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.

Systems and methods are provided for production of renewable jet fuel and/or jet fuel blending component fractions. The systems and methods provide for formation of jet boiling range fractions via hydrodeoxygenation and catalytic dewaxing of bio-derived feeds. The systems and methods for reducing or minimizing recycle and/or forming only a jet boiling range product and a lower boiling range product can be facilitated based on selection of a suitable feedstock and/or based on selection of suitable reaction conditions and catalyst for the catalytic dewaxing.

Systems and methods are provided for production of renewable jet fuel and/or jet fuel blending component fractions. The systems and methods provide for formation of jet boiling range fractions via hydrodeoxygenation and catalytic dewaxing of bio-derived feeds. The systems and methods for reducing or minimizing recycle and/or forming only a jet boiling range product and a lower boiling range product can be facilitated based on selection of a suitable feedstock and/or based on selection of suitable reaction conditions and catalyst for the catalytic dewaxing.

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 hydrogenation reactions of different fractions in oil refining. It also relates to a process device applicable thereto for hydrogenation of various feedstocks, such as arrangements during campaign changes.

The present disclosure relates to hydrogenation reactions of different fractions in oil refining. It also relates to a process device applicable thereto for hydrogenation of various feedstocks, such as arrangements during campaign changes.

Systems and methods are provided for producing naphthenic compositions corresponding to various types of products, such as naphthenic base oil, specialty industrial oils, and/or hydrocarbon fluids. The methods of producing the naphthenic compositions can include exposing a heavy fraction from a fluid catalytic cracking (FCC) process, such as a FCC bottoms fraction (i.e., a catalytic slurry oil), to hydroprocessing conditions corresponding to hydrotreating and/or aromatic saturation conditions. Naphthenic compositions formed from processing of FCC fractions are also provided.

Systems and methods are provided for production of base stocks with a viscosity index of at least 120 and/or a sulfur content of 300 wppm or less and/or a kinematic viscosity at 100 C. of 3.0 cSt to 8.0 cSt by hydroconversion of a raffinate from aromatic extraction of a feed. The base stocks can further have a reduced content of 3+ ring naphthenes, such as 4.0 wt % or less, or 1.0 wt % or less. The base stocks can be produced by performing an elevated amount of feed conversion relative to 370 C. during hydroconversion of the raffinate, and optionally additional conversion during catalytic dewaxing of the hydroconverted raffinate. The base stocks can optionally be blended with additional base stocks and/or lubricant additives for production of lubricant compositions.