A process for converting inferior feedstock oil includes several steps. In step a) the inferior feedstock oil is subjected to a low severity hydrogenation reaction. The reaction product is separated to produce a gas, a hydrogenated naphtha, a hydrogenated diesel and a hydrogenated residual oil. In step b) the hydrogenated residual oil obtained in step a) is subjected to a first catalytic cracking reaction, the reaction product is separated to produce a first dry gas, a first LPG, a first gasoline, a first diesel and a first FCC-gas oil. In step c) the first FCC-gas oil obtained in step b) is subjected to a hydrogenation reaction of gas oil, the reaction product is separated to produce a hydrogenated gas oil, and in step d) the hydrogenated gas oil obtained in step c) is subjected to the first catalytic cracking reaction of step b) or a second catalytic cracking reaction.

A fluid catalytic cracking catalyst for hydrocarbon oil that is a blend of two types of fluid catalytic cracking catalysts each of which has a different hydrogen transfer reaction activity or has a pore distribution within a specific range after being pseudo-equilibrated. One catalyst is a catalyst containing a zeolite and matrix components, and the other catalyst is a catalyst containing a zeolite and matrix components. This catalyst is composed of the one catalyst and the other catalyst blended at a mass ratio within a range of 10:90 to 90:10.

A system that combines partial hydrocarbon oxidation with methane reforming is provided. The system advantageously uses products or partial products from the partial hydrocarbon oxidation to form the syngas, mixture of alcohols and other oxygenated hydrocarbons.

A pyrolysis oil fractionation system for treating a pyrolysis oil feed includes a fractionation column, at least one treatment catalyst bed, and a plurality of distillation trays. The system further includes a condenser to receive a light fraction and produce a condensed gasoline product and a vapor, a receiver coupled to the condenser, a knockout drum, and a distillate stripper coupled to the fractionation column. A method for treating a pyrolysis oil feed includes, in a fractionating column, dehydrohalogenating, decontaminating, and/or dehydrating a pyrolysis oil feed in at least one treatment catalyst bed, and distilling the treated pyrolysis oil feed into a light fraction, a middle fraction, a heavy fraction, and a bottom fraction. The method further includes condensing the light fraction and producing a condensed gasoline product and a vapor, separating a fuel gas product from the vapor, and stripping the middle fraction to produce a distillate product.

An integrated refinery process for removing mercaptans from a hydrocarbon stream containing mercaptans and converting by-product disulfide oil to useful products. The process includes introducing the hydrocarbon stream containing mercaptans into an extraction vessel containing an alkaline solution and passing the hydrocarbon stream through an extraction section of the extraction vessel which includes one or more liquid-liquid contacting decks for reaction to convert the mercaptans to alkali metal alkanethiolates. Further, the process includes withdrawing a hydrocarbon product stream free of mercaptans from the extraction vessel and recovering spent caustic containing alkali metal alkanethiolates from the extraction vessel. Additionally, the process includes subjecting the spent caustic containing alkali metal alkanethiolates to air oxidation to produce a by-product stream containing disulfide oils (DSO) and sulfides and processing the by-product stream in a steam cracking unit to produce a DSO free product stream.

The present invention relates to processes for the preparation of biofuel from biomass by fast hydropyrolysis or fast pyrolysis, using hydrogen generated by sorption enhanced steam reforming. The present invention also relates to fixed bed tandem catalytic-upgrading processes, and reactors and hydrodeoxygenation (HDO) catalysts useful in those processes.

Carbon nanofiber doped alumina (Al—CNF) supported MoCo catalysts in hydrodesulfurization (HDS), and/or boron doping, e.g., up to 5 wt % of total catalyst weight, can improve catalytic efficiency. Al-CNF-supported MoCo catalysts, (Al-CNF-MoCo), can reduce the sulfur concentration in fuel, esp. liquid fuel, to below the required limit in a 6 h reaction time. Thus, Al-CNF-MoCo has a higher catalytic activity than Al-MoCo, which may be explained by higher mesoporous surface area and better dispersion of MoCo metals on the AlCNF support relative to alumina support. The BET surface area of Al-MoCo may be 75% less than Al-CNF-MoCo, e.g., 166 vs. 200 m.sup.2/g. SEM images indicate that the catalyst nanoparticles can be evenly distributed on the surface of the CNF. The surface area of the AlMoCoB5% may be 206 m.sup.2/g, which is higher than AlMoCoB0% and AlMoCoB2%, and AlMoCoB5% has the highest HDS activity, removing more than 98% sulfur and below allowed levels.

Carbon nanofiber doped alumina (Al—CNF) supported MoCo catalysts in hydrodesulfurization (HDS), and/or boron doping, e.g., up to 5 wt % of total catalyst weight, can improve catalytic efficiency. Al—CNF-supported MoCo catalysts, (Al—CNF-MoCo), can reduce the sulfur concentration in fuel, esp. liquid fuel, to below the required limit in a 6 h reaction time. Thus, Al—CNF—MoCo has a higher catalytic activity than Al—MoCo, which may be explained by higher mesoporous surface area and better dispersion of MoCo metals on the AlCNF support relative to alumina support. The BET surface area of Al—MoCo may be 75% less than Al—CNF—MoCo, e.g., 166 vs. 200 m.sup.2/g. SEM images indicate that the catalyst nanoparticles can be evenly distributed on the surface of the CNF. The surface area of the AlMoCoB5% may be 206 m.sup.2/g, which is higher than AlMoCoB0% and AlMoCoB2%, and AlMoCoB5% has the highest HDS activity, removing more than 98% sulfur and below allowed levels.

The present invention relates to a process for converting the waste plastic along with the petroleum residue feedstock in a Delayed Coker unit employed in refineries. The invented process aims to convert any type of waste plastic including polystyrene, polypropylene, polyethylene etc. including metal additized multilayer plastics along with the petroleum residue material from crude oil refining such as reduced crude oil, vacuum residue etc. Value added light distillate products like motor spirit, LPG, middle distillates etc. are produced upon co-conversion in the invented process and is recovered and treated along with the products of thermal cracking of hydrocarbon residues. The residual metals in the metal additized plastics upon co-conversion in the invented process will be deposited in the solid petroleum coke.

The invention relates to a process for producing LPG and BTX, comprising a) subjecting a mixed hydrocarbon stream to first hydrocracking in the presence of a first hydrocracking catalyst to produce a first hydrocracking product stream; b) separating the first hydrocracking product stream to provide at least a light hydrocarbon stream comprising at least C2 and C3 hydrocarbons, a middle hydrocarbon stream consisting of C4 and/or C5 hydrocarbons and a heavy hydrocarbon stream comprising at least C6+ hydrocarbons and c) subjecting the heavy hydrocarbon stream to second hydrocracking in the presence of a second hydrocracking catalyst to produce a second hydrocracking product stream comprising BTX, wherein the second hydrocracking is more severe than the first hydrocracking, d) wherein at least part of the middle hydrocarbon stream is subjected to C4 hydrocracking optimized for converting C4 hydrocarbons into C3 hydrocarbons in the presence of a C4 hydrocracking catalyst to produce a C4 hydrocracking product stream.