CN101386809A - High pressure continuous hydrolysis technology for grease - Google Patents
High pressure continuous hydrolysis technology for grease Download PDFInfo
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- CN101386809A CN101386809A CNA2008101550840A CN200810155084A CN101386809A CN 101386809 A CN101386809 A CN 101386809A CN A2008101550840 A CNA2008101550840 A CN A2008101550840A CN 200810155084 A CN200810155084 A CN 200810155084A CN 101386809 A CN101386809 A CN 101386809A
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Abstract
The invention discloses a grease high-pressure continuous hydrolysis process, wherein raw grease reacts in a reaction tower at certain temperature and pressure and then is subjected to hydrolysis. The grease high-pressure continuous hydrolysis process has the advantages of easy continuous control, stable product quality, capability of reaching the degree of slight colouration or no colouration for the produced fatty acid, high hydrolysis pressure, short production period, high hydrolysis percentage which is generally more than 95 percent, simple and convenient operation, and capability of realizing automatic control and mass production.
Description
Technical field
The present invention relates to a kind of fat hydrolysis and produce lipid acid technology.
Background technology
At present, known fat hydrolyzing process has setting-out solution in normal pressure catalytic hydrolysis method and catalysis or the on-catalytic.
Normal pressure catalytic hydrolysis method is to depress the use an acidic catalyst long, adds the glycerine waste water of fresh water or lower concentration, comes hydrolysate oil with the open steam fractional digestion.The employed catalyzer of this method is sulphur and sulfuric acid normally.The shortcoming of water at atmospheric pressure solution be because the lipid acid color and luster that the sulfation of minute quantity or sulfonation produce hydrolysis is deepened, steam consumption is big, hydrolysis time is long, degree of hydrolysis is low, in the waste water glycerol content low, increased the cost that glycerine reclaims.Contain sulfuric acid and sulfonic acid simultaneously, big to the corrodibility of equipment.
The middle non-catalytic hydrolyzing method of pressing is to rely on certain pressure, temperature, amount of water and the hydrolysis time of control to make grease generation hydrolysis; In press the catalytic hydrolysis method except conditions such as needs possess certain pressure, temperature, amount of water, also needing to add a certain amount of catalyzer increases the solubleness of water in oil phase in the reaction process, improves the speed of reaction, guarantees certain degree of hydrolysis simultaneously.This method production cycle is relatively long, facility investment is big, degree of hydrolysis is relatively low.
Summary of the invention
The invention provides a kind of technology that can realize the hydrolysis of the continuous high pressure adverse current of grease.
In order to solve above technical problem, the processing step of continuous high pressure adverse current of the present invention hydrolysis is as follows:
A, raw material deionized water by high-pressure pump send into descend behind the cat head with the heat exchange of lipid acid liquid phase layer after enter in the tower;
B, raw oil material are pumped at the bottom of the tower in sparger sprays into tower by high pressure charging, in the raw oil material uphill process with hydrolysis after glycerol liquor carry out heat exchange after, enter external phase through water-oil interface;
C, high pressure steam spray into from tower body everywhere by variable valve control, keep the needed pressure and temperature of hydrolysis;
D, the liquid phase water counter current contact generation hydrolysis reflection in tower that is in the liquid phase grease in the uphill process and is in the decline process;
E, tower internal pressure are kept by the load of control lipid acid, and the lipid acid after hydrolysis cat head discharge again enters the flash tank degassing;
Water-oil interface are kept by control sugar water load in the F, tower, and the sugar water after the hydrolysis is discharged at the bottom of by tower and entered the flash tank degassing.
Described raw oil material enters the temperature of charge before the reaction tower: 60-100 ℃.
Described raw oil material and raw water are in the temperature of hydrolysis tower internal reaction: 200-280 ℃
Described in entire reaction course, system pressure is controlled at: 4.0-6.0MPa.
The profit mass ratio of described raw material control is: 1:0.4-0.6.
The advantage of the continuous high pressure adverse current of above-described a kind of grease hydrolysis process is: 1, the technology stepless control is easy, constant product quality, and the lipid acid of output can reach less painted or non-staining degree; 2, hydrolysis pressure height is with short production cycle, heat energy utilization rate height, and steam consumption quantity is few; 3, hydrolysis time is short, and percent hydrolysis height, degree of hydrolysis are easy to reach 98%, usually more than 95%; 4, easy and simple to handle, can realize automatic control; 5, the device turndown ratio is big, can realize scale operation.
Description of drawings
Figure is a technological process block-diagram of the present invention.
Embodiment
Embodiment 1,
As shown in the figure, the raw material deionization is continuously sent in the hydrolysis tower by high-pressure pump, continue to descend after raw water descends with after the heat exchange of lipid acid liquid phase layer, control profit mass ratio is 1:0.4, raw oil material continuously enters in the hydrolysis tower through high-pressure pump, in the raw oil material uphill process with hydrolysis after glycerol liquor carry out heat exchange after, enter external phase through water-oil interface.Air input by variable valve control high pressure steam, make the temperature in the hydrolysis tower be controlled at 200 ℃, pressure-controlling is at 4.8MPa, be in the liquid phase grease and the liquid phase water counter current contact generation hydrolysis reaction in tower that is in the decline process of uphill process, reacted croude fatty acids is discharged by cat head and is entered the flash tank degassing, and sugar water is discharged at the bottom of by tower and entered the flash tank degassing and concentrate.
Embodiment 2,
As shown in the figure, the raw material deionized water is continuously sent in the hydrolysis tower by high-pressure pump, continue to descend after raw water descends with after the heat exchange of lipid acid liquid phase layer, the control water oil ratio is 1:0.5, raw oil material continuously enters in the hydrolysis tower through high-pressure pump, in the raw oil material uphill process with hydrolysis after glycerol liquor carry out heat exchange after, enter external phase through water-oil interface.Air input by variable valve control high pressure steam, make the temperature in the hydrolysis tower be controlled at 260 ℃, pressure-controlling is at 5.0MPa, be in the liquid phase grease and the liquid phase water counter current contact generation hydrolysis reaction in tower that is in the decline process of uphill process, reacted croude fatty acids is discharged by cat head and is entered the flash tank degassing, and sugar water is discharged at the bottom of by tower and entered the flash tank degassing and concentrate.
Claims (5)
1. high pressure continuous hydrolysis technology for grease is characterized in that: be made up of following step:
A. the raw material deionized water by high-pressure pump send into descend behind the cat head with the heat exchange of lipid acid liquid phase layer after enter in the tower;
B. raw oil material is pumped at the bottom of the tower in sparger sprays into tower by high pressure charging, in the raw oil material uphill process with hydrolysis after glycerol liquor carry out heat exchange after, enter external phase through water-oil interface;
C. high pressure steam sprays into from tower body everywhere by variable valve control, keeps the needed pressure and temperature of hydrolysis;
D. be in liquid phase grease and the liquid phase water that is in decline process counter current contact generation hydrolysis reflection in tower in the uphill process;
E. the tower internal pressure is kept by the load of control lipid acid, and the lipid acid after hydrolysis cat head discharge again enters the flash tank degassing;
F. water-oil interface are kept by control sugar water load in the tower, and the sugar water after the hydrolysis is discharged at the bottom of by tower and entered the flash tank degassing.
2. a kind of high pressure continuous hydrolysis technology for grease according to claim 1 is characterized in that: described raw oil material enters the temperature of charge before the reaction tower: 60-100 ℃.
3. a kind of high pressure continuous hydrolysis technology for grease according to claim 1 is characterized in that: described raw oil material and raw water are in the temperature of hydrolysis tower internal reaction: 200-280 ℃.
4. a kind of high pressure continuous hydrolysis technology for grease according to claim 1 is characterized in that: described in entire reaction course, system pressure is controlled at: 4.0-6.0MPa.
5. a kind of high pressure continuous hydrolysis technology for grease according to claim 1 is characterized in that: the profit mass ratio of described raw material control is: 1:0.4-0.6.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008101550840A CN101386809A (en) | 2008-11-03 | 2008-11-03 | High pressure continuous hydrolysis technology for grease |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008101550840A CN101386809A (en) | 2008-11-03 | 2008-11-03 | High pressure continuous hydrolysis technology for grease |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101386809A true CN101386809A (en) | 2009-03-18 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2008101550840A Pending CN101386809A (en) | 2008-11-03 | 2008-11-03 | High pressure continuous hydrolysis technology for grease |
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| CN (1) | CN101386809A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101892126A (en) * | 2010-04-14 | 2010-11-24 | 江苏永林油脂化工有限公司 | Method for continuously hydrolyzing acidated vegetable oil |
| CN101928644A (en) * | 2010-09-07 | 2010-12-29 | 昆明理工大学 | Method for preparing fatty acid by illegal cooking oil |
| CN102510897A (en) * | 2009-08-13 | 2012-06-20 | 科学与工业研究委员会 | Process for producing fatty acids |
| CN104388194A (en) * | 2014-12-03 | 2015-03-04 | 南京大学 | Super-high-efficiency lipid hydrolysis reactor and reaction process |
| CN107354011A (en) * | 2017-08-30 | 2017-11-17 | 浙江嘉化能源化工股份有限公司 | Grease hydrolysis method |
| CN107619721A (en) * | 2017-09-25 | 2018-01-23 | 北京航空航天大学 | A kind of grease purification process and device |
| CN112195068A (en) * | 2020-10-29 | 2021-01-08 | 赞宇科技集团股份有限公司 | Process for producing fatty acid by taking soapstock as raw material and production equipment thereof |
-
2008
- 2008-11-03 CN CNA2008101550840A patent/CN101386809A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102510897A (en) * | 2009-08-13 | 2012-06-20 | 科学与工业研究委员会 | Process for producing fatty acids |
| CN101892126A (en) * | 2010-04-14 | 2010-11-24 | 江苏永林油脂化工有限公司 | Method for continuously hydrolyzing acidated vegetable oil |
| CN101928644A (en) * | 2010-09-07 | 2010-12-29 | 昆明理工大学 | Method for preparing fatty acid by illegal cooking oil |
| CN101928644B (en) * | 2010-09-07 | 2012-08-29 | 昆明理工大学 | Method for preparing fatty acid by illegal cooking oil |
| CN104388194A (en) * | 2014-12-03 | 2015-03-04 | 南京大学 | Super-high-efficiency lipid hydrolysis reactor and reaction process |
| CN104388194B (en) * | 2014-12-03 | 2017-09-12 | 南京大学 | A kind of grease hydrolysis reactor and reaction process |
| CN107354011A (en) * | 2017-08-30 | 2017-11-17 | 浙江嘉化能源化工股份有限公司 | Grease hydrolysis method |
| CN107619721A (en) * | 2017-09-25 | 2018-01-23 | 北京航空航天大学 | A kind of grease purification process and device |
| CN112195068A (en) * | 2020-10-29 | 2021-01-08 | 赞宇科技集团股份有限公司 | Process for producing fatty acid by taking soapstock as raw material and production equipment thereof |
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Open date: 20090318 |