CN101063040B - Method for preparing biological diesel by hogwash oil - Google Patents
Method for preparing biological diesel by hogwash oil Download PDFInfo
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- CN101063040B CN101063040B CN2006100352720A CN200610035272A CN101063040B CN 101063040 B CN101063040 B CN 101063040B CN 2006100352720 A CN2006100352720 A CN 2006100352720A CN 200610035272 A CN200610035272 A CN 200610035272A CN 101063040 B CN101063040 B CN 101063040B
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- 238000000034 method Methods 0.000 title claims description 23
- 150000002148 esters Chemical class 0.000 claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 238000005406 washing Methods 0.000 claims abstract description 29
- 238000003672 processing method Methods 0.000 claims abstract description 14
- 230000007935 neutral effect Effects 0.000 claims abstract description 11
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 90
- 239000002551 biofuel Substances 0.000 claims description 30
- 230000032050 esterification Effects 0.000 claims description 17
- 238000005886 esterification reaction Methods 0.000 claims description 17
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims description 15
- 238000007670 refining Methods 0.000 claims description 15
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 235000019387 fatty acid methyl ester Nutrition 0.000 claims description 10
- 239000012535 impurity Substances 0.000 claims description 9
- 238000000605 extraction Methods 0.000 claims description 8
- 230000018044 dehydration Effects 0.000 claims description 7
- 238000006297 dehydration reaction Methods 0.000 claims description 7
- 235000011187 glycerol Nutrition 0.000 claims description 7
- 238000003756 stirring Methods 0.000 claims description 7
- 238000002203 pretreatment Methods 0.000 claims description 6
- 229910001220 stainless steel Inorganic materials 0.000 claims description 6
- 239000010935 stainless steel Substances 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- 229910000831 Steel Inorganic materials 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000004821 distillation Methods 0.000 claims description 4
- 239000011521 glass Substances 0.000 claims description 4
- 230000035484 reaction time Effects 0.000 claims description 4
- 239000010959 steel Substances 0.000 claims description 4
- 238000000998 batch distillation Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims description 3
- DNXHEGUUPJUMQT-CBZIJGRNSA-N Estrone Chemical compound OC1=CC=C2[C@H]3CC[C@](C)(C(CC4)=O)[C@@H]4[C@@H]3CCC2=C1 DNXHEGUUPJUMQT-CBZIJGRNSA-N 0.000 claims 1
- 238000010438 heat treatment Methods 0.000 claims 1
- 125000004185 ester group Chemical group 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 9
- 239000003921 oil Substances 0.000 description 9
- 235000019198 oils Nutrition 0.000 description 9
- 239000002253 acid Substances 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 102000004895 Lipoproteins Human genes 0.000 description 2
- 108090001030 Lipoproteins Proteins 0.000 description 2
- 239000003225 biodiesel Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000010773 plant oil Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 235000015112 vegetable and seed oil Nutrition 0.000 description 2
- 239000008158 vegetable oil Substances 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 150000004702 methyl esters Chemical class 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000005809 transesterification reaction Methods 0.000 description 1
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Classifications
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- 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
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- Fats And Perfumes (AREA)
- Liquid Carbonaceous Fuels (AREA)
Abstract
The invention discloses a processing method with water oil to prepare biological diesel, which comprises the following steps: 1 pretreating rough water oil with water; getting refined water oil; 2 esterifying the refined water oil; proceeding ester exchange; getting rough eater; 3 washing the rough eater; getting neutral rough ester; 4 distilling the neutral rough ester; getting the product. The each technical index of this biological diesel can reach request, which possesses very high practical value.
Description
Technical field
The invention belongs to the preparing technical field of biofuel, be specifically related to a kind of processing method of utilizing hogwash fat to prepare biofuel.
Background technology
Biofuel is a kind of both compliance with environmental protection requirements, the reproducible again new green environment protection energy.In developed country, biofuel is developed rapidly; In China, the impetus of biofuel development is also very violent.At present, the manufacturing of biofuel is raw material still based on chemical method with the animal-plant oil, adds excessive methyl alcohol or ethanol and carry out transesterification reaction in the presence of catalyst acid or alkali, generates fatty acid methyl ester (biofuel).Excessive methyl alcohol recycles after reclaiming.These technologies all are to be raw material with the animal-plant oil, or the tankage behind the extraction Vegetable oil lipoprotein reintroduce grease system biofuel wherein.These technologies all are sophisticated, but raw materials cost is higher, make the cost of biofuel and use restricted unavoidably.And add excessive methyl alcohol and react, reclaiming methyl alcohol has increased energy consumption again.
Summary of the invention
The objective of the invention is to solve above-mentioned the deficiencies in the prior art, a kind of processing method of utilizing hogwash fat to prepare biofuel is provided.
In order to realize purpose of the present invention, the technical solution adopted in the present invention is as follows: this processing method of utilizing hogwash fat to prepare biofuel may further comprise the steps: 1. moisture thick hogwash fat is carried out pre-treatment, obtain refining hogwash fat; 2. refining hogwash fat is carried out esterification, transesterify, obtain thick ester; 3. thick ester is washed, obtained neutral thick ester; 4. the thick ester of neutrality is distilled, obtaining smart fatty acid methyl ester is biofuel.
Described step 1. in pretreatment process be: a, moisture thick hogwash fat is separated removal of impurities, except that anhydrating and residue; B, add clear water again and wash, separate then and remove waste water; C, can repeating step b many times; D, carry out vacuum hydro-extraction again, obtain the refining hogwash fat of water content≤0.2%.
Described step 2. in esterification, ester exchange method be: a, in refining hogwash fat, add the quantitative anhydrous methanol and the vitriol oil, be heated to fully reaction after the certain temperature; B, unnecessary methanol vapor is reclaimed; C, then mixture is separated, obtain thick ester and raw glycerine.
2. the step step can repeat repeatedly, and the condition of esterification, transesterify is as follows: 71～90 ℃ of temperature of reaction, the weight ratio of the vitriol oil and refining hogwash fat is 3～6/100, and the weight ratio of anhydrous methanol and refining hogwash fat is 14～22/100, and the reaction times is 3～6 hours.
Adopt band to stir and the stainless steel cauldron of mechanical seal or the reactor of steel lining F4 or glass in the 2. middle esterification of described step, the transesterify process, and this reactor has the condensation retrieving arrangement of methyl alcohol, fails to participate in reaction on a small quantity and becomes gasiform methyl alcohol to reclaim; Also adopt volume pump to control methyl alcohol and add speed, suitable methanol concentration is arranged in order to Controlling System.
Described step 3. in thick ester method for washing be: a, in the thick ester that 2. obtains through step, add the clear water washing, separate after fully stirring, remove oily(waste)water; But b repeating step a many times, and isolated oily(waste)water in the follow-up washing can be used for the washing of front, reduce water consumption; C, carry out vacuum hydro-extraction then, obtain neutral thick ester.
Described step 3. in the control condition of thick ester washing be: 30～50 ℃ of washing temperature, each clear water that adds is 30/100 with the weight ratio of thick ester, the washing time is 0.5～1.0 hour at every turn, the wash interval time is 2～3 hours.
4. described step carries out the distillatory method to the thick ester of neutrality: a, the neutral thick ester that 3. the process step is obtained carry out the low-voltage vacuum dehydration; B, carry out vacuum distilling then, finally obtaining smart fatty acid methyl ester is biofuel.
4. described step carries out the distillatory condition to the thick ester of neutrality: 100～120 ℃ of low-voltage vacuum dehydration temperaturres, dewatering pressure-0.05～-0.10MPa, dewatering time 20～30 minutes, vacuum distilling pressure is-0.095MPa, it is 180～248 ℃ that smart fatty acid methyl ester is collected temperature, and low-boiling-point substance is collected 120～180 ℃ of temperature.
4. described step is distilled and can be carried out in stainless steel equipment the thick ester of neutrality, can adopt continous way distillation or batch distillation.
A kind of processing method of utilizing hogwash fat to prepare biofuel of the present invention is compared with conventional art, has following characteristics:
1). water oil component complexity, the pre-treatment difficulty is big, is combined in esterification, the transesterify process with simple and easy pre-treatment, the technology of separation of glycerin removal of impurities simultaneously, simplified impurity removal process, reduced the pre-treatment cost, the while also is applicable to the production technique of the tankage production biofuel behind the extraction Vegetable oil lipoprotein.
2). adopt the normal pressure that is different from other technology to feed methyl alcohol continuously, secondary esterification, ester exchange process, can be by control methyl alcohol add speed (application volume pump), Controlling System has preferable methanol concentration, can suitably improve temperature of reaction and speed of reaction again, improve equipment capacity, can reduce the energy consumption that reclaims methyl alcohol again.
3). by adopting different methyl alcohol to add speed and different temperature of reaction, realize that the minimizing side reaction is improved the quality of products and the purpose of product efficiency in the esterification different steps.
4). temperature, time and stir speed (S.S.) by the control washing are removed the acid number of intermediates, and need not use alkali cleaning-water wash procedures, and the hydrolysis reaction that has reduced alkaline cleaning procedure has improved recovery rate, has saved dosing simultaneously, has simplified flow process.
Description of drawings
Fig. 1 is the pretreatment technology schema;
Fig. 2 is esterification, ester exchange process schema;
Fig. 3 is the washing process schema;
Fig. 4 is the distil process schema.
Embodiment
The invention will be further described below in conjunction with accompanying drawing.
A kind of processing method of utilizing hogwash fat to prepare biofuel may further comprise the steps: 1. moisture thick hogwash fat is carried out pre-treatment, obtain refining hogwash fat; 2. refining hogwash fat is carried out esterification, transesterify, obtain thick ester; 3. thick ester is washed, obtained neutral thick ester; 4. the thick ester of neutrality is distilled, obtaining smart fatty acid methyl ester is biofuel.Below in conjunction with accompanying drawing each step is described in detail.
As shown in Figure 1, step 1. in pretreatment process be: a, moisture thick hogwash fat is separated removal of impurities, except that anhydrating and residue; B, add clear water again and wash, separate then and remove waste water; C, can repeating step b many times; D, carry out vacuum hydro-extraction again, obtain the refining hogwash fat of water content≤0.2%.Existing preparation method of bio-diesel oil, hogwash fat will be through the acidifying removal of impurities of coming unstuck, and processing method of the present invention directly enters down operation more after drying and carries out esterification, transesterify after separating removal of impurities, when separation of glycerin impurity is further told.
As shown in Figure 2, step 2. in esterification, ester exchange method be: a, in refining hogwash fat, add the quantitative anhydrous methanol and the vitriol oil, be heated to fully reaction after the certain temperature; B, unnecessary methanol vapor is reclaimed; C, then mixture is separated, obtain thick ester and raw glycerine.The reaction mechanism equation of esterification, transesterify is:
This process can be a batch technology, and oil product enters the reaction that the subordinate phase reactor carries out subordinate phase again after the fs feeds methyl alcohol continuously in other words.Also can oil product enter continuously and enter second reactor more continuously behind first section reactor and react, become full continuous processing.Reactor adopts band to stir and the stainless steel cauldron of mechanical seal or the reactor of steel lining F4 or glass.The condensation retrieving arrangement of reactor band methyl alcohol is failed to participate in reaction on a small quantity and is become gasiform methyl alcohol to reclaim.
The condition of esterification, transesterify is: 71～90 ℃ of temperature of reaction, the weight ratio of the vitriol oil and refining hogwash fat are 3～6/100, and the weight ratio of anhydrous methanol and refining hogwash fat is 14～22/100, and the reaction times is 3～6 hours.Shown in the table specific as follows:
As shown in Figure 3, step 3. in thick fat method for washing be: a, in the thick fat that 2. obtains through step, add the clear water washing, separate after fully stirring, remove oily(waste)water; But b repeating step a many times, and isolated oily(waste)water in the follow-up washing can be used for the washing of front, reduce water consumption; C, carry out vacuum hydro-extraction then, obtain neutral thick fat.Processing method of the present invention does not adopt conventional alkali cleaning-washing process, but thick ester is directly adopted (three times) washing deacidification, as long as operate by the condition of this technology, can realize that the product acid number meets the quality product requirement.Washing is carried out with the steel lining F4 of band agitating function or the reactor of glass.Step 3. in the control condition of thick fat washing be: 30～50 ℃ of washing temperature, each clear water that adds is 30/100 with the weight ratio of thick fat, the washing time is 0.5～1.0 hour at every turn, the wash interval time is 2～3 hours.Shown in the table specific as follows:
| Washing temperature (℃) | Each water consumption (w/w) | Each washing time (h) | The residence time (h) | Washing times |
| 30～50 | Oil: water=1:0.3 | 0.5～1.0 | 2～3 | Be determined by experiment |
As shown in Figure 4,4. step is carried out the distillatory method to the thick ester of neutrality and is: a, the neutral thick ester that 3. obtains through step is carried out the low-voltage vacuum dehydration; B, carry out vacuum distilling then, finally obtaining smart fatty acid methyl ester is biofuel.4. step carries out the distillatory condition to the thick ester of neutrality: 100～120 ℃ of low-voltage vacuum dehydration temperaturres, dewatering pressure-0.05～-0.10MPa, dewatering time 20～30 minutes, vacuum distilling pressure is-0.095MPa, it is 180～248 ℃ that smart fatty acid methyl ester is collected temperature, and low-boiling-point substance is collected 120～180 ℃ of temperature.Shown in the table specific as follows:
| Dehydration temperaturre (℃) | Dewatering pressure (MPa) | Dewatering time (min) | Distillation pressure (MPa) | Low-boiling-point substance collection temperature (℃) | Smart methyl esters collection temperature (℃) |
| 100～120 | -0.05～-0.10 | 20～30 | -0.095 | 120～180 | 180～248 |
This process can be carried out in stainless steel equipment, can adopt continous way distillation or batch distillation.
Biofuel and U.S.'s biodiesel technology index through processing method preparation of the present invention are compared as follows shown in the table:
| Sequence number | Test item | Unit | Biofuel desired value (U.S. ASTM PS121-99) | Detected result (self-control biofuel) |
| 1 | Cetane value | --- | >40 | 61.5 |
| 2 | Boiling range: | |||
| 50% recovered temperature | ℃ | --- | 330.5 | |
| 90% recovered temperature | ℃ | --- | 337.0 | |
| 95% recovered temperature | ℃ | --- | 342.5 | |
| 3 | Kinematic viscosity (20 ℃) | mm 2/s | --- | 6.951 |
| 4 | Kinematic viscosity (40 ℃) | mm 2/s | 1.9～6.0 | 4.336 |
| 5 | 10% steams surplus carbon residue | ％(m/m) | 0.05 | 0.020 |
| 6 | Ash content | ％(m/m) | 0.02 | 0.002 |
| 7 | Moisture | ％(m/m) | <0.05 | Vestige |
| 8 | Mechanical impurity | ％(m/m) | Do not have | Do not have |
| Sequence number | Test item | Unit | Biofuel desired value (U.S. ASTM PS121-99) | Detected result (self-control biofuel) |
| 9 | Sulphur content | ％(m/m) | ≤0.05 | 0.020 |
| 10 | Flash-point (remaining silent) | ℃ | >100 | 164 |
| 11 | Copper corrosion (50 ℃, 3h) | Level | 3 | 1a |
| 12 | Neutralization value | mgKOH/g | <0.8 | 0.477 |
| 13 | Condensation point | ℃ | --- | +7 |
| 14 | Cold filter clogging temperature | ℃ | --- | +8 |
| 15 | Colourity | Number | --- | Less than 0.5 |
| 16 | Density (20 ℃) | Kg/m 3 | --- | 874.2 |
| 17 | Free glycerol | ％(m/m) | <0.02 | 0.0016 |
| 18 | Total glycerine | ％(m/m) | <0.24 | 0.235 |
As can be seen from the above table, the biofuel through processing method preparation of the present invention has good quality.
Claims (3)
1. processing method of utilizing hogwash fat to prepare biofuel is characterized in that may further comprise the steps:
1. moisture thick hogwash fat is carried out pre-treatment
A, moisture thick hogwash fat is separated removal of impurities, remove and anhydrate and residue; B, add clear water again and wash, separate then and remove waste water; C, can repeating step b many times; D, carry out vacuum hydro-extraction again, obtain the refining hogwash fat of water content≤0.2% by weight;
2. refining hogwash fat is carried out secondary esterification, transesterify, obtain thick ester
One-level esterification, transesterify: in refining hogwash fat, add the quantitative anhydrous methanol and the vitriol oil, oil, vitriol oil weight ratio: 1: 0.03～1: 0.06, oil, methyl alcohol weight ratio: 1: 0.14～1: 0.22,71～90 ℃ of Heating temperatures, reaction times 3～6h, methanol vapor reclaims, and then mixture is separated, and obtains thick ester and raw glycerine;
Secondary esterification, transesterify: temperature of reaction: 90～80 ℃, the weight ratio of the oil and the vitriol oil: 1: 0.03～1: 0.06, oil, methyl alcohol weight ratio: 1: 0.14～1: 0.22, reaction times 3～6h;
3. thick ester is washed, obtained neutral thick ester
In the thick ester that 2. obtains through step, add the clear water washing, separate after fully stirring, remove oily(waste)water, repeat repeatedly the clear water washing, isolated oily(waste)water in the follow-up washing is used for the washing of front, reduce water consumption carries out vacuum hydro-extraction then, obtains neutral thick ester, 30～50 ℃ of washing temperature, each clear water that adds is 30/100 with the weight ratio of thick ester, and the washing time is 0.5～1.0 hour at every turn, and the wash interval time is 2～3 hours;
4. the thick ester of neutrality is distilled, obtaining smart fatty acid methyl ester is biofuel
3. the neutral thick ester that obtains through step is carried out the low-voltage vacuum dehydration, carry out vacuum distilling then, finally obtaining smart fatty acid methyl ester is biofuel, 100～120 ℃ of low-voltage vacuum dehydration temperaturres, dewatering pressure-0.05～-0.10MPa, dewatering time 20～30 minutes, vacuum distilling pressure is-0.095Mpa, it is 180～248 ℃ that smart fatty acid methyl ester is collected temperature, and low-boiling-point substance is collected 120～180 ℃ of temperature.
2. the processing method of preparation biofuel according to claim 1, it is characterized in that: adopt band to stir and the stainless steel cauldron of mechanical seal or the reactor of steel lining F4 or glass in the 2. middle esterification of described step, the transesterify process, and this reactor has the condensation retrieving arrangement of methyl alcohol, fails to participate in reaction on a small quantity and becomes gasiform methyl alcohol to reclaim; Also adopt volume pump to control methyl alcohol and add speed, suitable methanol concentration is arranged in order to Controlling System.
3. the processing method of preparation biofuel according to claim 1 is characterized in that: 4. described step is distilled in stainless steel equipment the thick ester of neutrality and is carried out, and adopts continous way distillation or batch distillation.
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| CN2006100352720A CN101063040B (en) | 2006-04-29 | 2006-04-29 | Method for preparing biological diesel by hogwash oil |
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| CN2006100352720A CN101063040B (en) | 2006-04-29 | 2006-04-29 | Method for preparing biological diesel by hogwash oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1560197A (en) * | 2004-03-05 | 2005-01-05 | 王聚亮 | Process of preparing biologic diesel oil by swill oil |
| CN1699516A (en) * | 2005-06-01 | 2005-11-23 | 清华大学 | Process for preparing bio-diesel-oil by using microalgae fat |
| JP2005350632A (en) * | 2004-06-14 | 2005-12-22 | Electric Power Dev Co Ltd | Method for producing biodiesel fuel |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1560197A (en) * | 2004-03-05 | 2005-01-05 | 王聚亮 | Process of preparing biologic diesel oil by swill oil |
| JP2005350632A (en) * | 2004-06-14 | 2005-12-22 | Electric Power Dev Co Ltd | Method for producing biodiesel fuel |
| CN1699516A (en) * | 2005-06-01 | 2005-11-23 | 清华大学 | Process for preparing bio-diesel-oil by using microalgae fat |
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Assignee: Guangzhou Yinlu Environmental Scientific & Technology Development Co., Ltd. Assignor: Chen Feng Contract record no.: 2011440000072 Denomination of invention: Method for preparing biological diesel by hogwash oil Granted publication date: 20100818 License type: Exclusive License Open date: 20071031 Record date: 20110225 |
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