CN101338212B - Method for preparing biodesel - Google Patents
Method for preparing biodesel Download PDFInfo
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- CN101338212B CN101338212B CN2007101184159A CN200710118415A CN101338212B CN 101338212 B CN101338212 B CN 101338212B CN 2007101184159 A CN2007101184159 A CN 2007101184159A CN 200710118415 A CN200710118415 A CN 200710118415A CN 101338212 B CN101338212 B CN 101338212B
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- 238000000034 method Methods 0.000 title claims abstract description 37
- 239000002253 acid Substances 0.000 claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims abstract description 18
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 13
- 235000011187 glycerol Nutrition 0.000 claims abstract description 9
- 238000005809 transesterification reaction Methods 0.000 claims abstract description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 63
- 239000004519 grease Substances 0.000 claims description 25
- 239000002551 biofuel Substances 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 15
- 150000002191 fatty alcohols Chemical class 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 239000002283 diesel fuel Substances 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 2
- 239000003225 biodiesel Substances 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 150000002148 esters Chemical class 0.000 description 14
- 239000000463 material Substances 0.000 description 14
- 239000003921 oil Substances 0.000 description 10
- 235000019198 oils Nutrition 0.000 description 10
- 230000032050 esterification Effects 0.000 description 7
- 238000005886 esterification reaction Methods 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 6
- 239000012043 crude product Substances 0.000 description 6
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 5
- 238000007670 refining Methods 0.000 description 5
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 150000002194 fatty esters Chemical class 0.000 description 4
- 239000010409 thin film Substances 0.000 description 4
- 102000004190 Enzymes Human genes 0.000 description 3
- 108090000790 Enzymes Proteins 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 235000019387 fatty acid methyl ester Nutrition 0.000 description 3
- 235000021588 free fatty acids Nutrition 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 239000003377 acid catalyst Substances 0.000 description 2
- 239000010775 animal oil Substances 0.000 description 2
- 238000005815 base catalysis Methods 0.000 description 2
- 239000010953 base metal Substances 0.000 description 2
- OGBUMNBNEWYMNJ-UHFFFAOYSA-N batilol Chemical class CCCCCCCCCCCCCCCCCCOCC(O)CO OGBUMNBNEWYMNJ-UHFFFAOYSA-N 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 235000014113 dietary fatty acids Nutrition 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229930195729 fatty acid Natural products 0.000 description 2
- 239000000194 fatty acid Substances 0.000 description 2
- 150000004665 fatty acids Chemical class 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 1
- 238000007171 acid catalysis Methods 0.000 description 1
- 238000009874 alkali refining Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000004332 deodorization Methods 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 239000003974 emollient agent Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 150000007522 mineralic acids Chemical group 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 239000010773 plant oil Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000000344 soap Substances 0.000 description 1
- JOXIMZWYDAKGHI-UHFFFAOYSA-N toluene-4-sulfonic acid Chemical compound CC1=CC=C(S(O)(=O)=O)C=C1 JOXIMZWYDAKGHI-UHFFFAOYSA-N 0.000 description 1
- 235000015112 vegetable and seed oil Nutrition 0.000 description 1
- 239000008158 vegetable oil Substances 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
Landscapes
- Fats And Perfumes (AREA)
- Liquid Carbonaceous Fuels (AREA)
Abstract
一种生物柴油的制备方法，包括：将油脂和醇提供给反应器，进行酯交换反应，分离并收集生物柴油和甘油，反应温度为100～260℃，反应压力是0.2～7MPa。按照本发明提供的方法，产物收率可达80w％以上。本发明方法特别适合加工酸值较高的非精炼油，可省去工序繁杂的预处理过程，使能耗、设备投资下降。本发明方法基本无三废排放，是一个环境友好的绿色工艺。A method for preparing biodiesel, comprising: providing oil and alcohol to a reactor, performing transesterification, separating and collecting biodiesel and glycerin, the reaction temperature is 100-260°C, and the reaction pressure is 0.2-7MPa. According to the method provided by the invention, the product yield can reach more than 80w%. The method of the invention is especially suitable for processing non-refined oil with high acid value, can save complicated pretreatment process, and reduce energy consumption and equipment investment. The method of the invention basically does not discharge three wastes, and is an environmentally friendly green process.
Description
Technical field
The present invention relates to a kind of by grease and monohydroxy-alcohol prepared in reaction method of bio-diesel oil.
Background technology
Biofuel can be that triglyceride level and low-carbon alcohol are carried out transesterification reaction and made through grease; Fatty ester and mono-glycerides, two sweet esters, glycerine, pure and mild unreacted triglyceride level are arranged in the reaction product; Can obtain biofuel through separating; Wherein mainly be fatty ester, also contain a spot of mono-glycerides and two sweet esters.
The preparation method of biofuel can be divided into acid catalyzed process, base catalysis method, enzyme catalysis method and supercritical methanol technology.
CN1412278A discloses a kind of acid catalyzed process, with the method for preparing biological diesel oil from high acid value waste animal and plant oil, it with sulfuric acid as catalyzer; Operation according to raw material dehydration, esterification and transesterify, phase-splitting, decolouring is carried out, and raw material dewaters under the vacuum earlier at 60-100 ℃; Then, under 40～85 ℃, sulfuric acid add-on 2～6%; Carried out esterification and transesterification reaction 6 hours, and told the fatty acid methyl ester phase, with atlapulgite 90～125 ℃ of decolourings get final product biofuel.
It is raw material that CN1473907A adopts the tankage of vegetable oil refining and the edible oil of recovery; Catalyzer is inorganic and organic acid is composite forms by sulfuric acid, hydrochloric acid, tosic acid, Witco 1298 Soft Acid, naphthene sulfonic acid etc.; Produce through operations such as acidifying removal of impurities, continous vacuum dehydration, esterification, layering, underpressure distillation; Esterif iotacation step catalyzer add-on 1～3%, 60～80 ℃ of esterification temperatures, 6 hours reaction times.Reaction product neutralization is earlier removed catalyzer, and then, layering removes and anhydrates, and the after product that anhydrates obtains biofuel through underpressure distillation.
The acid catalysis existing problems are that speed of response is slow, have a large amount of spent acid, waste water generation in addition.
The speed of response of base catalysis method is faster than acid catalyzed process; If but free fatty acid content is more in the grease; Directly use alkaline catalysts can produce fatty acid soaps, alkaline catalysts must be excessive in this case, can cause the fatty ester layer to separate with glycerin layer like this and become difficulty.For avoiding these problems, DE3444893 discloses a kind of method, at first; Oil plant is carried out preparatory esterification treatment; With acid catalyst, normal pressure, 50～120 ℃, free fatty acids and alcohol are carried out esterification, add then in the excessive base metal catalysts and the residual acid catalyst of esterification in advance; Carry out transesterification reaction again, the requirement of base metal catalysts has bigger increase.Adopt that the pre-esterifying process existing problems are that technical process is long, step is many, facility investment, energy consumption significantly rise, and in addition, needs from reaction process and product, remove acid, basic catalyst, needs with a large amount of washing water the generation great amount of wastewater.
US5713965A discloses a kind of method, in the presence of lypase, makes solvent with hexane, through grease and pure prepared in reaction fatty acid methyl ester.Though adopt the enzyme catalyst reaction conditions to relax, long reaction time, efficient are lower, need solvent, and enzyme are more expensive, in high purity methanol, are prone to inactivation.
PCT/JP99/0543 discloses the method for a kind of grease and monohydroxy-alcohol prepared in reaction fatty ester, at 270～280 ℃, under 11～12MPa, methyl alcohol is reacted with oil plant, and the fatty acid methyl ester yield is 55～60%.This method severe reaction conditions is high to equipment requirements.
Summary of the invention
It is a kind of under than the demulcent condition that the present invention provides, and need not the high yield of catalyzer and prepare method of bio-diesel oil, and not only reaction conversion ratio is near 100w%, and the biofuel yield is high.
The preparation method of biofuel provided by the invention comprises: with grease and alcohol reactor drum is provided, carries out transesterification reaction, separate and collection of biological diesel oil and glycerine.
Said grease is a fatty acid triglycercide; Be mainly derived from animal oil or vegetables oil; Comprise also that in addition acid value of oil and fat can change in the larger context, for example 1～190mgKOH/g from the oil plant in the materials such as mikrobe, algae; Preferred 20～160mgKOH/g, more preferably 30～130mgKOH/g.High-acid value grease in above-mentioned acid number scope can be crude oil, waste grease or rotten grease etc.Wherein crude oil is meant without the grease that does not reach product standard after refining or refining, the refining step operations such as matter, alkali refining, dephosphorization matter, decolouring, deodorization that include but not limited to come unstuck.High-acid value grease in above-mentioned acid number scope also can obtain through extra adding free fatty acids in grease.
Said monohydroxy-alcohol is meant that carbon number is 1～6 Fatty Alcohol(C12-C14 and C12-C18), can be single Fatty Alcohol(C12-C14 and C12-C18), also can be the mixture of one or more Fatty Alcohol(C12-C14 and C12-C18), particular methanol and ethanol.
Said reactor drum is fixed-bed reactor, preferred tubular reactor.Grease and alcohol can offer reactor drum separately, or with offering reactor drum after their pre-mixings, before offering reactor drum; Available preheater also can directly get into reactor drum, like this with the material preheating; Reactor drum had both played the effect of preheater, also played the effect of reactor drum.As adopt preheater, preheating together after can or mixing grease and alcohol difference preheating.
100～260 ℃ of temperature of reactor, preferred 140～235 ℃, more preferably 170～220 ℃; Pressure 0.2～7MPa, preferred 1～6MPa, more preferably 2～5MPa; Oil/pure mass ratio is 0.4～8:1, is preferably 1～7:1, more preferably 2～7:1.Liquid hourly space velocity is 0.1～5h
-1, preferred 0.3～2h
-1
For the reacting coarse product that obtains, can steam monohydroxy-alcohol through flash distillation; From the mixture behind the flash distillation monohydroxy-alcohol, separate then mixed ester mutually with glycerine mutually, can separate the separation of optimum fiber bundle through settlement separate or fibrous bundle separator; Separation condition is 20～150 ℃ of temperature; Preferred 40～100 ℃, pressure greater than a normal atmosphere or normal pressure all can, air speed 0.1-10h
-1, preferred 1～4h
-1Then mixed methyl phase and glycerine are distilled respectively; Can be through rectification under vacuum tower or thin-film evaporator distillation, pressure is less than 0.1MPa, preferably less than 0.04MPa; Reflux ratio 0.1～10:1 in the rectifying tower; Preferred 1～6:1, tower still or thin film evaporation actuator temperature are 100～300 ℃, preferably less than 280 ℃.
According to method provided by the invention, product yield can reach more than the 80w%.Technology of the present invention is particularly suitable for processing the higher non-refining oil of acid number, can save the numerous and diverse preprocessing process of operation, and energy consumption, facility investment are descended.The basic three-waste free discharge of this technology is an eco-friendly friendly process.
Embodiment
Further specify the present invention through instance below, but the present invention is not limited to this.
Relevant nominal definition is following among the embodiment:
Yield=(biofuel weight/grease weight) * 100%
The oil quantity that liquid hourly space velocity=unit volume reactor drum unit time handles
W% representes weight percentage.
Embodiment 1
Grease and the methyl alcohol of acid number 104.7mgKOH/g are provided in the preheater liquid hourly space velocity 0.6h with the speed of 600 Grams Per Hours and 100 Grams Per Hours respectively
-1, 160 ℃ of preheater temperature continuously are provided to the material after the preheating in the tubular reactor, 200～205 ℃ of temperature of reaction, and pressure 2.0～2.5MPa, reacting coarse product gets into flashing tower,<remove methyl alcohol for 150 ℃, and methyl alcohol is reclaimed, reuses, leftover materials are got into the fibrous bundle separator, at 20 ℃ of temperature, liquid hourly space velocity 5h
-1, tell the mixed ester phase, the middle mutually content of triglyceride 2.4w% of mixed ester, mixed ester gets into thin-film evaporator mutually, at pressure 6mmHg, under the condition that temperature is 240 ℃, steams biofuel, yield 85.2w%.
Embodiment 2
Grease and the methyl alcohol of acid number 58.1mgKOH/g are provided in the preheater liquid hourly space velocity 0.7h with the speed of 600 Grams Per Hours and 100 Grams Per Hours respectively
-1, 160 ℃ of preheater temperature continuously are provided to the material after the preheating in the tubular reactor, 220 ℃ of temperature of reaction, and pressure 5.5～6.0MPa, the crude product of outflow reactor gets into flashing tower,<remove methyl alcohol and methyl alcohol is reclaimed, reuses for 150 ℃.Leftover materials are got into the fibrous bundle separator, at 30 ℃ of temperature, liquid hourly space velocity 10h
-1Under the condition, tell continuously mixed ester mutually with glycerine mutually, the middle mutually content of triglyceride 0 of ester, mixed ester gets into the rectification under vacuum tower mutually, at pressure 11mmHg, 267 ℃ of tower stills under the condition of reflux ratio 3:1, steam biofuel, yield 93w%.
Embodiment 3
Grease and the methyl alcohol of acid number 49.3mgKOH/g are provided in the preheater liquid hourly space velocity 0.6h with the speed of 600 Grams Per Hours and 110 Grams Per Hours respectively
-1, 140 ℃ of preheater temperature continuously are provided to the material after the preheating in the tubular reactor, 200～205 ℃ of temperature of reaction, and pressure 3.5～4MPa, the reacting coarse product of outflow reactor gets into flashing tower,<remove methyl alcohol and methyl alcohol is reclaimed, reuses for 150 ℃, leftover materials are got into the fibrous bundle separator, at 60 ℃ of temperature, liquid hourly space velocity 5h
-1, divide the ester output phase, the middle mutually content of triglyceride 1.25w% of ester, ester gets into the rectification under vacuum tower mutually, and at pressure 15mmHg, 279 ℃ of tower stills under the condition of reflux ratio 0.6:1, steam biofuel, and yield can reach 88.2w%.
Embodiment 4
Grease and the methyl alcohol of acid number 35.3mgKOH/g are provided in the preheater liquid hourly space velocity 0.6h with the speed of 600 Grams Per Hours and 128 Grams Per Hours respectively
-1, 140 ℃ of preheater temperature continuously are provided to the material after the preheating in the tubular reactor, and temperature of reaction 225-230 ℃, pressure 0.7～0.9MPa, the crude product of outflow reactor gets into flashing tower,<remove methyl alcohol and methyl alcohol is reclaimed, reuses for 150 ℃, leftover materials carry out settlement separate, divide ester output mutually with glycerine mutually; Mixed ester gets into thin-film evaporator mutually, at pressure 11mmHg, under the condition that temperature is 255 ℃; Steam biofuel, yield 74.4w%.
Embodiment 5
Grease and the methyl alcohol of acid number 125.7mgKOH/g are provided in the preheater liquid hourly space velocity 0.6h with the speed of 600 Grams Per Hours and 100 Grams Per Hours respectively
-1, 170 ℃ of preheater temperature continuously are provided to the material after the preheating in the tubular reactor; 200～205 ℃ of temperature of reaction, pressure 3.5～4MPa, the crude product of outflow reactor separates by the method for embodiment 3; Obtain biofuel, yield 71.4w%.
Embodiment 6
Grease and the methyl alcohol of acid number 81.2mgKOH/g are provided in the preheater liquid hourly space velocity 0.7h with the speed of 600 Grams Per Hours and 100 Grams Per Hours respectively
-1, 140 ℃ of preheater temperature continuously are provided to the material after the preheating in the tubular reactor, 180 ℃ of temperature of reaction, and pressure 5.8～6.0MPa, the crude product of outflow reactor separates by the method for embodiment 2, steams biofuel, yield 90.7w%.
Embodiment 7
Grease and the methyl alcohol of acid number 22.5mgKOH/g are provided in the preheater liquid hourly space velocity 0.6h with the speed of 600 Grams Per Hours and 100 Grams Per Hours respectively
-1, 170 ℃ of preheater temperature continuously are provided to the material after the preheating in the tubular reactor; 210～215 ℃ of temperature of reaction, pressure 2.0～2.5MPa, the crude product of outflow reactor separates by the method for embodiment 4; Steam biofuel, yield 51.2w%.
Comparative example 1
Grease and the methyl alcohol of acid number 0.4mgKOH/g are provided in the preheater liquid hourly space velocity 0.6h with the speed of 600 Grams Per Hours and 100 Grams Per Hours respectively
-1, 170 ℃ of preheater temperature continuously are provided to the material after the preheating in the tubular reactor; 210～215 ℃ of temperature of reaction, pressure 2.0～2.5MPa, the crude product of outflow reactor separates by the method for embodiment 1; Steam biofuel, yield 19.7w%.
Claims (9)
1. the preparation method of a biofuel need not catalyzer, may further comprise the steps: with grease and alcohol extracting supply response device; Carry out transesterification reaction; Separate and collection of biological diesel oil and glycerine, said acid value of oil and fat is 30～104.7mgKOH/g, and temperature of reaction is 205～260 ℃; Reaction pressure is 0.2～4MPa, and said reactor drum is a tubular reactor.
2. according to the described method of claim 1, it is characterized in that said alcohol is the Fatty Alcohol(C12-C14 and C12-C18) of carbon number 1～6.
3. according to the described method of claim 1, it is characterized in that said alcohol is methyl alcohol or ethanol.
4. according to the described method of claim 1, it is characterized in that temperature of reaction is 205～235 ℃.
5. according to the described method of claim 1, it is characterized in that oil/pure mass ratio is 0.4～8: 1.
6. according to the described method of claim 5, it is characterized in that oil/pure mass ratio is 1～7: 1.
7. according to the described method of claim 5, it is characterized in that oil/pure mass ratio is 2～7: 1.
8. according to the described method of claim 1, it is characterized in that liquid hourly space velocity is 0.1～5h
-1
9. according to the described method of claim 1, it is characterized in that liquid hourly space velocity is 0.3～2h
-1
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| CN2007101184159A CN101338212B (en) | 2007-07-05 | 2007-07-05 | Method for preparing biodesel |
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| CN2007101184159A CN101338212B (en) | 2007-07-05 | 2007-07-05 | Method for preparing biodesel |
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| CN101338212B true CN101338212B (en) | 2012-02-15 |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101812375B (en) * | 2010-04-13 | 2013-03-06 | 南京工业大学 | Production method of autocatalytic esterification and ester exchange of biodiesel |
| CN101985580B (en) * | 2010-11-15 | 2012-10-17 | 江苏永林油脂化工有限公司 | Method for preparing biodiesel from low-boiling-point substance through continuous rectification of oleic acid |
| CN102649920B (en) * | 2012-05-07 | 2013-04-03 | 唐山金利海生物柴油股份有限公司 | Device and method for continuously preparing biodiesel under intermediate-temperature and medium-pressure condition |
| CN102690726A (en) * | 2012-05-29 | 2012-09-26 | 东南大学 | Method for preparing biodiesel by fixed bed catalytic membrane reactor |
| CN103756715B (en) * | 2014-01-20 | 2015-11-04 | 厦门大学 | A kind of preparation method of high carbon hydrocarbon |
| CN104403805B (en) * | 2014-09-29 | 2017-02-15 | 成都新柯力化工科技有限公司 | Biodiesel preparation method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6768015B1 (en) * | 2003-05-16 | 2004-07-27 | Stepan Company | Method of making alkyl esters using pressure |
| CN1923959A (en) * | 2005-08-31 | 2007-03-07 | 中国石油化工股份有限公司 | Method of preparing organism diesel oil from mixing plant oil |
| CN1952047A (en) * | 2005-10-19 | 2007-04-25 | 中国石油化工股份有限公司 | Production process of biological diesel oil |
-
2007
- 2007-07-05 CN CN2007101184159A patent/CN101338212B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6768015B1 (en) * | 2003-05-16 | 2004-07-27 | Stepan Company | Method of making alkyl esters using pressure |
| CN1923959A (en) * | 2005-08-31 | 2007-03-07 | 中国石油化工股份有限公司 | Method of preparing organism diesel oil from mixing plant oil |
| CN1952047A (en) * | 2005-10-19 | 2007-04-25 | 中国石油化工股份有限公司 | Production process of biological diesel oil |
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