CN101440298B - Method for preparing -20 DEC C biodiesel from waste lipid by distillation process - Google Patents
Method for preparing -20 DEC C biodiesel from waste lipid by distillation process Download PDFInfo
- Publication number
- CN101440298B CN101440298B CN200810143872A CN200810143872A CN101440298B CN 101440298 B CN101440298 B CN 101440298B CN 200810143872 A CN200810143872 A CN 200810143872A CN 200810143872 A CN200810143872 A CN 200810143872A CN 101440298 B CN101440298 B CN 101440298B
- Authority
- CN
- China
- Prior art keywords
- acid
- biodiesel
- mentioned
- fractionation
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
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
Abstract
The invention relates to a process for preparing -20# biodiesel from waste lipin based on a rectification process. The waste lipin is used as a raw material and is added with methanol and other catalysts for reaction to prepare a product through a six-step method of material selection, hydrolysis, fractionation, esterification, neutralization, dealcoholization and rectification; the process overcomes the disadvantages that biodiesel produced through the prior preparation method has low output, few breeds and poor performance and can not be suitable for a low-temperature environment, enlarges the functions of the prior biodiesel, provides a new approach for the production of new breeds of the biodiesel; the product has stable performance and good applicability, does not solidify between room temperature and 20 DEG C below zero, can be freely mixed with diesel, has no toxicity or corrosion performance, does not damage a mechanical part, is easy to biodegrade, is environment-friendly, can be used for all weather, has high boiling point and flash point, belongs to non-dangerous goods and has safe storage and transportation and huge commercial potential; and the method is suitable for the production of preparing biodiesel with low freezing point through using the waste lipin as the main material.
Description
Technical field
The present invention relates to a kind of preparation-20# method of bio-diesel oil, especially a kind ofly from waste oil, prepare-the 20# method of bio-diesel oil based on rectification process.
Background technology
Existing biofuel of producing with animal-plant oil, staple is Uniphat A60, methyl stearate, Witconol 2301, methyl linoleate.Because of differences such as grease kind, the place of production, weathers, wherein various lipid acid components have very big difference, therefore, the component of biofuel and congealing point also have a great difference.Wherein, the congealing point of Uniphat A60: 28.5 ℃～29.5 ℃, the congealing point of methyl stearate: 37 ℃～38 ℃, the congealing point of Witconol 2301 :-19.5 ℃～-20.5 ℃, the congealing point of methyl linoleate :-34 ℃～-35 ℃.When temperature was lower than 10 ℃, the component of high congealing point will be solidified as the white solid thing and separates out in the biofuel, can clogged oil line when being applied to diesel motor, influence biofuel use in the winter time.
Summary of the invention
To above-mentioned situation, the object of the present invention is to provide a kind ofly from waste oil, to prepare-the 20# method of bio-diesel oil based on rectification process, it had both increased kind, the function of biofuel, did not solidify when reducing to-20 ℃ again in envrionment temperature; Ability and diesel oil mix arbitrarily, nontoxic non-corrosiveness, and readily biodegradable also has technology simple; Operation easily, production cost is low, and output is big; Productive rate is high, storing safety, and raw material sources are wide.
For realizing above-mentioned purpose, from waste oil, prepare-the 20# method of bio-diesel oil based on rectification process, it is chosen waste oil and makes main raw material, adds catalyzer such as methyl alcohol, sulfuric acid and reacts, and processes product through Six Steps, and its step is following:
I, technical process
Select materials-hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product;
II, operation steps
1. choose discarded animal and plant grease and do raw material and clear water input grease adverse current hydrolysis tower, hydrolysis;
2. hydrolysising reacting temperature is 200 ℃-250 ℃, and pressure is 2.5MPa-3.0MPa, and oil is 1:0.4-0.5 with the ratio of water, and the reaction times is 4-8 hours, separates to obtain croude fatty acids and aqueous glycerin solution;
3. get above-mentioned croude fatty acids input separation column and carry out fractionation; Reaction conditions is vacuum residual voltage < 2 mmhg in the tower body; Distillation temperature is 200 ℃-250 ℃, makes the lipid acid fractionation, mixture and sub product palmitinic acid, the Triple Pressed Stearic Acid of oleic acid, linoleic acid plus linolenic acid;
4. get the mixture and the methanol mixed of above-mentioned oleic acid, linoleic acid plus linolenic acid, add sulfuric acid, esterification reaction temperature is 70 ℃-85 ℃, and the reaction times is 4-8 hours, gets carboxylate and water simultaneously;
5. after adding soda ash neutralizes in above-mentioned carboxylate, remove free acid earlier, remove methyl alcohol again, and reclaim methyl alcohol;
6. the carboxylate suction rectifying tower after the above-mentioned dealcoholysis carries out rectifying, and the rectification process condition is that < 5 mmhg, temperature of reaction are 200 ℃-230 ℃ to vacuum residual voltage in the tower body, remove residue, get the biofuel finished product.
For realizing above-mentioned purpose, its further step is:
The consisting of of raw material (volume unit):
100 parts of greases
Methyl alcohol 11-15 part
Sulfuric acid 0.2-0.4 part
Soda ash 0.1-0.25 part
Vitriolic concentration is 93% concentration-98% concentration.Step finished product congealing point 6. is not for being higher than-20 ℃.
The present invention's employing is chosen waste oil and is made main raw material; Adding catalyzer such as methyl alcohol, sulfuric acid reacts; Through select materials-Six Steps of hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product processes-technical scheme of 20# biofuel, overcome the biofuel that adopts the traditional preparation process method to produce, kind is few; Poor performance can't adapt to the defective that temperature uses than low environment.
Beneficial effect of the present invention:
(I) the present invention makes full use of waste grease and makes raw material, has enlarged the function of traditional biological diesel oil, for the production of biofuel new variety provides-the bar new way; (II) the present invention makes main raw material with waste oil, and its preparation technology is simple, processing ease, and facility investment is few, and production cost is low, and is with short production cycle, and output is big, and productive rate is high, and raw material sources are wide; (III) the present invention is that main raw material makes with the waste oil, and its product performance are stable, and flexibility is good, does not solidify acid number＜1 in room temperature during to-20 ℃; Color and luster (iron cobalt colourimetry)＜2, ability and diesel oil mix nontoxic non-corrosiveness, not loss parts arbitrarily; Readily biodegradable, environmentally friendly, can round-the-clockly use, higher is arranged; Flash-point belongs to non-dangerous goods, storing safety, and business potential is huge.
The present invention is fit to do with waste oil the production of the low congealing point biofuel of main feedstock production.
Below in conjunction with accompanying drawing and embodiment the present invention is done further detailed explanation.
Fig. 1 is the diagram method () of more excellent embodiment of the present invention.
Fig. 2 is the diagram method (two) of more excellent embodiment of the present invention.
Embodiment
Embodiment 1
The consisting of of A, raw material (volume unit):
100 parts of greases
15 parts of methyl alcohol
0.4 part in sulfuric acid
0.25 part of soda ash.
The step of B, preparation-20# biofuel:
I, technical process
Select materials-hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product;
II, operation steps
1. choose discarded animal and plant grease and make raw material and clear water, drop into the hydrolysis of grease adverse current hydrolysis tower;
2. hydrolysising reacting temperature is 210 ℃, and pressure is 2.5MPa, and oil is 1:0.4 with the ratio of water, and the reaction times is 8 hours, separates to obtain croude fatty acids and aqueous glycerin solution;
3. get above-mentioned croude fatty acids and drop into separation column and carry out fractionation, reaction conditions be vacuum residual voltage in the tower body 2 mmhg, distillation temperature is 200 ℃, makes the lipid acid fractionation, mixture and sub product palmitinic acid, the Triple Pressed Stearic Acid of oleic acid, linoleic acid plus linolenic acid;
4. get above-mentioned oleic acid, linolic acid, linolenic acid mixture and methanol mixed, add sulphating, esterification reaction temperature is 70 ℃, and the reaction times is 8 hours, gets carboxylate and water simultaneously;
5. after adding soda ash neutralizes in above-mentioned carboxylate, remove free acid earlier, remove methyl alcohol again, and reclaim methyl alcohol;
6. the carboxylate after the above-mentioned dealcoholysis drops into rectifying tower and carries out rectifying, and the rectification process condition is that < 5 mmhg, temperature is 200 ℃ to vacuum residual voltage in the tower body, removes residue, gets product.
Embodiment 2
The consisting of of A, raw material (volume unit):
100 parts of greases
14.5 parts of methyl alcohol
0.4 part in sulfuric acid
0.25 part of soda ash.
The step of B, preparation-20# biofuel:
I, technical process
Select materials-hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product;
II, operation steps
1. choose discarded animal and plant grease and do raw material and the hydrolysis of clear water input grease adverse current hydrolysis tower;
2. hydrolysising reacting temperature is 215 ℃, and pressure is 2.55MPa, and oil is 1:0.45 with the ratio of water, and the reaction times is 7 hours, separates to obtain croude fatty acids and aqueous glycerin solution;
3. get above-mentioned croude fatty acids and drop into separation column and carry out fractionation, reaction conditions be vacuum residual voltage in the tower body 2 mmhg, distillation temperature is 205 ℃, makes the lipid acid fractionation, mixture and sub product palmitinic acid, the Triple Pressed Stearic Acid of oleic acid, linoleic acid plus linolenic acid;
4. get above-mentioned oleic acid, linolic acid, linolenic acid mixture and methanol mixed, add sulphating, esterification reaction temperature is 75 ℃, and the reaction times is 6.5 hours, gets carboxylate and water simultaneously;
5. after adding soda ash neutralizes in above-mentioned carboxylate, remove free acid earlier, remove methyl alcohol again, and reclaim methyl alcohol;
6. the carboxylate after the above-mentioned dealcoholysis drops into rectifying tower and carries out rectifying, and the rectification process condition is that < 5 mmhg, temperature is 210 ℃ to vacuum residual voltage in the tower body, removes residue, gets product.
Embodiment 3
The consisting of of A, raw material (volume unit):
100 parts of greases
13.5 parts of methyl alcohol
0.35 part in sulfuric acid
0.22 part of soda ash.
The step of B, preparation-20# biofuel:
I, technical process
Select materials-hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product;
II, operation steps
1. choose discarded animal and plant grease and make raw material and clear water, drop into the hydrolysis of grease adverse current hydrolysis tower;
2. hydrolysising reacting temperature is 225 ℃, and pressure is 2.65MPa, and oil is 1:0.46 with the ratio of water, and the reaction times is 5.5 hours, separates to obtain croude fatty acids and aqueous glycerin solution;
3. get above-mentioned croude fatty acids and drop into separation column and carry out fractionation, reaction conditions be vacuum residual voltage in the tower body 2 mmhg, distillation temperature is 215 ℃, makes the lipid acid fractionation, mixture and sub product palmitinic acid, the Triple Pressed Stearic Acid of oleic acid, linoleic acid plus linolenic acid;
4. get above-mentioned oleic acid, linolic acid, linolenic acid mixture and methanol mixed, add sulphating, esterification reaction temperature is 78 ℃, and the reaction times is 6 hours, gets carboxylate and water simultaneously;
5. after adding soda ash neutralizes in above-mentioned carboxylate, remove free acid earlier, remove methyl alcohol again, and reclaim methyl alcohol;
6. the carboxylate after the above-mentioned dealcoholysis drops into rectifying tower and carries out rectifying, and the rectification process condition is that < 5 mmhg, temperature is 215 ℃ to vacuum residual voltage in the tower body, removes residue, gets product.
Embodiment 4
The consisting of of A, raw material (volume unit):
100 parts of greases
13 parts of methyl alcohol
0.3 part in sulfuric acid
0.2 part of soda ash.
The step of B, preparation-20# biofuel:
I, technical process
Select materials-hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product;
II, operation steps
1. choose discarded animal and plant grease and make raw material and clear water, drop into the hydrolysis of grease adverse current hydrolysis tower;
2. hydrolysising reacting temperature is 240 ℃, and pressure is 2.8MPa, and oil is 1:0.47 with the ratio of water, and the reaction times is 5 hours, separates to obtain croude fatty acids and aqueous glycerin solution;
3. get above-mentioned croude fatty acids and drop into separation column and carry out fractionation, reaction conditions be vacuum residual voltage in the tower body 2 mmhg, distillation temperature is 235 ℃, makes the lipid acid fractionation, mixture and sub product palmitinic acid, the Triple Pressed Stearic Acid of oleic acid, linoleic acid plus linolenic acid;
4. get above-mentioned oleic acid, linolic acid, linolenic acid mixture and methanol mixed, add sulphating, esterification reaction temperature is 80 ℃, and the reaction times is 5.5 hours, gets carboxylate and water simultaneously;
5. after adding soda ash neutralizes in above-mentioned carboxylate, remove free acid earlier, remove methyl alcohol again, and reclaim methyl alcohol;
6. the carboxylate after the above-mentioned dealcoholysis drops into rectifying tower and carries out rectifying, and the rectification process condition is that < 5 mmhg, temperature is 228 ℃ to vacuum residual voltage in the tower body, removes residue, gets product.
Embodiment 5
The consisting of of A, raw material (volume unit):
100 parts of greases
12 parts of methyl alcohol
0.28 part in sulfuric acid
0.18 part of soda ash.
The step of B, preparation-20# biofuel:
I, technical process
Select materials-hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product;
II, operation steps
1. choose discarded animal and plant grease and make raw material and clear water, drop into the hydrolysis of grease adverse current hydrolysis tower;
2. hydrolysising reacting temperature is 245 ℃, and pressure is 2.9MPa, and oil is 1:0.49 with the ratio of water, and the reaction times is 4.5 hours, separates to obtain croude fatty acids and aqueous glycerin solution;
3. get above-mentioned croude fatty acids and drop into separation column and carry out fractionation, reaction conditions be vacuum residual voltage in the tower body 2 mmhg, distillation temperature is 245 ℃, makes the lipid acid fractionation, mixture and sub product palmitinic acid, the Triple Pressed Stearic Acid of oleic acid, linoleic acid plus linolenic acid;
4. get above-mentioned oleic acid, linolic acid, linolenic acid mixture and methanol mixed, add sulphating, esterification reaction temperature is 82 ℃, and the reaction times is 5 hours, gets carboxylate and water simultaneously;
5. after adding soda ash neutralizes in above-mentioned carboxylate, remove free acid earlier, remove methyl alcohol again, and reclaim methyl alcohol;
6. the carboxylate after the above-mentioned dealcoholysis drops into rectifying tower and carries out rectifying, and the rectification process condition is that < 5 mmhg, temperature is 228 ℃ to vacuum residual voltage in the tower body, removes residue, gets product.
Embodiment 6
The consisting of of A, raw material (volume unit):
100 parts of greases
11 parts of methyl alcohol
0.25 part in sulfuric acid
0.15 part of soda ash.
The step of B, preparation-20# biofuel:
I, technical process
Select materials-hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product;
II, operation steps
1. choose discarded animal and plant grease and make raw material and clear water, drop into the hydrolysis of grease adverse current hydrolysis tower;
2. hydrolysising reacting temperature is 250 ℃, and pressure is 3.0MPa, and oil is 1:0.5 with the ratio of water, and the reaction times is 4 hours, separates to obtain croude fatty acids and aqueous glycerin solution;
3. get above-mentioned croude fatty acids and drop into separation column and carry out fractionation, reaction conditions be vacuum residual voltage in the tower body 2 mmhg, distillation temperature is 250 ℃, makes the lipid acid fractionation, mixture and sub product palmitinic acid, the Triple Pressed Stearic Acid of oleic acid, linoleic acid plus linolenic acid;
4. get above-mentioned oleic acid, linolic acid, linolenic acid mixture and methanol mixed, add sulphating, esterification reaction temperature is 85 ℃, and the reaction times is 4 hours, gets carboxylate and water simultaneously;
5. after adding soda ash neutralizes in above-mentioned carboxylate, remove free acid earlier, remove methyl alcohol again, and reclaim methyl alcohol;
6. the carboxylate after the above-mentioned dealcoholysis drops into rectifying tower and carries out rectifying, and the rectification process condition is that < 5 mmhg, temperature is 230 ℃ to vacuum residual voltage in the tower body, removes residue, gets product.
Embodiment 7
The consisting of of A, raw material (volume unit):
100 parts of greases
13 parts of methyl alcohol
0.2 part in sulfuric acid
0.25 part of soda ash.
The step of B, preparation-20# biofuel:
I, technical process
Select materials-hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product;
II, operation steps
1. choose discarded animal and plant grease and make raw material and clear water, drop into the hydrolysis of grease adverse current hydrolysis tower;
2. hydrolysising reacting temperature is 250 ℃, and pressure is 3.0MPa, and oil is 1:0.5 with the ratio of water, and the reaction times is 4 hours, separates to obtain croude fatty acids and aqueous glycerin solution;
3. get above-mentioned croude fatty acids and drop into separation column and carry out fractionation, reaction conditions be vacuum residual voltage in the tower body 2 mmhg, distillation temperature is 250 ℃, makes the lipid acid fractionation, mixture and sub product palmitinic acid, the Triple Pressed Stearic Acid of oleic acid, linoleic acid plus linolenic acid;
4. get above-mentioned oleic acid, linolic acid, linolenic acid mixture and methanol mixed, add sulphating, esterification reaction temperature is 85 ℃, and the reaction times is 4 hours, gets carboxylate and water simultaneously;
5. after adding soda ash neutralizes in above-mentioned carboxylate, remove free acid earlier, remove methyl alcohol again, and reclaim methyl alcohol;
6. the carboxylate after the above-mentioned dealcoholysis drops into rectifying tower and carries out rectifying, and the rectification process condition is that < 5 mmhg, temperature is 230 ℃ to vacuum residual voltage in the tower body, removes residue, gets product.
Above embodiment catalyst system therefor vitriolic concentration is 93% concentration-98% concentration.
More excellent embodiment instance
1, with 100 parts of greases (is example with the depleted food oils), add 40 parts of water, at pressure 2.5MPa, under the condition that temperature is 230 ℃, hydrolysis tower internal reaction 6 hours, 90 parts of croude fatty acids, 50 parts of aqueous glycerin solutions;
2,90 parts of croude fatty acids are got into separation columns, vacuum residual voltage in tower body 2 mmhg under the condition that temperature is 225 ℃, carry out the lipid acid fractionation, and 25 parts of sub product palmitinic acids, Triple Pressed Stearic Acid, 65 parts in the mixture of oleic acid, linoleic acid plus linolenic acid;
3, with 65 parts of oleic acid, linoleic acid plus linolenic acid mixture and 13 parts of methanol mixed, add 0.2 part of 93% concentration sulfuric acid, reacted 6 hours down at 78 ℃, be divided into 4 parts of water simultaneously.When acid number 1 the time, and 68 parts of carboxylates;
4,0.25 part of soda ash of adding neutralizes and removes free acid in carboxylate, removes methyl alcohol again, reclaims 6 parts of methyl alcohol;
5, the carboxylate after the dealcoholysis, < 5 mmhg under the condition that temperature is 215 ℃, carry out rectifying, remove 3 parts of residues, obtain 65 parts of low congealing point biofuel of the present invention in the vacuum residual voltage.
The present invention is based on that rectification process prepares from waste oil-technical indicator of 20# biofuel is following.
1. proportion: (20 ℃) 0.86-0.90
2. flash-point: ℃ 110-150
3. congealing point: ℃≤-20
4. acid number: mg KOH/g≤1
5. ester content: % >=98
6. moisture content: %≤0.1.
Claims (4)
1. from waste oil, prepare-the 20# method of bio-diesel oil based on rectification process, it is characterized in that it chooses waste oil and make main raw material, add methyl alcohol, sulfuric acid catalyst reacts, and processes product through Six Steps, its step is following:
I, technical process
Select materials-hydrolysis-fractionation-esterification-neutralization-dealcoholysis-rectifying-finished product;
II, operation steps
1. choose discarded animal and plant grease and do raw material and clear water input grease adverse current hydrolysis tower, hydrolysis;
2. hydrolysising reacting temperature is 200 ℃-250 ℃, and pressure is 2.5MPa-3.0MPa, and oil is 1:0.4-0.5 with the ratio of water, and the reaction times is 4-8 hour, separates to obtain croude fatty acids and aqueous glycerin solution;
3. get above-mentioned croude fatty acids input separation column and carry out fractionation; Reaction conditions is vacuum residual voltage in the tower body＜2 mmhg; Distillation temperature is 200 ℃-250 ℃, makes the lipid acid fractionation, mixture and sub product palmitinic acid, the Triple Pressed Stearic Acid of oleic acid, linoleic acid plus linolenic acid;
4. get the mixture and the methanol mixed of above-mentioned oleic acid, linoleic acid plus linolenic acid, add sulfuric acid, esterification reaction temperature is 70 ℃-85 ℃, and the reaction times is 4-8 hour, gets carboxylate and water simultaneously;
5. after adding soda ash neutralizes in above-mentioned carboxylate, remove free acid earlier, remove methyl alcohol again, and reclaim methyl alcohol;
6. the carboxylate suction rectifying tower after the above-mentioned dealcoholysis carries out rectifying, and the rectification process condition is vacuum residual voltage in the tower body＜5 mmhg, and temperature of reaction is 200 ℃-230 ℃, removes residue, gets biofuel.
2. according to claim 1ly from waste oil, prepare-the 20# method of bio-diesel oil, it is characterized in that the volume unit that consists of of raw material based on rectification process:
3. according to claim 1ly from waste oil, prepare-the 20# method of bio-diesel oil, it is characterized in that vitriolic concentration is 93%-98% based on rectification process.
4. according to claim 1ly from waste oil, prepare-the 20# method of bio-diesel oil, it is characterized in that step finished product congealing point 6. is not for being higher than-20 ℃ based on rectification process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810143872A CN101440298B (en) | 2008-12-09 | 2008-12-09 | Method for preparing -20 DEC C biodiesel from waste lipid by distillation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810143872A CN101440298B (en) | 2008-12-09 | 2008-12-09 | Method for preparing -20 DEC C biodiesel from waste lipid by distillation process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101440298A CN101440298A (en) | 2009-05-27 |
| CN101440298B true CN101440298B (en) | 2012-09-12 |
Family
ID=40724911
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200810143872A Expired - Fee Related CN101440298B (en) | 2008-12-09 | 2008-12-09 | Method for preparing -20 DEC C biodiesel from waste lipid by distillation process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101440298B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103275809A (en) * | 2013-05-17 | 2013-09-04 | 石家庄市潇洒油脂化工有限公司 | Clean biodiesel for vehicles |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES2369831B1 (en) * | 2010-05-13 | 2012-10-17 | Abengoa Solar New Technologies, S.A. | PLANT FOR THE RECOVERY OF DEGRADED CALOPORTER OIL FROM A THERMAL SOLAR INSTALLATION AND METHOD FOR SUCH RECOVERY. |
| CN102382716A (en) * | 2010-09-03 | 2012-03-21 | 陕西渭力生物能源有限公司 | Method and equipment for preparing biodiesel with high-acid-value waste oil |
| CN102965201B (en) * | 2012-12-12 | 2014-08-06 | 中国科学院长春应用化学研究所 | Preparation method of diesel antiwear agent |
| CN103435468A (en) * | 2013-08-26 | 2013-12-11 | 苏勇 | Method for producing stearic acid by utilizing cottonseed oil soapstock |
| CN104830544B (en) * | 2015-05-21 | 2016-03-30 | 西安中粮工程研究设计院有限公司 | Utilize the method for waste grease co-producing biodiesel and plant sterol |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1557914A (en) * | 2004-02-04 | 2004-12-29 | 罗羽林 | Biological diesel oil and method for preparing same |
| CN1827742A (en) * | 2006-04-06 | 2006-09-06 | 河南省商丘油脂化学厂 | Application of selective hydrolysis process in bio-diesel oil production |
| CN101230288A (en) * | 2007-01-24 | 2008-07-30 | 新疆协力新能源有限责任公司 | Method for producing biological diesel oil |
-
2008
- 2008-12-09 CN CN200810143872A patent/CN101440298B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1557914A (en) * | 2004-02-04 | 2004-12-29 | 罗羽林 | Biological diesel oil and method for preparing same |
| CN1827742A (en) * | 2006-04-06 | 2006-09-06 | 河南省商丘油脂化学厂 | Application of selective hydrolysis process in bio-diesel oil production |
| CN101230288A (en) * | 2007-01-24 | 2008-07-30 | 新疆协力新能源有限责任公司 | Method for producing biological diesel oil |
Non-Patent Citations (2)
| Title |
|---|
| Gerhard Knothe."Dependence of biodiesel fuel propertier on the structure of fatty acid alkyl esters".《Fuel Processing Technology》.2005,(第86期),第1059-1070页. * |
| 陈秀等."脂肪酸甲酯结构对生物柴油十六烷值的影响".《石油与天然气化工》.2007,第36卷(第6期),第481-484页. |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103275809A (en) * | 2013-05-17 | 2013-09-04 | 石家庄市潇洒油脂化工有限公司 | Clean biodiesel for vehicles |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101440298A (en) | 2009-05-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101440298B (en) | Method for preparing -20 DEC C biodiesel from waste lipid by distillation process | |
| CN101541929B (en) | Preparation of fatty acid esters of glycerol formal and use thereof as biofuel | |
| CN100434164C (en) | Catalyst system and biological diesel oil producing process with the catalyst system | |
| CN101195572A (en) | Method for synthesizing fatty acid methyl ester | |
| CN1995288A (en) | Process for preparing biodiesel oil | |
| CN101215233B (en) | Technique for producing fatty acid methyl ester | |
| CN1473907A (en) | Process for producing biological diesel oil | |
| CN101440299B (en) | Method for preparing -10 DEC C biodiesel from waste lipid by distillation process | |
| CN1844319A (en) | Process for preparing bio- diesel oil by conversion of subcritical - supercritical fluid | |
| CN1891786B (en) | Production technology for preparing biodiesel from tallowseed oil | |
| CN101205489A (en) | Fuel oil additive composition, preparation and use thereof | |
| CN102260596B (en) | Method for preparing biodiesel by two-step process | |
| CN102041177B (en) | Method for preparing biodiesel | |
| CN101113361A (en) | Method for producing biodiesel capable of being applied for industrial production | |
| CN102586027A (en) | Continuous production method of biodiesel from waste oil/fat | |
| CN103087788B (en) | Method for preparing biodiesel by using high-acid value oil | |
| CN105194996B (en) | A kind of method of comprehensive utilization of yellow phosphoric tail gas | |
| CN112175744A (en) | Method for preparing biodiesel from high-acid-value kitchen waste grease | |
| CN103436368A (en) | Method for synchronously preparing biodiesel and glycerol carbonate by using alkali-earth oxide as catalyst | |
| CN100526427C (en) | Method and catalyst for producing biological diesel oil by high-acid value grease | |
| CN103045311B (en) | Micro-emulsified diesel oil and preparation method thereof | |
| CN104560411A (en) | Technique for preparing fatty acid methyl ester by biological process | |
| CN102108319B (en) | Continuous system and method for preparing biodiesel | |
| CN201330241Y (en) | Device for producing refined biodiesel with high acid value oil | |
| CN101012392B (en) | Method of removing soap and dissociative glycerin in biological diesel oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120912 Termination date: 20181209 |