involves hydrotreatment of the oxygenated feedstock in a first hydrotreating reactor and a further hydrotreatment in a second hydrotreating reactor, where between the two reactors, the gaseous phase is removed. The specific process setup effectively removes nitrogen impurities from the resultant hydrocarbon product causing an improved cloud point after isomerisation.

A steam-assisted catalytic cracking process for a hydrocarbon feed is provided. The process includes: introducing the hydrocarbon feed, a fluid catalytic cracking (FCC) catalyst, and steam to a FCC reactor with a mass ratio of steam to hydrocarbon feed between 0.05 and 1.0; cracking the hydrocarbon feed in the presence of the FCC catalyst and steam to produce a cracked hydrocarbon feed and spent FCC catalyst, the spent FCC catalyst comprising coke deposits and hydrocarbon deposits; stripping the hydrocarbon deposits from the spent FCC catalyst with steam in a stripper to obtain a hydrocarbon-stripped spent FCC catalyst; regenerating the hydrocarbon-stripped spent FCC catalyst in a regenerator by subjecting the stripped spent FCC catalyst to heat in the presence of oxygen to combust the coke deposits on the stripped spent FCC catalyst and produce a regenerated FCC catalyst; recycling the regenerated FCC catalyst.

The present invention relates to a device and to a process for the fluidized bed catalytic cracking of a hydrocarbon feedstock, in which: a first feedstock (2) is cracked in a dense fluidized bed reactor (1) in the presence of a catalyst (3) to produce a first effluent; and at least one second feedstock (10) is cracked in a transport fluidized bed reactor (4) in the presence of the catalyst (3) supplied by the dense fluidized bed reactor (1) to produce a second effluent, the second feedstock (10) being a heavier feedstock than the first feedstock (2).

A multi-phase combination reaction system has at least one fixed bed hydrogenation reactor. The fixed bed hydrogenation reactor has, arranged from top to bottom, a first hydrogenation reaction area, a gas-liquid separation area, a second hydrogenation reaction area and a third hydrogenation reaction area. The gas-liquid separation area is provided with a raw oil inlet. A hydrogen inlet is provided between the second hydrogenation reaction area and the third hydrogenation reaction area. The system is capable of simultaneously obtaining two fractions in one hydrogenation reactor.

A process for separation of a liquid phase from a gas phase and a process for production of a hydrocarbon product employing such a separation as well as a fractionation section and a hydrocracker section for carrying out such processes. The separation process includes: directing a feed for separation to a feed inlet of a means of separation; directing a stripping medium to a stripping medium inlet of the means of separation; withdrawing a liquid product stream from a means of separation; withdrawing a gaseous fraction comprising the stripping medium from the means of separation; directing the stripping medium fraction or the gaseous fraction as a recycled stripping medium; pressurizing at least an amount of the recycled stripping medium and directing it as the stripping medium, wherein the stripping medium comprises at least 80% vol/vol % of gases from the group comprising N.sub.2, H.sub.2, He, Ar, Ne and CO.sub.2.