The hydrogenation capacity of an upflow hydrocarbon hydrotreatment reactor is increased by expanding the gas-liquid contact surface.

This application relates to renewable diesel production and to production of renewable naphtha in a renewable diesel unit. Disclosed herein is an example of a method of renewable diesel production. Examples embodiments of the method may include hydrotreating the biofeedstock by reaction with hydrogen to form a hydrotreated biofeedstock; contacting at least a portion of the hydrotreated biofeedstock with a dewaxing catalyst to produce a renewable diesel product and a renewable naphtha product; separating the renewable diesel product and the renewable naphtha product in a product splitter; and monitoring an octane number of the renewable naphtha product with an analyzer.

A method for desulfurizing crude oil and sulfur rich petroleum refinery fractions is disclosed. The method includes feeding the crude oil and sulfur rich petroleum refinery fractions to a reactor. An oxidation catalyst is added to the crude oil and sulfur rich petroleum refinery fractions. The crude oil and sulfur rich petroleum refinery fractions and the oxidation catalyst are stirred to form co-polymers of sulfur-containing heterocyclic compounds. The co-polymers of sulfur-containing heterocyclic compounds are separated by filtration or by centrifugation.

A method for desulfurizing crude oil and sulfur rich petroleum refinery fractions is disclosed. The method includes feeding the crude oil and sulfur rich petroleum refinery fractions to a reactor. An oxidation catalyst is added to the crude oil and sulfur rich petroleum refinery fractions. The crude oil and sulfur rich petroleum refinery fractions and the oxidation catalyst are stirred to form co-polymers of sulfur-containing heterocyclic compounds. The co-polymers of sulfur-containing heterocyclic compounds are separated by filtration or by centrifugation.

The present disclosure relates to the thermal liquefaction of lignin, and more particularly to lignin solvolysis of a lignin feedstock chosen based on its molecular weight. The process comprises subjecting a feed mixture (30) of lignin feedstock (10) and solvent (20) to a thermal liquefaction step by heating (110) the feed mixture (30) at a temperature between 360 and 420 ° C., separating (120) a liquid product mix (50) from a product mix (40); and recirculating at least part of said liquid product mix (50) as an oil fraction of said solvent (20).

The present disclosure relates to the thermal liquefaction of lignin, and more particularly to lignin solvolysis of a lignin feedstock chosen based on its molecular weight. The process comprises subjecting a feed mixture (30) of lignin feedstock (10) and solvent (20) to a thermal liquefaction step by heating (110) the feed mixture (30) at a temperature between 360 and 420 ° C., separating (120) a liquid product mix (50) from a product mix (40); and recirculating at least part of said liquid product mix (50) as an oil fraction of said solvent (20).

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to improve the quality of vacuum residue. The improved quality of vacuum residue can be provided by one or more of reduced viscosity, reduced density (increased API gravity), reduced asphaltene content, reduced carbon residue content, reduced sulfur content, and reduced sediment. Vacuum residue of improved quality can be produced while operating the upgraded ebullated bed reactor at the same or higher severity, temperature, throughput and/or conversion. Similarly, vacuum residue of same or higher quality can be produced while operating the upgraded ebullated bed reactor at higher severity, temperature, throughput and/or conversion.

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to improve the quality of vacuum residue. The improved quality of vacuum residue can be provided by one or more of reduced viscosity, reduced density (increased API gravity), reduced asphaltene content, reduced carbon residue content, reduced sulfur content, and reduced sediment. Vacuum residue of improved quality can be produced while operating the upgraded ebullated bed reactor at the same or higher severity, temperature, throughput and/or conversion. Similarly, vacuum residue of same or higher quality can be produced while operating the upgraded ebullated bed reactor at higher severity, temperature, throughput and/or conversion.

Systems and methods are provided for producing upgraded raffinate and extract products from lubricant boiling range feeds and/or other feeds having a boiling range of 400° F. (204° C.) to 1500° F. (816° C.) or more. The upgraded raffinate and/or extract products can have a reduced or minimized concentration of sulfur, nitrogen, metals, or a combination thereof. The reduced or minimized concentration of sulfur, nitrogen, and/or metals can be achieved by hydrotreating a suitable feed under hydrotreatment conditions corresponding to relatively low levels of feed conversion. Optionally, the feed can also dewaxed, such as by catalytic dewaxing or by solvent dewaxing. Because excessive aromatic saturation is not desired, the pressure for hydrotreatment (and optional dewaxing) can be 500 psig (˜3.4 MPa) to 1200 psig (˜8.2 MPa).

Systems and methods are provided for producing upgraded raffinate and extract products from lubricant boiling range feeds and/or other feeds having a boiling range of 400° F. (204° C.) to 1500° F. (816° C.) or more. The upgraded raffinate and/or extract products can have a reduced or minimized concentration of sulfur, nitrogen, metals, or a combination thereof. The reduced or minimized concentration of sulfur, nitrogen, and/or metals can be achieved by hydrotreating a suitable feed under hydrotreatment conditions corresponding to relatively low levels of feed conversion. Optionally, the feed can also dewaxed, such as by catalytic dewaxing or by solvent dewaxing. Because excessive aromatic saturation is not desired, the pressure for hydrotreatment (and optional dewaxing) can be 500 psig (˜3.4 MPa) to 1200 psig (˜8.2 MPa).