CN220834174U - Dibutyl phthalate high-efficiency production system - Google Patents
Dibutyl phthalate high-efficiency production system Download PDFInfo
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- CN220834174U CN220834174U CN202322565126.0U CN202322565126U CN220834174U CN 220834174 U CN220834174 U CN 220834174U CN 202322565126 U CN202322565126 U CN 202322565126U CN 220834174 U CN220834174 U CN 220834174U
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- China
- Prior art keywords
- tank
- heat exchange
- dibutyl phthalate
- production system
- premixing
- Prior art date
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- DOIRQSBPFJWKBE-UHFFFAOYSA-N dibutyl phthalate Chemical compound CCCCOC(=O)C1=CC=CC=C1C(=O)OCCCC DOIRQSBPFJWKBE-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 27
- 238000004821 distillation Methods 0.000 claims abstract description 25
- 239000002994 raw material Substances 0.000 claims abstract description 24
- 238000003860 storage Methods 0.000 claims abstract description 7
- 238000003756 stirring Methods 0.000 claims description 17
- 239000007791 liquid phase Substances 0.000 claims description 15
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 claims description 14
- 238000010438 heat treatment Methods 0.000 claims description 12
- 239000012071 phase Substances 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 6
- 238000009413 insulation Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 17
- 238000000926 separation method Methods 0.000 abstract description 6
- 230000035484 reaction time Effects 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 5
- 238000011084 recovery Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 description 3
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to the technical field of dibutyl phthalate production, in particular to a dibutyl phthalate efficient production system. The dibutyl phthalate high-efficiency production system comprises a heat exchange tank, wherein the heat exchange tank is connected with a rectifying tower through a premixing tank, the lower part of the rectifying tower is connected with a product storage tank through a pipeline, a condenser is arranged inside the rectifying tower, a heat exchange coil is arranged inside the heat exchange tank, a U-shaped feeder is arranged inside the premixing tank, the rectifying tower is connected with the heat exchange coil through a normal temperature distillation tower, and the rectifying tower is connected with the U-shaped feeder through an induced draft fan. The system mixes the reaction raw materials more uniformly after premixing the reaction raw materials by arranging the premixing tank and the U-shaped feeder, thereby greatly improving the reaction efficiency and saving the reaction time; through the cooperation of heat transfer tank and normal atmospheric temperature distillation tower, with the high temperature waste water of separation for to the intensification of raw materials, promoted energy utilization efficiency greatly, practiced thrift manufacturing cost.
Description
Technical Field
The utility model relates to the technical field of dibutyl phthalate production, in particular to a dibutyl phthalate efficient production system.
Background
Dibutyl phthalate is an organic compound with a chemical formula of C 16H22O4 and a CAS registry number of 84-74-2, and is a colorless transparent oily liquid. Is mainly used as a primary plasticizer for cellulose, resin, synthetic rubber and polyvinyl chloride. Is insoluble in water and soluble in alcohol, ether, acetone and benzene.
In the prior art, continuous production is mostly adopted in the dibutyl phthalate production process. However, in production, the reaction is insufficient only in the rectifying tower, and the temperature of the generated product is high due to the high reaction temperature, and particularly, after alcohol-water separation, the separated high-temperature water is directly discharged to generate energy waste.
Patent application CN206502759U, published time 2017.09.19. Discloses a device for preparing dibutyl phthalate by catalytic reaction rectification; comprises a reaction rectifying tower, a dehydrating tower, an alcohol recovery tower, a phase separation tank and an evaporator; the upper part of the reaction rectifying tower is provided with a phthalic anhydride and butanol mixture flow feed inlet, the bottom of the reaction rectifying tower is provided with a reboiler, and a tower top gas phase extraction outlet is connected to a middle feed inlet of the dehydrating tower; the top of the dehydration tower is provided with a condenser, the bottom of the tower is provided with a reboiler, the outlet of the condenser is connected to the inlet of the phase separator, the upper liquid outlet of the phase separator is connected to the reflux liquid inlet at the top of the dehydration tower, and the lower liquid outlet is connected to the feed inlet at the middle part of the alcohol recovery tower; the top of the alcohol recovery tower is provided with a condenser, the bottom of the tower is provided with a reboiler, the outlet of the condenser is connected to the inlet of the phase separator, the upper liquid outlet of the phase separator is connected to the reflux liquid inlet at the top of the alcohol recovery tower, and the lower liquid outlet is connected to the middle feed inlet of the dehydration tower. However, the reaction efficiency is low and the energy is wasted.
Disclosure of utility model
According to the defects in the prior art, the utility model aims to provide the dibutyl phthalate high-efficiency production system, and the reaction raw materials are premixed more uniformly through the arrangement of the premixing tank and the U-shaped feeder, so that the reaction efficiency is greatly improved, and the reaction time is saved; through the cooperation of heat transfer tank and normal atmospheric temperature distillation tower, with the high temperature waste water of separation for to the intensification of raw materials, promoted energy utilization efficiency greatly, practiced thrift manufacturing cost.
The utility model is realized by adopting the following technical scheme:
The dibutyl phthalate high-efficiency production system comprises a heat exchange tank, wherein the heat exchange tank is connected with a rectifying tower through a premixing tank, the lower part of the rectifying tower is connected with a product storage tank through a pipeline, a condenser is arranged inside the rectifying tower, a heat exchange coil is arranged inside the heat exchange tank, a U-shaped feeder is arranged inside the premixing tank, the rectifying tower is connected with the heat exchange coil through a normal temperature distillation tower, and the rectifying tower is connected with the U-shaped feeder through an induced draft fan.
The heat exchange tank is used for heating the raw materials, and the premixing tank is used for pre-mixing and heating the reaction raw materials. The U-shaped feeder is used for enlarging the contact area between raw materials.
The heat exchange tank is connected with a butanol feeding pipeline, a premixing tank feeding pump is arranged between the heat exchange tank and the premixing tank, and a liquid phase discharging pipeline is connected to the heat exchange coil.
The premixing tank is internally provided with a stirring paddle driven by a stirring motor, the stirring paddle is positioned in the U-shaped feeder, and a heating coil is arranged between the stirring paddle and the U-shaped feeder.
The outside of the premixing tank is provided with an insulating layer, and the premixing tank is provided with a raw material feeding pipeline and a gas phase discharging pipeline.
A rectifying tower feeding pump is arranged between the premixing tank and the rectifying tower, and a reboiler is connected on the rectifying tower.
And a normal temperature distillation tower inlet pump is arranged between the rectifying tower and the normal temperature distillation tower, and the joint of the normal temperature distillation tower inlet pump and the rectifying tower is positioned below the condenser.
A liquid phase return pump is arranged between the normal temperature distillation tower and the heat exchange coil, and a heat inlet coil pipe is arranged between the liquid phase return pump and the heat exchange coil.
An induced draft fan is arranged between the rectifying tower and the U-shaped feeder, and a U-shaped feeder pipeline is arranged between the induced draft fan and the U-shaped feeder.
The U-shaped feeder is provided with a feeding hole.
The working principle of the utility model is as follows:
The phthalic anhydride enters the premixing tank through the raw material feeding pipeline, the stirring motor drives the stirring paddle to start rotating, and the heating coil starts working; after premixing, raw materials enter a rectifying tower through a rectifying tower feed pump to react, then gas phase enters a U-shaped feeder through a draught fan, condensed liquid phase enters a normal temperature distillation tower through a normal temperature distillation tower pump to carry out alcohol-water separation, then high temperature water enters a heat exchange coil through a liquid phase return pump to exchange heat, and a product enters a product storage tank through a pipeline to be temporarily stored. The heat exchange tank is used for heating the raw materials, and the premixing tank is used for pre-mixing and heating the reaction raw materials. The U-shaped feeder is used for enlarging the contact area between raw materials.
Compared with the prior art, the utility model has the beneficial effects that:
By adopting the efficient dibutyl phthalate production system, the reaction raw materials are premixed by the arrangement of the premixing tank and the U-shaped feeder, so that the reaction raw materials are mixed more uniformly, the reaction efficiency is greatly improved, and the reaction time is saved; through the cooperation of heat transfer tank and normal atmospheric temperature distillation tower, with the high temperature waste water of separation for to the intensification of raw materials, promoted energy utilization efficiency greatly, practiced thrift manufacturing cost.
Drawings
FIG. 1 is a schematic diagram of the efficient dibutyl phthalate production system of the present utility model;
FIG. 2 is a schematic view of the structure of the U-shaped feeder of the present utility model;
In the figure: 1. a heat exchange tank; 2. a premix tank; 3. a rectifying tower; 4. a normal temperature distillation tower; 5. a product storage tank; 6. a reboiler; 7. a butanol feed line; 8. a stirring motor; 9. stirring paddles; 10. a heating coil; 11. a U-shaped feeder; 12. a heat preservation layer; 13. a condenser; 14. a premix tank feed pump; 15. a rectifying column feed pump; 16. pumping into a normal temperature distillation tower; 17. a liquid phase return pump; 18. an induced draft fan; 19. a heat exchange coil pipe; 20. a U-feed pipe; 21. a heat exchange coil; 22. a liquid phase discharge pipeline; 23. a raw material feed pipe; 24. a gas phase discharge pipe; 25. and a feed hole.
Detailed Description
The present utility model will be described in further detail with reference to the accompanying drawings, in order to make the objects and technical solutions of the present utility model more apparent.
Example 1
As shown in FIG. 1, the dibutyl phthalate high-efficiency production system comprises a heat exchange tank 1, wherein the heat exchange tank 1 is connected with a rectifying tower 3 through a premixing tank 2, the lower part of the rectifying tower 3 is connected with a product storage tank 5 through a pipeline, a condenser 13 is arranged inside the rectifying tower 3, a heat exchange coil 21 is arranged inside the heat exchange tank 1, a U-shaped feeder 11 is arranged inside the premixing tank 2, the rectifying tower 3 is connected with the heat exchange coil 21 through a normal temperature distillation tower 4, and the rectifying tower 3 is connected with the U-shaped feeder 11 through an induced draft fan 18. The heat exchange tank 1 is used for heating the raw materials, and the premixing tank 2 is used for pre-mixing and heating the reaction raw materials. The heat exchange tank 1 is connected with a butanol feeding pipeline 7, a premixing tank feeding pump 14 is arranged between the heat exchange tank 1 and the premixing tank 2, and a liquid phase discharging pipeline 22 is connected with a heat exchange coil 21. The inside stirring rake 9 that is driven by agitator motor 8 that is equipped with of premix jar 2, stirring rake 9 are located the inside of U type feeder 11, are equipped with heating coil 10 between stirring rake 9 and the U type feeder 11. An insulating layer 12 is arranged on the outer side of the premixing tank 2, and a raw material feeding pipeline 23 and a gas phase discharging pipeline 24 are arranged on the premixing tank 2. A rectifying tower feeding pump 15 is arranged between the premixing tank 2 and the rectifying tower 3, and the rectifying tower 3 is connected with a reboiler 6. A normal temperature distillation tower pump 16 is arranged between the rectifying tower 3 and the normal temperature distillation tower 4, and the joint of the normal temperature distillation tower pump 16 and the rectifying tower 3 is positioned below the condenser 13. A liquid phase return pump 17 is arranged between the normal temperature distillation tower 4 and the heat exchange coil 21, and a heat inlet coil pipe 19 is arranged between the liquid phase return pump 17 and the heat exchange coil 21. An induced draft fan 18 is arranged between the rectifying tower 3 and the U-shaped feeder 11, and a U-shaped feeder inlet pipeline 20 is arranged between the induced draft fan 18 and the U-shaped feeder 11. As shown in fig. 2, the U-shaped feeder 11 is provided with a feed hole 25.
The dibutyl phthalate high-efficiency production system comprises the following steps when in operation:
(1) Butanol enters the heat exchange tank 1 through the butanol feeding pipeline 7, enters the U-shaped feeder 11 through the premixing tank feeding pump 14 after heat exchange is completed, and meanwhile phthalic anhydride enters the premixing tank through the raw material feeding pipeline 23, the stirring motor 8 drives the stirring paddle 9 to start rotating, and the heating coil 10 starts working; (2) After premixing, raw materials enter a rectifying tower 3 through a rectifying tower feed pump 15 to react, then gas phase enters a U-shaped feeder 11 through a draught fan 18, condensed liquid phase enters a normal temperature distillation tower 4 through a normal temperature distillation tower pump 16 to carry out alcohol-water separation, then high temperature water enters a heat exchange coil 21 through a liquid phase return pump 17 to exchange heat, and products enter a product storage tank 5 through a pipeline to be temporarily stored.
Claims (9)
1. The utility model provides a dibutyl phthalate high-efficient production system, a serial communication port, including heat transfer tank (1), heat transfer tank (1) link to each other with rectifying column (3) through premixing jar (2), rectifying column (3) below links to each other with product storage jar (5) through the pipeline, rectifying column (3) inside is equipped with condenser (13), heat transfer tank (1) inside is equipped with heat exchange coil (21), premixing jar (2) inside is equipped with U type feeder (11), rectifying column (3) link to each other with heat exchange coil (21) through normal atmospheric temperature distillation tower (4), rectifying column (3) link to each other with U type feeder (11) through draught fan (18).
2. The dibutyl phthalate high-efficiency production system according to claim 1, wherein the heat exchange tank (1) is connected with a butanol feeding pipeline (7), a premixing tank feeding pump (14) is arranged between the heat exchange tank (1) and the premixing tank (2), and the heat exchange coil (21) is connected with a liquid phase discharging pipeline (22).
3. The efficient dibutyl phthalate production system according to claim 1, characterized in that a stirring paddle (9) driven by a stirring motor (8) is arranged inside the premixing tank (2), the stirring paddle (9) is positioned inside the U-shaped feeder (11), and a heating coil (10) is arranged between the stirring paddle (9) and the U-shaped feeder (11).
4. The efficient dibutyl phthalate production system according to claim 1, wherein an insulation layer (12) is arranged on the outer side of the premixing tank (2), and a raw material feeding pipeline (23) and a gas phase discharging pipeline (24) are arranged on the premixing tank (2).
5. The efficient dibutyl phthalate production system according to claim 1, characterized in that a rectifying tower feed pump (15) is arranged between the premixing tank (2) and the rectifying tower (3), and a reboiler (6) is connected to the rectifying tower (3).
6. The efficient dibutyl phthalate production system according to claim 1, characterized in that a normal temperature distillation column pump (16) is arranged between the rectifying column (3) and the normal temperature distillation column (4), and the joint of the normal temperature distillation column pump (16) and the rectifying column (3) is positioned below the condenser (13).
7. The efficient dibutyl phthalate production system according to claim 1, characterized in that a liquid phase return pump (17) is arranged between the normal temperature distillation tower (4) and the heat exchange coil (21), and a heat exchange coil inlet pipeline (19) is arranged between the liquid phase return pump (17) and the heat exchange coil (21).
8. The efficient dibutyl phthalate production system according to claim 1, characterized in that an induced draft fan (18) is arranged between the rectifying tower (3) and the U-shaped feeder (11), and a U-shaped feeder inlet pipeline (20) is arranged between the induced draft fan (18) and the U-shaped feeder (11).
9. The efficient dibutyl phthalate production system according to claim 1, characterized in that the U-shaped feeder (11) is provided with a feed hole (25).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322565126.0U CN220834174U (en) | 2023-09-21 | 2023-09-21 | Dibutyl phthalate high-efficiency production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322565126.0U CN220834174U (en) | 2023-09-21 | 2023-09-21 | Dibutyl phthalate high-efficiency production system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220834174U true CN220834174U (en) | 2024-04-26 |
Family
ID=90786592
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322565126.0U Active CN220834174U (en) | 2023-09-21 | 2023-09-21 | Dibutyl phthalate high-efficiency production system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220834174U (en) |
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2023
- 2023-09-21 CN CN202322565126.0U patent/CN220834174U/en active Active
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