Methods of processing bio-based material feed (“bio-feed”) and a petroleum feed, using combinations of hydrotreating beds, dewaxing beds, post-treatment beds, and liquid quenching zones. Some methods comprise processing the petroleum feed through first hydrotreating reactor beds; then processing the output with a bio-feed together through second hydrotreating reactor beds; then processing the output through the plurality of dewaxing beds to create a dewaxed stream; and, processing the dewaxed stream through the plurality of post-treatment beds to create a product stream. Other methods comprise processing the petroleum feed through the plurality of first hydrotreating reactor beds; then processing the output through the plurality of dewaxing beds to create a dewaxed stream; and, processing the dewaxed stream and the bio-feed together through the plurality of liquid quenching beds zones to create a mixed stream; and, processing the mixed stream through the plurality of post-treatment beds to create a product stream.

Methods of processing bio-based material feed (“bio-feed”) and a petroleum feed, using combinations of hydrotreating beds, dewaxing beds, post-treatment beds, and liquid quenching zones. Some methods comprise processing the petroleum feed through first hydrotreating reactor beds; then processing the output with a bio-feed together through second hydrotreating reactor beds; then processing the output through the plurality of dewaxing beds to create a dewaxed stream; and, processing the dewaxed stream through the plurality of post-treatment beds to create a product stream. Other methods comprise processing the petroleum feed through the plurality of first hydrotreating reactor beds; then processing the output through the plurality of dewaxing beds to create a dewaxed stream; and, processing the dewaxed stream and the bio-feed together through the plurality of liquid quenching beds zones to create a mixed stream; and, processing the mixed stream through the plurality of post-treatment beds to create a product stream.

In an aspect, the application discloses a method for producing renewable hydrocarbon fuels where the method includes electrolysis of a mixture to produce an electrolysis product comprising a renewable diesel and optionally a renewable gasoline, where the mixture includes (i) free fatty acids from a biorenewable feedstock, and (ii) terminal monomethyl-branched carboxylic acids, and where the renewable diesel includes terminal monomethyl-branched paraffins and terminal monomethyl-branched alkenes.

The present invention relates to a micro-interface strengthening reaction system and method for heavy oil hydrogenation preparation of ship fuel, including a liquid phase feed unit, a gas phase feed unit, a micro-interface generator, a fixed-bed reactor and a separation tank. The present invention may reduce the pressure during the reaction by 10-80% while ensuring the efficiency of the reaction by breaking the gas to form micro-sized micro-bubbles and making the micro-bubbles mix with heavy oil to form an emulsion to increase the area between the gas and the liquid phase and to achieve the effect of enhancing mass transfer in a lower preset range. And, the present invention greatly enhances the mass transfer, so that the gas-liquid ratio can be greatly reduced. Also, the method of the present invention has low process severity, high production safety, low product cost per ton, and strong market competitiveness.

According to one or more embodiments, presently disclosed are processes for producing petrochemical products from a hydrocarbon material. The process may include separating the crude oil into at least a lesser boiling point fraction and a greater boiling point fraction. At least 90 wt. % of the crude oil may be present in the combination of the greater boiling point fraction and the lesser boiling point fraction. The process may further include hydroprocessing the lesser boiling point fraction to form a first hydroprocessed effluent and hydroprocessing the greater boiling point fraction to form a second hydroprocessed effluent. The hydroprocessing of the lesser boiling point fraction may occur at a first pressure, the hydroprocessing of the lesser boiling point fraction may occur at a second pressure, and the second pressure may be at least 25 bar greater than the first pressure. The method may further include cracking at least a portion of the first hydroprocessed effluent and at least a portion of the second hydroprocessed effluent to form cracking reaction products.

Hydroprocessed residual fuel and/or fuel blending components are provided that have a sulfur and nitrogen level comparable to liquefied natural gas (LNG). Because of the low starting level of sulfur and/or nitrogen, the severity of the hydroprocessing that is needed for the crude oil or bottoms fraction in order to remove sulfur to a level that is comparable to LNG is reduced or minimized. This can allow the resulting marine residual fuels to have low carbon intensity, low SOx and NOx emission and high energy density. Since the hydroprocessed fractions correspond to a fuel oil product, the resulting marine fuel can be used in existing fleets, and can be distributed in existing bunkering systems.

Distillate boiling range and/or diesel boiling range compositions are provided that are formed from crude oils with unexpected combinations of high naphthenes to aromatics weight and/or volume ratio and a low sulfur content. This unexpected combination of properties is characteristic of crude oils that can be fractionated to form distillate/diesel boiling range compositions that can be used as fuels/fuel blending products with reduced or minimized processing. The resulting distillate boiling range fractions and/or diesel boiling range fractions can have an unexpected combination of a high naphthenes to aromatics weight and/or volume ratio, a low but substantial aromatics content, and a low sulfur content. By reducing, minimizing, or avoiding the amount of hydroprocessing needed to meet fuel and/or fuel blending product specifications, the fractions derived from the high naphthenes to aromatics ratio and low sulfur crudes can provide fuels and/or fuel blending products having a reduced or minimized carbon intensity.

Distillate boiling range and/or diesel boiling range compositions are provided that are formed from crude oils with unexpected combinations of high naphthenes to aromatics weight and/or volume ratio and a low sulfur content. This unexpected combination of properties is characteristic of crude oils that can be fractionated to form distillate/diesel boiling range compositions that can be used as fuels/fuel blending products with reduced or minimized processing. The resulting distillate boiling range fractions and/or diesel boiling range fractions can have an unexpected combination of a high naphthenes to aromatics weight and/or volume ratio, a low but substantial aromatics content, and a low sulfur content. By reducing, minimizing, or avoiding the amount of hydroprocessing needed to meet fuel and/or fuel blending product specifications, the fractions derived from the high naphthenes to aromatics ratio and low sulfur crudes can provide fuels and/or fuel blending products having a reduced or minimized carbon intensity.

A system for producing primarily diesel with some heavy fuel from plastic feedstock is described. The feedstock is received into a pyrolizer. There are two zones in the pyrolizer—one where the temperature is elevated during conveyance, and a second where the temperature is maintained. A distillation vessel receives fuel oils from the pyrolizer and agitates the oils at high temperature. A hydrogenation vessel then mixes the fuel liquid with H.sub.2 at a high pressure while recirculating to and from an expansion vessel to create converted fuel oil. A diesel distillation tank receives the converted fuel oil and creates diesel gas, which is then condensed to form a usable diesel product. Any remaining fuel oil is sent the heavy fuel oil tank.

The invention is an integrated process for treating residual oil of a hydrocarbon feedstock. The oil is first subjected to delayed coking and then oxidative desulfurization. Additional, optional steps including hydrodesulfurization, and hydrocracking, may also be incorporated in to the integrated process.