CN205188176U - Di n butyl phthalate plasticizer esterification reaction system - Google Patents
Di n butyl phthalate plasticizer esterification reaction system Download PDFInfo
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- CN205188176U CN205188176U CN201520966637.6U CN201520966637U CN205188176U CN 205188176 U CN205188176 U CN 205188176U CN 201520966637 U CN201520966637 U CN 201520966637U CN 205188176 U CN205188176 U CN 205188176U
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Abstract
The utility model relates to a plasticizer apparatus for producing, concretely relates to di n butyl phthalate plasticizer esterification reaction system. Di n butyl phthalate plasticizer esterification reaction system, including the esterification reaction cauldron, esterification reaction cauldron, esterification column, first condenser, alcohol -water separation jar, extraction jar, pure storage tank are consecutive, pure storage tank still links to each other with the esterification column top, establishes the booster pump between pure storage tank and the esterification column, establishes the hot -air line in the extraction jar, the esterification reaction cauldron is still consecutive with second condenser, ester storage tank, and esterification reaction cauldron top is passed through the feed valve and is linked to each other with the feed inlet. The utility model discloses can accelerate the reaction rate, the side reaction is few, and product quality is stable, and output is big, and product purity is high.
Description
Technical field
The utility model relates to a kind of plasticizer production device, is specifically related to a kind of Plasticized with Dibutyl Phthalate agent esterification system.
Background technology
Dibutyl phthalate (DBP) is that a kind of plasticizing efficiency is high, broad-spectrum softening agent product, and the main primary plasticizer being used as celluosic resin and polrvinyl chloride product, is specially adapted to nitrocellulose resin.Have excellent solvability, decomposability and tackiness, the flexibility of paint film and stability are also good.Good with the consistency of dyestuff, can be used for film, leatheroid and plastics.This product also can be used as the softening agent of natural rubber, tenderizer, can improve the rebound resilience of goods.
It is slow to there is speed of response in tradition DBP production system, the problems such as side reaction is many, unstable product quality, and output is little, and product purity is low.
Utility model content
According to above deficiency of the prior art, the technical problems to be solved in the utility model is: provide a kind of Plasticized with Dibutyl Phthalate agent esterification system, can fast reaction speed, and side reaction is few, constant product quality, and output is large, and product purity is high.
The utility model solves the technical scheme that its technical problem adopts:
Plasticized with Dibutyl Phthalate agent esterification system described in the utility model, comprise reaction kettle of the esterification, reaction kettle of the esterification, esterification column, the first condenser, alcohol-water separation tank, extractor, alcohol storage tank are connected successively, alcohol storage tank is also connected with esterification column top, establish topping-up pump between alcohol storage tank and esterification column, extractor is established warm air line;
Reaction kettle of the esterification is also connected successively with the second condenser, ester storage tank, and reaction kettle of the esterification top is connected with opening for feed by feed valve.
Described reaction kettle of the esterification inside arranges agitator.
Described reaction kettle of the esterification inside arranges inner coil pipe.
Described alcohol-water separation tank is connected with water pot.
Principle of work and process:
Raw material phthalic anhydride, propyl carbinol and solid acid catalyst are added in reaction kettle of the esterification by opening for feed, then closes feed valve.Under the effect that agitator stirs, use inner coil pipe heating, be progressively warming up to temperature of reaction and react, the ester that reaction generates enters ester storage tank and stores after the second condenser cooling.Enter the first condenser after the gas phase evaporated in reaction kettle of the esterification enters that backflow alcohol that esterification column and tower top enter is reverse and contacts to cool, enter alcohol-water separation tank and carry out alcohol aqueous phase separation, water saturation alcohol is from alcohol-water separation tank upper return to extractor, after abundant extraction, adopt the method for forced refluence, the alcohol being entered into alcohol storage tank by extractor gets back to gas-phase reverse that esterification column tower top and reaction kettle of the esterification evaporate to contacting after topping-up pump supercharging.In alcohol-water separation tank, isolated water enters water pot storage.
After having reacted, led in warm air to extractor process extraction agent by warm air line, extraction agent recycles.
The beneficial effect that the utility model has is:
(1) reaction kettle of the esterification adopts inner coil pipe heating, and the outer coil pipe eliminating traditional technology is frequent owing to colding and heat succeed each other, the shortcoming easily revealed.
(2) described system have employed recycle alcohol alcohol-water separation method, after extractor extraction, the water in recycle alcohol is extracted, avoid the water steamed to enter reaction kettle of the esterification again, accelerate speed of response, make every still speed of response accelerate 20%, energy expenditure reduces 15%.Extractor is established warm air line regenerate extraction agent, can reuse.
(3) adopt batch esterification technique, side reaction is few, constant product quality, and output is large, and product purity is high.
Accompanying drawing explanation
Fig. 1 is the utility model structural representation;
In figure: 1, reaction kettle of the esterification; 2, esterification column; 3, the first condenser; 4, alcohol-water separation tank; 5, extractor; 6, alcohol storage tank; 7, topping-up pump; 8, opening for feed; 9, feed valve; 10, inner coil pipe; 11, agitator; 12, the second condenser; 13, ester storage tank; 14, warm air line; 15, water pot.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described further:
As shown in Figure 1, the utility model comprises reaction kettle of the esterification 1, reaction kettle of the esterification 1, esterification column 2, first condenser 3, alcohol-water separation tank 4, extractor 5, alcohol storage tank 6 are connected successively, alcohol storage tank 6 is also connected with esterification column 2 top, establish topping-up pump 7 between alcohol storage tank 6 and esterification column 2, extractor 5 is established warm air line 14;
Reaction kettle of the esterification 1 is also connected successively with the second condenser 12, ester storage tank 13, and reaction kettle of the esterification 1 top is connected with opening for feed 8 by feed valve 9.
Described reaction kettle of the esterification 1 inside arranges agitator 11.
Described reaction kettle of the esterification 1 inside arranges inner coil pipe 10.
Described alcohol-water separation tank 4 is connected with water pot 15.
Raw material phthalic anhydride, propyl carbinol and solid acid catalyst are added in reaction kettle of the esterification 1 by opening for feed 8, then closes feed valve 9.Under the effect that agitator 11 stirs, use inner coil pipe 10 to heat, be progressively warming up to temperature of reaction and react, the ester that reaction generates enters ester storage tank 13 and stores after the second condenser 12 cools.Enter the first condenser 3 after the gas phase evaporated in reaction kettle of the esterification 1 enters that backflow alcohol that esterification column 2 and tower top enter is reverse and contacts to cool, enter alcohol-water separation tank 4 and carry out alcohol aqueous phase separation, water saturation alcohol is from alcohol-water separation tank 4 upper return to extractor 5, after abundant extraction, adopt the method for forced refluence, the alcohol being entered into alcohol storage tank 6 by extractor 5 gets back to gas-phase reverse that esterification column 2 tower top and reaction kettle of the esterification 1 evaporate to contacting after topping-up pump 7 supercharging.In alcohol-water separation tank 4, isolated water enters water pot 15 and stores.
After having reacted, lead to warm air by warm air line 14 and process extraction agent in extractor 5, extraction agent recycles.
Claims (4)
1. a Plasticized with Dibutyl Phthalate agent esterification system, comprise reaction kettle of the esterification (1), it is characterized in that: reaction kettle of the esterification (1), esterification column (2), the first condenser (3), alcohol-water separation tank (4), extractor (5), alcohol storage tank (6) are connected successively, alcohol storage tank (6) is also connected with esterification column (2) top, establish topping-up pump (7) between alcohol storage tank (6) and esterification column (2), extractor (5) is established warm air line (14);
Reaction kettle of the esterification (1) is also connected successively with the second condenser (12), ester storage tank (13), and reaction kettle of the esterification (1) top is connected with opening for feed (8) by feed valve (9).
2. Plasticized with Dibutyl Phthalate agent esterification system according to claim 1, is characterized in that: described reaction kettle of the esterification (1) inside arranges agitator (11).
3. Plasticized with Dibutyl Phthalate agent esterification system according to claim 1, is characterized in that: described reaction kettle of the esterification (1) inside arranges inner coil pipe (10).
4. Plasticized with Dibutyl Phthalate agent esterification system according to claim 1, is characterized in that: described alcohol-water separation tank (4) is connected with water pot (15).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520966637.6U CN205188176U (en) | 2015-11-26 | 2015-11-26 | Di n butyl phthalate plasticizer esterification reaction system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520966637.6U CN205188176U (en) | 2015-11-26 | 2015-11-26 | Di n butyl phthalate plasticizer esterification reaction system |
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| CN205188176U true CN205188176U (en) | 2016-04-27 |
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| CN201520966637.6U Active CN205188176U (en) | 2015-11-26 | 2015-11-26 | Di n butyl phthalate plasticizer esterification reaction system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105837446A (en) * | 2016-05-26 | 2016-08-10 | 安庆盛峰化工股份有限公司 | Ester recovery device for dibutyl phthalate production |
| CN106810450A (en) * | 2017-02-23 | 2017-06-09 | 天津大学 | The apparatus and method that a kind of catalytic reaction rectification prepares dibutyl phthalate |
| CN114984888A (en) * | 2022-04-28 | 2022-09-02 | 华东理工大学 | Continuous esterification circulating reactor system for producing plasticizer |
-
2015
- 2015-11-26 CN CN201520966637.6U patent/CN205188176U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105837446A (en) * | 2016-05-26 | 2016-08-10 | 安庆盛峰化工股份有限公司 | Ester recovery device for dibutyl phthalate production |
| CN106810450A (en) * | 2017-02-23 | 2017-06-09 | 天津大学 | The apparatus and method that a kind of catalytic reaction rectification prepares dibutyl phthalate |
| CN106810450B (en) * | 2017-02-23 | 2023-08-08 | 天津大学 | Device and method for preparing dibutyl phthalate by catalytic reaction rectification |
| CN114984888A (en) * | 2022-04-28 | 2022-09-02 | 华东理工大学 | Continuous esterification circulating reactor system for producing plasticizer |
| CN114984888B (en) * | 2022-04-28 | 2023-10-03 | 华东理工大学 | Circulation reactor system for continuous esterification for producing plasticizer |
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