The invention relates to a process for the manufacture of diesel range hydrocarbons wherein a feed is hydrotreated in a hydrotreating step and isomerised in an isomerisation step, and a feed comprising fresh feed containing more than 5 wt % of free fatty acids and at least one diluting agent is hydrotreated at a reaction temperature of 200-400° C., in a hydrotreating reactor in the presence of catalyst, and the ratio of the diluting agent/fresh feed is 5-30:1.

A process for reducing the benzene content of a light reformate refinery stream comprises the following steps: a) reducing the benzene content by exposing the light reformate to hydrogenation conditions in a benzene-saturation reactor bed, b) increasing the octane number of the hydrogenated light reformate produced in step a) by exposing it to isomerization conditions, c) further reducing the benzene content by exposing the light reformate refinery stream to further hydrogenation conditions, wherein the isomerization of step b) occurs after step a), the hydrogenation of step c) does not precede the isomerization step b), and steps a), b) and c) are all carried out within the same reactor.

Described herein are novel and inventive dewaxing processes that employ dewaxing catalysts which are co-extrusions of two different zeolites, particularly two different 10MR zeolites or a co-extrusion of a 10MR zeolite and a 12MR zeolite in combination with a hydrogenation component. The hydrogenation component can be a mixture of non-noble metal components or a mixture of noble metal components. This novel and inventive process demonstrated a significant activity boost (as measured by increased cloud point reduction) and/or selectivity boost (as measured by reduced diesel loss) compared to either single zeolite component.

Methods are provided for using a molecular sieve catalyst for dewaxing formed using a synthesis mixture comprising a morphology modifier. The catalyst may be used, for example, for production of a lubricant base stock. For example, ZSM-48 crystals formed using the morphology modifier (and/or formulated catalysts made using such crystals) can have an increased activity and/or can provide an improved yield during catalytic dewaxing of lubricant base stocks.

Methods are provided for using a molecular sieve catalyst for dewaxing formed using a synthesis mixture comprising a morphology modifier. The catalyst may be used, for example, for production of a lubricant base stock. For example, ZSM-48 crystals formed using the morphology modifier (and/or formulated catalysts made using such crystals) can have an increased activity and/or can provide an improved yield during catalytic dewaxing of lubricant base stocks.

A multi-stage process for the production of an ISO 8217 Table 2 residual marine fuel Product Heavy Marine Fuel Oil from a Feedstock Heavy Marine Fuel Oil that is ISO 8217:2017 Table 2 compliant except for the Environmental Contaminants involves 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 an Environmental Contaminant level less than 0.5 wt % and preferably a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 0.5 mass %. A process plant for conducting the process for conducting the process is also disclosed.

A process 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 8217 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 device for conducting the process is also disclosed.

A process 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 8217 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 device for conducting the process is also disclosed.

Systems and methods are provided for hydroprocessing of bio-derived feeds, such as bio-oils and/or other types of feeds including triglycerides, fatty acids, and/or fatty acid derivatives. The systems and methods can assist with maintaining a desired temperature profile within a reactor while performing hydroprocessing on a feed with substantial oxygen content. In various aspects, the initial bed of the reactor can be exposed to 30 vol % or less of the total fresh feed. The remaining portions of the fresh feed can be introduced below one or more of the catalyst beds in the reactor. By reducing or minimizing the amount of fresh feed introduced upstream from the initial catalyst bed that contains a catalyst with hydrodeoxygenation activity, the net amount of product recycle can be reduced or minimized while still maintaining a target temperature profile across individual catalyst beds and/or across the reactor.

Provided are an apparatus and a method for refining pyrolysis oil in which a dechlorination reaction is performed under a first hydrotreating catalyst. Hydrogen chloride as a by-product is removed, and then a denitrification reaction is performed under a second hydrotreating catalyst, thereby preventing production of an ammonium salt (NH.sub.4Cl), and providing refined oil. It is excellent in prevention of corrosion of a reactor, improvement of durability, occurrence of differential pressure, process efficiency, has very low contents of impurities such as chlorine, nitrogen, and metal and olefin, and has excellent quality.