CN1861751A - Method for preparing biodiesel by using microchannel reactor - Google Patents
Method for preparing biodiesel by using microchannel reactor Download PDFInfo
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- CN1861751A CN1861751A CNA2006100854337A CN200610085433A CN1861751A CN 1861751 A CN1861751 A CN 1861751A CN A2006100854337 A CNA2006100854337 A CN A2006100854337A CN 200610085433 A CN200610085433 A CN 200610085433A CN 1861751 A CN1861751 A CN 1861751A
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- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000003225 biodiesel Substances 0.000 title claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 89
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000000203 mixture Substances 0.000 claims abstract description 17
- 239000004519 grease Substances 0.000 claims abstract description 16
- 239000003054 catalyst Substances 0.000 claims abstract description 9
- 150000007529 inorganic bases Chemical class 0.000 claims abstract description 8
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 6
- 239000000463 material Substances 0.000 claims abstract description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 42
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical group [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 42
- 239000003921 oil Substances 0.000 claims description 16
- 235000019198 oils Nutrition 0.000 claims description 16
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 235000019484 Rapeseed oil Nutrition 0.000 claims description 12
- 239000002551 biofuel Substances 0.000 claims description 12
- 239000003549 soybean oil Substances 0.000 claims description 7
- 235000012424 soybean oil Nutrition 0.000 claims description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 6
- WQDUMFSSJAZKTM-UHFFFAOYSA-N Sodium methoxide Chemical compound [Na+].[O-]C WQDUMFSSJAZKTM-UHFFFAOYSA-N 0.000 claims description 6
- 229910001220 stainless steel Inorganic materials 0.000 claims description 6
- 239000010935 stainless steel Substances 0.000 claims description 6
- 235000014121 butter Nutrition 0.000 claims description 5
- 102000004895 Lipoproteins Human genes 0.000 claims description 4
- 108090001030 Lipoproteins Proteins 0.000 claims description 4
- 241001465754 Metazoa Species 0.000 claims description 4
- 210000000582 semen Anatomy 0.000 claims description 4
- 235000015112 vegetable and seed oil Nutrition 0.000 claims description 4
- 239000008158 vegetable oil Substances 0.000 claims description 4
- 229910052742 iron Inorganic materials 0.000 claims description 3
- ZEMPKEQAKRGZGQ-AAKVHIHISA-N 2,3-bis[[(z)-12-hydroxyoctadec-9-enoyl]oxy]propyl (z)-12-hydroxyoctadec-9-enoate Chemical compound CCCCCCC(O)C\C=C/CCCCCCCC(=O)OCC(OC(=O)CCCCCCC\C=C/CC(O)CCCCCC)COC(=O)CCCCCCC\C=C/CC(O)CCCCCC ZEMPKEQAKRGZGQ-AAKVHIHISA-N 0.000 claims description 2
- 241000272525 Anas platyrhynchos Species 0.000 claims description 2
- 235000019483 Peanut oil Nutrition 0.000 claims description 2
- 239000008157 edible vegetable oil Substances 0.000 claims description 2
- 239000000312 peanut oil Substances 0.000 claims description 2
- 239000010453 quartz Substances 0.000 claims description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- BFKJFAAPBSQJPD-UHFFFAOYSA-N tetrafluoroethene Chemical group FC(F)=C(F)F BFKJFAAPBSQJPD-UHFFFAOYSA-N 0.000 claims description 2
- 239000010496 thistle oil Substances 0.000 claims description 2
- 239000002699 waste material Substances 0.000 claims description 2
- 239000008159 sesame oil Substances 0.000 claims 1
- 235000011803 sesame oil Nutrition 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 14
- 230000035484 reaction time Effects 0.000 abstract description 9
- -1 fatty acid ester Chemical class 0.000 abstract description 4
- 238000002360 preparation method Methods 0.000 abstract description 4
- 235000014113 dietary fatty acids Nutrition 0.000 abstract description 3
- 239000000194 fatty acid Substances 0.000 abstract description 3
- 229930195729 fatty acid Natural products 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract description 3
- 208000012839 conversion disease Diseases 0.000 abstract 1
- 125000004185 ester group Chemical group 0.000 abstract 1
- 150000004702 methyl esters Chemical class 0.000 description 13
- 240000002791 Brassica napus Species 0.000 description 10
- 235000004977 Brassica sinapistrum Nutrition 0.000 description 10
- 238000012546 transfer Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 5
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000009776 industrial production Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000006184 cosolvent Substances 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000011541 reaction mixture Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 2
- 244000000231 Sesamum indicum Species 0.000 description 1
- 235000003434 Sesamum indicum Nutrition 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000011187 glycerol Nutrition 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000001020 rhythmical effect Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000005809 transesterification reaction Methods 0.000 description 1
- 235000013311 vegetables Nutrition 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
The invention relates to a preparation method of biodiesel, in particular to a method for producing fatty acid ester (biodiesel for short) by using grease and alcohol as raw materials and carrying out ester exchange reaction through a microchannel reactor. The method comprises the following steps: injecting a mixture of grease, low-carbon alcohol and an inorganic base catalyst in a certain proportion into a microchannel reactor, reacting at normal pressure and a certain temperature (20-65 ℃), and preparing the biodiesel by controlling the residence time (1-20 min) of reaction materials in the microchannel reactor. The method has the characteristics of mild reaction conditions, extremely short reaction time, extremely high reaction conversion rate and selectivity, simple production device and the like. The method for preparing the biodiesel by the microchannel reactor can prepare the biodiesel production device which is easy to assemble, disassemble and move and is convenient to carry.
Description
Technical field:
The present invention relates to a kind of preparation method of biofuel, relating in particular to a kind of is raw material with grease and alcohol, carries out the method that transesterification reaction is produced fatty acid ester (abbreviation biofuel) by micro passage reaction.
Background technology:
The energy dilemma aggravation of recent years, mineral substance energy worsening shortages.In addition, the use of a large amount of mineral substance energy brings many harm to environment, such as acid rain, Greenhouse effect etc.Biofuel is owing to its superior performance, and close friend and recyclability to environment have obtained the attention of countries in the world, becomes new forms of energy development and hot of research and development.
It is the atmospheric low-temperature ester-interchange method of catalyzer that the industrial production of present biofuel mainly adopts with alkali (sodium methylate, sodium hydroxide or potassium hydroxide), and reaction intermittently or in the continuous stirred tank reactor (CSTR) is being carried out usually.Exist the reaction times longer; Rhythmic reaction needs non-cutting time, plant factor not high, is difficult for realizing automatization control; The whipping device energy consumption is big, production run expense height in industrial production; The stirring reaction mass transfer is undesirable, the not high defective of transformation efficiency and yield.There is the immiscible problem of alcohol oil at this reaction system, it is more abundant for alcohol oil two is contacted, improve the rate of mass transfer of reaction system, United States Patent (USP) 6712867,6642399 and Chinese patent 1370140 all propose to add cosolvent in reaction system, as tetrahydrofuran (THF) etc., make this reaction system become homogeneous phase.Thereby significantly improved speed of reaction, the reaction times was shortened to about ten minutes.But the use of cosolvent and follow-up separation can increase production cost undoubtedly.United States Patent (USP) 6187939 and European patent 0985654 disclose a kind of any catalyzer that need not to add, grease at least and alcohol both one of be under the condition of supercritical state, grease and alcohol ester exchange prepare the method for fatty acid ester.This method reaction times is short, the productive rate height, and product separation is simple.But patent is mentioned, and vegetables oil is transformed as far as possible, and temperature of reaction must be controlled at 300 ℃, and pressure is more than 6.5MPa, and is quite high to equipment requirements, and energy consumption is big.Therefore, develop a kind of operation continuously, the reaction conditions gentleness, the reaction times is extremely short, and it is particularly necessary that the preparation method that biodiesel production rate is high just seems.
Summary of the invention:
Technical problem to be solved by this invention is: the long reaction time, the plant factor that exist in the present biodiesel manufacture technology are low in order to overcome, transformation efficiency and the not high shortcoming of yield and proposed a kind ofly to prepare method of bio-diesel oil with micro passage reaction.Adopt this method can prepare miniaturization, mobile modularized production of biodiesel device.Thereby move according to production site, change of production and regulate.
Technical scheme of the present invention is: micro passage reaction is meant the small-sized reactive system of making by little processing and precision processing technology, its inner microchannel size for fluid flow from submicron to the submillimeter order of magnitude.Compare with the popular response system, micro passage reaction has advantages such as microscale, bigger serface, small volume, continuous, the quick amplification of process, flexible production, process safety, distributing production, is showing extraordinary ability aspect heat transfer, the mass transfer.In micro passage reaction, immiscible liquid-liquid two-phase is owing to exist the difference of character such as surface tension, flow velocity, viscosity and density, mainly be Laminar Flow with forms such as slug flow, slug flow-annular-flow, annular-flow, stratified flows, therefore diffusion becomes the major control factor of mass transfer process.Because the specific surface area of microchannel is very big, can reach 10000m
2M
-3-50000m
2M
-3, two alternate mass transfer areas increase greatly.Less channel size has shortened the molecular diffusion distance again, thereby has strengthened mass transfer process, and mixing time can reach Millisecond.Great deal of research results shows: for the reaction process of being transmitted control, adopt micro passage reaction can realize operate continuously, improve speed of reaction, shorten the residence time, can suppress side reaction effectively, improve transformation efficiency and purpose product selectivity, have higher space-time yield.Therefore, we are introduced in the preparation process of biofuel.
The concrete technical scheme of the present invention is: a kind of employing micro passage reaction prepares method of bio-diesel oil, it is characterized in that: with the mixture of grease, low-carbon alcohol and inorganic base catalyst, be injected in the micro passage reaction that internal diameter is 0.1～3.0mm, under the temperature of reaction of normal pressure and 20～65 ℃, the control reaction mass stops 1～20min in micro passage reaction, can prepare biofuel.
Wherein said grease is Vegetable oil lipoprotein, animal grease or their mixture; Vegetable oil lipoprotein is rapeseed oil, soybean oil, peanut oil, Oleum Gossypii semen, Semen Maydis oil, plam oil, Thistle oil, Oleum Cocois, Viscotrol C or sesame wet goods; Described animal grease is lard, butter, butter, duck oil or waste edible oil etc.
Wherein said low-carbon alcohol is methyl alcohol or ethanol etc.Described inorganic base catalyst is potassium hydroxide, sodium hydroxide or sodium methylate etc.
Wherein said micro passage reaction material is stainless steel, quartz, iron or tetrafluoroethylene.The internal diameter of preferred micro passage reaction is 0.25～1mm.Micro passage reaction is market stainless steel on sale/iron kapillary, stainless steel/quartzy chromatographic column, polytetrafluoroethylene capillary.
Among the present invention, the amount that grease is converted into biofuel depends on multiple factor, as kind, alcohol and the greasy mol ratio of grease and alcohol, the internal diameter of micro passage reaction, consumption, reaction time and the temperature of reaction etc. of inorganic base catalyst.In general, preferred alcohols and greasy mol ratio are 3～20: 1; Preferred alcohols and greasy mol ratio are 3～10: 1.The inorganic base catalyst catalyst levels is 0.25～2% of an oil quality.The internal diameter of micro passage reaction is more little, and that grease is converted into the reaction of biofuel is favourable more; But if internal diameter is too little, the output of single micro passage reaction will reduce, preferred 0.25～1mm.Reaction time is preferably 2～10min.Preferred 40～60 ℃ of temperature of reaction.
The biofuel that the present invention obtains can be separated according to actual needs with glycerine and purified to required purity.
Have a mind to effect:
Biodiesel oil preparing process provided by the invention is a consecutive steps, and reaction conditions relaxes, and desired reaction temperature is low, and required reaction time is extremely short, the biodiesel production rate height.It is simple to have production equipment, easy to assemble, the feature that is easy to carry and moves.Working method is simple, can regulate easily by increasing and decreasing microchannel quantity simply according to raw material supply situation and biofuel demand.There is not ubiquitous on the industrial production " scale effect ".
Description of drawings
Fig. 1 micro passage reaction prepares biofuel device schematic flow sheet, 1-reaction mixture wherein, 2-constant flow pump, 3-micro passage reaction, 4-temperature control unit, 5-reaction product.
Embodiment
Embodiment 1
With 8.007g rapeseed oil and the reaction mixture 1 that contains the 1.637g methyl alcohol of 0.146g potassium hydroxide, by constant flow pump 2, being injected into the internal diameter that normal pressure, temperature be controlled at 40 ℃ is in the micro passage reaction 3 of 0.53mm, and the residence time of conditioned reaction thing in micro passage reaction is 3.3min.Collecting reaction product 5, utilizing gas chromatographic analysis to obtain the rapeseed methylester yield is 95.6%.
Example 2
With the 7.455g soybean oil with after containing the 2.729g methanol mixed of 0.091g potassium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.53mm that internal diameter is by constant flow pump, the temperature of control reaction is 25 ℃, the residence time is 21.3min.It is 83.6% that reaction obtains soybean oil methyl esters yield.
Example 2
With the 8.007g rapeseed oil with after containing the 1.728g methanol mixed of 0.097g potassium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.53mm that internal diameter is by constant flow pump, the temperature of control reaction is 60 ℃, the residence time is 2.6min.The rapeseed methylester yield that reaction obtains is 90.2%.
Example 3
With the 8.007g rapeseed oil with after containing the 1.637g methanol mixed of 0.097g potassium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.53mm that internal diameter is by constant flow pump, the temperature of control reaction is 60 ℃, the residence time is 6.0min.The rapeseed methylester yield that reaction obtains is 96.7%.
Example 4
With the 8.007g rapeseed oil with after containing the 1.364g methanol mixed of 0.097g potassium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.53mm that internal diameter is by constant flow pump, the temperature of control reaction is 40 ℃, the residence time is 1.1min.The rapeseed methylester yield that reaction obtains is 77.9%.
Example 5
With the 8.007g rapeseed oil with after containing the 1.637g methanol mixed of 0.073g potassium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.53mm that internal diameter is by constant flow pump, the temperature of control reaction is 60 ℃, the residence time is 5.4min.The rapeseed methylester yield that reaction obtains is 94.7%.
Example 6
With the 8.007g rapeseed oil with after containing the 0.819g methanol mixed of 0.049g potassium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.53mm that internal diameter is by constant flow pump, the temperature of control reaction is 60 ℃, the residence time is 14.5min.The rapeseed methylester yield that reaction obtains is 64.7%.
Example 7
With the 8.007g rapeseed oil with after containing the 1.637g methanol mixed of 0.097g potassium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.25mm that internal diameter is by constant flow pump, the temperature of control reaction is 60 ℃, the residence time is 5.3min.The rapeseed methylester yield that reaction obtains is 98.8%.
Example 8
With the 8.007g rapeseed oil with after containing the 1.637g methanol mixed of 0.073g potassium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.25mm that internal diameter is by constant flow pump, the temperature of control reaction is 60 ℃, the residence time is 5.3min.The rapeseed methylester yield that reaction obtains is 96.8%.
Example 9
With the 8.007g rapeseed oil with after containing the 1.364g methanol mixed of 0.097g potassium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.25mm that internal diameter is by constant flow pump, the temperature of control reaction is 60 ℃, the residence time is 6.3min.The rapeseed methylester yield that reaction obtains is 97.7%.
Example 10
With the 21.195g rapeseed oil with after containing the 4.334g methanol mixed of 0.258g potassium hydroxide, mixture is injected in the stainless steel micro passage reaction of the 3.0mm that internal diameter is by constant flow pump, the temperature of control reaction is 60 ℃, the residence time is 8.2min.The rapeseed methylester yield that reaction obtains is 78.6%.
Example 11
With the 7.455g soybean oil with after containing the 1.637g methanol mixed of 0.078g sodium hydroxide, mixture is injected in the quartzy micro passage reaction of the 0.53mm that internal diameter is by constant flow pump, the temperature of control reaction is 60 ℃, the residence time is 4.1min.The soybean oil methyl esters yield that reaction obtains is 89.6%.
Example 12
After 0.01mol butter and the 0.06mol ethanol that contains 0.087g sodium hydroxide mixed, by constant flow pump mixture is injected in the stainless steel micro passage reaction of the 0.75mm that internal diameter is, the temperature of control reaction is 40 ℃, and the residence time is 6.9min.The soybean oil methyl esters yield that reaction obtains is 78.5%.
Claims (10)
1, a kind of employing micro passage reaction prepares method of bio-diesel oil, it is characterized in that: with the mixture of grease, low-carbon alcohol and inorganic base catalyst, be injected in the micro passage reaction that internal diameter is 0.1～3.0mm, under the temperature of reaction of normal pressure and 20～65 ℃, the control reaction mass stops 1～20min in micro passage reaction, can prepare biofuel.
2, in accordance with the method for claim 1, it is characterized in that described grease is Vegetable oil lipoprotein, animal grease or their mixture.
3, in accordance with the method for claim 2, it is characterized in that described Vegetable oil lipoprotein is rapeseed oil, soybean oil, peanut oil, Oleum Gossypii semen, Semen Maydis oil, plam oil, Thistle oil, Oleum Cocois, Viscotrol C or sesame oil; Described animal grease is lard, butter, butter, duck oil or waste edible oil.
4, in accordance with the method for claim 1, it is characterized in that described low-carbon alcohol is methyl alcohol or ethanol.
5, in accordance with the method for claim 1, it is characterized in that described inorganic base catalyst is potassium hydroxide, sodium hydroxide or sodium methylate.
6, in accordance with the method for claim 1, the internal diameter that it is characterized in that described micro passage reaction is 0.25～1mm.
7, in accordance with the method for claim 1, it is characterized in that described micro passage reaction material is stainless steel, quartz, iron or tetrafluoroethylene.
8, in accordance with the method for claim 1, it is characterized in that low-carbon alcohol and greasy mol ratio are 3～20: 1, preferred 3～10: 1.
9, in accordance with the method for claim 1, it is characterized in that the consumption of inorganic base catalyst is 0.25～2% of an oil quality.
10, in accordance with the method for claim 1, it is characterized in that described temperature of reaction is 40～60 ℃, described reaction mass residence time in micro passage reaction is 2～10min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100854337A CN100372915C (en) | 2006-06-15 | 2006-06-15 | Method for preparing biodiesel by using microchannel reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100854337A CN100372915C (en) | 2006-06-15 | 2006-06-15 | Method for preparing biodiesel by using microchannel reactor |
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| Publication Number | Publication Date |
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| CN1861751A true CN1861751A (en) | 2006-11-15 |
| CN100372915C CN100372915C (en) | 2008-03-05 |
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| CNB2006100854337A Expired - Fee Related CN100372915C (en) | 2006-06-15 | 2006-06-15 | Method for preparing biodiesel by using microchannel reactor |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101333451A (en) * | 2007-06-28 | 2008-12-31 | 拜耳技术工程（上海）有限公司 | Method for synthesizing bio-diesel |
| CN101550082A (en) * | 2008-04-02 | 2009-10-07 | 拜耳技术工程（上海）有限公司 | Method and device for continuously producing carboxylic ether |
| CN101148409B (en) * | 2007-10-30 | 2010-06-02 | 南京工业大学 | Method for preparing fatty acid ester by using microchannel reactor |
| CN103074165A (en) * | 2013-01-18 | 2013-05-01 | 天津大学 | Continuous ester interchange reaction method and reactor in production process of natural vitamin E and phytosterin |
| CN103103025A (en) * | 2013-01-30 | 2013-05-15 | 大连理工大学 | Method for continuous synthesis of biodiesel through microreactor |
| CN103122278A (en) * | 2013-03-07 | 2013-05-29 | 中国石油大学(华东) | Preparation method of biodiesel |
| CN103666773A (en) * | 2013-09-23 | 2014-03-26 | 北京石油化工学院 | Method for producing biodiesel in micro-structure reactor |
| CN104045770A (en) * | 2013-03-13 | 2014-09-17 | 中国石油化工股份有限公司 | Preparation method of C9 petroleum resin |
| CN104745310A (en) * | 2015-03-20 | 2015-07-01 | 南京工业大学 | Method for producing biodiesel by adopting microchannel reactor |
| CN104962397A (en) * | 2015-03-20 | 2015-10-07 | 南京工业大学 | Method for producing biodiesel through ester exchange in continuous flow microchannel reactor |
| CN106318648A (en) * | 2015-06-30 | 2017-01-11 | 中国科学院大连化学物理研究所 | Transesterification method based on microchannel reactor |
| CN107779266A (en) * | 2016-08-26 | 2018-03-09 | 中国科学院大连化学物理研究所 | The directly transesterification method of aqueous microalgae biomass based on micro passage reaction |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1238468C (en) * | 2003-12-31 | 2006-01-25 | 中国农业科学院油料作物研究所 | Production method of biodiesel oil using high acid ralue animal and vegetable grease |
-
2006
- 2006-06-15 CN CNB2006100854337A patent/CN100372915C/en not_active Expired - Fee Related
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101333451A (en) * | 2007-06-28 | 2008-12-31 | 拜耳技术工程（上海）有限公司 | Method for synthesizing bio-diesel |
| CN101148409B (en) * | 2007-10-30 | 2010-06-02 | 南京工业大学 | Method for preparing fatty acid ester by using microchannel reactor |
| CN101550082A (en) * | 2008-04-02 | 2009-10-07 | 拜耳技术工程（上海）有限公司 | Method and device for continuously producing carboxylic ether |
| CN103074165A (en) * | 2013-01-18 | 2013-05-01 | 天津大学 | Continuous ester interchange reaction method and reactor in production process of natural vitamin E and phytosterin |
| CN103103025A (en) * | 2013-01-30 | 2013-05-15 | 大连理工大学 | Method for continuous synthesis of biodiesel through microreactor |
| CN103103025B (en) * | 2013-01-30 | 2014-08-27 | 大连理工大学 | Method for continuous synthesis of biodiesel through microreactor |
| CN103122278A (en) * | 2013-03-07 | 2013-05-29 | 中国石油大学(华东) | Preparation method of biodiesel |
| CN104045770A (en) * | 2013-03-13 | 2014-09-17 | 中国石油化工股份有限公司 | Preparation method of C9 petroleum resin |
| CN103666773A (en) * | 2013-09-23 | 2014-03-26 | 北京石油化工学院 | Method for producing biodiesel in micro-structure reactor |
| CN104745310A (en) * | 2015-03-20 | 2015-07-01 | 南京工业大学 | Method for producing biodiesel by adopting microchannel reactor |
| CN104962397A (en) * | 2015-03-20 | 2015-10-07 | 南京工业大学 | Method for producing biodiesel through ester exchange in continuous flow microchannel reactor |
| CN106318648A (en) * | 2015-06-30 | 2017-01-11 | 中国科学院大连化学物理研究所 | Transesterification method based on microchannel reactor |
| CN107779266A (en) * | 2016-08-26 | 2018-03-09 | 中国科学院大连化学物理研究所 | The directly transesterification method of aqueous microalgae biomass based on micro passage reaction |
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