CN219815330U - Process system for preparing isopropanol by extraction and rectification - Google Patents
Process system for preparing isopropanol by extraction and rectification Download PDFInfo
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- CN219815330U CN219815330U CN202321269558.0U CN202321269558U CN219815330U CN 219815330 U CN219815330 U CN 219815330U CN 202321269558 U CN202321269558 U CN 202321269558U CN 219815330 U CN219815330 U CN 219815330U
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- tower
- extraction
- reboiler
- regeneration
- light component
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- 238000000605 extraction Methods 0.000 title claims abstract description 116
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 title claims abstract description 81
- 238000000034 method Methods 0.000 title claims abstract description 26
- 230000008569 process Effects 0.000 title claims abstract description 19
- 230000008929 regeneration Effects 0.000 claims abstract description 44
- 238000011069 regeneration method Methods 0.000 claims abstract description 44
- 230000018044 dehydration Effects 0.000 claims abstract description 41
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 41
- 238000000895 extractive distillation Methods 0.000 claims description 6
- 230000001172 regenerating effect Effects 0.000 claims description 4
- 238000000926 separation method Methods 0.000 abstract description 9
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 3
- 238000010992 reflux Methods 0.000 description 32
- 239000000463 material Substances 0.000 description 15
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 14
- 239000000498 cooling water Substances 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000005984 hydrogenation reaction Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 239000007789 gas Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 2
- XTUSEBKMEQERQV-UHFFFAOYSA-N propan-2-ol;hydrate Chemical compound O.CC(C)O XTUSEBKMEQERQV-UHFFFAOYSA-N 0.000 description 2
- ZAFNJMIOTHYJRJ-UHFFFAOYSA-N Diisopropyl ether Chemical compound CC(C)OC(C)C ZAFNJMIOTHYJRJ-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000010533 azeotropic distillation Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000002304 perfume Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
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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
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- Extraction Or Liquid Replacement (AREA)
Abstract
The utility model belongs to the field of rectification separation, and relates to a process system for preparing isopropanol by extraction and rectification, which comprises the following steps: the light component extraction device comprises a light component extraction tower, an extraction tower, a dehydration tower and a regeneration tower which are sequentially connected, wherein an extraction tower heat exchange reboiler is arranged at the tower bottom of the extraction tower, an extractant feed inlet is arranged at the upper part of the extraction tower, a tower bottom extraction outlet of the regeneration tower is connected with a shell side inlet of the extraction tower heat exchange reboiler through a pipeline, and a shell side outlet of the extraction tower heat exchange reboiler is connected with the extractant feed inlet of the extraction tower through a pipeline. The utility model optimizes the isopropanol rectification process, produces isopropanol by an extraction rectification method, and returns the extractant at the bottom of the regeneration tower to the upper part of the extraction tower after exchanging heat for the reboiler at the bottom of the extraction tower, thereby recycling the extractant and greatly reducing the energy consumption.
Description
Technical Field
The utility model belongs to the field of rectification separation, and particularly relates to a process system for preparing isopropanol by extraction and rectification.
Background
Isopropyl alcohol (IPA), also known as 2-propanol, is an organic compound of the formula C 3 H 8 O is an isomer of n-propanol, is colorless transparent liquid, has smell similar to a mixture of ethanol and acetone, and can be dissolved in water, alcohol, ether, benzene, chloroform and other organic solvents. Isopropyl alcohol is an important chemical product and raw material, and is mainly used for pharmacy, cosmetics, plastics, perfume, paint and the like.
The synthetic routes of isopropanol are as follows: propylene water and ester hydrogenation and acetone hydrogenation, wherein the acetone hydrogenation process route is simple and accounts for about 60 percent of the isopropanol productivity. And the acetone, the water, the isopropyl alcohol, the isopropyl ether, the heavy components and the like are produced as byproducts when the acetone and the hydrogen react to produce the isopropyl alcohol, and the light components, the heavy components and the water are required to be removed by rectification separation in order to obtain the isopropyl alcohol with high purity.
In general, besides light and heavy removal, the dehydration of isopropanol mainly adopts methods such as azeotropic distillation and membrane separation, for example, CN104447199B discloses a method for separating acetone hydrogenation reaction products by a salt-adding extractive distillation method, and the separation process mainly comprises three distillation towers of coarse separation, extraction and dehydration, and the salt-adding extractive distillation method is mainly used for an extraction tower. The acetone hydrogenation reaction product is separated into light components and azeotrope at the top of the crude separation tower, the light components and the azeotrope are returned to the inlet of the reactor for recycling, the heavy components are extracted from the tower bottom, and the isopropanol water solution is extracted from the lateral line at the lower part of the crude separation tower. And separating the isopropanol water solution in the extraction tower by adopting a salt extraction rectification method, and extracting an isopropanol product meeting the requirements from the tower top.
The patent has unreasonable flow arrangement and high energy consumption. Therefore, there is a need for improvements over the prior art to save energy.
Disclosure of Invention
The utility model aims to overcome the defects of the prior art, and provides a process system for preparing isopropanol by extraction and rectification.
The technical scheme adopted for solving the technical problems is as follows:
a process system for preparing isopropanol by extractive distillation, comprising: the light component extraction device comprises a light component extraction tower, an extraction tower, a dehydration tower and a regeneration tower which are sequentially connected, wherein an extraction tower heat exchange reboiler is arranged at the tower bottom of the extraction tower, an extractant feed inlet is arranged at the upper part of the extraction tower, a tower bottom extraction outlet of the regeneration tower is connected with a shell side inlet of the extraction tower heat exchange reboiler through a pipeline, and a shell side outlet of the extraction tower heat exchange reboiler is connected with the extractant feed inlet of the extraction tower through a pipeline.
Further, a light component removing tower reboiler is arranged at the tower bottom of the light component removing tower, and a light component removing tower condenser is arranged at the tower top.
Further, the tower kettle of the extraction tower is provided with an extraction tower steam reboiler, and the tower top is provided with an extraction tower condenser.
Further, a dehydration tower reboiler is arranged at the tower bottom of the dehydration tower, and a dehydration tower condenser is arranged at the tower top.
Further, a regeneration tower reboiler is arranged at the tower bottom of the regeneration tower, and a regeneration tower condenser is arranged at the tower top.
Further, the light component removing tower is an atmospheric tower, and the regenerating tower is a vacuum tower.
The utility model has the advantages and positive effects that:
the utility model optimizes the isopropanol rectification process, produces isopropanol by an extraction rectification method, and returns the extractant at the bottom of the regeneration tower to the upper part of the extraction tower after exchanging heat for the reboiler at the bottom of the extraction tower, thereby recycling the extractant and greatly reducing the energy consumption.
Drawings
FIG. 1 is a block diagram of a process system for producing isopropyl alcohol by extractive distillation according to the present utility model.
1-a light component removing tower; 2-a light ends column reboiler; 3-a light component removal tower condenser; 4-a reflux tank of the light component removal tower; 5-an extraction tower; 6-an extraction tower heat exchange reboiler; 7-an extraction column steam reboiler; 8-an extraction column condenser; 9-an extraction tower reflux drum; 10-a dehydration tower; 11-a dehydration column reboiler; 12-a dehydration column condenser; 13-a dehydration tower reflux drum; 14-a regeneration tower; 15-a regenerator reboiler; 16-a regenerator condenser; 17-a regeneration tower reflux drum.
Detailed Description
The utility model is further illustrated by the following examples, which are intended to be illustrative only and not limiting in any way.
A process system for preparing isopropanol by extractive distillation, comprising: the light component removing tower 1, the extraction tower 5, the dehydrating tower 10 and the regeneration tower 14 which are sequentially connected, wherein an extraction tower heat exchange reboiler 6 is arranged at the tower bottom of the extraction tower 5, an extractant feed inlet is arranged at the upper part of the extraction tower 5, a tower bottom extraction outlet of the regeneration tower 14 is connected with a shell side inlet of the extraction tower heat exchange reboiler 6 through a pipeline, and a shell side outlet of the extraction tower heat exchange reboiler 6 is connected with the extractant feed inlet of the extraction tower 5 through a pipeline.
According to the utility model, the isopropanol rectification process is optimized, the isopropanol raw material enters the extraction tower 5 after light components are removed by the light component removal tower 1, the isopropanol product is obtained at the top of the tower through extraction separation of the extraction tower 5 under the action of the extractant, the extractant containing water and other impurities at the bottom of the tower is subjected to water removal by the dehydration tower 10, and the extractant is recycled after the impurities are removed by the regeneration tower 14. For energy saving and consumption reduction, the extractant extracted from the bottom of the regeneration tower 14 is returned to the upper part of the extraction tower 5 after heat exchange of the reboiler 7 at the bottom of the extraction tower.
The tower kettle of the light component removing tower 1 is provided with a light component removing tower reboiler 2, and the tower top is provided with a light component removing tower condenser 3. The light component removing tower 1 is provided with a feed inlet, a tower top extraction outlet, a tower top reflux outlet and a tower bottom extraction outlet, wherein the tower top extraction outlet of the light component removing tower 1 is connected with the inlet of the light component removing tower condenser 3 through a pipeline, the outlet of the light component removing tower condenser 3 is connected with the inlet of the light component removing tower reflux tank 4, and the outlet of the light component removing tower reflux tank 4 is connected to the tower top reflux outlet through a pump. The shell side inlet of the light component removal tower reboiler 2 is connected with a steam ST pipeline, and the shell side outlet is connected with a steam condensate RW pipeline. The shell side inlet of the light component removal tower condenser 3 is connected with a circulating cooling water feeding CWS pipeline, and the shell side outlet is connected with a circulating cooling water backwater CWR pipeline.
The isopropanol raw material is sent into a light component removing tower 1, the light component removing tower 1 is provided with a light component removing tower reboiler 2, and steam is used as a heat source; the light component removing tower 1 is an atmospheric tower, the temperature of the tower top is 50-70 ℃, and the temperature of the tower bottom is 80-100 ℃; the gas phase at the top of the light component removal tower 1 enters a light component removal tower condenser 3 for condensation, the condensed liquid enters a light component removal tower reflux tank 4, the materials in the light component removal tower reflux tank 4 are conveyed by a pump, and part of the materials return to the light component removal tower 1 as reflux, and the other part of materials are extracted as light components.
The bottom extraction outlet of the light component removal tower 1 is connected to the feed inlet of the extraction tower 5 through a pipeline. The tower bottom of the extraction tower 5 is provided with an extraction tower steam reboiler 7, and the tower top is provided with an extraction tower condenser 8. The extraction tower 5 is provided with a feed inlet, a tower top extraction outlet, a tower top reflux inlet and a tower bottom extraction outlet, the tower top extraction outlet of the extraction tower 5 is connected with the inlet of the extraction tower condenser 8 through a pipeline, the outlet of the extraction tower condenser 8 is connected with the inlet of the extraction tower reflux tank 9, and the outlet of the extraction tower reflux tank 9 is connected to the tower top reflux inlet through a pump. The shell side inlet of the extraction tower steam reboiler 7 is connected with a steam ST pipeline, and the shell side outlet is connected with a steam condensate RW pipeline. The shell side inlet of the extraction tower condenser 8 is connected with a circulating cooling water feeding CWS pipeline, and the shell side outlet is connected with a circulating cooling water backwater CWR pipeline.
The bottom material of the light component removal tower 1 is conveyed into an extraction tower 5 through a pump, the extraction tower 5 is provided with two reboilers, one is an extraction tower steam reboiler 7, steam is used as a reboiler heat source, the other is an extraction tower heat exchange reboiler 6, and an extractant at the bottom of a regeneration tower 14 is used as a heat source; the extraction tower 5 is a vacuum tower, the tower top pressure is-90 kpa-normal pressure, the tower top temperature is 40-70 ℃, and the tower bottom temperature is 140-170 ℃; the extractant enters the extraction tower 5 from the middle upper part of the extraction tower 5, the gas phase at the top of the extraction tower 5 enters an extraction tower condenser 8 for condensation, the condensed liquid enters an extraction tower reflux tank 9, the materials in the extraction tower reflux tank 9 are conveyed by a pump, a part of the materials return to the extraction tower 5 as reflux, and a part of the materials are extracted as isopropanol products.
The bottom extraction port of the extraction column 5 is connected to the feed port of the dehydration column 10 through a pipeline. The tower kettle of the dehydration tower 10 is provided with a dehydration tower reboiler 11, and the tower top is provided with a dehydration tower condenser 12. The dehydration tower 10 is provided with a feed inlet, a tower top extraction outlet, a tower top reflux inlet and a tower bottom extraction outlet, wherein the tower top extraction outlet of the dehydration tower 10 is connected with the inlet of the dehydration tower condenser 12 through a pipeline, the outlet of the dehydration tower condenser 12 is connected with the inlet of the dehydration tower reflux tank 13, and the outlet of the dehydration tower reflux tank 13 is connected with the tower top reflux inlet through a pump. The shell side inlet of the dehydration tower reboiler 11 is connected with a steam ST pipeline, and the shell side outlet is connected with a steam condensate RW pipeline. The shell side inlet of the dehydration tower condenser 12 is connected with a circulating cooling water feeding CWS pipeline, and the shell side outlet is connected with a circulating cooling water backwater CWR pipeline.
The tower bottom material of the extraction tower 5 is conveyed to a dehydration tower 10 through a pump, the dehydration tower 10 is provided with a dehydration tower reboiler 11, and steam is used as a reboiler heat source; the dehydration tower 10 is a vacuum tower, the tower top pressure is-90 kpa-normal pressure, the tower top temperature is 60-100 ℃, and the tower bottom temperature is 150-180 ℃; the gas phase at the top of the dehydration tower 10 enters a dehydration tower condenser 12 for condensation, the condensed liquid enters a dehydration tower reflux tank 13, the materials in the dehydration tower reflux tank 13 are conveyed by a pump, a part of the materials return to the top of the dehydration tower 10 as reflux, and the other part of the materials are extracted as wastewater.
The bottom outlet of the dehydration column 10 is connected to the feed inlet of the regeneration column 14 through a pipeline. The tower bottom of the regeneration tower 14 is provided with a regeneration tower reboiler 15, and the tower top is provided with a regeneration tower condenser 16. The regeneration tower 14 is provided with a feed inlet, a tower top extraction outlet, a tower top reflux outlet and a tower bottom extraction outlet, the tower top extraction outlet of the regeneration tower 14 is connected with the inlet of the regeneration tower condenser 16 through a pipeline, the outlet of the regeneration tower condenser 16 is connected with the inlet of the regeneration tower reflux tank 17, and the outlet of the regeneration tower reflux tank 17 is connected with the tower top reflux outlet through a pump. The shell side inlet of the regeneration tower reboiler 15 is connected with a steam ST pipeline, and the shell side outlet is connected with a steam condensate RW pipeline. The shell side inlet of the regeneration tower condenser 16 is connected with a circulating cooling water feeding CWS pipeline, and the shell side outlet is connected with a circulating cooling water backwater CWR pipeline.
The tower bottom material of the dehydration tower 10 is conveyed to a regeneration tower 14 through a pump, and the regeneration tower 14 is provided with a regeneration tower reboiler 15, and steam is used as a reboiler heat source; the regeneration tower 14 is a vacuum tower, the tower top pressure is-90 kpa-normal pressure, the tower top temperature is 70-100 ℃, and the tower bottom temperature is 160-190 ℃; the gas phase at the top of the regeneration tower 14 enters a regeneration tower condenser 16 to be condensed, the condensed liquid enters a regeneration tower reflux tank 17, the materials in the regeneration tower reflux tank 17 are conveyed by a pump, a part of the materials return to the top of the regeneration tower 14 as reflux, and the other part of the materials are extracted as heavy components; the extractant at the bottom of the regeneration tower 14 is conveyed by a pump, enters the extraction tower heat exchange reboiler 6 for heat exchange and cooling, and is recycled at the middle upper part of the return extraction tower 5.
The foregoing is merely a preferred embodiment of the present utility model, and it should be noted that it will be apparent to those skilled in the art that variations and modifications can be made without departing from the scope of the utility model.
Claims (8)
1. A process system for producing isopropyl alcohol by extractive distillation, comprising: the light component removing device comprises a light component removing tower (1), an extraction tower (5), a dehydrating tower (10) and a regenerating tower (14) which are sequentially connected, wherein an extraction tower heat exchange reboiler (6) is arranged at the tower kettle of the extraction tower (5), an extractant feeding port is arranged at the upper part of the extraction tower (5), a tower bottom extraction port of the regenerating tower (14) is connected with a shell side inlet of the extraction tower heat exchange reboiler (6) through a pipeline, and a shell side outlet of the extraction tower heat exchange reboiler (6) is connected with an extractant feeding port of the extraction tower (5) through a pipeline.
2. The process system for preparing isopropanol by extraction and rectification according to claim 1, wherein a light component removing tower reboiler (2) is arranged at the tower bottom of the light component removing tower (1), and a light component removing tower condenser (3) is arranged at the tower top.
3. The process system for preparing isopropanol by extraction and rectification according to claim 1 or 2, wherein an extraction tower steam reboiler (7) is arranged at the tower bottom of the extraction tower (5), and an extraction tower condenser (8) is arranged at the tower top.
4. A process system for preparing isopropanol by extraction and rectification as claimed in claim 3, wherein a dehydration tower reboiler (11) is arranged at the tower bottom of the dehydration tower (10), and a dehydration tower condenser (12) is arranged at the tower top.
5. The process system for preparing isopropanol by extraction and rectification according to claim 1 or 2, wherein a dehydration tower reboiler (11) and a dehydration tower condenser (12) are arranged at the tower bottom and the tower top of the dehydration tower (10).
6. The process system for preparing isopropanol by extraction and rectification according to claim 1 or 2, wherein a regeneration tower reboiler (15) is arranged at the tower bottom of the regeneration tower (14), and a regeneration tower condenser (16) is arranged at the tower top.
7. The process system for preparing isopropanol by extraction and rectification as claimed in claim 4, wherein a regeneration tower reboiler (15) is arranged at the tower bottom of the regeneration tower (14), and a regeneration tower condenser (16) is arranged at the tower top.
8. The process system for preparing isopropanol by extraction and rectification according to claim 1, wherein the light component removing tower (1) is an atmospheric tower, and the regenerating tower (14) is a vacuum tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321269558.0U CN219815330U (en) | 2023-05-24 | 2023-05-24 | Process system for preparing isopropanol by extraction and rectification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321269558.0U CN219815330U (en) | 2023-05-24 | 2023-05-24 | Process system for preparing isopropanol by extraction and rectification |
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| Publication Number | Publication Date |
|---|---|
| CN219815330U true CN219815330U (en) | 2023-10-13 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321269558.0U Active CN219815330U (en) | 2023-05-24 | 2023-05-24 | Process system for preparing isopropanol by extraction and rectification |
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| Country | Link |
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| CN (1) | CN219815330U (en) |
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2023
- 2023-05-24 CN CN202321269558.0U patent/CN219815330U/en active Active
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