A process and device for reducing the environmental contaminants in a ISO 8217 compliant Feedstock Heavy Marine Fuel Oil, the process involving: mixing a quantity of the Feedstock Heavy Marine Fuel Oil with a quantity of Activating Gas mixture to give a feedstock mixture; contacting the feedstock mixture with one or more catalysts to form a Process Mixture from the feedstock mixture; separating the Product Heavy Marine Fuel Oil liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil is compliant with ISO 821 7 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05% wt. to 0.5% wt. The Product Heavy Marine Fuel Oil can be used as or as a blending stock for an ISO 8217 compliant, IMO MARPOL Annex VI (revised) compliant low sulfur or ultralow sulfur heavy marine fuel oil.

A process for producing high yields of higher quality (API Group II, Group III′) lubricating oil basestock fractions which allows the production of two or more types of high quality lubes in continuous mode (no blocked operation mode) without transition times and feed or intermediate product tankage segregation. Two consecutive hydroprocessing steps are used: the first step processes a wide cut feed at a severity needed to match heavy oil lube properties. The second step hydroprocesses a light oil after fractionation of the liquid product from the first step at a severity higher than for the heavy oil fraction. The two hydroprocessing steps will normally be carried out in separate reactors but they may be combined in a single reactor which allows for the two fractions to be processed with different degrees of severity.

A process for producing high yields of higher quality (API Group II, Group III′) lubricating oil basestock fractions which allows the production of two or more types of high quality lubes in continuous mode (no blocked operation mode) without transition times and feed or intermediate product tankage segregation. Two consecutive hydroprocessing steps are used: the first step processes a wide cut feed at a severity needed to match heavy oil lube properties. The second step hydroprocesses a light oil after fractionation of the liquid product from the first step at a severity higher than for the heavy oil fraction. The two hydroprocessing steps will normally be carried out in separate reactors but they may be combined in a single reactor which allows for the two fractions to be processed with different degrees of severity.

A process and apparatus is disclosed for recovering hydrotreating effluent from a hydrotreating unit utilizing a hot stripper and a cold stripper. Only the hot hydrotreating effluent is heated in a fired heater prior to product fractionation, resulting in substantial operating and capital savings. The cold stripped stream from the cold stripper bottoms line may be passed directly to a diesel pool when VGO is hydrotreated in the hydrotreating reactor bypassing the product fractionation column.

A process and apparatus is disclosed for recovering hydrotreating effluent from a hydrotreating unit utilizing a hot stripper and a cold stripper. Only the hot hydrotreating effluent is heated in a fired heater prior to product fractionation, resulting in substantial operating and capital savings. The cold stripped stream from the cold stripper bottoms line may be passed directly to a diesel pool when VGO is hydrotreated in the hydrotreating reactor bypassing the product fractionation column.

In a hydrocracking process, the product from the first stage reactor passes through a steam stripper to remove hydrogen, H.sub.2S, NH.sub.3, light gases (C.sub.1-C.sub.4), naphtha and diesel products. The stripper bottoms are separated from hydrogen, H.sub.2S, NH.sub.3, light gases (C.sub.1-C.sub.4), naphtha, and diesel products and treated in a second stage reactor. The effluent stream from the second stage reactor, along with the stream of separated hydrogen, H.sub.2S, NH.sub.3, light gases (C.sub.1-C.sub.4), naphtha, and diesel products, are passed to a separation stage for separating petroleum fractions. Preferably, the effluent stream from the first stage reactor is passed through a steam generator prior to the steam stripping step. In an alternate embodiment, the effluent stream from the first stage reactor is passed through a vapor/liquid separator stripper vessel prior to the steam stripping step.

In a hydrocracking process, the product from the first stage reactor passes through a steam stripper to remove hydrogen, H.sub.2S, NH.sub.3, light gases (C.sub.1-C.sub.4), naphtha and diesel products. The stripper bottoms are separated from hydrogen, H.sub.2S, NH.sub.3, light gases (C.sub.1-C.sub.4), naphtha, and diesel products and treated in a second stage reactor. The effluent stream from the second stage reactor, along with the stream of separated hydrogen, H.sub.2S, NH.sub.3, light gases (C.sub.1-C.sub.4), naphtha, and diesel products, are passed to a separation stage for separating petroleum fractions. Preferably, the effluent stream from the first stage reactor is passed through a steam generator prior to the steam stripping step. In an alternate embodiment, the effluent stream from the first stage reactor is passed through a vapor/liquid separator stripper vessel prior to the steam stripping step.

A process for the treatment of a gasoline containing sulphur-containing compounds, olefins and diolefins, comprising the following steps: a) fractionating the gasoline in a manner such as to recover at least one intermediate gasoline cut, MCN, comprising hydrocarbons and wherein the temperature difference (ΔT) between the 5% and 95% by weight distillation points is less than 60° C.; b) desulphurizing the intermediate gasoline cut MCN alone and in the presence of a hydrodesulphurization catalyst and hydrogen in a manner such as to produce a partially desulphurized intermediate gasoline cut MCN; and c) fractionating, in a splitter, the at least partially desulphurized intermediate gasoline cut MCN which has not undergone catalytic treatment subsequent to step b), in a manner such as to recover an intermediate gasoline with low sulphur and mercaptans contents from the column head and a cut of hydrocarbons containing sulphur-containing compounds including mercaptans from the column bottom.

A process for the treatment of a gasoline containing sulphur-containing compounds, olefins and diolefins, comprising the following steps: a) fractionating the gasoline in a manner such as to recover at least one intermediate gasoline cut, MCN, comprising hydrocarbons and wherein the temperature difference (ΔT) between the 5% and 95% by weight distillation points is less than 60° C.; b) desulphurizing the intermediate gasoline cut MCN alone and in the presence of a hydrodesulphurization catalyst and hydrogen in a manner such as to produce a partially desulphurized intermediate gasoline cut MCN; and c) fractionating, in a splitter, the at least partially desulphurized intermediate gasoline cut MCN which has not undergone catalytic treatment subsequent to step b), in a manner such as to recover an intermediate gasoline with low sulphur and mercaptans contents from the column head and a cut of hydrocarbons containing sulphur-containing compounds including mercaptans from the column bottom.

A method of producing aromatic hydrocarbons including: supplying a raw material stream to a C6 separation column, supplying an upper discharge stream from the C6 separation column to a first gasoline hydrogenation unit, and supplying a lower discharge stream from the C6 separation column to a C7 separation column; supplying an upper discharge stream from the C7 separation column to the first gasoline hydrogenation unit and supplying a lower discharge stream from the C7 separation column to a C8 separation column; separating benzene and toluene from a discharge stream from the first gasoline hydrogenation unit; removing a lower discharge stream from the C8 separation column and supplying an upper discharge stream from the C8 separation column to a second extractive distillation column; and separating styrene from a lower discharge stream from the second extractive distillation column and separating xylene from an upper discharge stream from the second extractive distillation column.