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WO2015178633A1 - Appareil de production de dérivé d'acide gras et appareil de recyclage de sous-produits - Google Patents

Appareil de production de dérivé d'acide gras et appareil de recyclage de sous-produits Download PDF

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Publication number
WO2015178633A1
WO2015178633A1 PCT/KR2015/004917 KR2015004917W WO2015178633A1 WO 2015178633 A1 WO2015178633 A1 WO 2015178633A1 KR 2015004917 W KR2015004917 W KR 2015004917W WO 2015178633 A1 WO2015178633 A1 WO 2015178633A1
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WIPO (PCT)
Prior art keywords
reaction
fatty acid
regeneration
reactor
acid derivative
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/KR2015/004917
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English (en)
Korean (ko)
Inventor
문영기
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Pathwel Co ltd
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Pathwel Co ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from KR1020140062312A external-priority patent/KR101430393B1/ko
Priority claimed from KR1020140062319A external-priority patent/KR101436285B1/ko
Application filed by Pathwel Co ltd filed Critical Pathwel Co ltd
Publication of WO2015178633A1 publication Critical patent/WO2015178633A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids

Definitions

  • the present invention relates to a fatty acid derivative production apparatus and a byproduct regeneration apparatus applied to a fatty acid derivative production process, and more particularly, it is possible to save a time required for preparing a reaction by providing a plurality of reaction apparatuses, as well as to proceed with the reaction process.
  • Fatty acid derivative production equipment that can reduce raw materials and reduce contaminants by recovering ammonia generated from the reaction apparatus, and input it into a reaction equipment that is preparing for reaction, and recycles the fatty acid and ammonia to produce fatty acid derivatives.
  • the present invention relates to a by-product regeneration device applied to a fatty acid derivative production process that can be reused by recycling the by-products generated in the reaction.
  • Fatty acid derivatives are very useful substances widely used as raw materials for surfactants, soaps, cosmetics, pharmaceuticals, lubricants or biodiesel.
  • Fatty acid derivatives can be produced by reacting fatty acids with ammonia (NH 3 ) or ester (ester), and are known materials that have been produced for a long time.
  • 1 is a view showing a schematic process of conventionally producing a fatty acid derivative using ammonia.
  • the fatty acid derivative is produced through a reaction process 10, a treatment process 30, a purification process 50, a powdering process 70, and a packaging process 90.
  • Fatty acid is added to the reactor to purge nitrogen, and then ammonia (NH 3 ) is added to react.
  • Reaction step 10 is a reaction temperature of 150 ⁇ 250 °C, the reaction pressure is 5 ⁇ 15Kg / cm 2
  • the treatment step 30 is carried out.
  • the treatment process 30 may be made in a reaction apparatus or may be made in a separate treatment apparatus.
  • the treatment step 30 is a step of separating caustic soda (NaOH, sodium hydroxide) into the fatty acid after the reaction in the reaction step 10 to separate the unreacted fatty acid from the completed fatty acid.
  • caustic soda NaOH, sodium hydroxide
  • the treatment step 30 is a step of separating caustic soda (NaOH, sodium hydroxide) into the fatty acid after the reaction in the reaction step 10 to separate the unreacted fatty acid from the completed fatty acid.
  • the reaction is completed and the fatty acid which has not been reacted is separated and the reaction is completed and the fatty acid is sent to the purification step 50.
  • the refining step 50 only the fatty acid having completed the reaction is purified with high purity, and in the powdering step 70, the high-purity fatty acid derivative is powdered and packaged in the packing step 90.
  • the fatty acid derivative production method of the above-described manner is a well-known technique widely used in the prior art, and further detailed description thereof will be omitted.
  • one conventional reaction apparatus used in the reaction process 10 consists of one.
  • the reaction apparatus due to the time required for the reaction preparation step, the fatty acid derivative is used.
  • the overall process time to produce is long. That is, the fatty acid is added to the reactor to purge nitrogen, and the temperature of the reactor is heated to 150 to 250 ° C. in order to proceed with the reaction step 10 by adding ammonia. It takes a lot of time, which increases the overall process time.
  • ammonia (NH 3 ) emitted in the reaction process 10 is discarded as it is, there is a problem of raising the production cost due to waste of raw materials and causing environmental pollution.
  • the present invention has been made to solve the above problems, by constructing a plurality of reaction apparatus used in the reaction process by preparing the reaction in advance in the other reaction apparatus while the reaction process is carried out in one reaction apparatus, the product is made continuously
  • the purpose is to make.
  • a fatty acid derivative production apparatus that can reduce production costs and reduce environmental pollution by recovering ammonia flowing from the reaction device in the reaction process to be put into the reactor to prepare the reaction to reuse.
  • the purpose is.
  • Another object of the present invention is to provide a by-product regeneration apparatus applied to a fatty acid derivative production process that can reduce and reuse sodium salt by-products generated in a treatment process to fatty acids.
  • the fatty acid derivative production apparatus includes a reaction apparatus for reacting a fatty acid, a processing apparatus for separating a completed fatty acid from the fatty acid reacted in the reaction apparatus, and in the processing apparatus.
  • Fatty acid derivative production apparatus comprising a refining apparatus for refining the separated fatty acid is completed, a powdering apparatus for powdering the fatty acid derivatives purified in the refining apparatus and a packaging device for packaging the powdered fatty acid derivatives
  • the reaction apparatus includes a first reaction apparatus and a second reaction apparatus, and while the first reaction apparatus proceeds with the reaction process, the second reaction apparatus proceeds with the reaction preparation process to process the fatty acid having completed the reaction process. It can be fed continuously into the device.
  • the by-product regeneration apparatus applied to the fatty acid derivative production process includes a reaction apparatus for reacting fatty acids, a treatment apparatus for separating the completed fatty acid from the fatty acids reacted in the reaction apparatus, and a reaction separated from the treatment apparatus.
  • Regeneration of by-products applied to the fatty acid derivative production process comprising a refining apparatus for refining the completed fatty acid, a powdering apparatus for powdering the fatty acid derivatives purified in the refining apparatus, and a packaging apparatus for packaging the powdered fatty acid derivatives.
  • the treatment apparatus is further provided with a regeneration device
  • the regeneration device is a by-product storage tank for storing the by-products generated in the processing device and a regeneration reaction device for regenerating the by-product stored in the by-product storage tank and the
  • the water tank for supplying water to the regeneration reactor and the regeneration reactor It can comprise a purification unit for purifying waste water by receiving subjected to the regeneration device and a sulfuric acid tank for supplying a fatty acid and a playback storage tank for storing the reproduced fatty acid in the regeneration device.
  • the reaction process may be continuously performed by including a plurality of reaction apparatuses in the reaction process and proceeding the reaction preparation process in another reaction apparatus while the reaction process is performed in one reaction apparatus.
  • the overall production time is reduced, thereby reducing the production cost.
  • the amount of ammonia used can be reduced and environmental pollution caused by ammonia emissions can be reduced. have.
  • 1 is a view showing a schematic process of conventionally producing fatty acid derivatives using ammonia.
  • FIG. 2 shows an example of a reaction apparatus and a treatment apparatus according to the present invention.
  • Figure 3 is a view showing another embodiment of the fatty acid derivative production apparatus according to the present invention.
  • FIG. 2 is a view showing an example of an apparatus for producing fatty acid derivatives according to the present invention.
  • the fatty acid derivative production apparatus is a reaction device for reacting fatty acids (refer to the apparatus applied to the reaction process in Figure 1, 10) and the fatty acid reacted in the reaction device (10)
  • Treatment apparatus for separating the reaction is completed in the treatment apparatus (refer to the apparatus applied to the treatment process in Figure 1, 30), and purification apparatus (refining process in Figure 1) the purified reaction of the fatty acid separated in the treatment apparatus 30 50), and a powdering apparatus for powdering fatty acid derivatives purified in the refining apparatus 50 (refer to the apparatus applied to the powdering process in Figure 1, 70) and the powdered fatty acid derivatives
  • Packaging device for packaging the is configured, the reactor 10 is composed of a first reactor 110 and a second reactor 130 The first reactor 110 performs a reaction process.
  • the second reaction device 130 may proceed with the reaction preparation step so that the fatty acid that has completed the reaction process may be continuously introduced into the treatment device.
  • the treatment device 30 mixes a fatty acid and ammonia, and adds caustic soda (NaOH; sodium hydroxide) to the ammonia that has been reacted to separate the raw material that is partially present in the non-reacted raw material.
  • the refining device 50 serves to make a high purity fatty acid derivative by re-purifying the reaction is completed in the separated raw material
  • the powdering device 70 serves to make a high purity fatty acid derivative in powder form
  • the packaging device 90 serves to package the powdered fatty acid derivative.
  • the fatty acid derivative production process and apparatus as described above are well known in the art and detailed description thereof will be omitted.
  • the reaction device 10 is a reaction process is performed, the reaction process may be composed of a reaction preparation step and the reaction step.
  • the reaction preparation process consists of adding a fatty acid to the reactor to purge the nitrogen and purging the reactor to a temperature necessary for the reaction.
  • ammonia NH 3
  • NH 3 ammonia
  • the fatty acid derivative production device includes a first reaction device 110 in which the reaction device 10 performs a reaction preparation process and a second reaction device 130 in which the reaction process is performed.
  • the time required by the treatment device 30 or the purification device 50 is shorter than the time required by the reaction process.
  • the time required for the reaction preparation process in the reaction process is quite long, the time required for the entire process tends to be determined by the time of the reaction process. Therefore, the time required for the reaction process is a factor that determines the productivity, reducing the reaction process time can improve the productivity.
  • the fatty acid derivative production apparatus includes at least two or more reaction apparatuses in a reaction process, and performs a preparation process required for the reaction in another reaction apparatus while the reaction process is performed in one reaction apparatus. This can reduce the time required. According to the fatty acid derivative production method according to the present invention, it has been shown that the production process of 4 to 6 hours can be shortened as compared with the production method generally used in the related art.
  • the first reactor 110 and the second reactor 130 may be configured in parallel as shown in FIG. 2. That is, the first reactor 110 and the second reactor 130 may be processed. Each connected to 30 may be directly input from the first reaction apparatus 110 to the processing apparatus 30, or may be directly input from the second reaction apparatus 130 to the processing apparatus 30. Therefore, the reaction preparation process and the reaction process are performed in the first reaction device 110, and immediately after the reaction process is completed, the reaction device 30 is directly added to the treatment device 30, and the second reaction device 130 separately prepares the reaction preparation process and the reaction process. After performing the reaction, the completed fatty acid may be added to the treatment step 30.
  • the driving time of the first reaction device 110 and the second reaction device 130 are different from each other, and after the treatment process is completed in the processing device 30, the first reaction device 110 completes the reaction.
  • the second reaction apparatus 130 may allow the fatty acids that have completed the reaction to be sequentially introduced into the treatment apparatus 30. have.
  • this configuration represents an example of the present invention, the first reactor 110 and the second reactor 130 is connected in series so that any one reactor performs only the reaction preparation process, the other reaction
  • the apparatus may be adapted to carry out only the reaction process. That is, the first reaction apparatus 110 performs only a reaction preparation process to transfer the fatty acid having completed the reaction preparation process to the second reaction apparatus 130, and the second reaction apparatus 130 performs only a reaction process to process the apparatus ( 30).
  • the first reactor 110 and the second reactor 130 are connected by an ammonia pump 150 to transfer ammonia generated in one reactor to another reactor. You can do that.
  • the fatty acid and ammonia are reacted at about 150 to 250 ° C. and a reaction pressure of 5 to 15 kg / cm 2 .
  • a part of ammonia is discharged in a liquid or gaseous state, but conventionally, the ammonia thus discharged is discarded as it is.
  • the amount of ammonia lost in the next reaction process must be replenished, and as a result, the raw materials used in the reaction process are wasted. It can also cause a worsening of the environment.
  • an ammonia pump 150 is provided between the first reactor 110 and the second reactor 130, and the ammonia pump 150 reacts with the first reactor 110 and the second reactor through a pipe.
  • the device 130 By being connected to the device 130, some ammonia discharged from the reaction process can be injected into the reaction preparation process. As such, by collecting and recycling the discarded ammonia, not only the production cost can be reduced, but also the environmental pollution and the working environment can be improved.
  • the ammonia pump 150 serves to transfer the ammonia discharged from the reaction process to the reaction preparation process. Accordingly, when the first reactor 110 and the second reactor 130 are connected in parallel, the direction in which the ammonia pump 150 flows out of the ammonia pump 150 varies according to the processes performed in each reactor. do. When the reactors are connected in parallel, the reaction preparation process is carried out in one reactor and the reaction process is progressed in the other reactors. Transfer to another reactor running.
  • the ammonia pump 150 may further include an ammonia accommodating part (not shown) capable of temporarily accommodating ammonia discharged from the reaction process.
  • an ammonia accommodating part capable of temporarily accommodating ammonia discharged from the reaction process.
  • the ammonia pump 150 may be further provided with a cooling device (not shown) to liquefy gaseous ammonia generated in the second reaction device 130 to be transferred to the first reaction device 110.
  • a cooling device not shown
  • Various types of well-known cooling apparatuses may be applied, and for example, the pipe connecting the first reactor 110 and the second reactor 130 may be cooled with coolant or the like to liquefy ammonia inside the transfer pipe. .
  • the first reactor 110 and the second reactor 130 may be composed of a reaction tank 120 and the stirring device 121 provided in the reaction tank 120, respectively, the reaction tank 120
  • the reaction tank 120 On the outside of the heating device 123 for heating the reaction tank 120 and the heat insulating portion 125 to surround the whole or a portion of the heating device 123 and the reaction tank 120 may be provided,
  • the heat insulating part 125 may be formed in an airgel (aerogel) heat insulating layer and may be provided in a form that completely or partially covers the reaction tank 120.
  • the driving method of the fatty acid derivative production apparatus in the configuration as described above, first reacted by mixing the fatty acid and ammonia in the reaction step, and then transfer the completed fatty acid to the processing device (30) unreacted The fatty acid is separated from the completed fatty acid.
  • the first reaction device 110 and the second reaction device 130 may be provided so as to be in charge of the reaction preparation step and the reaction step required for the reaction, respectively.
  • the time required for the reaction process can be shortened.
  • the ammonia discharged from the reaction process can be recovered and re-injected into the reaction apparatus performing the reaction preparation process to prevent waste of raw materials and to prevent environmental pollution.
  • T1 which is not described in the drawings, is a tank in which nitrogen for nitrogen purging is stored
  • T2 is a tank in which fatty acids are stored
  • T3 is a tank in which ammonia is stored
  • T4 is a tank in which caustic soda is stored
  • Re represents a regeneration process.
  • Figure 3 is a view showing another embodiment of the fatty acid derivative production apparatus according to the present invention.
  • the fatty acid derivative producing apparatus may further include a regeneration device 200 in the processing device 30.
  • the regeneration apparatus 200 may include a by-product storage tank 210, a regeneration reaction apparatus 230, a water tank 250, a sulfuric acid tank 270, a regeneration fatty acid storage tank 280 and a purification device 290. .
  • the reaction is completed, the fatty acid is not 100% reaction, but usually only about 85 to 95% of the reaction is completed because there is an unreacted fatty acid of about 5 to 15%.
  • the reaction yield increases as the fatty acid reacts for a long time, but there is a problem that the product cost increases because the productivity decreases as the reaction time increases. Therefore, when the reaction of the yield with good efficiency over time is completed, the reaction process is stopped and the reaction apparatus separates the unreacted fatty acid and the completed fatty acid. After the reaction is completed, the fatty acid becomes a finished product through the purification apparatus 50, the powdering apparatus 70, and the packaging apparatus 90 as described above.
  • the untreated fatty acid separated from the treatment device 30 is discharged as a by-product in the form of sodium salt.
  • the by-product discharged from the treatment device 30 is treated as waste.
  • by-products discharged from the treatment device 30 are classified as industrial wastes, resulting in a high treatment cost, resulting in a double loss in which raw materials are wasted.
  • the by-product regeneration apparatus applied to the fatty acid derivative production process according to the present invention can reduce the by-products generated in the processing device 30 to fatty acids and reuse them.
  • the by-product storage tank 210 is connected to the processing device 30 and the pipe serves to temporarily store the by-product discharged from the processing device 30.
  • the regeneration reaction apparatus 230 performs a reaction for reducing by-products stored in the by-product storage tank 210 to fatty acids, and a heating apparatus 233 for heating the regeneration tank 231 and the regeneration tank 231. It may be configured to include a heat insulating part 235 to insulate the regeneration tank 231 heated by the heating device 233.
  • an agitator 237 may be further provided inside the regeneration tank 231 to agitate the sulfuric acid solution used for the by-product and the reduction reaction in the regeneration process.
  • the heating device 233 may be applied with various known heating means and may be provided inside or outside the regeneration tank 231.
  • the heat insulating part 235 may be configured to surround all or a part of the regeneration tank 231, and may be preferably formed of an aerogel insulating layer.
  • the stirring device 237 is provided with a spiral blade inside the regeneration tank 231 to rotate the blade using a motor.
  • the water tank 250 and the sulfuric acid tank 270 are connected to the regeneration reaction apparatus 230 through a pipe.
  • the water supplied from the water tank 250 and the sulfuric acid (H 2 SO 4 ) supplied from the sulfuric acid tank 270 are mixed to form an aqueous sulfuric acid solution of about 5 to 25% to be introduced into the regeneration reactor 230.
  • the regeneration fatty acid storage tank 280 and the purification device 290 are connected to the lower portion of the regeneration reaction device 230 through a pipe to receive waste water and fatty acids after the regeneration process is completed.
  • the by-product in the form of sodium salt (Sodium salt) is reacted with the sulfuric acid solution in the regeneration reaction unit 230 is converted into fatty acids and water (including sulfuric acid), the fatty acid is floated in water because the specific gravity is about 0.85. Therefore, after a certain time after the regeneration reaction is completed, water and fatty acids are separated, it can be separated while sequentially discharging water and fatty acids to the lower portion of the regeneration reaction device (230).
  • the discharged water is sent to the purification device 290, and then discarded, and the fatty acid can be stored and reused in the regeneration fat storage tank 280.
  • the regeneration fatty acid storage tank 280 may be further provided with a cleaning device (not shown).
  • the fatty acid separated from the regeneration reaction apparatus 230 may be washed 5 to 7 times with water to recover the final product.
  • the sodium salt is reduced to fatty acids.
  • the fatty acid floats on the upper side of the regeneration reaction tank 230, and water (water containing sulfuric acid) is lowered and separated.
  • the water located in the lower portion of the regeneration reaction tank 230 is discharged first, the fatty acid located in the upper portion is discharged later. Therefore, it is possible to separate and store water and fatty acids in the regeneration fatty acid storage tank 280 and the purification device 290 connected to the outlet.
  • the water stored in the purification device 290 is discharged after being purified to a certain level.
  • the fatty acid stored in the regeneration fatty acid storage tank 280 is still stained with sulfuric acid can be used after washing using a washing apparatus.

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Fats And Perfumes (AREA)

Abstract

La présente invention concerne un appareil de production de dérivé d'acide gras et un appareil de recyclage de sous-produit appliqué à un processus de production de dérivé d'acide gras. L'appareil de production de dérivé d'acide gras est conçu pour comprendre : un dispositif de réaction pour faire réagir un acide gras ; un dispositif de traitement pour séparer l'acide gras ayant achevé une réaction, de l'acide gras mis à réagir dans le dispositif de réaction ; un dispositif de raffinage pour purifier l'acide gras qui a achevé une réaction et a été séparé dans le dispositif de traitement ; un dispositif de réduction en poudre pour réduire en poudre un dérivé d'acide gras raffiné dans le dispositif de raffinage ; et un dispositif d'emballage pour emballer le dérivé d'acide gras réduit en poudre. Le dispositif de réaction comporte un premier dispositif de réaction et un deuxième dispositif de réaction, et tandis que le premier dispositif de réaction réalise un processus de réaction, le deuxième dispositif de réaction réalise un processus de préparation de réaction de sorte qu'un acide gras qui a achevé un processus de réaction peut ensuite être introduit dans le dispositif de traitement.
PCT/KR2015/004917 2014-05-23 2015-05-15 Appareil de production de dérivé d'acide gras et appareil de recyclage de sous-produits Ceased WO2015178633A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
KR1020140062312A KR101430393B1 (ko) 2014-05-23 2014-05-23 지방산 유도체 생산공정에 적용되는 부산물 재생장치
KR1020140062319A KR101436285B1 (ko) 2014-05-23 2014-05-23 지방산 유도체 생산장치
KR10-2014-0062312 2014-05-23
KR10-2014-0062319 2014-05-23

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WO2015178633A1 true WO2015178633A1 (fr) 2015-11-26

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Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH08113585A (ja) * 1994-10-17 1996-05-07 Mitsubishi Chem Corp ショ糖脂肪酸エステルの製品化方法
WO2001019781A1 (fr) * 1999-09-16 2001-03-22 Cognis Deutschland Gmbh & Co. Kg Procede de production d'amides d'acide gras
KR20010032350A (ko) * 1997-11-24 2001-04-16 노르만 에르건 지방산 메틸 에스테르 제조 방법 및 그를 실현하기 위한장치
US20020062035A1 (en) * 2000-11-22 2002-05-23 Nobuhiro Tatsumi Process for producing lower alkyl fatty esters
JP2007176973A (ja) * 2005-12-27 2007-07-12 Lion Corp 軽油代替燃料用の脂肪酸低級アルキルエステルの製造方法
WO2007088702A1 (fr) * 2006-01-31 2007-08-09 Revo International Inc. Procede de production d'ester d'alkyle d'acide gras et appareil de production correspondant
US20090301932A1 (en) * 2006-04-26 2009-12-10 Petroleo Braisleiro S.A. - Petrobras Process for hydroconversion of a mixture of organic oils of different origins
KR101265759B1 (ko) * 2006-04-28 2013-05-20 에스케이케미칼주식회사 지방산을 이용한 지방산알킬에스테르의 제조방법 및 장치
WO2013116342A2 (fr) * 2012-02-02 2013-08-08 Revolution Fuels, Inc. Systèmes de traitement mobiles et procédés pour la production de combustible biodiesel à partir d'huiles usées
KR101330835B1 (ko) * 2011-10-05 2013-11-19 김유근 바이오디젤 생산공정의 부산물인 폐글리세롤로부터 지방산을 회수하는 방법

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH08113585A (ja) * 1994-10-17 1996-05-07 Mitsubishi Chem Corp ショ糖脂肪酸エステルの製品化方法
KR20010032350A (ko) * 1997-11-24 2001-04-16 노르만 에르건 지방산 메틸 에스테르 제조 방법 및 그를 실현하기 위한장치
WO2001019781A1 (fr) * 1999-09-16 2001-03-22 Cognis Deutschland Gmbh & Co. Kg Procede de production d'amides d'acide gras
US20020062035A1 (en) * 2000-11-22 2002-05-23 Nobuhiro Tatsumi Process for producing lower alkyl fatty esters
JP2007176973A (ja) * 2005-12-27 2007-07-12 Lion Corp 軽油代替燃料用の脂肪酸低級アルキルエステルの製造方法
WO2007088702A1 (fr) * 2006-01-31 2007-08-09 Revo International Inc. Procede de production d'ester d'alkyle d'acide gras et appareil de production correspondant
US20090301932A1 (en) * 2006-04-26 2009-12-10 Petroleo Braisleiro S.A. - Petrobras Process for hydroconversion of a mixture of organic oils of different origins
KR101265759B1 (ko) * 2006-04-28 2013-05-20 에스케이케미칼주식회사 지방산을 이용한 지방산알킬에스테르의 제조방법 및 장치
KR101330835B1 (ko) * 2011-10-05 2013-11-19 김유근 바이오디젤 생산공정의 부산물인 폐글리세롤로부터 지방산을 회수하는 방법
WO2013116342A2 (fr) * 2012-02-02 2013-08-08 Revolution Fuels, Inc. Systèmes de traitement mobiles et procédés pour la production de combustible biodiesel à partir d'huiles usées

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