CN100503785C - Application of selective hydrolysis process in bio-diesel oil production - Google Patents
Application of selective hydrolysis process in bio-diesel oil production Download PDFInfo
- Publication number
- CN100503785C CN100503785C CNB2006100176339A CN200610017633A CN100503785C CN 100503785 C CN100503785 C CN 100503785C CN B2006100176339 A CNB2006100176339 A CN B2006100176339A CN 200610017633 A CN200610017633 A CN 200610017633A CN 100503785 C CN100503785 C CN 100503785C
- Authority
- CN
- China
- Prior art keywords
- oil
- hydrolysis
- oil plants
- phosphatide
- ester
- 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
Landscapes
- Fats And Perfumes (AREA)
- Liquid Carbonaceous Fuels (AREA)
Abstract
The application of selective hydrolyzation process in the biological fuel-oil production is disclosed, which consists of making the woody plant oil plants and the discarded animal vegetable oil plants first enter into the noncatalytic selective hydrolyzation process to destroy the waxy substance, protein, colloid, and phosphatide contained in the oil plants, and translating the phosphatide into glycerin and aliphatic acid, the hydrolyzed oil plants coming into the presterification process, first changing the produced aliphatic acid into fatty acid formate, then coming into the alcoholysis process. The invention is of simple process and convenient operation, the availability ratio of the fatty oil can reach more than 98.5 % and the yield rate increases by more than 23 %, can largely reduce the cost, and the raw materials adaptability is wide, not only rape oil and soya oil can be used, but also woody plant oil plants and the discarded animal vegetable oil plants can be used.
Description
One, technical field
The present invention relates to a kind of production technique of biofuel.
Two, background technology
Production biofuel in countries in the world mainly is to use chemical method production at present, and main raw material adopts the rapeseed oil and the soybean oil of low condensation point.Promptly use low-carbon alcohol such as these greases and methyl alcohol or ethanol under acid or basic catalyst and high temperature (230-250 ℃), to carry out transesterification, generate corresponding fatty acid methyl ester or fatty-acid ethyl ester, be drying to obtain biofuel through washing again.But Chemical bond becomes biofuel that following shortcoming is arranged: complex process, and alcohol must be excessive, and subsequent technique must have corresponding pure retrieving arrangement, energy consumption height; Because unsaturated fatty acids is at high temperature apt to deteriorate in the fat, color and luster is dark; Esterification products is difficult to reclaim the cost height; Production process has waste lye discharging, contaminate environment.Quite high with rapeseed oil and soybean oil production biofuel cost, according to pertinent data, the U.S., Austria, Brazil, Germany, France etc., the utilization ratio of rapeseed oil is no more than 75%.
In addition, utilize prior art only to be applicable to subzero rapeseed oil, soybean oil, and be the raw material production biofuel with the xylophyta oil plant, must earlier crude oil be carried out alkali refining, remove the objectionable impurities in the crude oil, as wax, colloid, protein and solid impurity etc., acid value of lipids is dropped to below 1, just can carry out ester and become reaction or enzyme transesterification reaction, still with methyl alcohol, the problem that exists is: will discharge a large amount of salt, alkali waste water, contaminate environment in oil and fat refining.If not refining can cause poisoning by enzyme, the enzyme transesterification reaction is difficult to carry out, and adopts ester to hand over reaction exactly, also can reduce greasy utilization ratio greatly; Grease oil in refining is lost in more than 25%, and the grease utilization ratio reduces, and improve yield, must carry out processing and utilizing to refining gained oil foot material, like this since operational path increase, facility investment increases, the production cost rising; If adopt whole hydrolysis process routes, energy consumption raises in the hydrolysis, can only adopt esterification, can not adopt the enzyme transesterification reaction.
Three, summary of the invention
The objective of the invention is and to select hydrolysis process to be applied in the production technique of biofuel, utilize and select hydrolysis process, remove wax in the oil plant, colloid, phosphatide, protein etc., can improve the oil plant utilization ratio greatly.
Implementation procedure of the present invention is such:
Xylophyta oil plant class or waste oils and fats material class are at first selected hydrolysis process by no catalyst, destroy wax, protein, colloid and phosphatide in the oil plant, and make phosphatide be converted into glycerine and lipid acid; Oil plant after the hydrolysis enters pre-esterifying process, changes lipid acid into fatty acid methyl ester earlier, and then enters ester friendship reaction process, becomes crude fatty acid methyl ester after extraction glycerine and the dealcoholysis, promptly gets biofuel through rectification under vacuum.
Positively effect of the present invention is: technology is simple, and is easy to operate, and the grease availability reaches more than 98.5%, and yield improves more than 23%, can reduce production costs greatly; The raw material suitability is wide, not only can use rapeseed oil, soybean oil, can also use xylophyta oil plant (as Chinese tallow tree bark oil, Chinese catalpa oil, Fructus Zanthoxyli oil, palm wet goods) and waste oils and fats material.
Four, description of drawings
Accompanying drawing is a process route chart of the present invention.
Five, embodiment
Xylophyta oil plant or waste oils and fats material are added water in hydrolysis tower, at 190 ℃, 10kg/cm
2Pressure, under the 1200kg/h flow, select hydrolysis, time is 3-4 hours, purpose is the wax of destroying in the oil plant, protein, colloid and phosphatide, and make wax and phosphatide be converted into glycerine and lipid acid, reclaim glycerine, neutral oil after the hydrolysis and partial fatty acid enter the pre-esterification reactor tower after 120 ℃ of normal pressure dehydrations, 125 ℃ methanol steam enters at the bottom of tower, oil plant from cat head drench into, control oil plant flow is 400kg/h, and the methanol steam flow is 300kg/h, reverse contact, make the reaction of lipid acid and methanol vapor generate fatty acid methyl ester, and then enter conventional ester friendship reaction, and become croude fatty acids methyl alcohol after extraction glycerine and the dealcoholysis, promptly get biofuel through rectification under vacuum.
Claims (1)
1, selects the application of hydrolysis process in production of biodiesel, its gordian technique is: at first vegetable oil material or waste oils and fats material are not had catalyst selection hydrolysis, destroy wax, protein, colloid and phosphatide in the oil plant, and make it be converted into glycerine and lipid acid, oil plant after the hydrolysis enters pre-esterifying process, and then entering ester friendship reaction process, no catalyst selects hydrolysis at 190 ℃, 10kg/cm
2Carry out under the flow of pressure, 1200kg/h; Methanol steam with 125 ℃ carries out pre-ester reaction under normal pressure afterwards, and the methanol steam flow is 300kg/h, control oil plant flow 400kg/h; Enter ester then and hand over reaction process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100176339A CN100503785C (en) | 2006-04-06 | 2006-04-06 | Application of selective hydrolysis process in bio-diesel oil production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100176339A CN100503785C (en) | 2006-04-06 | 2006-04-06 | Application of selective hydrolysis process in bio-diesel oil production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1827742A CN1827742A (en) | 2006-09-06 |
| CN100503785C true CN100503785C (en) | 2009-06-24 |
Family
ID=36946298
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100176339A Expired - Fee Related CN100503785C (en) | 2006-04-06 | 2006-04-06 | Application of selective hydrolysis process in bio-diesel oil production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100503785C (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101595203A (en) | 2006-12-01 | 2009-12-02 | 北卡罗来纳州立大学 | The method of conversion of biomass to fuel |
| CN100465249C (en) * | 2006-12-28 | 2009-03-04 | 浙江大学 | Method for preparing biodiesel oil |
| CN101440298B (en) * | 2008-12-09 | 2012-09-12 | 湘潭昭山油化科技有限公司 | Method for preparing -20 DEC C biodiesel from waste lipid by distillation process |
| CN101440299B (en) * | 2008-12-09 | 2012-11-14 | 湘潭昭山油化科技有限公司 | Method for preparing -10 DEC C biodiesel from waste lipid by distillation process |
| 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 |
| CN103254996B (en) * | 2013-05-29 | 2015-09-09 | 深圳市腾浪再生资源发展有限公司 | Waste grease is utilized to adopt gas phase alcoholysis method to manufacture method and the esterification column of biofuel |
| CN104342215A (en) * | 2013-08-05 | 2015-02-11 | 上海顶源石油化工有限公司 | Method for preparing biodiesel with alcoholysis one-step method |
| CN103540414B (en) * | 2013-10-22 | 2016-01-06 | 惠州市神州创宇低碳技术发展有限公司 | The method and apparatus of a kind of palm dregs of fat and acidification oil refining biofuel |
| KR102495262B1 (en) * | 2015-07-27 | 2023-02-03 | 에스케이에코프라임 주식회사 | Method and apparatus for preparing biodiesel from oils containing polar lipids |
-
2006
- 2006-04-06 CN CNB2006100176339A patent/CN100503785C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1827742A (en) | 2006-09-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100503785C (en) | Application of selective hydrolysis process in bio-diesel oil production | |
| Keneni et al. | Oil extraction from plant seeds for biodiesel production | |
| Yaakob et al. | Overview of the production of biodiesel from waste cooking oil | |
| Sulaiman et al. | Reactive extraction of solid coconut waste to produce biodiesel | |
| CN1328353C (en) | Technology of preparing biological diesel oil from animal and vegetable oil | |
| CN100494316C (en) | Process for preparing biological diesel oil using palm oil | |
| Gomes Filho et al. | Biodiesel production from Sterculia striata oil by ethyl transesterification method | |
| CN100569912C (en) | A kind of processing method for preparing biofuel | |
| CN101215233B (en) | Technique for producing fatty acid methyl ester | |
| KR102327852B1 (en) | Method for preparing fatty acid alkyl ester using fat | |
| Qian et al. | Cogeneration of biodiesel and nontoxic rapeseed meal from rapeseed through in-situ alkaline transesterification | |
| Chaker Ncibi et al. | Recent research and developments in biodiesel production from renewable bioresources | |
| Hasan et al. | Prospect of rice bran for biodiesel production in Bangladesh | |
| CN105132192A (en) | Biodiesel preparation method | |
| Echim et al. | Production of biodiesel from side-stream refining products | |
| Ala’a Alsoudy et al. | Influence on process parameters in transesterification of vegetable and waste oil–a review | |
| CN102453613A (en) | Method for producing diesel oil by esterification deacidification of rice bran oil | |
| CN105273851A (en) | Method for preparing fatty acid ester | |
| CN102108319B (en) | Continuous system and method for preparing biodiesel | |
| CN102492561A (en) | Method for preparing bio-diesel by using fresh rice bran | |
| KR102411079B1 (en) | Method for preparing of bio-diesel and fatty acid using microalgae oil | |
| Soulayman et al. | Synthesis Parameters of Biodiesel From Frying Oils Wastes. | |
| CN1974724B (en) | High efficiency preparation process of biological diesel oil | |
| Oniya et al. | Optimization of biodiesel production from milk bush (Thevetia peruviana) oil using snail shell as catalyst | |
| CN101684413A (en) | Method for preparing biodiesel by solvent reinforcement rapid in-situ transesterification |
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 | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090624 Termination date: 20130406 |