System for extractive distillation of isopropanol and water
An extractive distillation system consisting of an azeotropic tower, a distillation tower, and a recovery tower, combined with a heat exchange device, solves the problem of efficient separation of high-water-content isopropanol wastewater, achieving energy saving, consumption reduction, and efficient recovery of isopropanol.
Patent Information
- Application Number
- CN202422602801.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-10-28
- Publication Date
- 2025-11-07
- Estimated Expiration
- 2034-10-28
AI Technical Summary
Existing technologies are insufficient for efficiently separating industrial wastewater with high water content of isopropanol, and the introduction of additional heating or cooling systems increases equipment costs.
An extractive distillation system consisting of an azeotropic tower, a rectification tower, and a recovery tower, combined with a heat exchanger, is used to initially separate wastewater through the azeotropic tower, and further separate isopropanol through the rectification tower and the recovery tower. The heat is reused by the heat exchanger, thereby reducing energy consumption.
It achieves efficient separation of isopropanol with high water content, reduces equipment costs, saves energy consumption, and improves isopropanol recovery efficiency.
Smart Images
Figure CN223522322U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to the separation and purification technical field of chemical industry, especially relates to a system of extractive distillation of isopropyl alcohol and water. BACKGROUND
[0002] Isopropyl alcohol has a wide range of uses as an organic raw material and solvent. Among them, isopropyl alcohol is an indispensable component of semiconductor manufacturing, mainly used for cleaning of precision electronic components such as chips, liquid crystals, magnetic heads, printed circuit boards, etc. In addition, due to the compatibility of isopropyl alcohol and water, the mixture of isopropyl alcohol and water is often used for cleaning, which can improve the cleaning effect. A large amount of industrial wastewater containing isopropyl alcohol needs to be recovered and treated. On the one hand, due to the azeotropy of isopropyl alcohol and water, especially the high water content (60wt%-80wt%) in the isopropyl alcohol industrial wastewater generated by the semiconductor industry, it is difficult to obtain high-purity isopropyl alcohol by ordinary distillation; on the other hand, in the actual extractive distillation process, it is necessary to additionally introduce a heating system or a cooling system to preheat the feed material temperature or cool the discharge material, so that the heating system or the cooling system needs to be additionally introduced, which increases the equipment investment cost. SUMMARY
[0003] To solve the above technical problems, the utility model provides a system of extractive distillation of isopropyl alcohol and water, which can efficiently extract and distill isopropyl alcohol industrial wastewater with high water content.
[0004] The technical scheme of the utility model is:
[0005] A system of extractive distillation of isopropyl alcohol and water, characterized by comprising
[0006] An azeotropic tower, a azeotropic tower feed inlet is arranged in the middle of the azeotropic tower, the azeotropic tower feed inlet is communicated with a raw liquid feed pipeline, and a wastewater pipeline is communicated with the bottom of the azeotropic tower;
[0007] The top of the azeotropic tower is communicated with the middle of a rectifying tower, an extractant input pipeline is arranged in the upper segment of the rectifying tower, a finished product collection pipeline is arranged at the top of the rectifying tower, and the bottom of the rectifying tower is communicated with the middle of a recovery tower;
[0008] The bottom of the recovery tower is communicated with an extractant recovery pipeline, the extractant recovery pipeline is communicated with a heat exchange device, the heat exchange device is respectively communicated with the extractant input pipeline and the raw liquid feed pipeline, and the raw liquid feed pipeline is communicated with the azeotropic tower feed inlet through the heat exchange device.
[0009] Further, a first condensing device is arranged above the azeotropic tower, the inlet of the first condensing device is communicated with the top of the azeotropic tower, and the outlet of the first condensing device is communicated with the middle of the rectifying tower.
[0010] Further, the azeotrope tower is provided with a first reboiler below, which is communicated with the bottom and middle part of the azeotrope tower through a circulating pipeline.
[0011] Further, the rectification tower is provided with a second condensing device above, which is communicated with the top end of the rectification tower, and the second condensing device is communicated with the product collecting pipeline.
[0012] Further, the rectification tower is provided with a second reboiler below, which is communicated with the bottom and middle part of the rectification tower through a circulating pipeline.
[0013] Further, the recovery tower is provided with a third condensing device above, which is communicated with the top of the recovery tower, and the third condensing device is communicated with the raw liquid feeding pipeline.
[0014] Further, the recovery tower is provided with a third reboiler below, which is communicated with the bottom and middle part of the recovery tower through a circulating pipeline.
[0015] Further, the heat exchange device comprises a first heat exchanger and a second heat exchanger.
[0016] The first heat exchanger is provided with a first channel and a second channel, the extractant recovery pipeline is communicated with the first channel of the first heat exchanger, the first channel of the first heat exchanger is communicated with the second heat exchanger, and the second heat exchanger is communicated with the extractant input pipeline.
[0017] The raw liquid feeding pipeline is communicated with the second channel of the first heat exchanger, and the second channel of the first heat exchanger is communicated with the azeotrope tower feeding port.
[0018] The beneficial technical effects of the utility model are:
[0019] Firstly, the utility model discloses azeotrope tower before rectification tower, and the azeotrope tower is used for the primary rectification of isopropyl alcohol and water industrial wastewater, so as to reduce the water content in isopropyl alcohol and water industrial wastewater, and provide further extraction rectification basis for more efficient extraction rectification isopropyl alcohol.
[0020] Secondly, the utility model discloses heat exchange device, which can cool the tower bottom material of recovery tower, preheat isopropyl alcohol and water industrial wastewater simultaneously, make the heat of recovery tower bottom material be fully reused, and save energy and reduce consumption. DRAWINGS
[0021] Figure 1 It is the whole schematic diagram of the utility model.
[0022] Among them:
[0023] 100 - azeotrope column, 101 - raw liquid feeding pipeline, 200 - rectification column, 300 - recovery column, 400 - waste water pipeline, 401 - extractant input pipeline, 402 - product collection pipeline, 403 - extractant recovery pipeline, 404 - azeotrope column top pipeline, 405 - rectification column bottom pipeline, 501 - first condensing device, 502 - second condensing device, 503 - third condensing device, 601 - first reboiler, 602 - second reboiler, 603 - third reboiler, 700 - isopropyl alcohol product tank, 701 - extractant storage tank, 801 - first heat exchanger, 802 - second heat exchanger, 901 - first reflux tank, 902 - second reflux tank, 903 - third reflux tank. DETAILED DESCRIPTION
[0024] In order to make the technical means of the utility model more clearly understood, and can be implemented according to the content of the specification, the specific embodiments of the utility model are further described in detail below in conjunction with the drawings and examples, the following examples are used to illustrate the utility model, but not to limit the scope of the utility model.
[0025] As shown in Figure 1 The utility model provides a kind of system of extracting rectification isopropyl alcohol and water, it is applicable to the industrial wastewater extraction rectification of isopropyl alcohol and water, especially applicable to the industrial wastewater extraction rectification of extracting high water content isopropyl alcohol and water.
[0026] For more efficient extraction rectification high water content isopropyl alcohol and water of industrial wastewater, the utility model is equipped with azeotrope column 100 before rectification column 200, which is used for the preliminary rectification of isopropyl alcohol and water of industrial wastewater, to reduce the water content in isopropyl alcohol and water of industrial wastewater.
[0027] Azeotrope column 100 middle part is equipped with azeotrope column feed port, raw liquid feeding pipeline 101 is communicated with azeotrope column feed port, and isopropyl alcohol and water of industrial wastewater enter azeotrope column 100 by raw liquid feeding pipeline 101. Azeotrope column 100 bottom is equipped with waste water pipeline 400, and waste water pipeline 400 is connected with sewage treatment system. Azeotrope column 100 below is equipped with first reboiler 601, and first reboiler 601 is communicated with azeotrope column 100 bottom and middle part by circulation pipeline, which is used for providing heat source for material liquid in azeotrope column, to ensure that gas-liquid phase balance in the column. Azeotrope column 100 upper part is equipped with first condensing device 501, and the inlet of first condensing device 501 is communicated with the top of azeotrope column 100, and the outlet of first condensing device 501 is communicated with the inlet of first reflux tank 901, and the outlet of first reflux tank 901 is respectively communicated with azeotrope column top pipeline 404 and the top of azeotrope column 100;Azeotrope column top pipeline 404 is communicated with the middle part of rectification column 200.
[0028] Further, the wastewater pipeline 400 is communicated with a power pump, which is used for pumping the azeotropic column 100 bottom material into the sewage treatment system. The first reflux tank 901 is communicated with a power pump below, which is used for pumping the azeotropic column top material in the first reflux tank 901 into the azeotropic column top pipeline 404, so as to facilitate the azeotropic column top material into the rectifying column 200.
[0029] The upper end of the rectifying column 200 is connected with an extractant feeding port, one end of the extractant input pipeline 401 is communicated with the extractant feeding port, and the other end is communicated with the extractant storage tank 701. The extractant is placed in the extractant storage tank 701 and enters the rectifying column 200 through the extractant input pipeline 401. The upper end of the rectifying column 200 is provided with a second condensing device 502, the inlet of the second condensing device 502 is communicated with the top end of the rectifying column 200, the outlet of the second condensing device 502 is communicated with the second reflux tank 902, the outlet of the second reflux tank 902 is respectively communicated with the top end of the rectifying column 200 and the product collection pipeline 402, and the product collection pipeline 402 is communicated with the isopropanol product tank 700. The rectifying column 200 is provided with a second reboiler 602 below, and the second reboiler 602 is communicated with the bottom and middle part of the rectifying column 200 through a circulating pipeline, which is used for providing heat source for the material liquid in the rectifying column 200, so as to ensure the gas-liquid phase balance in the column. The bottom of the rectifying column 200 is communicated with the rectifying column bottom pipeline 403, and the rectifying column bottom pipeline 403 is communicated with the middle part of the recovery column 300.
[0030] Further, a power pump is arranged on the circulating pipeline communicated with the second reboiler 602, the extractant input pipeline 401, the product collection pipeline 402 and the rectifying column bottom pipeline 403, so as to facilitate the material flow in the above-mentioned pipeline and pipeline.
[0031] The middle part of the recovery column 300 is provided with a recovery column feeding port, the rectifying column bottom pipeline 403 is communicated with the recovery column feeding port, and the bottom material of the rectifying column 200 enters the recovery column 300 through the rectifying column bottom pipeline 403. The recovery column 300 is provided with a third reboiler 603 below, and the third reboiler 603 is communicated with the bottom and middle part of the recovery column 300 through a circulating pipeline, which is used for providing heat source for the material liquid in the recovery column 300, so as to ensure the gas-liquid phase balance in the column. The bottom of the recovery column 300 is communicated with the extractant recovery pipeline 403, the extractant recovery pipeline 403 is communicated with the heat exchange device, and the heat exchange device is respectively communicated with the extractant storage tank 701 and the raw liquid feeding pipeline 101.
[0032] Specifically, the heat exchange device comprises a first heat exchanger 801 and a second heat exchanger 802. The first heat exchanger 801 is provided with a first channel and a second channel, the extractant recovery pipeline 403 is communicated with the first channel of the first heat exchanger 801, the first channel of the first heat exchanger 801 is communicated with the second heat exchanger 802, and the second heat exchanger 802 is communicated with the extractant storage tank 701. The tower bottom material of the recovery tower 300 flows into the extractant storage tank 701 in sequence through the first channel of the first heat exchanger 801 and the second heat exchanger 802 through the extractant recovery pipeline 403. The above-mentioned raw liquid feeding pipeline 101 is communicated with the second channel of the first heat exchanger 801, and the second channel of the first heat exchanger 801 is communicated with the azeotrope tower feeding port, that is, the industrial wastewater of isopropyl alcohol and water flows through the second channel of the first heat exchanger 801 firstly through the raw liquid feeding pipeline 101, and the industrial wastewater exchanges heat with the extractant in the first channel of the first heat exchanger 801 and then flows into the azeotrope tower 100. The first heat exchanger 801 can not only cool the tower bottom material of the recovery tower, but also preheat the raw material, so that the heat of the tower bottom material of the recovery tower is fully reused, and energy consumption is reduced. The second heat exchanger 802 makes the temperature of the tower bottom material of the recovery tower lower, so as to facilitate the safe recovery of the tower bottom material.
[0033] The third condensing device 503 is arranged above the recovery tower 300, the inlet of the third condensing device 503 is communicated with the top of the recovery tower 300, the outlet of the third condensing device 503 is communicated with the third reflux tank 903, and the outlet of the third reflux tank 903 is respectively communicated with the top of the recovery tower 300 and the raw liquid feeding pipeline 101, that is, the tower top material of the recovery tower 300 is combined with the industrial wastewater of isopropyl alcohol and water, enters the azeotrope tower 100 through the raw liquid feeding pipeline 101 and the second channel of the first heat exchanger 801 to participate in extractive rectification, so that the isopropyl alcohol in the industrial wastewater is fully utilized.
[0034] Further, power pumps are arranged at the circulating pipeline communicated with the third reboiler 603, the extractant recovery pipeline 403 and the outlet end of the third reflux tank 903, so as to facilitate the flow of materials in the above-mentioned pipelines and pipelines.
[0035] The operation process of the utility model is as follows:
[0036] S1. The industrial wastewater of isopropyl alcohol and water is fed into the azeotropic column 100 through the raw material feeding pipeline 101 and the second passage of the first heat exchanger 801. After separation in the azeotropic column 100, the wastewater is obtained at the bottom of the azeotropic column 100 and is fed into the sewage treatment system through the wastewater pipeline 400. The azeotrope of isopropyl alcohol and water with a lower water content compared with the above-mentioned industrial wastewater is obtained at the top of the azeotropic column 100. The azeotrope of isopropyl alcohol and water is fed into the first reflux tank 901 through the first condensing device 501. Part of the azeotrope of isopropyl alcohol and water in the first reflux tank 901 flows into the azeotrope top pipeline 404 and then into the rectifying column 200 for rectification. The other part returns to the top of the azeotropic column 100 to keep the liquid composition on the column tray stable.
[0037] S2. The extractant in the extractant storage tank 701 is fed into the rectifying column 200 through the extractant input pipeline 401 to separate the azeotrope of isopropyl alcohol and water in step S1. The extractant is ethylene glycol. After separation in the rectifying column 200, the rectified isopropyl alcohol is obtained at the top of the rectifying column 200. The isopropyl alcohol is fed into the second reflux tank 902 through the second condensing device 502. Part of the isopropyl alcohol in the second reflux tank 902 is stored in the isopropyl alcohol product tank 700 through the product collection pipeline 402. The other part of the isopropyl alcohol returns to the top of the rectifying column 200 to keep the liquid composition on the column tray stable. The mixture of extractant and water is obtained at the bottom of the rectifying column 200 and is fed into the recovery column 300 through the rectifying column bottom pipeline 405.
[0038] S3. The mixture of extractant and water in step S2 is subjected to extractant recovery in the recovery column 300. The extractant is obtained at the bottom of the recovery column 300 and is fed into the first passage of the first heat exchanger 801, the second heat exchanger 802, and then the extractant storage tank 701 through the extractant recovery pipeline 403. On the one hand, the extractant is recycled. On the other hand, the extractant in the first passage of the first heat exchanger 801 is used as the heat source of the first passage to exchange heat with the industrial wastewater in the second passage of the first heat exchanger 801. The preheated industrial wastewater enters the azeotropic column 100 to save energy.
[0039] The overhead of the recovery column 300 is water containing a small amount of isopropyl alcohol. The water containing a small amount of isopropyl alcohol is fed into the third reflux tank 903 through the third condensing device 503. Part of the water containing a small amount of isopropyl alcohol in the third reflux tank 903 is combined with the isopropyl alcohol and water in the raw material feeding pipeline 101 to participate in the extractive rectification to make full use of the isopropyl alcohol in the industrial wastewater.
[0040] The above merely is preferred implementation manner of the present application, and is not used for limiting the present application, it should be pointed out, for ordinary skilled person in the technical field, on the premise of not departing from the technical principle of the present application, can also make several improvements and variations, these improvements and variations also should be regarded as the protection scope of the present application.
Claims
1. A system for extractive distillation of isopropyl alcohol and water, characterized in that, The application relates to a distillation device for extracting and recycling an extractant. The distillation device comprises azeotropic tower (100), which is provided with an azeotropic tower feed port in the middle part and is connected with a raw liquid feed pipeline (101); the bottom of the azeotropic tower (100) is connected with a waste water pipeline (400); The top of the azeotropic tower (100) is connected with the middle part of a rectifying tower (200), the upper part of the rectifying tower (200) is provided with an extractant input pipeline (401), the top of the rectifying tower (200) is provided with a product collection pipeline (402), and the bottom of the rectifying tower (200) is connected with the middle part of a recovery tower (300); The bottom of the recovery tower (300) is connected with an extractant recovery pipeline (403), the extractant recovery pipeline (403) is connected with a heat exchange device, the heat exchange device is respectively connected with the extractant input pipeline (401) and the raw liquid feed pipeline (101), and the raw liquid feed pipeline (101) is connected with the azeotropic tower feed port through the heat exchange device.
2. The system for extractive distillation of isopropyl alcohol and water according to claim 1, characterized in that, The top of the azeotropic tower (100) is provided with a first condensing device (501), the inlet of the first condensing device (501) is connected with the top of the azeotropic tower (100), and the outlet of the first condensing device (501) is connected with the middle part of the rectifying tower (200).
3. The system for extractive distillation of isopropyl alcohol and water according to claim 1, characterized in that, The bottom of the azeotropic tower (100) is provided with a first reboiler (601), and the first reboiler (601) is connected with the bottom and middle part of the azeotropic tower (100) through a circulating pipeline.
4. The system for extractive distillation of isopropyl alcohol and water according to claim 1, characterized in that, The top of the rectifying tower (200) is provided with a second condensing device (502), the inlet of the second condensing device (502) is connected with the top end of the rectifying tower (200), and the outlet of the second condensing device (502) is connected with the product collection pipeline (402).
5. The system for extractive distillation of isopropyl alcohol and water according to claim 1, wherein, The bottom of the rectifying tower (200) is provided with a second reboiler (602), and the second reboiler (602) is connected with the bottom and middle part of the rectifying tower (200) through a circulating pipeline.
6. The system for extractive distillation of isopropyl alcohol and water according to claim 1, wherein, The top of the recovery tower (300) is provided with a third condensing device (503), the inlet of the third condensing device (503) is connected with the top of the recovery tower (300), and the outlet of the third condensing device (503) is connected with the raw liquid feed pipeline (101).
7. The system for extractive distillation of isopropyl alcohol and water according to claim 1, wherein, The bottom of the recovery tower (300) is provided with a third reboiler (603), and the third reboiler (603) is connected with the bottom and middle part of the recovery tower (300) through a circulating pipeline.
8. The system for extractive distillation of isopropyl alcohol and water according to claim 1, characterized in that, The heat exchange device comprises a first heat exchanger (801) and a second heat exchanger (802); The first heat exchanger (801) is provided with a first channel and a second channel, the extractant recovery pipeline (403) is connected with the first channel of the first heat exchanger (801), the first channel of the first heat exchanger (801) is connected with the second heat exchanger (802), and the second heat exchanger (802) is connected with the extractant input pipeline (401); The raw liquid feed pipeline (101) is connected with the second channel of the first heat exchanger (801), and the second channel of the first heat exchanger (801) is connected with the azeotropic tower feed port.