CN107032984A - A kind of method that continuous catalyzing rectifying prepares ethyl lactate - Google Patents
A kind of method that continuous catalyzing rectifying prepares ethyl lactate Download PDFInfo
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- CN107032984A CN107032984A CN201610074788.XA CN201610074788A CN107032984A CN 107032984 A CN107032984 A CN 107032984A CN 201610074788 A CN201610074788 A CN 201610074788A CN 107032984 A CN107032984 A CN 107032984A
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- lactic acid
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C67/54—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention discloses a kind of method that continuous catalyzing rectifying prepares ethyl lactate, under the premise of esterification yield is ensured, esterification rate and continuous production, automation are improved, production cost is reduced.Comprise the following steps：（1）React workshop section：In the fixed bed reactors for loading acid cation exchange resin catalyst, by ethanol（Mass concentration 95%）And lactic acid（Mass concentration 95%）, fixed bed reactors lactonization reaction is sent into, ethyl lactate crude product is obtained.（2）Centrifugal station：Ethyl lactate crude product is subjected to rectifying separation, crude tower, ethanol tower, lactic acid tower and ethyl lactate tower is sequentially entered, obtains food grade lactic acid ethyl ester.Compared with existing production method, had the following advantages that using the method for the present invention：（1）Esterification rate is fast, and esterification time was at 3 ~ 5 hours；（2）Product yield is high, and product single yield is 60 ~ 80%；（3）Environmental protection；（4）Energy-conservation, saves steam energy consumption；（5）It is simple to operate.
Description
Technical field
The present invention relates to a kind of method that continuous catalyzing rectifying prepares ethyl lactate, belong to food and chemical field.
Background technology
The also known as ethyl α-hydroxypropionate of ethyl lactate, molecular formula is C5H10O3, -26 DEG C of fusing point, 154.5 DEG C of boiling point, dissolves each other and partial hydrolysis, is soluble in alcohol, ether, ketone and based organic solvent completely with water, with nontoxic and biodegradable performance, multicolored transparency liquid with aroma fragrance, is a kind of important flavorant, for food service industry drinks and the additive of essence；Lubricant and plasticizer in pharmaceuticals industry are alternatively arranged as, is a kind of green solvent that is new, meeting environmental requirement.
The compound probability of ethyl lactate typically uses batch esterification method, under concentrated sulfuric acid catalyst effect esterification occurs for lactic acid and ethanol, then using benzene or toluene as water entrainer, the water generated in elimination reaction system to balance positive movement, ethyl lactate crude product is obtained, then food grade products are obtained by interval vacuum distillation.This technique is poisonous because of water liquid benzene or toluene, the ethyl lactate of generation containing these materials often because limiting it as the purposes of green solvent, and the concentrated sulfuric acid can promote lactic acid to occur the side reactions such as intermolecular and intramolecular dehydration, condensation reaction and cyclization, so that ethyl lactate product color is bad, low yield.
Absolute ethyl alcohol of the document of Application No. 93118797.4 using purity as 99.1 ~ 99.6% is dehydrating agent, the water abjection that reaction system is generated, the light ethanol of tower top produces destilling tower in the azeotropic mixture form of second alcohol and water, obtain food grade lactic acid ethyl ester yield and reach 97.2%, it improves the yield of ethyl lactate, relatively industrial ethyl lactate yield 65 ~ 80% improves 20 ~ 30% at present.But use absolute ethyl alcohol to be water entrainer, the cost of raw material is added, and in these alcohol of recovered overhead so that running cost increase is a lot, therefore causes ethyl lactate cost to remain high, and is unfavorable for large-scale industrialization promotion.
The content of the invention
It is an object of the invention to provide a kind of method that continuous catalyzing rectifying prepares ethyl lactate, consider from industrialization angle, under the premise of esterification yield is ensured, improve esterification rate and equipment continuous production, automation, reduce production cost.
To achieve the above object, technical scheme of the invention comprises the following steps：（1）React workshop section：In the fixed bed reactors for loading acid cation exchange resin catalyst, by ethanol（Mass concentration 95%）And lactic acid（Mass concentration 95%）, catalytic esterification in fixed bed reactors is entered by raw material pump, ethyl lactate crude product is obtained；（2）Centrifugal station：Ethyl lactate crude product is subjected to rectifying separation, crude tower, ethanol tower, lactic acid tower and ethyl lactate tower is sequentially entered, obtains food grade lactic acid ethyl ester.
Described ethanol and the mol ratio of lactic acid are 2:1~4:1.
Described fixed bed reactors, 70 ~ 90 DEG C of reaction temperature, 0.1 ~ 0.3Mpa of reaction pressure, 3 ~ 5h-1 of air speed.
The operating pressure of described crude tower is normal pressure, and the optimum temperature of tower reactor reboiler is 120 ~ 140 DEG C, and the optimum temperature of overhead condenser is 80 ~ 95 DEG C, and reflux ratio is 0.2 ~ 0.5, and theoretical cam curve is 30 ~ 40.
The operating pressure of described ethanol tower is normal pressure, and the optimum temperature of tower reactor reboiler is 90 ~ 110 DEG C, and the optimum temperature of overhead condenser is 75 ~ 80 DEG C, and reflux ratio is 2 ~ 5, and theoretical cam curve is 35 ~ 45.
The operating pressure of described lactic acid tower is 5 ~ 10kpa, and the optimum temperature of tower reactor reboiler is 120 ~ 140 DEG C, and the optimum temperature of overhead condenser is 65 ~ 80 DEG C, and reflux ratio is 0.3 ~ 0.6, and theoretical cam curve is 30 ~ 40.
The operating pressure of described ethyl lactate tower is 15 ~ 20kpa, and the optimum temperature of tower reactor reboiler is 80 ~ 110 DEG C, and the optimum temperature of overhead condenser is 55 ~ 65 DEG C, and reflux ratio is 0.3 ~ 0.6, and theoretical cam curve is 30 ~ 40.
Described crude tower, ethanol tower, lactic acid tower and ethyl lactate tower is packed tower, and used filler is stainless steel random packing or structured packing.
Fig. 1 is the flow chart that continuous catalyzing rectifying prepares ethyl lactate process.
In Fig. 1,1 and 2 be respectively the head tank equipped with lactic acid and ethanol, 3 be the fixed bed reactors equipped with solid catalyst, 4 be crude tower, 5 be ethanol tower, and 6 be lactic acid tower, and 7 be ethyl lactate tower, 8 be the pipeline of fixed bed reactors, 9 be the pipeline into crude tower, and 10 be crude tower overhead line, and 11 be crude tower tower reactor pipeline, 12 be ethanol tower overhead line, 13 be ethanol tower tower reactor pipeline, and 14 be lactic acid column overhead pipeline, and 15 be lactic acid tower tower reactor pipeline, 16 be ethyl lactate overhead line, and 17 be ethyl lactate tower reactor pipeline.
Lactic acid and ethanol are well mixed into pipeline through raw material pump, enter fixed bed reactors through 8 and carry out esterification, esterification products enter crude tower through 9, overhead extraction second alcohol and water, enter ethanol tower through 10, tower reactor produces ethyl lactate, water and lactic acid, enter lactic acid tower through 11, ethanol tower overhead extraction second alcohol and water azeotropic is constituted, ethanol raw material tank is returned through 12, tower reactor waste water is through 13 outer rows, lactic acid column overhead produces ethyl lactate and water, enter ethyl lactate tower through 14, tower reactor is lactic acid, lactic raw material tank is returned through 15, ethyl lactate overhead extraction water, through 16 outer rows, tower reactor is ethyl lactate product, product zone is gone to through 17.
Using the method for the present invention, compared with existing production method, have the following advantages that：（1）Esterification rate is fast, during batch esterification, and esterification equilibrium point is general at 4 ~ 6 hours, counts charging, discharge and heating process in, the cycle of whole esterification workshop section was at 6 ~ 8 hours, and fixed bed reactors are continuously produced, and esterification time was at 3 ~ 5 hours；（2）Product yield is high, during Batch Process, and distillation process produces transition component to obtain ethyl lactate product so that product single yield is 45 ~ 55%, and when using continuous tower rectifying separation, and product single yield is 60 ~ 80%；（3）Environmental protection, intermittently operated further relates to the problems such as catalyst is reclaimed in addition to transition component is produced, and this method is continuously produced, excessive alkyd all reuses, in addition to reaction generation water discharge, without other pollutants；（4）Energy-conservation, ethanol tower, lactic acid tower and the ethyl lactate tower of this method centrifugal station because the boiling point of three kinds of materials differs greatly, two-by-two between differ 70 ~ 80 DEG C, tower operating reflux ratio is low, saves steam energy consumption, reduces production cost；（5）Equipment is continuously produced, simple to operate.The method of the present invention has good social benefit and economic value, it is easy to popularization and application.
With reference to specific embodiment, the present invention will be described in detail.The scope of the present invention is not limited with embodiment, but is limited by the scope of claim.
Embodiment
Embodiment 1
Technological process is as shown in figure 1, by lactic acid and ethanol in molar ratio 2:1st, the fixed bed reactors for being mounted with 10L solid acid catalysts are continuously introduced into 1.5L/h flow velocitys, 80 DEG C of reaction temperature, reaction pressure is 0.2Mpa, air speed is 4h-1.Reaction product through fixed bed reactors enters crude tower,Crude tower uses θ ring metal stainless steel helices,3 × 3mm of filler size,Tower diameter 80mm,Rectifying section height 700mm,Stripping section height 700mm,Reflux ratio 0.3,Atmospheric operation,85 DEG C of tower top temperature,130 DEG C of bottom temperature,Tower top produces ethanol with 0.45L/h flow velocitys and part water goes to ethanol tower,Tower reactor produces ethyl lactate with 1.05L/h flow velocitys,Lactic acid and part water go to lactic acid tower,Ethanol tower uses θ ring metal stainless steel helices,3 × 3mm of filler size,Tower diameter 80mm,Rectifying section height 700mm,Stripping section height 700mm,Reflux ratio 4,Atmospheric operation,78 DEG C of tower top temperature,95 DEG C of bottom temperature,Tower top is constituted with 0.4L/h flow velocitys extraction second alcohol and water azeotropic,Go to ethanol raw material tank,Tower reactor is with 0.05L/h flow velocity wastewater discharges,Lactic acid tower uses θ ring metal stainless steel helices,3 × 3mm of filler size,Tower diameter 80mm,Rectifying section height 700mm,Stripping section height 700mm,Reflux ratio 0.3,Tower top pressure 5kpa,68 DEG C of tower top temperature,130 DEG C of bottom temperature,Tower top produces ethyl lactate with 0.8L/h flow velocitys and part water goes to ethyl lactate tower,Tower reactor produces lactic acid with 0.25L/h flow velocitys,Go to lactic raw material tank,Ethyl lactate tower uses θ ring metal stainless steel helices,3 × 3mm of filler size,Tower diameter 80mm,Rectifying section height 700mm,Stripping section height 700mm,Reflux ratio 0.4,Tower top pressure 18kpa,57 DEG C of tower top temperature,105 DEG C of bottom temperature,Tower top is with 0.11L/h flow velocity wastewater discharges,Tower reactor produces ethyl lactate product with 0.69L/h flow velocitys,Go to products pot.
Embodiment 2
Technological process is as shown in figure 1, by lactic acid and ethanol in molar ratio 3:1st, the fixed bed reactors for being mounted with 10L solid acid catalysts are continuously introduced into 1.5L/h flow velocitys, 90 DEG C of reaction temperature, reaction pressure is 0.2Mpa, air speed is 3h-1.Reaction product through fixed bed reactors enters crude tower,Crude tower uses θ ring metal stainless steel helices,3.5 × 3.5mm of filler size,Tower diameter 80mm,Rectifying section height 700mm,Stripping section height 700mm,Reflux ratio 0.4,Atmospheric operation,87 DEG C of tower top temperature,133 DEG C of bottom temperature,Tower top produces ethanol with 0.6L/h flow velocitys and part water goes to ethanol tower,Tower reactor produces ethyl lactate with 0.9L/h flow velocitys,Lactic acid and part water go to lactic acid tower,Ethanol tower uses θ ring metal stainless steel helices,3.5 × 3.5mm of filler size,Tower diameter 80mm,Rectifying section height 700mm,Stripping section height 700mm,Reflux ratio 4.5,Atmospheric operation,78 DEG C of tower top temperature,96 DEG C of bottom temperature,Tower top is constituted with 0.54L/h flow velocitys extraction second alcohol and water azeotropic,Go to ethanol raw material tank,Tower reactor is with 0.06L/h flow velocity wastewater discharges,Lactic acid tower uses θ ring metal stainless steel helices,3.5 × 3.5mm of filler size,Tower diameter 80mm,Rectifying section height 700mm,Stripping section height 700mm,Reflux ratio 0.4,Tower top pressure 8kpa,70 DEG C of tower top temperature,133 DEG C of bottom temperature,Tower top produces ethyl lactate with 0.7L/h flow velocitys and part water goes to ethyl lactate tower,Tower reactor produces lactic acid with 0.2L/h flow velocitys,Go to lactic raw material tank,Ethyl lactate tower uses θ ring metal stainless steel helices,3.5 × 3.5mm of filler size,Tower diameter 80mm,Rectifying section height 700mm,Stripping section height 700mm,Reflux ratio 0.5,Tower top pressure 20kpa,59 DEG C of tower top temperature,108 DEG C of bottom temperature,Tower top is with 0.1L/h flow velocity wastewater discharges,Tower reactor produces ethyl lactate product with 0.6L/h flow velocitys,Go to products pot.
Claims (8)
1. a kind of continuous catalyzing rectifying prepares the method for ethyl lactate, it is characterized in that comprising the following steps：（1）React workshop section：In the fixed bed reactors for loading acid cation exchange resin catalyst, by ethanol（Mass concentration 95%）And lactic acid（Mass concentration 95%）, catalytic esterification in fixed bed reactors is entered by raw material pump, ethyl lactate crude product is obtained；（2）Centrifugal station：Ethyl lactate crude product is subjected to rectifying separation, crude tower, ethanol tower, lactic acid tower and ethyl lactate tower is sequentially entered, obtains food grade lactic acid ethyl ester.
2. the method that a kind of continuous catalyzing rectifying according to claim 1 prepares ethyl lactate, it is characterised in that described ethanol and the mol ratio of lactic acid are 2:1~4:1.
3. the method that a kind of continuous catalyzing rectifying according to claim 1 prepares ethyl lactate, it is characterised in that described fixed bed reactors, 70 ~ 90 DEG C of reaction temperature, 0.1 ~ 0.3Mpa of reaction pressure, 3 ~ 5h-1 of air speed.
4. the method that a kind of continuous catalyzing rectifying according to claim 1 prepares ethyl lactate, it is characterized in that the operating pressure of described crude tower is normal pressure, the optimum temperature of tower reactor reboiler is 120 ~ 140 DEG C, the optimum temperature of overhead condenser is 80 ~ 95 DEG C, reflux ratio is 0.2 ~ 0.5, and theoretical cam curve is 30 ~ 40.
5. the method that a kind of continuous catalyzing rectifying according to claim 1 prepares ethyl lactate, it is characterized in that the operating pressure of described ethanol tower is normal pressure, the optimum temperature of tower reactor reboiler is 90 ~ 110 DEG C, the optimum temperature of overhead condenser is 75 ~ 80 DEG C, reflux ratio is 2 ~ 5, and theoretical cam curve is 35 ~ 45.
6. the method that a kind of continuous catalyzing rectifying according to claim 1 prepares ethyl lactate, it is characterized in that the operating pressure of described lactic acid tower is 5 ~ 10kpa, the optimum temperature of tower reactor reboiler is 120 ~ 140 DEG C, the optimum temperature of overhead condenser is 65 ~ 80 DEG C, reflux ratio is 0.3 ~ 0.6, and theoretical cam curve is 30 ~ 40.
7. the method that a kind of continuous catalyzing rectifying according to claim 1 prepares ethyl lactate, it is characterized in that the operating pressure of described ethyl lactate tower is 15 ~ 20kpa, the optimum temperature of tower reactor reboiler is 80 ~ 110 DEG C, the optimum temperature of overhead condenser is 55 ~ 65 DEG C, reflux ratio is 0.3 ~ 0.6, and theoretical cam curve is 30 ~ 40.
8. the method that a kind of continuous catalyzing rectifying according to claim 1 prepares ethyl lactate, it is characterised in that described crude tower, ethanol tower, lactic acid tower and ethyl lactate tower is packed tower, used filler is stainless steel random packing or structured packing.
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| CN201610074788.XA CN107032984A (en) | 2016-02-03 | 2016-02-03 | A kind of method that continuous catalyzing rectifying prepares ethyl lactate |
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| CN201610074788.XA CN107032984A (en) | 2016-02-03 | 2016-02-03 | A kind of method that continuous catalyzing rectifying prepares ethyl lactate |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109942358A (en) * | 2019-04-16 | 2019-06-28 | 营创三征(营口)精细化工有限公司 | A kind of solid acid catalysis low-boiling point alcohol continuous esterification technique |
| CN113603585A (en) * | 2021-09-23 | 2021-11-05 | 福州大学 | Continuous production process of ultra-pure methyl lactate |
| CN113979862A (en) * | 2021-10-14 | 2022-01-28 | 寿光金远东变性淀粉有限公司 | Method for continuously producing D-lactate |
Citations (4)
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|---|---|---|---|---|
| US6664413B1 (en) * | 1998-11-19 | 2003-12-16 | A. E. Staley Manufacturing Co. | Process for production of esters |
| CN1613842A (en) * | 2004-08-27 | 2005-05-11 | 清华大学 | Process for synthesizing ethyl lactate by catalytic rectifying method |
| CN1720215A (en) * | 2002-12-05 | 2006-01-11 | 阿肯马公司 | Continuous ethyl lactate preparation method |
| CN102105430A (en) * | 2008-07-30 | 2011-06-22 | 银河股份公司 | Continuous process for obtaining a lactic ester |
-
2016
- 2016-02-03 CN CN201610074788.XA patent/CN107032984A/en not_active Withdrawn
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6664413B1 (en) * | 1998-11-19 | 2003-12-16 | A. E. Staley Manufacturing Co. | Process for production of esters |
| CN1720215A (en) * | 2002-12-05 | 2006-01-11 | 阿肯马公司 | Continuous ethyl lactate preparation method |
| CN1613842A (en) * | 2004-08-27 | 2005-05-11 | 清华大学 | Process for synthesizing ethyl lactate by catalytic rectifying method |
| CN102105430A (en) * | 2008-07-30 | 2011-06-22 | 银河股份公司 | Continuous process for obtaining a lactic ester |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109942358A (en) * | 2019-04-16 | 2019-06-28 | 营创三征(营口)精细化工有限公司 | A kind of solid acid catalysis low-boiling point alcohol continuous esterification technique |
| CN113603585A (en) * | 2021-09-23 | 2021-11-05 | 福州大学 | Continuous production process of ultra-pure methyl lactate |
| CN113979862A (en) * | 2021-10-14 | 2022-01-28 | 寿光金远东变性淀粉有限公司 | Method for continuously producing D-lactate |
| CN113979862B (en) * | 2021-10-14 | 2024-02-13 | 寿光金远东变性淀粉有限公司 | Method for continuously producing D-lactate |
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Address after: 300384 Nankai District Alex Hua Tian Road, Tianjin international business center, No. 6020, No. 2 Applicant after: Tianjin Zhongfu environmental Polytron Technologies Inc Address before: 300384 Nankai District Alex Hua Tian Road, Tianjin international business center, No. 6020, No. 2 Applicant before: TIANJIN ZHONGFU ENGINEERING TECHNOLOGY CO., LTD. |
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