CN204281647U - A kind of esterification device producing fatty acid triglycercide - Google Patents
A kind of esterification device producing fatty acid triglycercide Download PDFInfo
- Publication number
- CN204281647U CN204281647U CN201420736648.0U CN201420736648U CN204281647U CN 204281647 U CN204281647 U CN 204281647U CN 201420736648 U CN201420736648 U CN 201420736648U CN 204281647 U CN204281647 U CN 204281647U
- Authority
- CN
- China
- Prior art keywords
- fatty acid
- esterifying kettle
- lipid acid
- heaters
- acid
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a kind of esterification device producing fatty acid triglycercide.The device that object is to provide should have the feature that reaction efficiency is high, the reaction times is short, can produce high-content fatty acid triglycercide, and simple and stable structure, safe and reliable, failure rate is low, easy to operate.Technical scheme is: a kind of esterification device producing fatty acid triglycercide, comprises esterifying kettle; This reaction unit also comprises pre-mixing still, lipid acid pre-heaters; Pre-mixing still is communicated with catalyst feeds and glycerine feed mouth, and the outlet of pre-mixing still is by the spraying gun of pipeline communication esterifying kettle inner chamber; The intracavity bottom of esterifying kettle is provided with bubbling air sifter, and described lipid acid pre-heaters is communicated with fatty acid feedstock mouth, and the bubbling air sifter described in pipeline communication is also passed through in the outlet of lipid acid pre-heaters, to input the fatty acid ester of gasification; Lipid acid water cooler and vacuum unit interface are also sequentially connected by pipeline in esterifying kettle top, and the bottom of esterifying kettle also makes a discharge port.
Description
Technical field
The utility model relates to a kind of oil and fat chemical equipment, particularly a kind of esterification device producing fatty acid triglycercide.
Technical background
The esterification of lipid acid and glycerine is reacted for the production of classics that are edible, technical oils.Namely lipid acid and glycerine reaction generate mono-glycerides, and mono-glycerides and fatty acid response form two sweet esters, and two sweet esters react with mono-glycerides and form triglyceride level; As shown in the formula expression:
Traditional esterification device is stirring-type reactor, reactive mode also more is confined to liquid-liquid reaction, its ubiquitous problem is: reaction esterification is incomplete, mono-glycerides in product, two sweet ester contents are higher, traditional method is adopted to be difficult to directly obtain highly purified fatty acid triglycercide, high-purity fatty acid triglycercide of in the market more than 99% is many purifies through other means such as molecular distillations, not only complex process, and cost is higher.
Utility model content
The purpose of this utility model is the deficiency overcoming above-mentioned background technology, a kind of esterification device producing fatty acid triglycercide is provided, this device should have the feature that reaction efficiency is high, the reaction times is short, can produce high-content fatty acid triglycercide, and simple and stable structure, safe and reliable, failure rate is low, easy to operate.
The technical scheme that the utility model provides is:
Produce an esterification device for fatty acid triglycercide, comprise esterifying kettle; It is characterized in that this reaction unit also comprises pre-mixing still, lipid acid pre-heaters; Described pre-mixing still is communicated with catalyst feeds and glycerine feed mouth, the outlet of pre-mixing still by the spraying gun of pipeline communication esterifying kettle inner chamber, to input catalyzer and the glycerine of mist; The intracavity bottom of described esterifying kettle is provided with bubbling air sifter, and described lipid acid pre-heaters is communicated with fatty acid feedstock mouth, and the bubbling air sifter described in pipeline communication is also passed through in the outlet of lipid acid pre-heaters, to input the fatty acid ester of gasification; Lipid acid water cooler and vacuum unit interface are also sequentially connected by pipeline in esterifying kettle top, and the bottom of esterifying kettle also makes a discharge port.
The cavity arrangements of described esterifying kettle has some amount sieve plate.
Principle of work of the present utility model is: due to short chain fatty acid, medium chain fatty acid and middle longer chain fatty acid boiling point lower (boiling point≤300 DEG C), thus can realize heat up gasification lipid acid and glycerine carry out gas-liquid two phase reaction.For this reason, kettle is sprayed into after first catalyzer and glycerine premixed gas being atomized, directly react with the lipid acid gas in still, the glyceryl ester formed and unreacted glycerine flow at the bottom of still by sieve plate, also secondary esterification can be carried out with the lipid acid of gasification in way, the sustainable bubbling of bubbling air sifter of bottom of device, sinks to material at the bottom of still and lipid acid bubble carries out third time esterification, greatly can improve speed of reaction and product yield.
The utility model beneficial effect is:
(1) compared with traditional esterifications reactor, gas liquid reaction efficiency is high, and the reaction times is short, is conducive to the fatty acid triglycercide producing high-content (content is greater than 99%);
(2) device adopts atomized feed, and increases sieve plate in still, and bottom bubbling greatly can improve reaction efficiency, complete assembly simple and stable, safe and reliable, failure rate is low, and easy to operate, easy for installation, cost is low, and the material be suitable for is in extensive range.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Number in the figure: 1-catalyst feeds; 2-glycerine feed mouth; 3-fatty acid feedstock mouth; 4-pre-mixing still; 5-esterifying kettle; 6-spraying gun; 7-sieve plate; 8-bubbling air sifter; 9-lipid acid pre-heaters; 10-lipid acid water cooler; 11-discharge port, 12-vacuum unit interface.
Embodiment
The single chain fatty acid of the many fingers of lipid acid in triglyceride level, compared to other lipid acid, its boiling point is lower, and when lipid acid saturation ratio is certain, its boiling point reduces gradually along with the reduction of carbon chain lengths, particularly short chain fatty acid is (as formic acid, acetic acid, propionic acid, butyric acid, acid), medium chain fatty acid is (as sad, capric acid) and the lipid acid (as lauric acid) of middle Long carbon chain, such lipid acid boiling point is many below 300 DEG C (table 1), and esterification reaction temperature mostly is 200-300 DEG C, therefore, adopt the esterification technology of lipid acid (gas phase) and glycerine (liquid phase), by improving esterification device, the efficiency of esterification can be improved, obtain highly purified triglyceride level.
The different lipid acid of table 1 and boiling point thereof
The esterification device of the production fatty acid triglycercide that the utility model provides, comprises esterifying kettle 5, pre-mixing still 4, lipid acid pre-heaters 9.The catalyzer of input and glycerine are mixed by pipeline communication catalyst feeds 1 and glycerine feed mouth 2 by described pre-mixing still, then input esterifying kettle after exporting, and by spraying gun 6 (i.e. shower nozzle), catalyzer and glycerol mixture are sprayed with mist at esterifying kettle inner chamber.And described lipid acid pre-heaters is communicated with fatty acid feedstock mouth 3, after the lipid acid of input is heated into gaseous state, inputs esterifying kettle by the bubbling air sifter 8 of the intracavity bottom of esterifying kettle, the lipid acid of gaseous state and the catalyzer of mist and glycerine are reacted; Lipid acid water cooler and vacuum unit interface are also sequentially connected by pipeline in esterifying kettle top, controlled the temperature of reaction (temperature rise that inhibited reaction produces) of esterifying kettle inner chamber by lipid acid water cooler (conventional freezing machinery), and controlled the vacuum pressure of esterifying kettle inner chamber by vacuum unit (conventional air extractor).Liquid glycerin three ester that reaction generates then is exported by the discharge port of esterifying kettle bottom.
As recommendation, the inner chamber of described esterifying kettle is also furnished with the sieve plate 7 of some amount (being generally 5-15 sheet).Sieve plate is arranged and is recommended to adopt conventional arranged crosswise mode.
The equal buyable of pre-mixing still described in the utility model, esterifying kettle, sieve plate and bubbling air sifter obtains.
Embodiment 1
Acetic acid (boiling point 117 DEG C) mixing acid is entered esterifying kettle from bottom after the gasification of lipid acid pre-heaters, acetic acid gas is made to be full of still chamber, temperature in the kettle controls at 150 DEG C, after then catalyzer and glycerine being stirred 30min in pre-mixing still, is gone out from still top spray by spraying gun, react with the acetic acid gas in still, reaction times 40min, continues logical acetic acid gas, after reaction terminates in reaction process, stop logical acetic acid gas, reactant is by discharge hole for discharge.Product after esterification is colourless transparent oil liquid, and acid number (mg KOH/g) is 0.09, nitrilotriacetic content of triglyceride 99.5%.
Embodiment 2
By sad, capric acid mixing acid (sad boiling point 238 DEG C, capric acid boiling point 270 DEG C) after the gasification of lipid acid pre-heaters, enter esterifying kettle from bottom, mixing acid gas is made to be full of still chamber, temperature in the kettle controls at 275-280 DEG C, then after catalyzer and glycerine being stirred 30min in pre-mixing still, gone out from still top spray by spraying gun, react with the mixing acid gas in still, reaction times 1h, logical mixing acid gas is continued in reaction process, ensure the acid amount of skipping over, after reaction terminates, stop logical mixing acid gas, continue reaction 1h, reactant is by discharge hole for discharge.Product after esterification is in colourless transparent oil liquid after refining, and acid number (mg KOH/g) is 0.06, pungent Triglyceride DDD content 99.2%.
Embodiment 3
Lauric acid (boiling point 299 DEG C) mixing acid is entered esterifying kettle from bottom after the gasification of lipid acid pre-heaters, and make lauric acid gas be full of still chamber, temperature in the kettle controls at 300 DEG C, and vacuum interface connects vacuum unit, ensures controlled underbalance in still.After catalyzer and glycerine are stirred 30min in pre-mixing still, gone out from still top spray by spraying gun, react with the lauric acid gas in still, reaction times 1h, continue logical lauric acid gas in reaction process, after reaction terminates, stop logical lauric acid gas, continue reaction 1h, reactant is by discharge hole for discharge.Product after esterification is in white solid after refining cooling, and acid number (mg KOH/g) is 0.08, lauric acid three ester content 98.6%.
Claims (2)
1. produce an esterification device for fatty acid triglycercide, comprise esterifying kettle (5); It is characterized in that this reaction unit also comprises pre-mixing still (4), lipid acid pre-heaters (9); Described pre-mixing still is communicated with catalyst feeds (1) and glycerine feed mouth (2), the outlet of pre-mixing still by the spraying gun (6) of pipeline communication esterifying kettle inner chamber, to input catalyzer and the glycerine of mist; The intracavity bottom of described esterifying kettle is provided with bubbling air sifter (8), described lipid acid pre-heaters is communicated with fatty acid feedstock mouth (3), the bubbling air sifter described in pipeline communication is also passed through in the outlet of lipid acid pre-heaters, to input the fatty acid ester of gasification; Lipid acid water cooler (10) and vacuum unit interface (12) are also sequentially connected by pipeline in esterifying kettle top, and the bottom of esterifying kettle also makes a discharge port.
2. the esterification device of production fatty acid triglycercide according to claim 1, is characterized in that the cavity arrangements of described esterifying kettle has the sieve plate (7) of some amount.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420736648.0U CN204281647U (en) | 2014-11-28 | 2014-11-28 | A kind of esterification device producing fatty acid triglycercide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420736648.0U CN204281647U (en) | 2014-11-28 | 2014-11-28 | A kind of esterification device producing fatty acid triglycercide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204281647U true CN204281647U (en) | 2015-04-22 |
Family
ID=52864830
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420736648.0U Expired - Fee Related CN204281647U (en) | 2014-11-28 | 2014-11-28 | A kind of esterification device producing fatty acid triglycercide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204281647U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104496802A (en) * | 2014-11-28 | 2015-04-08 | 浙江赞宇科技股份有限公司 | Esterification reaction method and device for production of fatty acid triglyceride |
-
2014
- 2014-11-28 CN CN201420736648.0U patent/CN204281647U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104496802A (en) * | 2014-11-28 | 2015-04-08 | 浙江赞宇科技股份有限公司 | Esterification reaction method and device for production of fatty acid triglyceride |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| NZ543299A (en) | Transesterification method of preparing biodiesel from vegetable oil and meat fat | |
| US20090043118A1 (en) | Apparatus and method for producing biodiesel from fatty acid feedstock | |
| CN104370740B (en) | Compounding acetic isoborneol ester production method | |
| CN104152275B (en) | A kind of gas-phase methanol esterification device | |
| CN100590176C (en) | Ester interchange method for producing bio-diesel oil | |
| CN204281647U (en) | A kind of esterification device producing fatty acid triglycercide | |
| CN104496802B (en) | A kind of esterifying reaction method and esterification device of producing fatty acid triglycercide | |
| CN102586027A (en) | Continuous production method of biodiesel from waste oil/fat | |
| CN101337864B (en) | Method for preparing ethylene glycol mono-n-butyl ether by continuous pipe reaction | |
| CN203609904U (en) | Distillation system for triethylaluminium crude product | |
| CN108586252A (en) | A kind of efficient esterification process of trioctyl trimellitate (TOTM) | |
| CN201701927U (en) | Fatty acid methyl ester esterification reaction kettle | |
| CN1952048B (en) | Production process of biological diesel oil | |
| CN205731217U (en) | A kind of high-efficiency acetic acid ethyl ester reactor | |
| CN204342761U (en) | A kind of device realizing continuous prodution triglyceride level | |
| CN106632161A (en) | Method used for preparing gamma-valerolactone via high-selectivity catalysis | |
| CN202387467U (en) | Multi-effect mixing reactor | |
| CN201272776Y (en) | Apparatus for continuous preparation of biodiesel by neutral grease | |
| CN204816455U (en) | A device for making plasticizer DOTP | |
| CN104120039A (en) | Method for preparing fatty acid methyl ester through multi-stage ester exchange | |
| CN203448075U (en) | Gas-liquid double-circulation reaction device for preparing glyoxylic acid by utilizing air oxidation method | |
| TWI485242B (en) | Manufacturing method of biodiesel | |
| CN209872895U (en) | Deacidification deodorizing device for vegetable oil production and processing | |
| CN202044938U (en) | Fire retardant transfer system | |
| CN203209050U (en) | Reaction and separation integrated cracker |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: Hangzhou City, Zhejiang province 310009 City Shangcheng District No. 128 Lane Patentee after: Praise Technology Group Limited by Share Ltd Patentee after: Hangzhou Oil and Fat Chemical Co., Ltd. Address before: Hangzhou City, Zhejiang province 310009 City Shangcheng District No. 128 Lane Patentee before: Zhejiang Zanyu Technology Co., Ltd. Patentee before: Hangzhou Oil and Fat Chemical Co., Ltd. |
|
| 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: 20150422 Termination date: 20181128 |