A process for treating a plastics pyrolysis oil: a) selective hydrogenation of feedstock in the presence of hydrogen and at least one selective hydrogenation catalyst, at 100 to 150° C., a partial pressure of hydrogen of 1.0 to 10.0 MPa abs. and an hourly space velocity of 1.0 to 10.0 h.sup.−1, to obtain a hydrogenated effluent; b) hydrotreatment of hydrogenated effluent in the presence of hydrogen and at least one hydrotreatment catalyst, at 250 to 370° C., a partial pressure of hydrogen of 1.0 to 10.0 MPa abs. and an hourly space velocity of 1.0 to 10.0 h.sup.−1, to obtain a hydrotreatment effluent; c) separation of hydrotreatment effluent obtained from b) in the presence of an aqueous stream, at a temperature of 50 to 370° C., to obtain at least one gaseous effluent, an aqueous liquid effluent and a hydrocarbon liquid effluent.

A process for treating a plastics pyrolysis oil: a) selective hydrogenation of feedstock in the presence of hydrogen and at least one selective hydrogenation catalyst, at 100 to 150° C., a partial pressure of hydrogen of 1.0 to 10.0 MPa abs. and an hourly space velocity of 1.0 to 10.0 h.sup.−1, to obtain a hydrogenated effluent; b) hydrotreatment of hydrogenated effluent in the presence of hydrogen and at least one hydrotreatment catalyst, at 250 to 370° C., a partial pressure of hydrogen of 1.0 to 10.0 MPa abs. and an hourly space velocity of 1.0 to 10.0 h.sup.−1, to obtain a hydrotreatment effluent; c) separation of hydrotreatment effluent obtained from b) in the presence of an aqueous stream, at a temperature of 50 to 370° C., to obtain at least one gaseous effluent, an aqueous liquid effluent and a hydrocarbon liquid effluent.

Method of producing pyrolysis products from mixed plastics along with an associated system for processing mixed plastics. The method includes conducting pyrolysis of a plastic feedstock to produce plastic pyrolysis oil; feeding the plastic pyrolysis oil to a first fractionator to separate the plastic pyrolysis oil into a distillate fraction including naphtha and diesel and a vacuum gas oil fraction; and feeding the distillate fraction to a three step hydrotreating operation. The three step hydrotreating operation includes feeding the distillate fraction to a first hydrotreating unit to remove di-olefins to produce a first product stream, feeding the first product stream to a second hydrotreating unit to remove mono-olefins to produce a second product stream; and feeding the second product stream to a third hydrotreating unit to remove sulfur and nitrogen by hydrodesulfurization and hydrodenitrogenation to produce a third product stream. Such system may be integrated with a conventional refinery.

A process for treating plastics pyrolysis oil by a) selectively hydrogenating a feedstock in the presence hydrogen and a selective hydrogenation catalyst, at a temperature between 100 and 150° C., a hydrogen partial pressure between 1.0 and 10.0 MPa abs. and an hourly space velocity between 1.0 and 10.0 h.sup.−1, to obtain a hydrogenated effluent; b) hydrotreating the hydrogenated effluent in the presence of hydrogen and a hydrotreating catalyst, at a temperature between 250 and 370° C., a hydrogen partial pressure between 1.0 and 10.0 MPa abs. and an hourly space velocity between 0.1 and 10.0 h.sup.−1, to obtain a hydrotreating effluent; c) separating the hydrotreating effluent in the presence of an aqueous stream, at a temperature between 50 and 370° C., to obtain at least one gaseous effluent, a liquid aqueous effluent and a liquid hydrocarbon effluent; e) recycling at least one fraction of the product obtained.

A process for treating plastics pyrolysis oil by a) selectively hydrogenating a feedstock in the presence hydrogen and a selective hydrogenation catalyst, at a temperature between 100 and 150° C., a hydrogen partial pressure between 1.0 and 10.0 MPa abs. and an hourly space velocity between 1.0 and 10.0 h.sup.−1, to obtain a hydrogenated effluent; b) hydrotreating the hydrogenated effluent in the presence of hydrogen and a hydrotreating catalyst, at a temperature between 250 and 370° C., a hydrogen partial pressure between 1.0 and 10.0 MPa abs. and an hourly space velocity between 0.1 and 10.0 h.sup.−1, to obtain a hydrotreating effluent; c) separating the hydrotreating effluent in the presence of an aqueous stream, at a temperature between 50 and 370° C., to obtain at least one gaseous effluent, a liquid aqueous effluent and a liquid hydrocarbon effluent; e) recycling at least one fraction of the product obtained.

A method and apparatus for refining waste plastic pyrolysis oil has an effect of converting the waste plastic pyrolysis oil into high value-added hydrocarbon oil having a high content of naphtha and kerosene, lowering a content of impurities such as chlorine, nitrogen, oxygen, and metal of the hydrocarbon oil, operating under milder process conditions, having excellent process efficiency, and having high process stability to be able to continuously produce refined oil.

A catalytic cracking gasoline upgrading method is provided. First, in the presence of a prehydrogenation catalyst, the full-range FCC gasoline undergoes prehydrogenation in a prehydrogenation reactor to remove diolefins, mercaptans and sulfides, and then the prehydrogenation product undergoes selective hydrodesulfurization in the presence of a hydrodesulfurization-isomerization catalyst, and straight-chain olefins are isomerized into single-branched olefins or single-branched alkanes, thus obtaining a low-olefin, ultralow-sulfur and high-octane clean gasoline product.

A catalytic cracking gasoline upgrading method is provided. First, in the presence of a prehydrogenation catalyst, the full-range FCC gasoline undergoes prehydrogenation in a prehydrogenation reactor to remove diolefins, mercaptans and sulfides, and then the prehydrogenation product undergoes selective hydrodesulfurization in the presence of a hydrodesulfurization-isomerization catalyst, and straight-chain olefins are isomerized into single-branched olefins or single-branched alkanes, thus obtaining a low-olefin, ultralow-sulfur and high-octane clean gasoline product.

A selective hydrogenation catalyst comprising an active phase based on nickel and molybdenum, and a porous support consisting of alumina and/or nickel aluminate, characterized in that the molar ratio between the nickel and the molybdenum is greater than 2.5 mol/mol and less than 3.0 mol/mol.

A selective hydrogenation catalyst comprising an active phase based on nickel and molybdenum, and a porous support consisting of alumina and/or nickel aluminate, characterized in that the molar ratio between the nickel and the molybdenum is greater than 2.5 mol/mol and less than 3.0 mol/mol.