The invention relates to a method for processing black liquor soap, particularly to a method for producing and recovering fatty acid esters and resin acids from black liquor soap. The method is based on a catalytic selective esterification of the soap.

The invention relates to a method for processing black liquor soap, particularly to a method for producing and recovering fatty acid esters and resin acids from black liquor soap. The method is based on a catalytic selective esterification of the soap.

The invention relates to a method for producing an oil rich fraction (OF) from primary feedstock (FS) that comprises water, first salt, second salt, and biomass. The feedstock (FS) is provided to a first reaction zone (Z1) of a conversion reactor (100), where it is allowed to react at a temperature of at least 350° C. in a pressure of at least 160 bar to form converted primary feedstock. The method comprises separating from the converted primary feedstock a first salt rich fraction (SF1), a second salt rich fraction (SF2), and an oil rich fraction (OF). The method comprises withdrawing the oil rich fraction (OF) from the first reaction zone (Z1) and withdrawing the first salt rich fraction (SF1) and the second salt rich fraction (SF2) from the conversion reactor (100). In the method the first salt rich fraction (SF1) comprises at least some of the first salt dissolved in the water, the second salt rich fraction (SF2) comprises at least some of the second salt in solid form, and at least one of the first salt and the second salt is a salt capable of catalysing the reaction of the biomass of the primary feedstock (FS) with the water of the primary feedstock (FS) to produce the oil rich fraction (OF). A device for the same.

Provided are methods to destabilize emulsion feedstocks. In the methods, a moderate temperature is applied to the feedstock to create a first mixture. The moderate temperature may be between 120 and 220 degrees Celsius. The first mixture is mixed at the moderate temperature, such as by staged mixing in some embodiments. Moreover, the first mixture is retained at the moderate temperature for up to six hours. The first mixture is separated into an oil phase, convoluted phase, and a water phase. In some embodiments, the moderate temperature may be 125 to 150 degrees Celsius, such as between 125 and 130 degrees Celsius. Moreover, the first mixture may be retained at the moderate temperature for between forty-five minutes and four hours, such as from two to four hours. The separation may occur at the moderate temperature.

Provided are methods to destabilize emulsion feedstocks. In the methods, a moderate temperature is applied to the feedstock to create a first mixture. The moderate temperature may be between 120 and 220 degrees Celsius. The first mixture is mixed at the moderate temperature, such as by staged mixing in some embodiments. Moreover, the first mixture is retained at the moderate temperature for up to six hours. The first mixture is separated into an oil phase, convoluted phase, and a water phase. In some embodiments, the moderate temperature may be 125 to 150 degrees Celsius, such as between 125 and 130 degrees Celsius. Moreover, the first mixture may be retained at the moderate temperature for between forty-five minutes and four hours, such as from two to four hours. The separation may occur at the moderate temperature.

A method may include: providing bio waste stream wherein the bio waste stream comprises at least one bio waste selected from the group consisting of palm oil mill effluent, soapstock, and combinations thereof; introducing the bio waste effluent stream into a fluidized catalytic cracking unit; contacting the bio waste with a catalyst in the fluidized catalytic cacking unit; and cracking at least a portion of the bio waste stream to form cracked products that comprise a cracked product stream.

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.

Method for purifying crude tall oil soap from black liquor, wherein a washing liquid is used, which washing liquid is either pH-regulated residual liquid from a tall oil producing processing step (180) or a pH-regulated aqueous solution of ash, wherein black liquor-containing crude tall oil soap is mixed with said washing liquid, and wherein the crude tall oil soap is then separated out from the resulting mixture. The method comprises the steps 1. performing a first coarse separation (120,130) of crude tall oil soap from said black liquor, so that a first crude tall oil soap fraction is formed; 2. mixing (140) the first crude tall oil soap fraction with washing liquid, so that a first diluted fraction is formed; and 3. performing a separation (150) of the first diluted fraction using a first centrifugal separator of purificator type, so that a second crude tall oil soap fraction is achieved. The second crude tall oil soap fraction comprises smaller contents of black liquor than the first crude tall oil soap fraction. The invention also relates to a system.

Provided are methods to destabilize emulsion feedstocks. Benefits of the provided methods include a reducing or eliminating the amount of acid necessary to process the feedstocks, less processing time, cleaner separation of the resulting phases, and increased recovery of valuable products. In the methods, a moderate temperature is applied to the feedstock to create a first mixture. The moderate temperature may be between 120 and 220 degrees Celsius. The first mixture is mixed at the moderate temperature, such as by staged mixing in some embodiments. Moreover, the first mixture is retained at the moderate temperature for up to six hours. The first mixture is separated into an oil phase, convoluted phase, and a water phase. In some embodiments, the moderate temperature may be 125 to 150 degrees Celsius, such as between 125 and 130 degrees Celsius. Moreover, the first mixture may be retained at the moderate temperature for between forty-five minutes and four hours, such as from two to four hours. The separation may occur at the moderate temperature.