A device for improving ion liquid circulation efficiency

Abstract

The utility model discloses a device that improves ion liquid circulation efficiency, which comprises: a heat exchanger, which is connected with the lean liquid pipeline of a desulfurization system, so that part of the lean liquid after cooling can enter the heat exchanger for further heat exchange and cooling; a crystallization kettle, which is connected with the heat exchanger, so that the lean liquid after cooling can enter the crystallization kettle; a water-cooled screw rod low-temperature brine unit, which is connected with the heat exchange pipe in the crystallization kettle through a cooling water pipeline, and performs heat exchange and cooling on the lean liquid in the crystallization kettle; and a centrifugal machine, which is connected with the bottom outlet of the crystallization kettle through an inlet end. The utility model utilizes the freezing method to desalt and produce sodium sulfate, which not only solves the problem of low absorption efficiency, but also has certain economic benefits, and provides a scheme for the treatment of ion liquid desalination.

Description

Technical Field

[0001] This utility model relates to the field of smelting equipment technology, and in particular to a device for improving the circulation efficiency of ionic liquid. Background Technology

[0002] High-concentration sulfur dioxide flue gas generated during smelting processes is used for acid production. Methods for treating low-concentration sulfur dioxide flue gas include the limestone method, caustic soda method, activated coke method, ionic liquid method, sodium citrate absorption and desorption method, and ammonia method. However, the ionic liquid method for treating sulfur dioxide flue gas suffers from problems such as a continuous decrease in pH value and low absorption efficiency due to the recycling of the ionic liquid. This necessitates the addition of alkali to raise the pH value, leading to the continuous accumulation of sodium salts. Timely removal of sodium sulfate is then required to ensure stable system operation. To address this issue, a cryogenic desalination method is proposed to produce sodium sulfate. This method solves the problem of low absorption efficiency and offers certain economic benefits, providing a solution for ionic liquid desalination. Utility Model Content

[0003] To address the aforementioned technical problems, this utility model provides a device for improving the circulation efficiency of ionic liquids.

[0004] To achieve the above objectives, the technical solution of this utility model is as follows:

[0005] An apparatus for improving the efficiency of ionic liquid circulation, comprising:

[0006] The heat exchanger is connected to the lean liquid pipeline of the desulfurization system, so that some of the cooled lean liquid enters the heat exchanger for further heat exchange and cooling.

[0007] The crystallization vessel is connected to a heat exchanger, allowing the cooled lean liquor to enter the crystallization vessel.

[0008] The water-cooled screw low-temperature brine unit has its cooling water pipeline connected to the heat exchange tubes inside the crystallizer to exchange heat and cool down the lean liquor in the crystallizer.

[0009] The centrifuge's inlet is connected to the bottom outlet of the crystallizer.

[0010] The heat exchanger is connected to the lean liquid pipeline of the desulfurization system via valve one.

[0011] The crystallization vessel is equipped with a stirrer.

[0012] This utility model also includes:

[0013] An underground storage tank, the inlet of which is connected to the lean liquid outlet of a centrifuge;

[0014] The lean liquid storage tank is connected to an underground storage tank via a submersible pump at its inlet end.

[0015] The valves and the transfer pump are sequentially installed at the bottom outlet of the lean liquor storage tank. The transfer pump is connected to the lean liquor inlet of the absorption tower of the desulfurization system and enters the circulation system.

[0016] The beneficial effects of this invention are as follows: When removing sodium sulfate, the lean liquid, after being cooled by the lean-rich liquid heat exchanger, enters the heat exchanger again for further cooling before entering the crystallization kettle. Cold water produced by the water-cooled screw chiller is introduced into the heat exchange tubes in the crystallization kettle to cool the lean liquid. Under stirring, the sodium sulfate in the lean liquid in the crystallization kettle gradually crystallizes, forming sodium sulfate crystals. After cooling and crystallization in the crystallization kettle, the lean liquid enters a centrifuge for solid-liquid separation. The separated sodium sulfate crystals are sold externally, and the lean liquid is pumped into a lean liquid storage tank for later use. This invention, through the installation of a refrigeration unit, heat exchanger, crystallizer, centrifuge, etc., deeply removes sulfate ions from the lean liquid, ensuring the normal operation of the system. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of the present invention.

[0018] Among them, 1-Absorption tower, 2-Lean liquor inlet, 3-Flue gas inlet, 4-Liquid distribution device one, 5-Foam eliminator one, 6-Gas outlet, 7-Rich liquor pump, 8-Lean and rich liquor heat exchanger, 9-Lean liquor pump, 10-Regeneration tower, 11-Liquid distribution device two, 12-Foam eliminator two, 13-Flue gas outlet, 14-Valve one, 15-Valve two, 16-Underground storage tank, 17-Submersible pump, 18-Sodium sulfate, 19-Centrifuge, 20-Water-cooled screw cryogenic brine unit, 21-Crystallization kettle, 22-Heat exchange tube, 23-Agitator, 24-Heat exchanger, 25-Cooling water inlet, 26-Cooling water outlet, 27-Lean liquor storage tank, 28-Valve three, 29-Transfer pump. Detailed Implementation

[0019] To make the objectives, technical solutions, and advantages of this utility model clearer, the present utility model will be further described in detail below with reference to specific embodiments. It should be understood that these descriptions are merely exemplary and not intended to limit the scope of this utility model. Furthermore, descriptions of well-known structures and technologies are omitted in the following description to avoid unnecessarily obscuring the concept of this utility model.

[0020] like Figure 1As shown, a device for improving the efficiency of ion liquid circulation includes: a heat exchanger 24 connected to the lean liquid pipeline of the desulfurization system, allowing a portion of the cooled lean liquid to enter the heat exchanger 24 for further heat exchange and cooling; a crystallization vessel 21 connected to the heat exchanger 24, allowing the cooled lean liquid to enter the crystallization vessel 21; a water-cooled screw chiller unit 20, whose cooling water pipeline is connected to the heat exchange tube 22 inside the crystallization vessel 21, for heat exchange and cooling of the lean liquid in the crystallization vessel 21; and a centrifuge 19, with its inlet end connected to the bottom outlet of the crystallization vessel 21. The heat exchanger 24 is connected to the lean liquid pipeline of the desulfurization system via valve 14. A stirrer 23 is installed inside the crystallization vessel 21. This utility model also includes: an underground storage tank 16, the inlet of which is connected to the lean liquid outlet of the centrifuge 19; a lean liquid storage tank 27, the inlet of which is connected to the underground storage tank 16 via a submersible pump 17; a valve 28 and a transfer pump 29 are sequentially arranged at the bottom outlet of the lean liquid storage tank 27, and the transfer pump 29 is connected to the lean liquid inlet 2 of the absorption tower 1 of the desulfurization system and enters the circulation system.

[0021] When the desulfurization system is running, close valve 14, open valve 2 15, and start the rich liquid pump 7 and lean liquid pump 9. Flue gas enters the absorption tower 1 through the flue gas inlet 3. Inside the absorption tower 1, the flue gas comes into countercurrent contact with the ion-liquid lean liquid from the distribution device 4, absorbing sulfur dioxide from the flue gas. After the sulfur dioxide flue gas is absorbed by the ion-liquid lean liquid, the ion-liquid lean liquid is converted into ion-liquid rich liquid, which falls to the bottom of the absorption tower 1 and is pumped into the lean-rich liquid heat exchanger 8 by the rich liquid pump 7. After the rich liquid is heated by heat exchange in the lean-rich liquid heat exchanger 8, the ion-liquid... The rich liquid enters the distribution device 2 11 of the regeneration tower 10. The rich ionic liquid distributed by the distribution device 2 11 undergoes desorption within the regeneration tower 10, removing sulfur dioxide. After being demined by the demister 2 12, the sulfur dioxide is discharged from the flue gas outlet 13 and enters the next process. The lean ionic liquid falls to the bottom of the regeneration tower 10 and is pumped by the lean liquid pump 9 into the lean-rich liquid heat exchanger 8. After being cooled by heat exchange in the lean-rich liquid heat exchanger 8, the lean ionic liquid enters the distribution device 1 4 of the absorption tower 1 for continued circulation. When the flue gas concentration at the flue gas inlet 3 increases sharply or becomes too high, insufficient desorption in the regeneration tower 10 may occur, leading to a rapid drop in the pH value of the lean liquid, a decrease in absorption efficiency, and a risk of excessive sulfur dioxide emissions. To address sudden increases in inlet sulfur dioxide concentration, liquid alkali needs to be added to the ionic liquid to quickly raise the pH value and ensure that the flue gas meets emission standards. As the ionic liquid is recycled, sodium salts accumulate, requiring periodic removal of sodium sulfate to ensure stable system operation.

[0022] During sodium sulfate removal, valves 14 and 15 are adjusted. According to the production process parameters, a portion of the lean liquor after cooling enters heat exchanger 24 for further heat exchange and cooling before entering crystallization kettle 21. The water-cooled screw chiller unit 20 is turned on, and the cold water produced by the water-cooled screw chiller unit enters heat exchange tube 22 to cool the lean liquor in crystallization kettle 21. Under the stirring of stirrer 23, the sodium sulfate in the lean liquor in crystallization kettle 21 gradually crystallizes to form sodium sulfate crystals. After the lean liquor completes cooling and crystallization in crystallization kettle 21, it enters centrifuge 19 for solid-liquid separation. The separated sodium sulfate crystals 18 are sold externally, and the lean liquor enters underground storage tank 16. It is then pumped into lean liquor storage tank 27 by submersible pump 17 for later use. When lean liquor needs to be replenished, valve 3 28 is opened, and transfer pump 29 is turned on to send the lean liquor from lean liquor inlet 2 into absorption tower 1, which then enters the circulation system.

[0023] The cold water produced by the water-cooled screw low-temperature brine unit 20 enters the crystallization kettle 21 to exchange heat and cool down the lean liquid in the crystallization kettle 21, so that the sodium sulfate in the lean liquid gradually crystallizes to form sodium sulfate crystals.

[0024] It should be understood that the specific embodiments described above are merely illustrative or explanatory of the principles of this utility model and do not constitute a limitation thereof. Therefore, any modifications, equivalent substitutions, improvements, etc., made without departing from the spirit and scope of this utility model should be included within its protection scope. Furthermore, the appended claims are intended to cover all variations and modifications falling within the scope and boundaries of the appended claims, or equivalent forms of such scope and boundaries.

Claims

1. A device for improving the circulation efficiency of ionic liquids, characterized in that, include: The heat exchanger (24) is connected to the lean liquid pipeline of the desulfurization system, so that some of the cooled lean liquid enters the heat exchanger (24) for further heat exchange and cooling. The crystallization vessel (21) is connected to the heat exchanger (24) so ​​that the cooled lean liquid can enter the crystallization vessel (21). The water-cooled screw low-temperature brine unit (20) has its cooling water pipeline connected to the heat exchange tube (22) in the crystallizer (21) to exchange heat and cool the lean liquid in the crystallizer (21); The inlet of the centrifuge (19) is connected to the bottom outlet of the crystallizer (21).

2. The device for improving the circulation efficiency of ionic liquid according to claim 1, characterized in that, The heat exchanger (24) is connected to the lean liquid pipeline of the desulfurization system via valve one (14).

3. The device for improving the circulation efficiency of ionic liquid according to claim 1, characterized in that, A stirrer (23) is installed inside the crystallization vessel (21).

4. The device for improving the circulation efficiency of ionic liquid according to claim 1, characterized in that, Also includes: The inlet of the underground storage tank (16) is connected to the lean liquid outlet of the centrifuge (19); The lean liquid storage tank (27) is connected to the underground storage tank (16) via a submersible pump (17) at its inlet end; Valve 3 (28) and transfer pump (29) are sequentially installed at the bottom outlet of lean liquid storage tank (27). Transfer pump (29) is connected to lean liquid inlet (2) of absorption tower (1) of desulfurization system and enters the circulation system.

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