The present invention relates to the field of gasoline and gasoline compositions or blends. More specifically the invention relates to a novel fuel or gasoline composition with synergistic effects and use thereof, and in particular a synergistic effect with respect to the octane rating/octane number.

The present invention relates to processes for producing industrial products such as hydrocarbon products from non-polar lipids in a vegetative plant part. Preferred industrial products include alkyl esters which may be blended with petroleum based fuels.

The present invention relates to processes for producing industrial products such as hydrocarbon products from non-polar lipids in a vegetative plant part. Preferred industrial products include alkyl esters which may be blended with petroleum based fuels.

A process of producing a hydrocracking product in a slurry hydrocracking reactor. A pyrolysis oil, a hydrocarbon feedstock, and a hydrocracking catalyst is provided. The pyrolysis oil is combined with the hydrocarbon feedstock and the hydrocracking catalyst, the pyrolysis oil being maintained at a temperature of less than 100° C. until the pyrolysis oil contacts both the hydrocarbon feedstock and the hydrocracking catalyst. The hydrocarbon feedstock and the pyrolysis oil are hydrocracked in the slurry hydrocracking reactor in the presence of the hydrocracking catalyst and hydrogen gas. A fuel precursor obtainable by the process.

A process of producing a hydrocracking product in a slurry hydrocracking reactor. A pyrolysis oil, a hydrocarbon feedstock, and a hydrocracking catalyst is provided. The pyrolysis oil is combined with the hydrocarbon feedstock and the hydrocracking catalyst, the pyrolysis oil being maintained at a temperature of less than 100° C. until the pyrolysis oil contacts both the hydrocarbon feedstock and the hydrocracking catalyst. The hydrocarbon feedstock and the pyrolysis oil are hydrocracked in the slurry hydrocracking reactor in the presence of the hydrocracking catalyst and hydrogen gas. A fuel precursor obtainable by the process.

An integrated production plant system includes, at one production site at least two plants of different kinds selected from a renewable paraffinic fuel plant to produce renewable paraffinic fuel in a renewable paraffinic fuel process, a renewable fatty acid alkyl ester (FAAE) fuel plant to produce renewable FAAE fuel in a renewable FAAE process, a renewable base oil plant to produce renewable base oil in a renewable base oil process, and a renewable chemical plant to produce renewable chemical in a renewable chemical process. Each of the processes is provided with a respective renewable feed, where the feed of each of the processes originates from a common renewable system feed, and the feed to at least one of the processes is altered for example by directing at least part of the feed of at least one of the processes to another of the processes.

An integrated production plant system includes, at one production site at least two plants of different kinds selected from a renewable paraffinic fuel plant to produce renewable paraffinic fuel in a renewable paraffinic fuel process, a renewable fatty acid alkyl ester (FAAE) fuel plant to produce renewable FAAE fuel in a renewable FAAE process, a renewable base oil plant to produce renewable base oil in a renewable base oil process, and a renewable chemical plant to produce renewable chemical in a renewable chemical process. Each of the processes is provided with a respective renewable feed, where the feed of each of the processes originates from a common renewable system feed, and the feed to at least one of the processes is altered for example by directing at least part of the feed of at least one of the processes to another of the processes.

Disclosed is a method for preparing bio-oil, which can be used as bio heavy fuel oil and bio marine oil, from a fatty acid with high acid value. The method for preparing bio-oil comprises the steps of: inputting materials comprising glycerine and a fatty acid into respective material input ports positioned in the center of a column-type reactor and esterification reacting the material comprising glycerine and fatty acid in each tray of a reaction area, thereby producing glyceride and water, wherein the column-type reactor has the plurality of trays installed inside the reactor so as to form a plurality of compartments in the vertical direction inside the reactor, openings are formed in the plurality of trays to connect the compartments which are vertically adjacent, and the openings of the adjacent compartments are alternately formed in a crisscrossing manner; obtaining the produced glyceride through a lower part of the reactor; and vaporizing the water produced by the esterification reaction, moving the water in a vapor state to a distillation area in an upper part of the reactor to separate the water from active components (reaction material and bio-oil) comprised in the vapor, allowing the separated active components to flow into the reaction area, and removing the separated water through the upper part of the reactor in a vapor state. The acid value of the glyceride is 30 mgKOH/g or lower, and the esterification reaction is performed at a reaction temperature of 200 to 250° C. and at ordinary pressure without using a catalyst.

Disclosed is a method for preparing bio-oil, which can be used as bio heavy fuel oil and bio marine oil, from a fatty acid with high acid value. The method for preparing bio-oil comprises the steps of: inputting materials comprising glycerine and a fatty acid into respective material input ports positioned in the center of a column-type reactor and esterification reacting the material comprising glycerine and fatty acid in each tray of a reaction area, thereby producing glyceride and water, wherein the column-type reactor has the plurality of trays installed inside the reactor so as to form a plurality of compartments in the vertical direction inside the reactor, openings are formed in the plurality of trays to connect the compartments which are vertically adjacent, and the openings of the adjacent compartments are alternately formed in a crisscrossing manner; obtaining the produced glyceride through a lower part of the reactor; and vaporizing the water produced by the esterification reaction, moving the water in a vapor state to a distillation area in an upper part of the reactor to separate the water from active components (reaction material and bio-oil) comprised in the vapor, allowing the separated active components to flow into the reaction area, and removing the separated water through the upper part of the reactor in a vapor state. The acid value of the glyceride is 30 mgKOH/g or lower, and the esterification reaction is performed at a reaction temperature of 200 to 250° C. and at ordinary pressure without using a catalyst.

A method for conversion of food waste to biofuel can include a first fermentation in which food waste is converted C.sub.2-C.sub.4 short-chain carboxylic acids, and a second fermentation in which the C.sub.2-C.sub.4 short-chain carboxylic acid are elongated into C.sub.5-C.sub.8 medium-chain carboxylic acids. Medium-chain carboxylic acids can undergo hydrogenation-dehydration of the medium-chain carboxylic acids into C.sub.5-C.sub.8 linear olefins. The C.sub.5-C.sub.8 linear olefins are then oligomerized to a C.sub.10-C.sub.25 mixture comprising olefins, paraffin, cycloparaffins, and aromatics through dimerization; and saturated to C.sub.10-C.sub.25 mixture by hydrogenation to produce the biofuel.