A process for the intense conversion of a heavy hydrocarbon feed, comprising a) ebullated bed hydroconversion of the feed; b) separating at least a portion of hydroconverted liquid effluent obtained from a); c)i) either hydrotreatment of at least a portion of the gas oil fraction and of the vacuum gas oil fraction obtained from b), ii) or hydrocracking at least a portion of gas oil fraction and vacuum gas oil fraction obtained from b); d) fractionation of at least a portion of the effluent obtained from c)i) or c)ii); e) recycling at least a portion of unconverted vacuum gas oil fraction obtained from the fractionation d) to said first hydroconversion a); f) hydrocracking at least a portion of gas oil fraction obtained from fractionation d); g) recycling all or a portion of effluent obtained from f) to the fractionation d).

A process for the intense conversion of a heavy hydrocarbon feed, comprising a) ebullated bed hydroconversion of the feed; b) separating at least a portion of hydroconverted liquid effluent obtained from a); c)i) either hydrotreatment of at least a portion of the gas oil fraction and of the vacuum gas oil fraction obtained from b), ii) or hydrocracking at least a portion of gas oil fraction and vacuum gas oil fraction obtained from b); d) fractionation of at least a portion of the effluent obtained from c)i) or c)ii); e) recycling at least a portion of unconverted vacuum gas oil fraction obtained from the fractionation d) to said first hydroconversion a); f) hydrocracking at least a portion of gas oil fraction obtained from fractionation d); g) recycling all or a portion of effluent obtained from f) to the fractionation d).

The invention relates to a process for converting a feedstock comprising pyrolysis oil and a heavy hydrocarbon-based feedstock, with: a) a step of hydroconversion in a reactor; b) a step of separating the liquid effluent obtained from step a) into a naphtha fraction, a gas oil fraction, a vacuum gas oil fraction and an unconverted residue fraction; c) a step of hydrocracking of the vacuum gas oil fraction; d) a step of fractionating the hydrocracked liquid effluent obtained from step c) into a naphtha fraction, a gas oil fraction and a vacuum gas oil fraction; e) a step of steam cracking of a portion of the naphtha fraction obtained from step d); f) a step of fractionating at least a portion of the steam-cracked effluent obtained from step e); g) a step in which the pyrolysis oil fraction obtained from step f) is sent into step a).

A catalyst system for dewaxing of a hydrocarbon feedstock comprising at least two catalytic sections, the first section comprising a first dewaxing catalyst and a subsequent section comprising a second dewaxing catalyst, wherein the first dewaxing catalyst is a ZSM-12 zeolite based catalyst and the second dewaxing catalyst is a EU-2 and/or ZSM-48 zeolite based catalyst. The catalyst system displays enhanced performance when compared to systems containing either ony ZSM-12 based catalyst or EU-2/ZSM-48 based catalyst only.

A catalyst system for dewaxing of a hydrocarbon feedstock comprising at least two catalytic sections, the first section comprising a first dewaxing catalyst and a subsequent section comprising a second dewaxing catalyst, wherein the first dewaxing catalyst is a ZSM-12 zeolite based catalyst and the second dewaxing catalyst is a EU-2 and/or ZSM-48 zeolite based catalyst. The catalyst system displays enhanced performance when compared to systems containing either ony ZSM-12 based catalyst or EU-2/ZSM-48 based catalyst only.

A process plant and a process for production of a hydrocarbon suitable for use as jet fuel from a feedstock being a renewable feedstock or an oxygenate feedstock, including combining the feedstock with an amount of a liquid diluent, directing it to contact a material catalytically active in hydrodeoxygenation under hydrotreating conditions to provide a hydrodeoxygenated intermediate product, separating the hydrodeoxygenated intermediate product in at least two fractions; a vapor fraction and a liquid fraction, directing at least an amount of the liquid fraction to contact a material catalytically active in isomerization under isomerization conditions to provide an isomerized intermediate product, directing at least an amount of the isomerized intermediate product and a stream comprising sulfur to provide a hydrocracked intermediate product, and fractionating the hydrocracked intermediate product to provide at least a hydrocarbon suitable for use as jet fuel.

A hydrocracking process is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream having a T90 temperature of about 204° C. (399° F.) to about 238° C. (460° F.), a diesel stream having a T90 temperature of about 360° C. (680° F.) to about 383° C. (721° F.) and an unconverted oil stream. The kerosene stream, the unconverted oil stream, and a portion of the diesel stream is recycled to the hydrocracking reactor for hydrocracking.

A hydrocracking process is disclosed. The hydrocracking process comprises hydrocracking a hydrocarbon feed stream in a hydrocracking reactor in the presence of a hydrogen stream and a hydrocracking catalyst to produce a hydrocracked effluent stream. The hydrocracked effluent stream is separated in a separator to provide a vapor hydrocracked stream and a liquid hydrocracked stream. The liquid hydrocracked stream is fractionated to provide a naphtha stream, a kerosene stream having a T90 temperature of about 204° C. (399° F.) to about 238° C. (460° F.), a diesel stream having a T90 temperature of about 360° C. (680° F.) to about 383° C. (721° F.) and an unconverted oil stream. The kerosene stream, the unconverted oil stream, and a portion of the diesel stream is recycled to the hydrocracking reactor for hydrocracking.

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 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.