The present invention addresses to a process for the integrated production of H.sub.2 and aviation kerosene from renewable raw materials aiming at reducing CO.sub.2 emissions and consequently bringing benefits to reduce the impact of global warming on the planet. The process involves a hydrotreatment section to obtain n-paraffins followed by a hydroisomerization section to produce isoparaffins. The water and light hydrocarbons obtained in the isoparaffin production process are used for the production of H.sub.2 by the steam reforming process. An alcohol, such as ethanol or glycerin, with less than 6 carbon atoms, is fed into the hydrotreating section to make up the light hydrocarbon stream used in the production of renewable hydrogen.

The present invention addresses to a process for the integrated production of H.sub.2 and aviation kerosene from renewable raw materials aiming at reducing CO.sub.2 emissions and consequently bringing benefits to reduce the impact of global warming on the planet. The process involves a hydrotreatment section to obtain n-paraffins followed by a hydroisomerization section to produce isoparaffins. The water and light hydrocarbons obtained in the isoparaffin production process are used for the production of H.sub.2 by the steam reforming process. An alcohol, such as ethanol or glycerin, with less than 6 carbon atoms, is fed into the hydrotreating section to make up the light hydrocarbon stream used in the production of renewable hydrogen.

A process for treating effluent streams in a renewable transportation fuel production process is described. One or more of the sour water stream and an acid gas stream are treated directly in thermal oxidation section. The process allows the elimination or size reduction of a sour water stripper unit, waste water treatment plant, and sulfur recovery unit.

A process for treating effluent streams in a renewable transportation fuel production process is described. One or more of the sour water stream and an acid gas stream are treated directly in thermal oxidation section. The process allows the elimination or size reduction of a sour water stripper unit, waste water treatment plant, and sulfur recovery unit.

A system for producing needle coke and a method for producing needle coke using the system are provided. The system includes a coke tower, a pressure stabilization tower, a buffer tank and a coking fractionation tower. A pressure controller is provided at the top of the pressure stabilization tower for adjusting the pressure at the top thereof. An oil gas outlet of the coke tower is in communication with an oil gas inlet of the pressure stabilization tower through a pipeline. No pressure controller for adjusting the pressure at the top of the coke tower is provided in the coke tower or on the oil gas pipeline connecting the coke tower to the pressure stabilization tower.

The invention is a process for producing a white oil having an initial boiling point of at least 300° C., the process comprising a step of catalytically hydrogenating a hydrocarbon feedstock at a temperature of from 80 to 190° C., at a pressure of from 50 to 160 bars, a liquid hourly space velocity of 0.2 to 5 hr.sup.−1 and an hydrogen treat rate up to 200 Nm.sup.3/ton of feed, the hydrocarbon feedstock having a sulphur content of less than 10 ppm by weight, an initial boiling point within the range from 150 to 350° C. and a final boiling point within the range from 350 to 550° C.

The invention is a process for producing a white oil having an initial boiling point of at least 300° C., the process comprising a step of catalytically hydrogenating a hydrocarbon feedstock at a temperature of from 80 to 190° C., at a pressure of from 50 to 160 bars, a liquid hourly space velocity of 0.2 to 5 hr.sup.−1 and an hydrogen treat rate up to 200 Nm.sup.3/ton of feed, the hydrocarbon feedstock having a sulphur content of less than 10 ppm by weight, an initial boiling point within the range from 150 to 350° C. and a final boiling point within the range from 350 to 550° C.

A multi-stage process for the production of an ISO 8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a Reaction System composed of one or more reactor vessels selected from a group reactor wherein said one or more reactor vessels contains one or more reaction sections configured to promote the transformation of the Feedstock Heavy Marine Fuel Oil to the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil has a Environmental Contaminate level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed that can utilize a modular reactor vessel.

A multi-stage process for the production of an ISO 8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a Reaction System composed of one or more reactor vessels selected from a group reactor wherein said one or more reactor vessels contains one or more reaction sections configured to promote the transformation of the Feedstock Heavy Marine Fuel Oil to the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil has a Environmental Contaminate level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed that can utilize a modular reactor vessel.

Naphthenic process oils are made by blending one or more naphthenic vacuum gas oils in one or more viscosity ranges with a high C.sub.A content distilled aromatic extract feedstock to provide at least one blended oil, and hydrotreating the at least one blended oil to provide an enhanced C.sub.A content naphthenic process oil. The order of the vacuum distillation and blending steps may be reversed.