Methods are provided for modifying hydrogenation catalysts having silica supports (or other non-alumina supports) with additional alumina, and using such catalysts to achieve unexpectedly superior hydrogenation of feedstocks. The modified hydrogenation catalysts can have a relatively low cracking activity while providing an increased activity for hydrogenation.

The present disclosure relates to a process for reducing the amount of aromatics in a raw feed stream comprising hydrocarbons, more than 200 ppmw sulfur or 1000 ppmw sulfur as either hydrocarbon heteroatoms or as other sulfide compounds as well as at least 10% by weight di-aromatics or poly-aromatics and at least 30% by weight aromatics in total said process comprising the steps of hydrotreating said raw feed stream in the presence of hydrogen and a material catalytically active in hydrotreatment with a severity resulting in a conversion of sulfur hydro-carbon heteroatoms to hydrogen sulfide of at least 50% providing a pre-treated stream, separating said pre-treated stream at least into a second stage feed stream and a stream rich in hydrogen sulfide, directing said second stage feed stream to contact a material catalytically active in hydrocracking and ring opening, and to contact a material catalytically active in saturation of aromatics, wherein the material catalytically active in hydrocracking and ring opening is positioned upstream, downstream or mixed with said material catalytically active in saturation of aromatics, and withdrawing a dearomatized stream, wherein said the amount of aromatics of said dearomatized stream is less than 50%, 70%, 90% or 95% of the amount of aromatics in said raw feed stream, with the associated benefit of said process of providing efficient dearomatization with low yield loss.

The present invention describes a process for the production of technical white oils or edible or medicinal oils from waste oils originating from industrial use or engine use, said process using a deep hydrotreatment.

The present invention describes a process for the production of technical white oils or edible or medicinal oils from waste oils originating from industrial use or engine use, said process using a deep hydrotreatment.

A process of producing Group III base oils, along with a naphtha product and diesel product, from whole waxy crude oil is provided. The inventive process omits the typical vacuum distillation stage and separations to form the typical cuts off of the vacuum tower. By selecting a waxy crude oil suitable for processing without separations, the crude oil may be hydroprocessed, dearomatized, dewaxed, and hydrofinished to produce a Group III base oil. Additionally, the dewaxing catalyst will isomerize the naphtha range molecules to increase the octane value to a suitable level for blending into gasoline and the diesel range molecules to reduce the diesel cloud point.

A heavy oil hydrotreating system has a prehydrotreating reaction zone, a transition reaction zone, and a hydrotreating reaction zone that are connected in series successively, sensor units, and a control unit. In the initial reaction stage, the prehydrotreating reaction zone includes at least two prehydrotreating reactors connected in parallel, and the transition reaction zone includes or doesn't include prehydrotreating reactors; in the reaction process, the control unit controls material feeding to and material discharging from each prehydrotreating reactor in the prehydrotreating reaction zone according to pressure drop signals of the sensor units, so that when the pressure drop in any of the prehydrotreating reactors in the prehydrotreating reaction zone reaches a predetermined value, the prehydrotreating reactor in which the pressure drop reaches the predetermined value is switched from the prehydrotreating reaction zone to the transition reaction zone.

A heavy oil hydrotreating system has a prehydrotreating reaction zone, a transition reaction zone, and a hydrotreating reaction zone that are connected in series successively, sensor units, and a control unit. In the initial reaction stage, the prehydrotreating reaction zone includes at least two prehydrotreating reactors connected in parallel, and the transition reaction zone includes or doesn't include prehydrotreating reactors; in the reaction process, the control unit controls material feeding to and material discharging from each prehydrotreating reactor in the prehydrotreating reaction zone according to pressure drop signals of the sensor units, so that when the pressure drop in any of the prehydrotreating reactors in the prehydrotreating reaction zone reaches a predetermined value, the prehydrotreating reactor in which the pressure drop reaches the predetermined value is switched from the prehydrotreating reaction zone to the transition reaction zone.

A method for producing hydrocarbon solvents having a sulfur content of less than 10 ppm, aromatic hydrocarbon content of less than 500 ppm, an initial boiling point higher than or equal to 300? C. and final boiling point lower than or equal to 500? C., for a fraction interval of a maximum of 100? C., and pour point lower than ?25? C. according to the standard ASTM D5950, comprising of the following steps of: dewaxing of a hydrocarbon fraction having initial boiling point higher than 300? C. derived from the distillation of a gas oil fraction, hydrodearomatisation of all or part of the dewaxed effluent, in the presence of a catalyst comprising nickel on an alumina base, at a pressure ranging from 60 to 200 bar and a temperature ranging from 80? C. to 250? C., recovery of the dewaxed and dearomatised fraction, distillation in fractions of the dewaxed and dearomatised fraction, recovery of at least one 300? C.+ fraction having pour point lower than ?25? C., this fraction having a distillation interval lower than 100? C.

A method for producing hydrocarbon solvents having a sulfur content of less than 10 ppm, aromatic hydrocarbon content of less than 500 ppm, an initial boiling point higher than or equal to 300? C. and final boiling point lower than or equal to 500? C., for a fraction interval of a maximum of 100? C., and pour point lower than ?25? C. according to the standard ASTM D5950, comprising of the following steps of: dewaxing of a hydrocarbon fraction having initial boiling point higher than 300? C. derived from the distillation of a gas oil fraction, hydrodearomatisation of all or part of the dewaxed effluent, in the presence of a catalyst comprising nickel on an alumina base, at a pressure ranging from 60 to 200 bar and a temperature ranging from 80? C. to 250? C., recovery of the dewaxed and dearomatised fraction, distillation in fractions of the dewaxed and dearomatised fraction, recovery of at least one 300? C.+ fraction having pour point lower than ?25? C., this fraction having a distillation interval lower than 100? C.

The present disclosure relates to a process to obtain de-aromatized hydrocarbon solvents from a heavy hydrocarbon stream. The process comprises hydrotreatment and selective hydrogenation of a heavy hydrocarbon stream at optimized process conditions. De-aromatized hydrocarbon solvents are characterized by aromatic content of less than 100 ppm, and sulphur content of less than 10 ppm.

The de-aromatized hydrocarbon solvents thus obtained is suitable for use in applications such as printing inks, paint, coatings, metal working fluids, industrial and institutional cleaning, adhesives, sealants, and in drilling fluids.