Low-energy desulfurization methods

Abstract

This invention relates to the field of gas purification technology and discloses a low-energy desulfurization method: (1) acidic gas and foaming liquid are contacted in a microbubble generator to generate microbubbles, resulting in a gas-liquid mixture; wherein the foaming liquid includes ultrafine particles and complexed iron desulfurization liquid I, the particle size of which is 10-100 μm; (2) the mixture and complexed iron desulfurization liquid II are contacted counter-currently in an absorption tower to undergo an oxidation-reduction reaction, resulting in purified gas and desulfurized rich liquid; (3) the desulfurized rich liquid and air are oxidized and regenerated in an oxidation regeneration tank to obtain regenerated gas, regenerated lean liquid, and regenerated sulfur slurry; (4) the regenerated sulfur slurry is separated in a separator to obtain sulfur and filtrate; the regenerated lean liquid and / or filtrate are returned to the absorption tower for recycling. The low-energy desulfurization method provided in this invention can improve the bubble effect of the microbubble generator, reduce the impact energy consumption of the microbubble generator, improve the mass transfer efficiency of the absorption tower, and help reduce desulfurization energy consumption.

Description

Technical Field

[0001] This invention belongs to the field of gas purification technology, specifically relating to a low-energy desulfurization method. Background Technology

[0002] The complexed iron desulfurization technology is a wet oxidation method for removing hydrogen sulfide using complexed iron as a catalyst. The desulfurizing agent containing complexed iron comes into contact with acidic gas containing hydrogen sulfide. Under the action of iron ions, oxygen in the air is used to oxidize the hydrogen sulfide into elemental sulfur. Examples include the LO-CAT process and the SulFerox process.

[0003] This method is a novel desulfurization technology that is simple in process, has high sulfur capacity, and is environmentally friendly and non-toxic. It overcomes the drawbacks of traditional desulfurization processes, such as low sulfur capacity, complex desulfurization process, high by-product salt formation rate, and serious environmental pollution. After purification, the sulfur dioxide content in the flue gas after combustion is reduced to 20 mg / Nm³. 3 It can meet the ever-increasing environmental protection standards.

[0004] The desulfurization effect of this method is closely related to the mixing effect of the desulfurizing agent and the acidic gas. Gas-liquid phase mixing generally suffers from low mass transfer efficiency. Process intensification technology can obtain a certain amount of micron-sized bubbles through mechanical crushing, fluid impaction, and ultrasound, which helps to increase the mass transfer area and the overall mass transfer rate between gas and liquid, thereby significantly improving the gas-liquid phase mixing effect.

[0005] One process intensification technology is the use of microbubble generators. However, microbubble generators require a certain amount of energy to generate bubbles through high-speed collisions between the gas and liquid phases. They generally suffer from drawbacks such as high outlet pressure of the circulating pump, high energy consumption, and large pressure losses in the reaction liquid and feed gas.

[0006] Therefore, there is an urgent need to provide a low-energy desulfurization method that can improve mass transfer efficiency and desulfurization effect. Summary of the Invention

[0007] The purpose of this invention is to overcome the problems of low mass transfer efficiency, large reactor volume, and high energy consumption of impinging flow microbubble generator in the existing complex iron desulfurization technology, and to provide a low-energy desulfurization method.

[0008] To achieve the above objectives, the present invention provides a low-energy desulfurization method, wherein the method includes the following steps:

[0009] (1) Acidic gas and foaming liquid are brought into contact in a microbubble generator to generate microbubbles, thereby obtaining a gas-liquid mixture; wherein the foaming liquid includes ultrafine particles and complexed iron desulfurization liquid I, and the particle size of the ultrafine particles is 10-100μm;

[0010] (2) The mixture and complexed iron desulfurization liquid II are brought into countercurrent contact in the absorption tower to undergo a redox reaction, resulting in purified gas and desulfurized rich liquid;

[0011] (3) The desulfurized rich liquid is oxidized and regenerated with air in an oxidation regeneration tank to obtain regenerated gas, regenerated lean liquid and regenerated sulfur slurry;

[0012] (4) The regenerated sulfur slurry is separated in a separator to obtain sulfur and filtrate; wherein the regenerated lean liquid and / or filtrate is returned to the absorption tower for recycling.

[0013] The beneficial technical effects achieved by the present invention through the above technical solution are as follows:

[0014] 1) The low-energy desulfurization method provided in this invention can utilize ultrafine particles to change the surface tension of the solution to form stable bubbles, which can not only reduce the outlet pressure of the circulating pump and reduce the impact energy consumption of the microbubble generator, but also significantly improve the foaming effect of the microbubble generator, increase the mass transfer area in the absorption tower, improve the mass transfer efficiency, improve the absorption effect, and realize the recovery of sulfur resources.

[0015] 2) The low-energy desulfurization method provided in this invention has a small pressure difference between the gas-liquid mixture and the complexed iron desulfurization liquid II, and a small countercurrent contact resistance, which can reduce the operating energy consumption of the absorption tower.

[0016] 3) The low-energy desulfurization method provided in this invention can significantly reduce the equipment size, floor space, and production costs by setting the microbubble generator inside the absorption tower;

[0017] 4) The low-energy desulfurization method provided in this invention has a small equipment footprint, low energy consumption, and high desulfurization efficiency. It is suitable for industrial promotion and can be used in the removal of hydrogen sulfide and sulfur recovery processes in coal gas, natural gas and refinery gas. Attached Figure Description

[0018] Figure 1 This is a process flow diagram of the low-energy desulfurization method provided by the present invention.

[0019] Explanation of reference numerals in the attached figures

[0020] Detailed Implementation

[0021] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0022] This invention provides a low-energy desulfurization method, wherein the method includes the following steps:

[0023] (1) Acidic gas and foaming liquid are brought into contact in a microbubble generator to generate microbubbles, thereby obtaining a gas-liquid mixture; wherein the foaming liquid includes ultrafine particles and complexed iron desulfurization liquid I, and the particle size of the ultrafine particles is 10-100μm;

[0024] (2) The mixture and complexed iron desulfurization liquid II are brought into countercurrent contact in the absorption tower to undergo a redox reaction, resulting in purified gas and desulfurized rich liquid;

[0025] (3) The desulfurized rich liquid is oxidized and regenerated with air in an oxidation regeneration tank to obtain regenerated gas, regenerated lean liquid and regenerated sulfur slurry;

[0026] (4) The regenerated sulfur slurry is separated in a separator to obtain sulfur and filtrate; wherein the regenerated lean liquid and / or filtrate is returned to the absorption tower for recycling.

[0027] In step (1):

[0028] In some embodiments of the present invention, the acidic gas is a gas containing hydrogen sulfide, wherein the content of the hydrogen sulfide is 1-30 g / Nm³. 3 Preferably 5-10 g / Nm 3 .

[0029] In some embodiments of the present invention, the particle size of the ultrafine particles may be 10, 15, 20, 25, 30, 35, 40, 45, 50, 55, 60, 65, 70, 75, 80, 85, 90, 95, 100 μm, or any number between these values, preferably 20-60 μm.

[0030] In this invention, if the particle size of the ultrafine particles is too large, the generated bubbles are prone to coalescing into large, easily ruptured bubbles; if the particle size of the ultrafine particles is too small, the liquid viscosity of the gas-liquid mixture increases, easily leading to foaming and liquid carryover in the absorption tower. The desulfurization effect is optimal when the particle size of the ultrafine particles is between 20-60 μm.

[0031] In some embodiments of the present invention, the ultrafine particles are sulfur and / or ferrous sulfide, preferably sulfur.

[0032] In this invention, the added sulfur can be separated from the sulfur generated during the regeneration process by a separator. Ferrous sulfide can be oxidized into iron ions during the regeneration process, which will not have an adverse effect on the complexed iron desulfurization liquid.

[0033] In some embodiments of the present invention, the complexed iron desulfurization liquid I is the complexed iron desulfurization liquid disclosed in CN1168526C (removal of sulfides from gas by complexed iron method) or CN1354038A (removal of sulfides from gas by modified complexed iron method).

[0034] In this invention, there is no special limitation on the complexed iron desulfurization liquid I. All complexed iron desulfurization liquids known in the art can be used in this invention, such as the complexed iron desulfurization liquids disclosed in CN1168526C or CN1354038A.

[0035] In some embodiments of the present invention, the content of the ultrafine particles in the foaming liquid is 1-6 g / L, preferably 2.5-4 g / L.

[0036] In this invention, excessive ultrafine particulate matter content leads to an excessively high gas content in the gas-liquid mixture, which can easily cause foaming and liquid carryover in the absorption tower. Conversely, insufficient ultrafine particulate matter content results in low mass transfer efficiency and poor desulfurization effect in the absorption tower. When the ultrafine particulate matter content is preferably between 2.5-4 g / L, optimal mass transfer efficiency and desulfurization effect can be achieved while avoiding liquid carryover in the absorption tower.

[0037] In some embodiments of the present invention, the ratio of the acidic gas to the foaming liquid is 1 Nm. 3 : 1-3.5L, preferably 1Nm 3 : 1.5-2.5L.

[0038] In some embodiments of the present invention, the contact time between the acidic gas and the foaming liquid is 5-30 seconds, preferably 15-25 seconds.

[0039] In some embodiments of the present invention, the microbubble generator includes a foam generator and a circulation pump; wherein the foam generator is disposed inside the absorption tower and located at the lower end of the absorption tower; and the circulation pump is disposed outside the absorption tower.

[0040] In this invention, the bubble generator of the microbubble generator can be located outside or inside the absorption tower, preferably inside the absorption tower. Placing the bubble generator of the microbubble generator inside the absorption tower, at its lower end, can significantly reduce the equipment size, decrease the floor space required, and lower production costs.

[0041] In some embodiments of the present invention, the circulation rate of the circulating pump is 5-15 L / h, preferably 8-12 L / h.

[0042] In this invention, by controlling the amount of ultrafine particles added and / or the circulation rate of the circulating pump, the foaming effect of the microbubble generator can be adjusted, thereby maximizing the desulfurization effect while avoiding liquid buildup in the absorber.

[0043] In some embodiments of the present invention, the outlet pressure of the circulating pump is 50-150 kPa, preferably 80-120 kPa.

[0044] In this invention, by adding ultrafine particles, the outlet pressure of the circulating pump in the microbubble generator can be significantly reduced, enabling the microbubble generator to achieve good foaming effect at a lower pressure. At the same time, the pressure difference between the gas-liquid mixture and the absorption tower can be reduced, resistance can be minimized, and energy consumption for desulfurization can be further reduced.

[0045] In step (2):

[0046] In some embodiments of the present invention, the complexed iron desulfurization liquid II is the same as the complexed iron desulfurization liquid I.

[0047] In this invention, the complexed iron desulfurization liquid is divided into two parts, which are labeled as complexed iron desulfurization liquid I and complexed iron desulfurization liquid II for ease of description. Complexed iron desulfurization liquid I is used to mix with ultrafine particles to form a foaming liquid, so as to carry the ultrafine particles from the circulation pump pipeline into the microbubble generator. Complexed iron desulfurization liquid II is sprayed from the top of the absorption tower and comes into countercurrent contact with the mixture from the microbubble generator for absorbing hydrogen sulfide.

[0048] In some embodiments of the present invention, based on 1Nm 3 The acidic gas, the amount of the complexed iron desulfurization liquid II is 10-30L, preferably 15-25L.

[0049] In some embodiments of the present invention, the operating conditions of the absorption tower include: an absorption temperature of 30-50°C, preferably 40-45°C, and an absorption pressure of 10-80 kPa, preferably 20-50 kPa.

[0050] In this invention, the foaming liquid is first introduced into a microbubble generator to contact the acidic gas, and then countercurrently contacted with the complexed iron desulfurization liquid II. This significantly improves the mass transfer efficiency of the absorption tower and substantially enhances the desulfurization effect of hydrogen sulfide, resulting in a hydrogen sulfide content in the purified gas ≤20 mg / Nm³. 3 For example, the hydrogen sulfide content in the purified gas can be 0-20 mg / Nm³. 3 .

[0051] In step (3):

[0052] In some embodiments of the present invention, based on 1Nm3 The acidic gas, wherein the air consumption ratio is 100-250L, preferably 150-200L.

[0053] In some embodiments of the present invention, the operating conditions of the regeneration tower include: a regeneration temperature of 30-50°C, preferably 40-45°C; and a regeneration pressure of 2-10 kPa, preferably 4-6 kPa.

[0054] In step (4):

[0055] In some embodiments of the present invention, the separator includes a filter and / or a centrifuge, preferably a filter.

[0056] In this invention, the ultrafine particles introduced by the foaming liquid can serve as sulfur crystal nuclei to enrich the sulfur generated during the regeneration process. The sulfur generated during regeneration is adsorbed on the surface of the ultrafine particles, which helps to improve the separation effect of sulfur in the regenerated sulfur slurry. The obtained filtrate can be mixed with the regenerated lean liquor and returned to the absorption tower for recycling, or used to prepare the foaming liquid.

[0057] The present invention will be described in detail below through embodiments.

[0058] Examples and comparative examples are in Figure 1 The process flow of the low-energy desulfurization method shown is as follows: the microbubble generator 2 includes a bubble generator 21 and a circulating pump 22. The bubble generator is installed inside the absorption tower and is located in the bottom of the absorption tower. The circulating pump is installed outside the absorption tower. The volume of the bubble generator is 5.8L.

[0059] The bottom of the absorption tower 1 is connected in sequence to the rich liquid pump 3, the oxidation regeneration tank 4, the slurry pump 5, and the filter 6. The filter 6 is connected to the top of the absorption tower 1 in sequence through the replenishment pump 7, the oxidation regeneration tank 4, and the feed pump 8.

[0060] Acidic gas: H2S content is 6.2 g / Nm³. 3 The CO2 content is 5% (v / v), and the balance gas is nitrogen.

[0061] Example 1

[0062] (1) Acidic gas at 1.2 Nm 3 The acidic gas enters the microbubble generator at a flow rate of 2.5 L / h, while the foaming liquid enters the microbubble generator through its self-circulation pipeline. The acidic gas and the foaming liquid contact in the microbubble generator for 21 seconds to generate microbubbles, resulting in a gas-liquid mixture. The foaming liquid is a sulfur-containing complexed iron desulfurization liquid with an average sulfur particle size of 20 μm and a mass content of 3.2 g / L. The outlet pressure of the circulation pump is 100 kPa, and the circulation flow rate is 10 L / h.

[0063] (2) The above gas-liquid mixture leaves the microbubble generator and enters the absorption tower, where it comes into countercurrent contact with the complexed iron desulfurization liquid injected from the top of the absorption tower at a flow rate of 20 L / h. The mixture undergoes an oxidation-reduction reaction at 40℃ and 40 kPa to obtain purified gas and desulfurized rich liquid.

[0064] (3) The above-mentioned desulfurization rich liquid is discharged from the bottom of the absorption tower and then enters the oxidation regeneration tank, where it comes into contact with the air entering the regeneration tower at a flow rate of 180 L / h and undergoes an oxidation regeneration reaction at 42°C and 4 kPa to obtain regeneration gas, regeneration lean liquid and regeneration sulfur slurry.

[0065] (4) The above-mentioned regenerated sulfur slurry is first introduced into the filter for filtration to obtain sulfur and filtrate; the obtained filtrate is returned to the regeneration oxidation tank and returned to the absorption tower together with the regenerated lean liquid for recycling.

[0066] After 48 hours of operation, the gas content in the gas-liquid mixture leaving the microbubble generator was 37.9%, as measured by a conductivity probe. The hydrogen sulfide content in the purified gas extracted from the top of the absorption tower was 5 mg / Nm³. 3 .

[0067] Example 2

[0068] Similar to Example 1, except that the average particle size of sulfur in the foaming liquid is 60 μm and the mass content is 2.5 g / L; the foaming liquid enters the microbubble generator through the self-circulation pipeline of the microbubble generator at a flow rate of 1.8 L / h, the contact time between acid gas and foaming liquid is 25 s; the outlet pressure of the circulation pump is 120 kPa and the circulation flow rate is 8 L / h.

[0069] After 48 hours of operation, the gas content in the gas-liquid mixture leaving the microbubble generator was 36.4%, as measured by a conductivity probe. The hydrogen sulfide content in the purified gas extracted from the top of the absorption tower was 7 mg / Nm³. 3 .

[0070] Example 3

[0071] Similar to Example 1, except that the average particle size of sulfur in the foaming liquid is 40 μm and the mass content is 4.0 g / L. The foaming liquid enters the microbubble generator through the self-circulation pipeline of the microbubble generator at a flow rate of 3.0 L / h. The contact time between the acid gas and the foaming liquid is 15 s. The outlet pressure of the circulation pump is 80 kPa and the circulation flow rate is 12 L / h.

[0072] After 48 hours of operation, the gas content in the gas-liquid mixture leaving the microbubble generator was 34.7%, as measured by a conductivity probe. The hydrogen sulfide content in the purified gas extracted from the top of the absorption tower was 10 mg / Nm³. 3 .

[0073] Example 4

[0074] Similar to Example 1, except that the foaming liquid is a complexed iron desulfurization liquid containing ferrous sulfide, the average particle size of ferrous sulfide is 10 μm, and the mass content is 5 g / L; the foaming liquid enters the microbubble generator through the self-circulation pipeline of the microbubble generator at a flow rate of 1.2 L / h, the contact time between the acid gas and the foaming liquid is 10 s; the outlet pressure of the circulation pump is 150 kPa, and the circulation flow rate is 15 L / h.

[0075] After 48 hours of operation, the gas content in the gas-liquid mixture leaving the microbubble generator was 33.1%, as measured by a conductivity probe, and the hydrogen sulfide content in the purified gas extracted from the top of the absorption tower was 15 mg / Nm³. 3 .

[0076] Example 5

[0077] Similar to Example 1, except that the average particle size of sulfur in the foaming liquid is 80 μm and the mass content is 1.5 g / L. The foaming liquid enters the microbubble generator through the self-circulation pipeline of the microbubble generator at a flow rate of 3.6 L / h. The contact time between the acid gas and the foaming liquid is 30 s. The outlet pressure of the circulation pump is 70 kPa and the circulation flow rate is 5 L / h.

[0078] After 48 hours of operation, the gas content in the gas-liquid mixture leaving the microbubble generator was 31.7%, as measured by a conductivity probe. The hydrogen sulfide content in the purified gas extracted from the top of the absorption tower was 19 mg / Nm³. 3 .

[0079] Comparative Example 1

[0080] Same as Example 4, except that the foaming liquid is omitted.

[0081] After 48 hours of operation, the gas content in the gas-liquid mixture leaving the microbubble generator was 16%, as measured by a conductivity probe, and the hydrogen sulfide content in the purified gas extracted from the top of the absorption tower was 78 mg / Nm³. 3 .

[0082] Among them, by comparing Example 4 and Comparative Example 1, it can be seen that the microbubble generator has a poor foaming effect when the outlet pressure of the circulating pump is low.

[0083] Comparative Example 2

[0084] Similar to Example 4, except that the foaming liquid is omitted and the outlet pressure of the circulating pump is 300 kPa.

[0085] After 48 hours of operation, the gas content in the gas-liquid mixture leaving the microbubble generator was 33.4%, as measured by a conductivity probe. The hydrogen sulfide content in the purified gas extracted from the top of the absorption tower was 15 mg / Nm³.3 .

[0086] As shown in Comparative Example 4 and Comparative Example 2, adding ultrafine particles to the microbubble generator can achieve a similar foaming effect under low pressure as under high pressure. This indicates that ultrafine particles can significantly reduce the impact energy consumption of the microbubble generator, reduce the pressure difference between the gas-liquid mixture and the absorption tower, and help reduce the energy consumption of the desulfurization process.

[0087] Comparative Example 3

[0088] Similar to Example 4, except that the mass content of ferrous sulfide in the foaming liquid is 8 g / L.

[0089] After 48 hours of operation, the gas content in the gas-liquid mixture leaving the microbubble generator was 42.7%, as measured by a conductivity probe. The hydrogen sulfide content in the purified gas extracted from the top of the absorption tower was 48 mg / Nm³. 3 1.5 L / h of desulfurization liquid is carried out in the purified gas.

[0090] By comparing Example 4 and Comparative Example 3, it can be seen that when the solid content in the foaming liquid is 8g / L, the gas content in the gas-liquid mixture is greater than 40%, resulting in too many bubbles in the absorption tower, causing liquid to overflow in the absorption tower and poor desulfurization effect.

[0091] Comparative Example 4

[0092] Similar to Example 4, except that the particle size of ferrous sulfide in the foaming liquid is 120 μm.

[0093] After 48 hours of operation, the gas content in the gas-liquid mixture leaving the microbubble generator was 25%, as measured by a conductivity probe, and the hydrogen sulfide content in the purified gas extracted from the top of the absorption tower was 57 mg / Nm³. 3 .

[0094] By comparing Example 4 and Comparative Example 4, it can be seen that adding solid particles with large particle size results in low gas content of the gas-liquid mixture, large bubbles, and poor desulfurization effect.

[0095] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A low-energy desulfurization method, characterized in that, The method includes the following steps: (1) Acidic gas and foaming liquid are brought into contact in a microbubble generator to generate microbubbles, thereby obtaining a gas-liquid mixture; wherein the foaming liquid includes ultrafine particles and complexed iron desulfurization liquid I, and the particle size of the ultrafine particles is 10-100μm; (2) The mixture and complexed iron desulfurization liquid II are brought into countercurrent contact in the absorption tower to undergo a redox reaction, resulting in purified gas and desulfurized rich liquid; (3) The desulfurized rich liquid is oxidized and regenerated with air in an oxidation regeneration tank to obtain regenerated gas, regenerated lean liquid and regenerated sulfur slurry; (4) The regenerated sulfur slurry is separated in a separator to obtain sulfur and filtrate; The regenerated lean liquid and / or filtrate are returned to the absorption tower for recycling. The ultrafine particles are sulfur and / or ferrous sulfide; The ratio of acidic gas to foaming liquid is 1 Nm. 3 : 1-3.5L; Among them, based on 1Nm 3 The acidic gas, the amount of the complexed iron desulfurization liquid II is 10-30L; The content of the ultrafine particles is 1-6 g / L.

2. The method according to claim 1, wherein, The acidic gas is a gas containing hydrogen sulfide.

3. The method according to claim 2, wherein, The hydrogen sulfide content is 1-30 g / Nm³. 3 .

4. The method according to claim 3, wherein, The hydrogen sulfide content is 5-10 g / Nm³. 3 .

5. The method according to claim 1, wherein, The particle size of the ultrafine particles is 20-60 μm.

6. The method according to claim 1, wherein, The ultrafine particles are sulfur.

7. The method according to claim 1, wherein, The content of the ultrafine particles is 2.5-4 g / L.

8. The method according to claim 1, wherein, The ratio of the acidic gas to the foaming liquid is 1 Nm. 3 : 1.5-2.5L.

9. The method according to claim 1, wherein, The contact time between the acidic gas and the foaming liquid is 5-30 seconds.

10. The method according to claim 9, wherein, The contact time between the acidic gas and the foaming liquid is 15-25 seconds.

11. The method according to any one of claims 1-10, wherein, The microbubble generator includes a foam generator and a circulation pump; wherein the foam generator is disposed inside the absorption tower and located at the lower end of the absorption tower; and the circulation pump is disposed outside the absorption tower.

12. The method according to claim 11, wherein, The circulation pump has a circulation flow rate of 5-15 L / h.

13. The method according to claim 12, wherein, The circulation pump has a circulation rate of 8-12 L / h.

14. The method according to claim 11, wherein, The outlet pressure of the circulating pump is 50-150 kPa.

15. The method according to claim 14, wherein, The outlet pressure of the circulating pump is 80-120 kPa.

16. The method according to any one of claims 1-10, wherein, The complexed iron desulfurization solution II is the same as the complexed iron desulfurization solution I.

17. The method according to claim 1, wherein, Based on 1Nm 3 The acidic gas, the amount of the complexed iron desulfurization liquid II is 15-25L.

18. The method according to claim 1, wherein, The operating conditions of the absorption tower include: absorption temperature of 30-50℃ and absorption pressure of 10-80 kPa.

19. The method according to claim 18, wherein, The operating conditions of the absorption tower include: absorption temperature of 40-45℃ and absorption pressure of 20-50 kPa.

20. The method according to claim 1, wherein, Based on 1Nm 3 The acidic gas, wherein the air consumption ratio is 1:5-15L.

21. The method according to claim 20, wherein, Based on 1Nm 3 The acidic gas, wherein the air consumption ratio is 1:8-12L.

22. The method according to claim 1, wherein, The operating conditions of the oxidation regeneration tank include: regeneration temperature of 30-50℃ and regeneration pressure of 2-10 kPa.

23. The method according to claim 22, wherein, The operating conditions of the oxidation regeneration tank include: regeneration temperature of 40-45℃ and regeneration pressure of 4-6 kPa.

24. The method according to claim 1, wherein, The separator includes a filter and / or a centrifuge.

25. The method according to claim 24, wherein, The separator is a filter.

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