WO2005017075A1 - 副産物を生成しないバイオディーゼル燃料の無触媒製造法 - Google Patents
副産物を生成しないバイオディーゼル燃料の無触媒製造法 Download PDFInfo
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- WO2005017075A1 WO2005017075A1 PCT/JP2004/011485 JP2004011485W WO2005017075A1 WO 2005017075 A1 WO2005017075 A1 WO 2005017075A1 JP 2004011485 W JP2004011485 W JP 2004011485W WO 2005017075 A1 WO2005017075 A1 WO 2005017075A1
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- WIPO (PCT)
- Prior art keywords
- reaction
- biodiesel fuel
- fatty acid
- weight
- methanol
- Prior art date
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Classifications
-
- 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
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/003—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fatty acids with alcohols
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
- C10L1/026—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only for compression ignition
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/10—Liquid carbonaceous fuels containing additives
- C10L1/14—Organic compounds
- C10L1/18—Organic compounds containing oxygen
- C10L1/182—Organic compounds containing oxygen containing hydroxy groups; Salts thereof
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- the present invention relates to a method for producing biodiesel fuel from animal or vegetable fats or oils or waste cooking oil and methanol.
- biodiesel fuel which is used to produce animal and vegetable oils and fats or waste edible oil, has been used.
- Biodiesel fuel generally includes fatty acid methyl esters obtained by transesterification (hereinafter referred to as methanolysis reaction) of triacinoleglycerol, which is a main component of animal and vegetable fats and oils and waste cooking oil, with methanol. Refers to fuel as a component.
- the methanolysis reaction between triacylglycerol and methanol can be divided into three stages.
- one molecule of fatty acid methyl ester and one molecule of diacino glycerol are produced from one molecule of triacylglycerol and one molecule of methanol.
- the second stage is
- one molecule of fatty acid methyl ester and one molecule of monoacylglycerol are produced from one molecule of diacylglycerol and one molecule of methanol.
- one molecule of fatty acid methyl ester and one molecule of glycerin are generated from one molecule of monoacylglycerol and one molecule of methanol.
- a methanolysis reaction is generally performed using a catalyst such as an alkali catalyst or an acid catalyst.
- a catalyst such as an alkali catalyst or an acid catalyst.
- Product contamination eg, sodium hydroxide
- An object of the present invention is a method for producing a biodiesel fuel from animal or vegetable fats or waste cooking oil and methanol, which does not use a catalyst and does not produce glycerin as a by-product. To provide.
- the present invention includes the following inventions.
- a process for producing a biodiesel fuel comprising mixing an animal or vegetable fat or oil or waste cooking oil with methanol and performing a methanolysis reaction without using a catalyst under a reaction condition in which glycerin is not generated.
- reaction conditions in which glycerin is not produced are characterized in that the reaction temperature is 370 500 ° C., the reaction pressure is 20 60 MPa, and the reaction time is 412 minutes. ).
- the present invention provides a biodiesel fuel without generating glycerin by appropriately controlling various conditions in a methanolysis reaction to complete the first-stage reaction and suppress the third-stage reaction.
- the degree of the reaction in the second step may be arbitrary, but as the reaction in the second step proceeds, the concentration of diacylglycerol in the obtained biodiesel fuel decreases and the concentration of monoacylglycerol increases. Since the viscosity of the biodiesel fuel decreases as the temperature increases, it is preferred that the conditions of the methanolysis reaction be controlled so that the second-stage reaction is promoted.
- Decatalysis can be achieved by performing a methanolysis reaction under supercritical conditions.
- the yield of biodiesel fuel is improved.
- the yield which used to be about 80% of the feedstock, is now almost 100%.
- the biodiesel fuel produced by the method of the present invention contains fatty acid methyl ester, diacylglycerol and monoacylglycerol as main components.
- biodiesel fuel produced according to the prior art has fatty acid methyl esters as a main component and substantially no diacylglycerol or monoacylglycerol.
- diacino glycerol or monoacyl glycerol having a long-chain fatty acid group has a higher viscosity than fatty acid methyl ester, and is therefore often suitable for diesel fuel.
- the present invention further provides a fatty acid group having a carbon chain decomposing reaction in parallel with a methanolysis reaction to convert a long-chain fatty acid group into a medium-chain fatty acid group having about 6 to 12 carbon atoms. It is possible to reduce the viscosity of a mixture containing acid methyl ester, diacylglycerol and monoacylglycerol as main components, and to provide a biodiesel fuel having a viscosity usable as a biodiesel fuel.
- the present invention further relates to a biodiesel fuel containing fatty acid methyl ester, monoacylglycerol and diacylglycerol as main components.
- main component means that fatty acid methyl ester is 40% by weight or more, and monoacinoregglycerol is 10% by weight or more.
- diacino reglycerol in a proportion of 5% by weight or more.
- group III compounds less than 1% by weight of triacylglycerol and less than 1% by weight of glycerin.
- other aliphatic compounds refer to the description below.
- a biodiesel fuel having a cetane number of 49-65, a flash point of 100-200 ° C, a kinematic viscosity at 30 ° C of 3-20 mm 2 / sec., And a pour point of -5 ° C or less is used. is there.
- the methanolysis reaction in the present invention starts with a mixture of animal and vegetable fats or oils or waste cooking oil and methanol.
- vegetable oils and fats in the present invention include, but are not limited to, rapeseed oil, canola oil, corn oil, soybean oil, castor oil, and safflower oil.
- Animal fats and oils in the present invention include, but are not limited to, lard or tallow.
- Waste cooking oil refers to animal and vegetable fats and oils that have been used in cooking at homes, restaurants, fast food stores, lunch box manufacturing factories, etc. and then discarded due to deterioration.
- waste cooking oil of animal and vegetable fats and oils that can be used in the present invention include, but are not limited to, waste products of fried oil used for cooking such as tempura, tonkatsu, and fried chicken.
- the mixing ratio of animal and vegetable fats or waste cooking oil and methanol can be arbitrarily selected.
- animal and vegetable fats or waste cooking oil and methanol are mixed at a volume ratio of 1: 2-2: 2: 1.
- the methanolysis reaction in the present invention is carried out without using a catalyst under reaction conditions in which glycerin is not generated.
- reaction conditions under which glycerin is not generated can be arbitrarily selected as long as the requirement that "glycerin is not generated” is satisfied.
- the “reaction conditions under which glycerin is not generated” include glycerin that can be used only under conditions where no glycerin is generated. Reaction conditions that are not qualitatively produced are also included. “Reaction conditions under which glycerin is not substantially produced” means reaction conditions under which glycerin is produced but the produced glycerin is not separated from the biodiesel fuel.
- the amount of glycerin generated is small enough not to be separated from the biodiesel fuel, and the glycerin generated
- the biodiesel fuel power is further separated (for example, by being replaced with an OH-based S-methyl group) and the lipophilicity is increased.
- the reaction conditions are preferably a reaction temperature of 370-500 ° C., preferably 380-450 ° C., a reaction pressure of 2060 MPa, preferably 3050 MPa, most preferably 40 MPa, and a reaction time of 41-500 MPa.
- the condition is 12 minutes.
- the temperature of the mixture at the time of flowing into the reaction tube in which the reaction is performed is not less than 50 ° C.
- the decomposition reaction of the carbon chain of a fatty acid group is a reaction in which long-chain fatty acid groups (14 or more carbon atoms), which are often contained in animal and vegetable fats or waste cooking oil, are converted into medium-chain fatty acid groups (6 to 12 carbon atoms). Point.
- the reaction conditions are not particularly limited.
- an animal or vegetable fat or oil or waste cooking oil is mixed with methanol, and the reaction temperature is 390-500 ° C, preferably 390-450 ° C, and the reaction pressure is 20-60 MPa,
- the methanolysis reaction is performed under the conditions of preferably 30 to 50 MPa, most preferably 40 MPa, and reaction time of 12 minutes, the decomposition reaction of the carbon chain of the fatty acid group proceeds in parallel with the methanolysis reaction.
- the temperature of the mixture at the time of flowing into the reaction tube in which the reaction is performed be S250 ° C or more.
- Long chain fatty acid group Power S The mechanism of conversion to medium chain fatty acid groups is not always clear, but it is considered that unsaturated bonds in long chain fatty acid groups are cleaved under high temperature and high pressure to become medium chain fatty acid groups. You. There are various other "cut pieces” after cutting, for example, hydrocarbons, fatty acids, and aliphatic alcohols having about 612 carbon atoms. These "shards" are included in the final biodiesel fuel.
- unreacted methanol is removed from the reaction mixture by evaporating under reduced pressure and heating to obtain a final biodiesel fuel.
- the removed methanol is recovered by cooling and used again as a raw material in the methanolysis reaction.
- a methanolysis reaction can be carried out in any reaction vessel as long as the above reaction conditions can be realized.
- the methanolysis reaction is carried out in a Hastelloy tubular reaction tube capable of maintaining an appropriate mixed state. More preferably, the methanolysis reaction is carried out in a Hastelloy tubular reaction tube capable of uniformly heating the inside, having a sufficient length for the reaction, and maintaining an appropriate mixing state.
- Metals that are commonly used as materials for reaction vessels or reaction tubes in supercritical reactors include stainless steel, Hastelloy and Inconel. For the method of the present invention, Hastelloy is preferred.
- Hastelloy has various compositions such as Hastelloy 8, B, C, and F can also be used in the present invention.
- Hastelloy C is used.
- Specific examples of Hastelloy C that can be used in the present invention include HC-22 or HC-276 manufactured by Mitsubishi Materials Corporation.
- tubular reaction tube capable of uniformly heating to the inside means a tubular reaction tube capable of maintaining the temperature condition inside substantially uniformly so that the methanolysis reaction can proceed uniformly.
- a tubular reaction tube having a sufficient length for the reaction means a tubular reaction tube having a length sufficient to secure the reaction time necessary to obtain a biodiesel fuel having an appropriate composition. means. If the reaction tube is too short, a sufficient reaction time is not ensured and the methanolysis reaction does not proceed sufficiently, so that a biodiesel fuel having an appropriate composition cannot be obtained.
- the term "tubular reaction tube capable of maintaining an appropriate mixing state” refers to a tubular reaction tube capable of maintaining a mixed state in which a methanolysis reaction proceeds uniformly without producing glycerin as a by-product, and more specifically, stirring.
- the methanolysis reaction is performed in a tubular reaction tube manufactured by Hastelloy and having an inner diameter of 1.8 mm 7.0 mm, a length of 0.5 m to 15 m, and an inner volume of 14 ml to 600 ml.
- the tubular reaction tube can be used in any state For example, it may be linear, coiled, or folded in a zigzag pattern.
- the methanolysis reaction is carried out in a coiled tubular reaction tube of Hastelloy C, 1.8 mm inside diameter, 8 m length, 20 ml internal volume.
- the reaction apparatus including the reaction tube is, for example, schematically shown in FIG. According to this apparatus, stable continuous operation is possible by mixing the raw materials appropriately before heating by the mixer.
- the mixer is preferably a T-type mixer in which the ratio of the total area of the flow path before mixing to the total area of the flow path after mixing is 2: 1. According to this apparatus, unreacted methanol can be recovered by evaporating it by depressurization and heating, and can be reused as a raw material.
- the biodiesel fuel produced by the process of the present invention is preferably composed of 4060% by weight of fatty acid methyl ester, 10-30% by weight of monoacylglycerol, 20% by weight of diacylglycerol, and 5% by weight of other aliphatic compounds.
- the ⁇ other aliphatic compound '' is derived from glycerin generated when glycerin generated during the methanolysis reaction is further reacted as described above, for example, the OH group is replaced with a methyl group.
- Aliphatic compounds "cuts” generated when long-chain fatty acid groups are converted to medium-chain fatty acid groups as described above (for example, hydrocarbons having about 6 to 12 carbon atoms, fatty acids, fatty alcohols), And aliphatic compounds containing free fatty acids generated by other causes.
- the composition of the biodiesel fuel (the content of each of fatty acid methyl ester, monoacylglycerol, diacylglycerol, triacylglycerol, glycerin, and other aliphatic compounds) was determined under the following conditions. It was measured by chromatography mass spectrometry. Agilent Technologies Gas Chromatography 6890N and JEOL Datum Mass Spectrometer GC-mate II, HP-5TA (15m X 0.32m ⁇ ⁇ . ⁇ ⁇ ⁇ ) Agilent Technologies Column Was. Helium (a flow rate of 1.5 ml / min) was used as a carrier gas.
- the oven temperature is held at 50 ° C for 1 minute at the start of the measurement, then raised to 250 ° C in 10 ° CZ minutes, then to 15 ° C / min to 365 ° C, and then to 365 ° C. Hold for 8 minutes.
- the inlet temperature was 220 ° C
- the split ratio was 45: 1
- the sample injection volume was 2 ⁇ 1.
- Measurement sample is about It was diluted with 1-butanol to 20 mg / ml.
- the component was identified from the obtained mass spectrum, and the content was calculated based on the peak area of the gas chromatogram. Methyl tridecanoate or ethylene glycol was used as an internal standard.
- the composition of the fatty acid group cannot be analyzed. Therefore, the fatty acid composition of fatty acid methyl ester in biodiesel fuel was analyzed by gas chromatography mass spectrometry under the following conditions.
- the type of fatty acid was specified from the obtained mass spectrum, and its content was calculated based on the peak area of gas chromatography. Methyl tridecanoate was used as an internal standard.
- the fatty acid composition of the fatty acid methyl ester is almost the same as the composition of the fatty acid groups contained in all the molecular species constituting the biodiesel fuel. Can be This is because the methanolysis reaction in a supercritical fluid proceeds without being affected by the fatty acid chain length.
- biodiesel fuel produced by the process of the present invention is preferably a kinematic viscosity force in cetane number 49 one 65, a flash point of 100- 200 ° C, 30 ° C S3- 20mm 2 / se, flow The points are below -5 ° C.
- the cetane number was measured according to JIS K2280, the pour point was measured according to JIS # 2269, the kinematic viscosity (30 ° C) was measured according to JIS K2283, and the flash point (PMCC) was measured according to JIS # 2265.
- Biodiesel fuel was produced from commercially available canola oil using the equipment shown in Fig. 1 by the following procedure.
- the reaction tube used was a coil made of HC-22 (Hastelloji, Mitsubishi Materials Corporation) having an inner diameter of 1.8 mm, a length of 7.8 m, and an inner volume of about 20 ml, which was coiled.
- Canola oil (Nisshin Oil Co., Ltd., Oilio (trademark)) was charged to the raw material tank 1 with methanol (Wako Pure Chemical Industries, Ltd., special grade reagent) was placed in each of the raw material tanks 2, and the liquid feed pump was adjusted so that canola oil: methanol was mixed at a volume ratio of 2: 1.
- the temperature in the reaction tube was 395 ° C
- the pressure was 40MPa
- the passage time in the reaction tube was 4 minutes
- the temperature when flowing into the reaction tube was 270 ° C.
- the composition of the produced biodiesel fuel is about 50% by weight of various fatty acid methyl esters, about 25% by weight of monoacylglycerol, about 20% by weight of diacylglycerol, and about 5% by weight of other aliphatic compounds. %, Triacylglycerol and glycerin were each less than 1% by weight.
- the fuel properties are: cetane number 51.6, flash point (PMCC) 136 ° C, kinematic viscosity 15.10mm 2 / sec., Pour point 15.0 ° C, which is comparable to general rapeseed biodiesel fuel. It was almost equivalent.
- the fatty acid composition of the fatty acid methyl ester in the biodiesel fuel was 55% by weight of oleic acid (C18: 1), 16% by weight of linoleic acid (C18: 2), and 5% by weight of stearic acid (C18: 0). %, Palmitic acids (C16: 0 and C16: l) 12% by weight, eicosanoic acids (C20: 0, C20: l and C20: 2) 7% by weight, medium-chain fatty acids (C6-12) %Met.
- Biodiesel fuel was manufactured from waste cooking oil discharged from ordinary households using the equipment shown in Fig. 1 by the following procedure.
- the reaction tube used was made of HC-22 and had a diameter of 1.8 mm, a length of 7.8 m, and an inner volume of about 20 ml, which was wound in a coil shape.
- the fatty acid composition of the fatty acid methyl ester in the manufactured biodiesel fuel is as follows: 64% by weight of oleic acid (C18: l), 13% by weight of linoleic acid (C18: 2) and 13% by weight of stearic acid (C18: 0). 14% by weight of palmitic acid (C16: 0), 3% by weight of eicosanoic acids (C20: 0, C20: l and C20: 2), and 5% by weight of medium chain fatty acids (C6-12).
- the fatty acid composition of the fatty acid methyl ester in the manufactured biodiesel fuel is 60% by weight of oleic acid (C18: l), 0.6% by weight of linoleic acid (C18: 2), and 11% by weight of stearic acid (C18: 0) %, Palmitic acid (C16: 0) was 14% by weight, eicosanoic acids (C20: 0, C20: l and C20: 2) were 2% by weight, and medium-chain fatty acids (C6-12) were 12% by weight. .
- Biodiesel fuel was manufactured from commercially available lard using the equipment shown in Fig. 1 by the following procedure.
- the reaction tube used was a HC-22 coiled tube having an inner diameter of 1.8 mm, a length of 7.8 m, and an internal volume of about 20 ml.
- Lard Miyoshi Oil & Fat Co., Ltd., high-grade lard, fat content: 99.5%
- Methanol Waako Pure Chemical Industries, Ltd., special grade reagent
- the temperature in the reaction tube was 500 ° C
- the pressure was 40MPa
- the passage time in the reaction tube was 8 minutes
- the temperature when flowing into the reaction tube was 300 ° C.
- the composition of the produced biodiesel fuel is as follows: 56% by weight of various fatty acid methyl esters, 20% by weight of monoacylglycerol, 10% by weight of diacylglycerol, 14% by weight of other aliphatic compounds, and triacinoleglycerol. Mole and glycerin were each less than 1% by weight (not detectable).
- the fatty acid composition of the fatty acid methyl ester in the biodiesel fuel was 10% by weight of oleic acid (C18: 1), 25% by weight of stearic acid (C18: 0), and 33% by weight of palmitic acid (C16: 0).
- biodiesel fuel When biodiesel fuel is produced from lard by the conventional alkaline catalyst method, the fuel solidifies at about 10 ° C., but the biodiesel fuel produced according to the present example does not coagulate even at 0 ° C. Was.
- biodiesel fuel without generating glycerin as a by-product. That is, according to the present invention, a more completed carbon cycle energy system A stem can be built. In addition, the yield of biodiesel is improved because no by-products are generated. Furthermore, the elimination of the catalyst makes it possible to eliminate the necessity of pretreatment of raw materials, neutralization of products, washing and purification of washing water, which are essential for conventional production methods.
- FIG. 1 is an example of a schematic view of a manufacturing apparatus for the present invention.
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Abstract
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Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN2004800300015A CN1867650B (zh) | 2003-08-18 | 2004-08-10 | 无副产物生成的生物柴油燃料非催化生产方法 |
BRPI0413622-5A BRPI0413622A (pt) | 2003-08-18 | 2004-08-10 | processo não-catalìtico não-gerador de subprodutos para produção de combustìvel biodiesel |
US10/568,066 US20060288636A1 (en) | 2003-08-18 | 2004-08-10 | Process for non-catalytically producing biodiesel fuel without yielding by-product |
DE112004001460T DE112004001460T5 (de) | 2003-08-18 | 2004-08-10 | Nicht-Katalytisches Verfahren zur Erzeugung von Biodieseltreibstoff, das kein Nebenprodukt erzeugt |
AT0928204A AT503836A2 (de) | 2003-08-18 | 2004-08-10 | Nicht-katalytisches verfahren zur erzeugung von biodieseltreibstoff, das kein nebenprodukt erzeugt |
Applications Claiming Priority (2)
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JP2003294521A JP4122433B2 (ja) | 2003-08-18 | 2003-08-18 | 副産物を生成しないバイオディーゼル燃料の無触媒製造法 |
JP2003-294521 | 2003-08-18 |
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WO2005017075A1 true WO2005017075A1 (ja) | 2005-02-24 |
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PCT/JP2004/011485 WO2005017075A1 (ja) | 2003-08-18 | 2004-08-10 | 副産物を生成しないバイオディーゼル燃料の無触媒製造法 |
Country Status (9)
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US (1) | US20060288636A1 (ja) |
JP (1) | JP4122433B2 (ja) |
KR (1) | KR100693199B1 (ja) |
CN (1) | CN1867650B (ja) |
AT (1) | AT503836A2 (ja) |
BR (1) | BRPI0413622A (ja) |
DE (1) | DE112004001460T5 (ja) |
MY (1) | MY138548A (ja) |
WO (1) | WO2005017075A1 (ja) |
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CN101845336A (zh) * | 2010-06-03 | 2010-09-29 | 濮阳市中油石化有限公司 | 油品的加工设备 |
EP2862915A1 (en) | 2013-10-18 | 2015-04-22 | Rigas Tehniska universitate | Method for manufacturing biodiesel |
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US7943791B2 (en) * | 2007-09-28 | 2011-05-17 | Mcneff Research Consultants, Inc. | Methods and compositions for refining lipid feed stocks |
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- 2004-08-10 KR KR1020067002715A patent/KR100693199B1/ko not_active IP Right Cessation
- 2004-08-10 CN CN2004800300015A patent/CN1867650B/zh not_active Expired - Fee Related
- 2004-08-10 AT AT0928204A patent/AT503836A2/de not_active Application Discontinuation
- 2004-08-10 US US10/568,066 patent/US20060288636A1/en not_active Abandoned
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WO2006077023A2 (de) * | 2005-01-19 | 2006-07-27 | Cognis Ip Management Gmbh | Zusammensetzungen verwendbar als biotreibstoff |
WO2006077023A3 (de) * | 2005-01-19 | 2008-02-28 | Cognis Ip Man Gmbh | Zusammensetzungen verwendbar als biotreibstoff |
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CN101845336A (zh) * | 2010-06-03 | 2010-09-29 | 濮阳市中油石化有限公司 | 油品的加工设备 |
US10226032B2 (en) | 2010-06-17 | 2019-03-12 | Bergen Teknologioverforing As | Method for farming ascidians |
US10223637B1 (en) | 2013-05-30 | 2019-03-05 | Google Llc | Predicting accuracy of submitted data |
US11526773B1 (en) | 2013-05-30 | 2022-12-13 | Google Llc | Predicting accuracy of submitted data |
EP2862915A1 (en) | 2013-10-18 | 2015-04-22 | Rigas Tehniska universitate | Method for manufacturing biodiesel |
Also Published As
Publication number | Publication date |
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JP4122433B2 (ja) | 2008-07-23 |
CN1867650A (zh) | 2006-11-22 |
DE112004001460T5 (de) | 2006-09-07 |
BRPI0413622A (pt) | 2006-10-17 |
MY138548A (en) | 2009-06-30 |
KR100693199B1 (ko) | 2007-03-14 |
JP2005060591A (ja) | 2005-03-10 |
CN1867650B (zh) | 2011-06-15 |
US20060288636A1 (en) | 2006-12-28 |
AT503836A2 (de) | 2008-01-15 |
KR20060037430A (ko) | 2006-05-03 |
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