Supercritical upgrading reactors and reactor systems are provided for upgrading a petroleum-based composition using one or more purging fluid inlets to prevent plugging of the catalyst layer in the reactor. Processes for upgrading petroleum-based compositions by utilizing a reactor having at least one purging fluid inlet are also provided.

Supercritical upgrading reactors and reactor systems are provided for upgrading a petroleum-based composition using one or more purging fluid inlets to prevent plugging of the catalyst layer in the reactor. Processes for upgrading petroleum-based compositions by utilizing a reactor having at least one purging fluid inlet are also provided.

Provided herein are supercritical upgrading reactors and reactor systems for upgrading a petroleum-based composition by using one or more supercritical upgrading reactors and one or more supercritical standby reactors that alternate functions such that the supercritical upgrading reactor is converted to a supercritical standby reactor and the supercritical standby reactor is converted to a supercritical upgrading reactor. The supercritical upgrading reactor upgrades a combined feed stream while a supercritical standby reactor delivers a cleaning fluid into the supercritical standby reactor. The supercritical reactors may have one or more catalyst layers and one or more purging fluid inlets, and the catalyst layers may have differing void volume ratios.

Provided herein are supercritical upgrading reactors and reactor systems for upgrading a petroleum-based composition by using one or more supercritical upgrading reactors and one or more supercritical standby reactors that alternate functions such that the supercritical upgrading reactor is converted to a supercritical standby reactor and the supercritical standby reactor is converted to a supercritical upgrading reactor. The supercritical upgrading reactor upgrades a combined feed stream while a supercritical standby reactor delivers a cleaning fluid into the supercritical standby reactor. The supercritical reactors may have one or more catalyst layers and one or more purging fluid inlets, and the catalyst layers may have differing void volume ratios.

Processes and apparatus for maximizing production of heavy naphtha from a hydrocarbon stream are provided. The process comprises providing a hydrocarbon feed stream comprising vacuum gas oil to a first hydrocracking reactor. The hydrocarbon feed stream is hydrocracked at first hydrocracking conditions comprising a first hydrocracking pressure to provide a first hydrocracked effluent stream therein. At least a portion of the first hydrocracked effluent stream is fractionated in a fractionation column to provide a heavy naphtha fraction. A kerosene stream is hydrocracked in a second hydrocracking reactor operating at second hydrocracking conditions comprising a second hydrocracking pressure to provide a second hydrocracked effluent stream. In an aspect, the first hydrocracking pressure can be greater than the second hydrocracking pressure by at least about 6895 kPa (g). At least a portion of the second hydrocracked effluent stream is passed to the fractionation column to maximize the production of heavy naphtha.

Processes and apparatus for maximizing production of heavy naphtha from a hydrocarbon stream are provided. The process comprises providing a hydrocarbon feed stream comprising vacuum gas oil to a first hydrocracking reactor. The hydrocarbon feed stream is hydrocracked at first hydrocracking conditions comprising a first hydrocracking pressure to provide a first hydrocracked effluent stream therein. At least a portion of the first hydrocracked effluent stream is fractionated in a fractionation column to provide a heavy naphtha fraction. A kerosene stream is hydrocracked in a second hydrocracking reactor operating at second hydrocracking conditions comprising a second hydrocracking pressure to provide a second hydrocracked effluent stream. In an aspect, the first hydrocracking pressure can be greater than the second hydrocracking pressure by at least about 6895 kPa (g). At least a portion of the second hydrocracked effluent stream is passed to the fractionation column to maximize the production of heavy naphtha.

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 device for mixing fluids for a downflow catalytic reactor (1), having at least one substantially horizontal collector (5) provided with a substantially vertical collection conduit (7) receiving fluids collected by said collector (5); an injector (8) injecting a quench fluid opening into said collection conduit (7); a mixing chamber (9) located downstream of the collector (5) in the direction of movement of the fluids, having an inlet end connected directly to the collection conduit (7) and an outlet end (10) evacuating the fluids; and a pre-distribution plate (11) having a plurality of perforations and at least one riser (13), being located downstream of said mixing chamber (9) in the direction of movement of the fluids; the section of the mixing chamber (9) is a parallelogram and has at least one deflector (15) over at least one of the four internal walls of the mixing chamber (9) with a parallelogram section.

A device for mixing fluids for a downflow catalytic reactor (1), having at least one substantially horizontal collector (5) provided with a substantially vertical collection conduit (7) receiving fluids collected by said collector (5); an injector (8) injecting a quench fluid opening into said collection conduit (7); a mixing chamber (9) located downstream of the collector (5) in the direction of movement of the fluids, having an inlet end connected directly to the collection conduit (7) and an outlet end (10) evacuating the fluids; and a pre-distribution plate (11) having a plurality of perforations and at least one riser (13), being located downstream of said mixing chamber (9) in the direction of movement of the fluids; the section of the mixing chamber (9) is a parallelogram and has at least one deflector (15) over at least one of the four internal walls of the mixing chamber (9) with a parallelogram section.

A refinery built around a slurry phase hydrocracking process unit, such as a Veba Combi-Cracker (VCC), is simpler, produces more liquid product as transportation fuels and has much higher net cash margin than a refinery built around a coker or other bottoms upgrading processes. The VCC unit replaces one or more processing steps normally included in refineries as separate and distinct processing units including heavy distillate/gas oil cracking and optionally bottoms upgrading and deep desulfurization of diesel and gasoline range cuts. The refinery design is especially suited for heavy crude upgrading and can be tuned to provide a wide range of gasoline to distillate production ratios. The refinery design is bottomless in the sense that it produces no heavy fuel oil or asphalt as product and no solid fuel (e.g., petroleum coke).