CN101240182A - Preparation method for biological diesel oil - Google Patents
Preparation method for biological diesel oil Download PDFInfo
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- CN101240182A CN101240182A CNA2008100136699A CN200810013669A CN101240182A CN 101240182 A CN101240182 A CN 101240182A CN A2008100136699 A CNA2008100136699 A CN A2008100136699A CN 200810013669 A CN200810013669 A CN 200810013669A CN 101240182 A CN101240182 A CN 101240182A
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- oil
- esterification
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- biofuel
- preparation
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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
- 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
Abstract
The invention relates to a synthesis technique of biological oil plants, specifically, a preparation method of biological diesel. The technical plan is: after esterification reaction of preprocessed base oil added with catalyst, agitating and distilling it with controlled pressure and temperature, to obtain biological diesel. The production process is: 1, removing water and impurity from base oil as preprocessing; 2, processing esterification reaction for preprocessed base oil, to esterify free fatty acid in grease completely, after that, separating catalyst and glycerin from raw material; 3, processing esterification reaction again after removing catalyst, to eterify fatty acid and triglyceride completely; 4, putting it into vacuum tower, with tower pressure: 1mmHg to 6mmHg, and termperature: 240 deg C. to 270 deg C.; the base oil is waste oil, waste animal oil or waste vegetable oil, etc..The reaction condition of the invention is temperate; the reaction process is easy to control; and the raw material is easy to obtain and implement.
Description
Technical field:
The present invention relates to a kind of synthetic technology of bio-oil materials, specifically is a kind of preparation method of biofuel.
Background technology:
By changeing the longer chain fatty acid lipid material that the fat reaction generates, is a kind of novel pollution-free renewable energy source by animal-plant oil, is called as biofuel.Its combustionproperty can be that diesel oil matches in excellence or beauty with traditional oil, because objectionable impurities has reduced by 50% than traditional petrifaction diesel in the tail gas that biofuel burning rear engine gives off.Research of biofuel at present and application have been subjected to widely to be paid close attention to.
At present the production method of biofuel mainly is commentaries on classics fat to be taken place for animal-plant oil and some short chain alcohol (methyl alcohol, ethanol etc.) react and get under the katalysis of catalyzer.Wherein, animal oil has: lard, butter, sheep oil, chicken fat, duck oil.Vegetables oil has: soybean oil, peanut oil, Semen Maydis oil, Oleum Gossypii semen, plam oil or the like.Each is variant for its zero pour and stearic acid, free acid, triglyceride, phosphatide, existing processes is not well understood these characteristics, has therefore caused the use cost height of long reaction time, catalyzer.Because present technology all is to adopt the atmospheric pressure reflux reaction, methyl alcohol enters surge tank through condenser again and is back to reactor participation reaction again after the reactor vaporization, and surge tank to have one with the extraneous pneumostome that communicates, per hour have 2% methyl alcohol evaporate in the air through pneumostome through measuring and calculating.The national standard of methyl alcohol flash-point is 16 ℃, and the flash-point of a lot of methanol production producers does not also reach 16 ℃, if potential safety hazard is arranged slightly, just may cause a serious accident.Simultaneously, washing is one technology in the production of biodiesel in the past, and it need add basic materials in water, make oil reach neutral after washing.Its shortcoming is: the cost that has increased basic materials and washing process, and generally to wash 2-4 time, according to these technical matters, the time that once washing will be used in actual production (comprising settlement separate) is 5 hours, and the time of whole washing process is minimum more than 10 hours, the significant wastage of the water resources that causes and pollution.
Summary of the invention:
Purpose of the present invention is exactly the defective that exists at prior art, provides a kind of and can improve the preparation method that turnover ratio reduces the biofuel in reaction times.
Its technical scheme is: after stock oil of the present invention added the catalyzer esterification reaction, control pressure and temperature stirred and distill, and just obtain biofuel.Its production process is:
1, stock oil is carried out pre-treatment and slough moisture, impurity;
2, pretreated stock oil is carried out esterification, make the complete esterification of free fatty acids in the grease.Isolate catalyzer and glycerine in the material after the end;
3, the material of removing behind the catalyzer carries out transesterification reaction again, makes lipid acid in the oil, triglyceride level, esterification fully;
4, enter vacuum distillation tower, tower is pressed and is 1-6mmHg; Temperature is 240-270 ℃;
Described stock oil is sewer oil, depleted vegetable and animals oils or plant oil leftover etc.
Effect of the present invention is: the present invention makes oil from high acid value waste animal and plant through production technique such as esterification, transesterifys, has guaranteed that the product index of biofuel is qualified up to standard.By the optimization of new technology and technology, improved turnover ratio and reduced the reaction times.Reaction conditions gentleness of the present invention, have environment friendly, reaction process is simple and easy to control, and raw material is easy to get, implements easily.
Specific embodiment:
After stock oil of the present invention added the catalyzer esterification reaction, control pressure and temperature stirred and distill, and just obtain biofuel.Its production process is:
1, stock oil is carried out pre-treatment and slough moisture, impurity;
2, pretreated stock oil is carried out esterification, make the complete esterification of free fatty acids in the grease.Isolate catalyzer and glycerine in the material after the end;
3, the material of removing behind the catalyzer carries out transesterification reaction again, makes lipid acid in the oil, triglyceride level, esterification fully;
4, enter vacuum distillation tower, tower is pressed and is 1-6mmHg; Temperature is 240-270 ℃;
Described stock oil is sewer oil, depleted vegetable and animals oils or plant oil leftover etc.
Embodiment 1:
Get 1000 kilograms of sewer oils, the phosphoric acid of adding 3 ‰ stirred 10 minutes earlier, adding 5 ‰ hydrogen peroxide again stirred 10 minutes, sedimentation entered in the reactor after 1 hour, at vacuum tightness 0.08Mpa-0.095Mpa, temperature is extracted residual moisture out under 65 ℃-85 ℃ condition, the moisture controlled that makes raw material is below 0.2%.The consumption of methyl alcohol is pressed the 15%-30% of stock oil, and the sulfuric acid consumption is the 0.5%-0.7% of stock oil.With closeall import and export behind methyl alcohol and the sulfuric acid adding reactor, be heated with stirring to 60 ℃-80 ℃.The still internal pressure stops heating after reaching 4-6 kilogram pressure, reaction times is in 45-60 minute, detecting acid number is in the 2mgKOH/10, vacuum is taken out the methyl alcohol in the still, with grease squeeze into tapered jar in 60 ℃ of sedimentations of insulation 60 minutes, remove the glycerine of bottom, catalyzer gets 950 kilograms of thick esters, again thick fat is squeezed into reactor, add the methyl alcohol of 10%-20% and 0.5% NaOH again and carry out transesterification reaction, the confined reaction temperature is at 70 ℃-80 ℃, and pressure is at the 4-5 kilogram, 30 minutes time, acid number drops in the 0.5mgKOH/10, and vacuum 0.08mpa-0.098mpa extracts the methyl alcohol in the still out.Thick ester is entered distillation tower, the decompressing and continuous distillation, the distillation absolute pressure is 1-6mmHg.Distillating 931 kilograms of biofuel, to enter the storage tank acid number be to be finished product below the 0.8mgKOH/10.The rate of recovery reaches 98%.
Embodiment 2:
1000 kilograms of the pretreated cottonseed acid carburetion of learning from else's experience, the phosphoric acid of adding 4%0 stirred 10 minutes earlier, adding 5 ‰ hydrogen peroxide again stirred 10 minutes, sedimentation entered in the reactor after 1 hour, at vacuum tightness 0.08Mpa-0.095Mpa, temperature is extracted residual moisture out under 65 ℃-85 ℃ condition, the moisture controlled that makes raw material is below 0.2%.Methyl alcohol is pressed the 17%-25% of raw material, and the sulfuric acid consumption is the 0.4%-0.9% of raw material.With closeall import and export behind methyl alcohol and the sulfuric acid adding reactor, be heated with stirring to 65 ℃-75 ℃.The still internal pressure stops heating after reaching 2-5 kilogram pressure, reaction times is in 35-60 minute, detecting acid number is in the 2mgKOH/10, vacuum is taken out the methyl alcohol in the still, with grease squeeze into tapered jar in 60 ℃ of sedimentations of insulation 60 minutes, remove the glycerine of bottom, catalyzer gets 987 kilograms of thick esters, again thick fat is squeezed into reactor, add the methyl alcohol of 15%-25% and the KOH of 0.5%-0.8% again and carry out transesterification reaction, the confined reaction temperature is at 60 ℃-70 ℃, and pressure is at the 3-5 kilogram, time 30-45 minute, acid number drops in the 0.5mgKOH/10, and vacuum 0.08mpa extracts the methyl alcohol in the still out.Thick ester is entered distillation tower, the decompressing and continuous distillation, the distillation absolute pressure is 1-6mmHg.Distillate biofuel and enter storage tank for 957 kilograms, acid number is to be finished product below the 0.8mgKOH/10.The rate of recovery reaches 97%.
Embodiment 3:
Get and pass through the pre-treatment acid number 1000 kilograms of the high acid value soybean oil of 150mgKOH/10, the phosphoric acid of adding 5 ‰ stirred 10 minutes earlier, adding 7%0 hydrogen peroxide again stirred 10 minutes, sedimentation enters after 1 hour and enters in the reactor in the reactor, at vacuum tightness 0.08Mpa-0.095Mpa, temperature is extracted residual moisture out under 65 ℃-85 ℃ condition, the moisture controlled that makes raw material is below 0.2%.Methyl alcohol is pressed the 17%-27% of raw material, and the sulfuric acid consumption is the 0.5%-1.1% of raw material.With closeall import and export behind methyl alcohol and the sulfuric acid adding reactor, be heated with stirring to 60 ℃-80 ℃.The still internal pressure stops heating after reaching in the 4-8 kilogram, reaction times is in 50-60 minute, detecting acid number is in the 2mgKOH/10, vacuum is taken out the methyl alcohol in the still, with grease squeeze into tapered jar in 60 ℃ of sedimentations of insulation 60 minutes, remove the glycerine of bottom, catalyzer gets 990 kilograms of thick esters, again thick fat is squeezed into reactor, add the methyl alcohol of 20%-33% and the NaOH of 0.5%-1.0% again and carry out transesterification reaction, the confined reaction temperature is at 65 ℃-80 ℃, and pressure is at the 4-6 kilogram, time 30-45 minute, acid number drops in the 0.5mgKOH/10, and vacuum 0.08mpa extracts the methyl alcohol in the still out.Thick ester is entered distillation tower, the decompressing and continuous distillation, the distillation absolute pressure is 1-6mmHg.Distillate biofuel and enter storage tank for 960 kilograms, acid number is to be finished product below the 0.8mgKOH/10.The rate of recovery reaches 97%.
Claims (2)
1, a kind of preparation method of biofuel is characterized in that: after stock oil of the present invention added the catalyzer esterification reaction, control pressure and temperature stirred and distill, and just obtain biofuel.Its production process is:
(1) stock oil is carried out pre-treatment and slough moisture, impurity;
(2) pretreated stock oil is carried out esterification, make the complete esterification of free fatty acids in the grease.Isolate catalyzer and glycerine in the material after the end;
(3) material of removing behind the catalyzer carries out transesterification reaction again, makes lipid acid in the oil, triglyceride level, esterification fully;
(4) enter vacuum distillation tower, tower is pressed and is 1-6mmHg; Temperature is 240-270 ℃;
2, the preparation method of a kind of biofuel according to claim 1 is characterized in that: described stock oil is sewer oil, depleted vegetable and animals oils or plant oil leftover etc.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100136699A CN101240182A (en) | 2008-01-19 | 2008-01-19 | Preparation method for biological diesel oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100136699A CN101240182A (en) | 2008-01-19 | 2008-01-19 | Preparation method for biological diesel oil |
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| Publication Number | Publication Date |
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| CN101240182A true CN101240182A (en) | 2008-08-13 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNA2008100136699A Pending CN101240182A (en) | 2008-01-19 | 2008-01-19 | Preparation method for biological diesel oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112646664A (en) * | 2019-10-12 | 2021-04-13 | 常州市金坛区维格生物科技有限公司 | Method for preparing low-sulfur biodiesel from acidized oil |
| CN116656403A (en) * | 2023-05-25 | 2023-08-29 | 盐城工学院 | Preparation method for producing biodiesel by using cottonseed oil |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1861752A (en) * | 2006-06-12 | 2006-11-15 | 大连理工大学 | Process of producing biological diesel by high acid waste oil |
| CN1865400A (en) * | 2006-06-16 | 2006-11-22 | 刘火成 | Process for preparing biological diesel oil by using waste oil of plant and animal |
-
2008
- 2008-01-19 CN CNA2008100136699A patent/CN101240182A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1861752A (en) * | 2006-06-12 | 2006-11-15 | 大连理工大学 | Process of producing biological diesel by high acid waste oil |
| CN1865400A (en) * | 2006-06-16 | 2006-11-22 | 刘火成 | Process for preparing biological diesel oil by using waste oil of plant and animal |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112646664A (en) * | 2019-10-12 | 2021-04-13 | 常州市金坛区维格生物科技有限公司 | Method for preparing low-sulfur biodiesel from acidized oil |
| CN116656403A (en) * | 2023-05-25 | 2023-08-29 | 盐城工学院 | Preparation method for producing biodiesel by using cottonseed oil |
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Application publication date: 20080813 |