CN101928644B - Method for preparing fatty acid by illegal cooking oil - Google Patents
Method for preparing fatty acid by illegal cooking oil Download PDFInfo
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- CN101928644B CN101928644B CN2010102737847A CN201010273784A CN101928644B CN 101928644 B CN101928644 B CN 101928644B CN 2010102737847 A CN2010102737847 A CN 2010102737847A CN 201010273784 A CN201010273784 A CN 201010273784A CN 101928644 B CN101928644 B CN 101928644B
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- Prior art keywords
- water
- fatty acid
- pressure
- raw glycerine
- temperature
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- 235000014113 dietary fatty acids Nutrition 0.000 title claims abstract description 19
- 229930195729 fatty acid Natural products 0.000 title claims abstract description 19
- 239000000194 fatty acid Substances 0.000 title claims abstract description 19
- 150000004665 fatty acids Chemical class 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims abstract description 16
- 239000008162 cooking oil Substances 0.000 title abstract description 5
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims abstract description 79
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- 235000011187 glycerol Nutrition 0.000 claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 22
- 230000007062 hydrolysis Effects 0.000 claims abstract description 18
- 239000002253 acid Substances 0.000 claims description 29
- 150000002632 lipids Chemical class 0.000 claims description 26
- 239000004519 grease Substances 0.000 claims description 19
- 230000003301 hydrolyzing effect Effects 0.000 claims description 19
- 238000000926 separation method Methods 0.000 claims description 11
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 238000001704 evaporation Methods 0.000 claims description 5
- 239000003921 oil Substances 0.000 abstract description 23
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 230000009286 beneficial effect Effects 0.000 abstract 1
- 101100298225 Caenorhabditis elegans pot-2 gene Proteins 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000003814 drug Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 102000004882 Lipase Human genes 0.000 description 1
- 108090001060 Lipase Proteins 0.000 description 1
- 239000004367 Lipase Substances 0.000 description 1
- 238000005903 acid hydrolysis reaction Methods 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000008157 edible vegetable oil Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 235000019421 lipase Nutrition 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000009941 weaving Methods 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Fats And Perfumes (AREA)
Abstract
The invention provides a method for preparing fatty acid by illegal cooking oil. Water is sent into a steam generator, the temperature is controlled to be 100-110 DEG C, pressure is controlled to be 0.10-0.15MPa, so that the water is evaporated into steam; illegal cooking oil is sent into a hydrolysis kettle, the temperature is controlled to be 200-250 DEG C, and the pressure is controlled to be 0.09-0.12MPa; and the steam is sent into the hydrolysis kettle at the flow of 200-250m3/h, and the illegal cooking oil and the steam are subjected to a hydrolysis reaction under high temperature condition, thus obtaining fatty acid, crude glycerine, oil and water. Water and oil are all returned to be recycled, not only no pollute is discharged, but also cost is saved, water resource consumption is reduced, the entire process is continuous, reaction velocity is high, flow is short, equipment is simple, investment cost is low, production process is clean, and the method is beneficial to environmental protection.
Description
Technical field
The present invention relates to a kind of preparation method of lipid acid, particularly a kind ofly prepare the method for lipid acid, belong to the oil chemical technology field with sewer oil.
Background technology
Lipid acid is important chemical material, can be widely used in tensio-active agent, makeup, articles for washing, agrochemicals, medicine and other industrial chemicals.At present, lipid acid is mainly derived from natural fats and oils, and methods such as acid hydrolysis, basic hydrolysis, pyrohydrolysis and lipase hydrolysis are arranged in industry.Along with the widespread use of lipid acid at industrial trades such as food, medicine, weaving, daily-use chemical industry and plastics, lipid acid demonstrates huge development potentiality.Utilize sewer oil to produce lipid acid, not only can turn waste into wealth, can also find a way out, avoid flowing into edible oil market and be detrimental to health, also avoid flowing directly into the water drain contaminate environment for waste cooking oil.
Summary of the invention
Do not use sewer oil to produce the problem of lipid acid in the prior art as yet for solving, the object of the present invention is to provide a kind of method for preparing lipid acid with sewer oil.
The present invention realizes through following technical proposal: a kind of sewer oil prepares the method for lipid acid, it is characterized in that comprising the following steps:
A, Jiang Shui send in the vapour generator, and the temperature of control vapour generator is that 100～110 ℃, pressure are 0.10～0.15MPa, makes water evaporating into water vapor;
B, sewer oil is sent in the hydrolytic reaction pot, the control hydrolysis temperature of reaction kettle is that 200～250 ℃, pressure are 0.09～0.12MPa;
C, with the water vapor of A step with 200～250m
3The flow of/h is sent in the hydrolytic reaction pot of B step, make sewer oil under hot conditions with the water vapor hydrolytic reactions, hydrolysis obtains lipid acid and raw glycerine and grease;
D, C step gained lipid acid get in the condensing surface with water vapor, after conventional condensation, get in the fatty acid separation device again, and control fatty acid separation actuator temperature is that 50～80 ℃, pressure are 0.09～0.11MPa, separate fatty acid product and water;
E, the isolating water of D step is returned in the vapour generator of A step, realize the recycle of water;
F, C step gained raw glycerine and grease get in the raw glycerine separator, and control raw glycerine separator temperature is that 50～80 ℃, pressure are 0.09～0.12MPa, separate raw glycerine sub product and grease;
G, F step be grease obtained to be returned in the hydrolytic reaction pot of B step, carries out the next round hydrolysis.
Said F step gained raw glycerine gets the high purity glycerol product after routine is refining.
Advantage of the present invention and positively effect: adopt such scheme, but the continuous hydrolysis sewer oil makes it to become the lipid acid major product, obtains the raw glycerine sub product simultaneously; After conventional making with extra care, promptly get the high purity glycerol product again, and the isolating water of hydrolysis returns in the vapour generator, realizes the recycle of water, grease then returns in the hydrolytic reaction pot; Together carry out the hydrolysis of next round with initiate sewer oil, whole technology is the process of a connection, has not only improved hydrolysis reaction, realizes quick hydrolysis; And the water after separating and grease all return and recycle, and neither the outside any pollutent of discharging can be practiced thrift cost again, reduces water resources consumption; Flow process of the present invention is short, and equipment is simple, and cost of investment is low; The production process cleaning helps environmental protection, and efficient is high.
Description of drawings
Fig. 1 is the used device synoptic diagram of the inventive method.
Among the figure, 1 is the raw glycerine separator, and 2 is hydrolytic reaction pot, and 3 is vapour generator, and 4 is the fatty acid separation device, and 5 is condensing surface.
Embodiment
Below in conjunction with embodiment the present invention is done and to further describe.
The method of utilizing sewer oil to prepare lipid acid is:
A, Jiang Shui send in the vapour generator, and the temperature of control vapour generator is that 110 ℃, pressure are 0.10MPa, makes water evaporating into water vapor;
B. be that the sewer oil of 161mgKOH/g is sent in the hydrolytic reaction pot with acid number, the control hydrolysis temperature of reaction kettle is 200 ℃, and pressure is 0.10MPa;
C, with the water vapor of A step with 250m
3The flow of/h is sent in the hydrolytic reaction pot of B step, make sewer oil under hot conditions with the water vapor hydrolytic reactions, hydrolysis obtains lipid acid and raw glycerine and grease;
D, C step gained lipid acid get in the condensing surface with water vapor, after conventional condensation, get in the fatty acid separation device again, and control fatty acid separation actuator temperature is that 50 ℃, pressure are 0.11MPa, separate fatty acid product and water;
E, the isolating water of D step is returned in the vapour generator of A step, realize the recycle of water;
F, C step gained raw glycerine and grease get in the raw glycerine separator, and control raw glycerine separator temperature is that 80 ℃, pressure are 0.09MPa, separate raw glycerine sub product and grease, raw glycerine after routine is refining, the high purity glycerol product.
The method of utilizing sewer oil to prepare lipid acid is:
A, Jiang Shui send in the vapour generator 3, and the temperature of control vapour generator 3 is that 105 ℃, pressure are 0.12MPa, makes water evaporating into water vapor;
B. be that the sewer oil of 163mgKOH/g is sent in the hydrolytic reaction pot 2 with acid number, the temperature of control hydrolysis reaction kettle 2 is 250 ℃, and pressure is 0.12MPa;
C, with the water vapor of A step with 200m
3The flow of/h is sent in the hydrolytic reaction pot 2 of B step, make sewer oil under hot conditions with the water vapor hydrolytic reactions, hydrolysis obtains lipid acid and raw glycerine and grease;
D, C step gained lipid acid get in the condensing surface 5 with water vapor, after conventional condensation, get in the fatty acid separation device 4 again, and the temperature of control fatty acid separation device 4 is that 50 ℃, pressure are 0.09MPa, separate fatty acid product and water;
E, the isolating water of D step is returned in the vapour generator 3 of A step, realize the recycle of water;
F, C step gained raw glycerine and grease get in the raw glycerine separator 1, and the temperature of control raw glycerine separator 1 is that 65 ℃, pressure are 0.10MPa, separate raw glycerine sub product and grease, raw glycerine after routine is refining, the high purity glycerol product.
The method of utilizing sewer oil to prepare lipid acid is:
A, Jiang Shui send in the vapour generator 3, and the temperature of control vapour generator 3 is that 100 ℃, pressure are 0.15MPa, makes water evaporating into water vapor;
B. be that the sewer oil of 162mgKOH/g is sent in the hydrolytic reaction pot 2 with acid number, the temperature of control hydrolysis reaction kettle 2 is 230 ℃, and pressure is 0.09MPa;
C, with the water vapor of A step with 225m
3The flow of/h is sent in the hydrolytic reaction pot 2 of B step, make sewer oil under hot conditions with the water vapor hydrolytic reactions, hydrolysis obtains lipid acid and raw glycerine and grease;
D, C step gained lipid acid get in the condensing surface 5 with water vapor, after conventional condensation, get in the fatty acid separation device 4 again, and the temperature of control fatty acid separation device 4 is that 80 ℃, pressure are 0.10MPa, separate fatty acid product and water;
E, the isolating water of D step is returned in the vapour generator 3 of A step, realize the recycle of water;
F, C step gained raw glycerine and grease get in the raw glycerine separator 1, and the temperature of control raw glycerine separator 1 is that 80 ℃, pressure are 0.12MPa, separate raw glycerine sub product and grease, raw glycerine after routine is refining, the high purity glycerol product.
Claims (1)
1. a sewer oil prepares the method for lipid acid, it is characterized in that comprising the following steps:
A, Jiang Shui send in the vapour generator, and the temperature of control vapour generator is that 100～110 ℃, pressure are 0.10～0.15MPa, makes water evaporating into water vapor;
B, sewer oil is sent in the hydrolytic reaction pot, the control hydrolysis temperature of reaction kettle is that 200～250 ℃, pressure are 0.09～0.12MPa;
C, with the water vapor of A step with 200～250m
3The flow of/h is sent in the hydrolytic reaction pot of B step, make sewer oil under hot conditions with the water vapor hydrolytic reactions, hydrolysis obtains lipid acid and raw glycerine and grease;
D, C step gained lipid acid get in the condensing surface with water vapor, after conventional condensation, get in the fatty acid separation device again, and control fatty acid separation actuator temperature is that 50～80 ℃, pressure are 0.09～0.11MPa, separate fatty acid product and water;
E, the isolating water of D step is returned in the vapour generator of A step, realize the recycle of water;
F, C step gained raw glycerine and grease get in the raw glycerine separator, and control raw glycerine separator temperature is that 50～80 ℃, pressure are 0.09～0.12MPa, separate raw glycerine sub product and grease;
G, F step be grease obtained to be returned in the hydrolytic reaction pot of B step, carries out the next round hydrolysis.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102737847A CN101928644B (en) | 2010-09-07 | 2010-09-07 | Method for preparing fatty acid by illegal cooking oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102737847A CN101928644B (en) | 2010-09-07 | 2010-09-07 | Method for preparing fatty acid by illegal cooking oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101928644A CN101928644A (en) | 2010-12-29 |
| CN101928644B true CN101928644B (en) | 2012-08-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102737847A Expired - Fee Related CN101928644B (en) | 2010-09-07 | 2010-09-07 | Method for preparing fatty acid by illegal cooking oil |
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Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102787020B (en) * | 2012-07-17 | 2014-12-17 | 诸暨兴绿油脂有限公司 | Process for producing fatty acid special for rubber emulsification with hogwash oil as raw material |
| CN103172851A (en) * | 2013-03-21 | 2013-06-26 | 安徽理工大学 | Method for preparing polyglycerol fatty acid ester with illegal cooking oil |
| CN104304731A (en) * | 2014-09-24 | 2015-01-28 | 合肥市好旺养殖科技有限公司 | Shrimp feed |
| CN104673352B (en) * | 2015-01-30 | 2016-09-14 | 浙江大学 | A kind of method preparing long chain alkane for raw material low hydrogen consumption with waste oil |
| CN105061233B (en) * | 2015-08-11 | 2017-03-01 | 西京学院 | The preparation method of the twin waste oil cationic surfactant of paper softener |
| CN105255594A (en) * | 2015-10-30 | 2016-01-20 | 杭州油脂化工有限公司 | Grease high-pressure hydrolysis production method and production device by recycling sweet water |
| CN105670800A (en) * | 2016-04-05 | 2016-06-15 | 浙江宇翔生物科技有限公司 | Method for preparing fatty acid by utilizing illegal cooking oil |
| CN106520381A (en) * | 2016-11-11 | 2017-03-22 | 云南磷化集团有限公司 | Decoloration and deodorization method for drainage oil fatty acid |
| CN107698186B (en) * | 2017-07-06 | 2020-05-12 | 清华大学 | Preparation method and application of modified illegal cooking oil for preparing grinding aid |
| CN107446707B (en) * | 2017-09-22 | 2021-05-04 | 山东理工大学 | Process for preparing fatty acid by membrane separation reinforced lard normal pressure hydrolysis reaction |
| CN109897731A (en) * | 2019-04-10 | 2019-06-18 | 淮南泉润环保科技有限公司 | A method of utilizing preparing fatty acid by illegal cooking oil |
| CN112980590A (en) * | 2020-12-31 | 2021-06-18 | 汕头市楷洽化工有限公司 | Hydrolysis distillation process for fatty acid production |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1687342A (en) * | 2005-05-16 | 2005-10-26 | 浙江大学 | Method for preparing fatty acid through continuous hydrolyzing grease without catalysis in near critical aqueous medium |
| CN1844319A (en) * | 2006-05-10 | 2006-10-11 | 昆明理工大学 | Process for preparing bio- diesel oil by conversion of subcritical - supercritical fluid |
| CN101386809A (en) * | 2008-11-03 | 2009-03-18 | 如皋市双马化工有限公司 | High pressure continuous hydrolysis technology for grease |
-
2010
- 2010-09-07 CN CN2010102737847A patent/CN101928644B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1687342A (en) * | 2005-05-16 | 2005-10-26 | 浙江大学 | Method for preparing fatty acid through continuous hydrolyzing grease without catalysis in near critical aqueous medium |
| CN1844319A (en) * | 2006-05-10 | 2006-10-11 | 昆明理工大学 | Process for preparing bio- diesel oil by conversion of subcritical - supercritical fluid |
| CN101386809A (en) * | 2008-11-03 | 2009-03-18 | 如皋市双马化工有限公司 | High pressure continuous hydrolysis technology for grease |
Non-Patent Citations (2)
| Title |
|---|
| 余灯华.高酸值废油脂制备生物柴油工艺研究进展.《现代化工》.2007,第27卷(第S2期),117-120. * |
| 张勇.利用地沟油制备生物柴油.《中国油脂》.2008,第33卷(第11期),48-50. * |
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| CN101928644A (en) | 2010-12-29 |
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