Oxidation reaction extraction device for producing hydrogen peroxide

Abstract

The utility model relates to an oxidation reaction extraction device for producing hydrogen peroxide, which comprises an oxidation extraction tower, an oxidation liquid separator, an extraction tower, a coalescer and a dehydrator, the top of the oxidation extraction tower is provided with a hydrogenation liquid inlet for introducing hydrogenation liquid to be oxidized from the tower top, and the lower part of the oxidation extraction tower is provided with an oxygen-containing gas inlet for introducing oxygen-containing gas from the tower bottom; a dilute hydrogen peroxide inlet is formed in the middle-lower part of the tower body and positioned above the oxygen-containing gas inlet, and is used for introducing a dilute hydrogen peroxide for extraction from the middle-lower part of the tower body, so that an oxidation extraction process of whole-tower countercurrent oxidation and tower-bottom parallel flow extraction is formed; according to the scheme provided by the utility model, high oxidation efficiency, high extraction efficiency and low extraction back mixing can be ensured at the same time.

Description

TECHNICAL FIELD

[0001] The utility model relates to the field of hydrogen peroxide prepared by anthraquinone method, concretely relates to an oxidation reaction extraction device for producing hydrogen peroxide. BACKGROUND

[0002] Hydrogen peroxide is an important inorganic chemical raw material, which is widely used in papermaking, textile, chemical industry, environmental protection and electronic component manufacturing and many other fields. At present, the method for producing hydrogen peroxide in industry is anthraquinone method, which uses alkyl anthraquinone dissolved in mixed organic solvent as the carrier for cyclic hydrogenation and oxidation, and a certain concentration of hydrogen peroxide is obtained through a series of processes such as hydrogenation, oxidation, extraction and post-treatment.

[0003] The existing oxidation tower for producing hydrogen peroxide by anthraquinone method is mostly two or three sections, and hydrogenation liquid and compressed air are contacted in parallel in the tower and oxidation reaction occurs. Such oxidation tower has the following problems: (1) due to serious back mixing in the oxidation tower, and the oxygen concentration in the air and the hydrogen anthraquinone concentration in the oxidation liquid at the tower discharge end are both at a low concentration, the reaction speed is very slow, so the general oxidation yield is low. (2) the oxidation tail gas of such oxidation tower is generally at a high temperature, which has a safety hazard. (3) due to the water contained in the air or hydrogenation liquid, and the self-decomposition of hydrogen peroxide obtained by oxidation reaction, there is oxidation residual liquid at the bottom of the oxidation tower, which needs to be discharged regularly, and the operation is complicated and has a safety hazard.

[0004] The existing extraction tower needs to be provided with a very large number of trays to meet the separation requirement due to the very small density difference between water and oil, and the tray efficiency is very low. The oil phase outlet of the extraction tower has a high extraction residue, and a vacuum dehydration device needs to be provided, and if the water separation of the extraction tower is not good, there is a great safety risk, and the energy consumption is also increased.

[0005] CN106672911A discloses a process in which oxidation liquid and oxygen-containing gas are contacted in parallel in an oxidation extraction tower, and are extracted with extraction agent in countercurrent, which realizes the functions of both oxidation reaction and extraction in the oxidation extraction tower. Although this method achieves a certain integration in oxidation and extraction functions, due to serious back mixing, the oxidation efficiency is not high, and the working liquid after extraction has a high extraction residue, which cannot be directly returned to the upstream hydrogenation, and there is no obvious advantage.

[0006] CN204265444U discloses a vapor-liquid countercurrent reactor for producing hydrogen peroxide, in which oxidation liquid and oxygen-containing gas are contacted in countercurrent in the tower, and compared with parallel reaction scheme, countercurrent contact can effectively improve the mass transfer efficiency of the reactor; but this scheme only focuses on the oxidation process, and does not mention how to further integrate the extraction and purification steps.

[0007] CN217868137U discloses an anthraquinone method for preparing hydrogen peroxide oxidation system, which also discloses the oxidation scheme of countercurrent contact of oxidation liquid and oxygen-containing gas in the oxidation tower, and the patent also mentions that the obtained oxidation liquid is sent to the extraction tower for extraction after vapor-liquid separation. However, the patent does not disclose the specific extraction process, and does not give a solution to the serious backmixing defect in the existing extraction process.

[0008] Therefore, how to organically combine the oxidation process and the extraction process of the anthraquinone method for preparing hydrogen peroxide system, while ensuring high mass transfer reaction efficiency and low extraction backmixing rate, so as to efficiently prepare high-purity hydrogen peroxide has become a problem to be solved in the field. SUMMARY

[0009] In view of the shortcomings of the prior art, the utility model aims at providing an oxidation reaction extraction device for producing hydrogen peroxide, which integrates the oxidation reaction and the extraction process, has very high oxidation yield and extraction efficiency, and directly obtains high-concentration hydrogen peroxide without increasing the concentration device.

[0010] Specifically, the utility model provides an oxidation reaction extraction device for producing hydrogen peroxide, which comprises an oxidation extraction tower 15, an oxidation liquid separator 16, an extraction tower 17 and a coalescer 19, wherein the oxidation extraction tower 15 adopts countercurrent oxidation and concurrent extraction, is provided with a hydrogenation liquid inlet 1 at the top for introducing hydrogenation liquid to be oxidized from the top of the tower, is provided with an oxygen-containing gas inlet 2 at the lower part for introducing oxygen-containing gas from the bottom of the tower, is provided with a hydrogen peroxide diluent inlet 4 at the middle lower part and above the oxygen-containing gas inlet 2 for introducing hydrogen peroxide diluent for extraction from the middle lower part of the tower body, the oxidation liquid and the hydrogen peroxide diluent flow from top to bottom in the oxidation extraction tower 15, and the oxygen-containing gas flows from bottom to top in the oxidation extraction tower 15, so as to form an oxidation extraction process of countercurrent oxidation throughout the tower and concurrent extraction at the bottom. The top of the oxidation extraction tower 15 is provided with a medium-pressure tail gas outlet 3 for discharging medium-pressure oxidation tail gas.

[0011] The bottom of the oxidation extraction tower 15 is provided with a concentrated oxidation liquid outlet 5 connected to the oxidation liquid separator 16 through a pipeline; the oxidation liquid separator 16 is a phase separation device, has a box-shaped structure as a whole, is provided with an overflow partition plate inside, and is provided with a water phase outlet 6 and an oil phase outlet 7 on the two sides of the overflow partition plate respectively; the water phase outlet 6 is located at the bottom of the oxidation liquid separator 16 and is used for discharging hydrogen peroxide concentrate after oil-water separation; the oil phase outlet 7 is connected to the bottom of the extraction tower 17 through a pipeline and is used for sending the dilute oxidation liquid after oil-water separation to the extraction tower 17; the top of the oxidation liquid separator 16 is also provided with an oxidation tail gas outlet.

[0012] As the extraction agent running to the bottom of the oxidation extraction column 15, the hydrogen peroxide has reached the highest concentration, at this time, the reverse mixing of the extraction process has the greatest impact on the extraction efficiency. The utility model discloses the concentrated oxidizing liquid outlet 5 is arranged below the oxygen-containing gas inlet 2, which can further eliminate the extraction reverse mixing phenomenon caused by gas disturbance, and ensure the extraction efficiency in the oxidation extraction column 15.

[0013] The top of the extraction column 17 is provided with an extraction agent inlet 9 for inputting the pure water extraction agent added with a stabilizing agent into the extraction column 17; the bottom of the extraction column 17 is provided with a hydrogen peroxide dilution outlet connected to the hydrogen peroxide dilution inlet 4 in the middle and lower parts of the oxidation extraction column 15, and a hydrogen peroxide dilution pump 18 is arranged on the pipeline; the top of the extraction column 17 is provided with a second oxidation tail gas outlet, which is jointly collected with the aforementioned oxidation tail gas outlet into the low-pressure oxidation tail gas pipe 8; the sidewall of the top of the extraction column 17 is provided with a raffinate outlet 10 connected to the coalescer 19 through a pipeline; the coalescer 19 is internally provided with a coalescing filter element, and the filter element is made of at least one of fluoropolymer or polyphenylene sulfide; the coalescer 19 is provided with a drain port 11 and a working liquid outlet 12 for respectively discharging water and working liquid generated after the coalescing treatment of the raffinate.

[0014] Further comprising a dehydrator 20 having a containing cavity connected to the aforementioned working liquid outlet 12 through a pipeline to receive the working liquid discharged from the coalescer 19; meanwhile, the outlet end of the low-pressure oxidation tail gas pipe 8 extends into the bottom of the containing cavity and is immersed below the liquid level of the working liquid; the top of the dehydrator 20 is provided with a tail gas outlet 14, and the bottom is provided with a dehydrated working liquid outlet 13. The working liquid from which most of the water is removed by the coalescer 19 is in contact with the oxidation tail gas from the low-pressure oxidation tail gas pipe 8 in the dehydrator 20 to further remove the water carried by the working liquid through stripping.

[0015] The oxidation extraction column 15 is a plate column, and the number of trays is 8.

[0016] The extraction column 7 is a plate column, and the number of trays is 15, and a polymeric material grid or woven mesh is arranged below the trays, and the polymeric material is at least one of polypropylene or fluoropolymer.

[0017] The aforementioned oxidation reaction extraction device for producing hydrogen peroxide can be operated by the following method, specifically including the following steps:

[0018] (1) introducing the hydrogenation liquid from the top of the oxidation extraction column 15 and introducing the oxygen-containing gas 2 from the bottom of the oxidation extraction column 15, which are countercurrently contacted in the oxidation extraction column 15 and continuously generate hydrogen peroxide through oxidation reaction.

[0019] (2) Step (1) is performed while adding dilute hydrogen peroxide to the middle and lower part of the oxidation extraction column 15, and the hydrogen peroxide produced by the reaction is gradually extracted into the water phase.

[0020] (3) The concentrated oxidation liquid at the bottom of the oxidation extraction column 15 is introduced into the oxidation liquid separator 16 to separate the water and oil phases, the water phase is taken out at the outlet 6 as concentrated hydrogen peroxide, and the dilute oxidation liquid is introduced into the bottom of the extraction column 17 at the outlet 7.

[0021] (4) The pure water and dilute oxidation liquid added with a stabilizer are countercurrently contacted in the extraction column 17, the dilute hydrogen peroxide is obtained at the bottom of the extraction column 17, and is sent to the dilute hydrogen peroxide inlet 4 of the oxidation extraction column 15 after being pressurized by the dilute hydrogen peroxide pump 18; the raffinate is obtained at the top of the extraction column 17, and is sent to the coalescer 19 for coalescence and dehydration.

[0022] (5) The raffinate is separated from the entrained water in the coalescer 19, and the oxidation liquid in the oxidation liquid separator 16 and the extraction column 17 is sent to the dehydration device 20 through the low-pressure oxidation tail gas pipe 8 to perform bubbling, and the remaining water in the working liquid is taken away.

[0023] The tail gas discharged from the dehydration device 20 is sent to a tail gas treatment device, and the dehydrated working liquid is returned to the upstream hydrogenation reactor.

[0024] In the oxidation extraction process of the utility model, the hydrogenation liquid, the oxygen-containing gas and the dilute hydrogen peroxide enter the oxidation extraction column 15 at the same time. The hydrogenation liquid and the dilute hydrogen peroxide are contacted in the middle and lower part of the oxidation extraction column 15 and then perform co-current extraction, and the hydrogenation liquid and the oxygen-containing gas are countercurrently contacted in the whole column of the oxidation extraction column 15 (not considering the vapor-liquid contact mode of the column segment below the oxygen-containing gas inlet 2) to perform the oxidation reaction and the extraction process.

[0025] The hydrogenation efficiency (the hydrogen peroxide content of the unit volume of the hydrogenation liquid after oxidation) of the hydrogenation liquid fed into the oxidation extraction column 15 is 6-20 g / L, the oxygen concentration of the oxygen-containing gas is 20-100 vol%, and the concentration of the dilute hydrogen peroxide is 26-36 wt%.

[0026] The oxidation yield of the oxidation extraction column 15 is 96-98%. The operating pressure of the oxidation extraction column 15 is 0.2-1.0 MPaG, and the operating temperature is 45-58℃.

[0027] The residence time of the water-oil phase separation in the oxidation liquid separator 16 is 2-15 minutes, the concentration of the water phase is 33-43 wt%, and the content of the hydrogen peroxide in the oil phase is 6-10 g / L.

[0028] The oxidation liquid separator 16 and the extraction column 7 are in gas communication, and the operating pressure is 0.03-0.25 MPaG.

[0029] The dehydrator 20 uses the low-pressure oxidation tail gas discharged from the oxidizing liquid separator 16 and the extraction tower 7 to remove residual water in the working liquid, the flow ratio of the tail gas to the working liquid entering the dehydrator 20 is 1:20-1:5 (v / v%), the water content in the dehydrated working liquid discharged from the dehydrator 20 is 300-3000 ppm. The operating pressure of the dehydrator 20 is 0.005-0.1 MPaG, and the operating temperature is 45-55 DEG C.

[0030] The working liquid is a mixed liquid of alkylanthraquinone, heavy aromatic hydrocarbon and polar solvent. The alkylanthraquinone is at least one of 2-ethylanthraquinone, 2-butylanthraquinone and 2-pentylanthraquinone. The polar solvent is at least one of trioctyl phosphate, 2-methylcyclohexyl acetate, tetrabutyl urea and diisobutyl carbinol.

[0031] Compared with the prior art, the utility model has at least the following beneficial effects:

[0032] The utility model discloses a whole tower countercurrent oxidation plus front section countercurrent extraction and rear section concurrent extraction operation, wherein, compared with traditional concurrent oxidation process, whole tower countercurrent oxidation can greatly improve mass transfer driving force, improve oxidation efficiency, and then reduce the number of trays required for oxidation tower, front section countercurrent extraction operation can make the extraction agent and the to-be-extracted stream fully turbulent contact, and high mass transfer driving force of countercurrent extraction ensures that the front section extraction process has high extraction efficiency, although countercurrent extraction inevitably produces obvious back mixing, but since the hydrogen peroxide concentration in the extraction agent is low during the front section extraction process, and there is no discharge requirement (referring to no need to output extraction product), the negative influence of back mixing is limited, and in the extraction rear section, since there is discharge requirement, and the hydrogen peroxide concentration in the extraction agent is already very high at this time, small degree of back mixing also has great influence on the concentration of hydrogen peroxide in the discharge, based on this, the utility model creatively adopts the combined oxidation extraction process of whole tower countercurrent oxidation plus front section countercurrent extraction plus rear section concurrent extraction, simultaneously ensuring high oxidation efficiency, high extraction efficiency and low extraction back mixing influence, introducing hydrogen peroxide diluent into the oxidation tower can quickly transfer the generated hydrogen peroxide from the oil phase to the water phase, which is beneficial to promoting the progress of the oxidation reaction, on the other hand, can also greatly reduce the load of the downstream extraction tower, thus allowing to use smaller size extraction tower, after the hydrogenation liquid is subjected to countercurrent oxidation and concurrent extraction, and then is subjected to water-oil phase separation in the oxidizing liquid separator, high-concentration hydrogen peroxide can be directly produced, without additional concentration device, thereby reducing energy consumption, and reducing the safety risk of high-concentration hydrogen peroxide heating decomposition during concentration. The utility model adopts pressurized extraction, and the separation efficiency is higher, and the tail gas released under reduced pressure is used as the stripping feed gas of the dehydrator, which can take out the water in the working liquid, reduces the energy consumption, and also makes the production process safer. BRIEF DESCRIPTION OF DRAWINGS

[0033] Figure 1Schematic diagram of the oxidation extraction process for producing hydrogen peroxide.

[0034] In the figure: 1. hydrogenated liquid inlet, 2. oxygen-containing gas inlet, 3. medium-pressure oxidation tail gas, 4. hydrogen peroxide diluent inlet, 5. concentrated oxidation liquid outlet, 6. water phase outlet, 7. oil phase outlet, 8. low-pressure oxidation tail gas pipe, 9. pure water with stabilizer added to the extractant inlet, 10. raffinate outlet, 11. coalescer water discharge, 12. dewatered raffinate, 13. stripped raffinate outlet, 14. tail gas outlet, 15. oxidation extraction column, 16. oxidation liquid separator, 17. extraction column, 18. hydrogen peroxide diluent pump, 19. coalescer, 20. dewaterer. Specific embodiments

[0035] The technical solutions of the present application are described below with specific examples, but the scope of protection of the present application is not limited to this.

[0036] Example 1

[0037] Based on the oxidation reaction extraction device as described above, the diameter of the oxidation extraction column 15 is 600 mm, the height is 10 m, and the number of trays is 8; the diameter of the oxidation liquid separator 16 is 600 mm, and the length is 3 m; the diameter of the extraction column 7 is 600 mm, the height is 12 m, and the number of trays is 15; the diameter of the coalescer 19 is 600 mm, and the length is 3 m; the diameter of the dewaterer 20 is 800 mm, and the height is 2 m. The flow rate of the hydrogenated liquid is 5 m 3 / h, the hydrogenation efficiency is 6.5 g / L, and the oxygen-containing gas is 140 Nm 3 / h. The operating pressure of the oxidation extraction column is 0.3 MPaG, and the operating temperature is 45-55°C. The results show that the oxidation yield of the oxidation extraction column 15 is 97.2%, the concentrated hydrogen peroxide output by the oxidation liquid separator 16 is 33 wt%, and the water content of the working liquid output by the dewaterer 20 is 2300 ppm.

[0038] Example 2

[0039] Based on the oxidation reaction extraction device as described above, the diameter of the oxidation extraction column 15 is 600 mm, the height is 10 m, and the number of trays is 8; the diameter of the oxidation liquid separator 16 is 600 mm, and the length is 3 m; the diameter of the extraction column 7 is 600 mm, the height is 12 m, and the number of trays is 15; the diameter of the coalescer 19 is 600 mm, and the length is 3 m; the diameter of the dewaterer 20 is 800 mm, and the height is 2 m. The flow rate of the hydrogenated liquid is 5 m 3 / h, the hydrogenation efficiency is 8 g / L, and the oxygen-containing gas is 173 Nm 3The operating pressure of the oxidation extraction column is 0.3 MPaG, and the operating temperature is 45-55°C. The results show that the oxidation yield of the oxidation extraction column is about 96%, the concentrated hydrogen peroxide output by the oxidation liquid separator 16 is 37 wt%, and the water content of the working liquid output by the dehydrator 20 is 2150 ppm.

[0040] Example 3

[0041] According to the oxidation reaction extraction device as described above, the diameter of the oxidation extraction column 15 is 600 mm, the height is 10 m, and the number of trays is 8; the diameter of the oxidation liquid separator is 600 mm, and the length is 3 m; the diameter of the extraction column is 600 mm, the height is 12 m, and the number of trays is 15; the diameter of the coalescer is 600 mm, and the length is 3 m; the diameter of the dehydrator is 800 mm, and the height is 2 m. The flow rate of the hydrogenation liquid is 5 m 3 / h, the hydrogenation efficiency is 12 g / L, and the oxygen-containing gas is 260 Nm 3 / h. The operating pressure of the oxidation extraction column is 0.3 MPaG, and the operating temperature is 45-55°C. The results show that the oxidation yield of the oxidation extraction column is about 96%, the concentrated hydrogen peroxide output by the oxidation liquid separator 16 is 37 wt%, and the water content of the working liquid output by the dehydrator 20 is 2150 ppm.

[0042] Comparative Example 1

[0043] The oxidation extraction process uses a conventional oxidation column and an extraction column. The oxidation column has two sections, with a diameter of 600 mm and a height of 5 m, and the number of trays in each section is 4. The extraction column has a diameter of 600 mm, a height of 12 m, and a number of trays of 15. The hydrogenation liquid enters the upper section from the bottom and flows upward with the air from the lower section, and is separated into gas and liquid at the top. The gas is treated as tail gas, and the liquid overflows to the bottom of the lower section and flows upward with the air from the bottom of the lower section. Similarly, the gas and liquid are separated at the top of the lower section, and the gas goes to the bottom of the upper section, and the liquid is discharged as oxidation liquid. After buffering in the oxidation liquid storage tank, it enters the bottom of the extraction column and contacts with the pure water from the top in countercurrent. The crude hydrogen peroxide is obtained at the bottom of the extraction column, and the raffinate liquid from the top enters the coalescer for separation and dehydration. The flow rate of the hydrogenation liquid is 5 m 3 / h, the hydrogenation efficiency is 8 g / L, and the oxygen-containing gas is 190 Nm 3 / h. The operating pressure of the oxidation column is 0.25 MPaG, and the operating temperature is 45-55°C. The operating pressure of the extraction column is atmospheric pressure, and the operating temperature is 50°C. The results show that the oxidation yield of the oxidation column is about 90%, the crude hydrogen peroxide output by the extraction column is 23 wt%, and the water content of the working liquid output by the coalescer is 5000 ppm.

[0044] Comparative Example 2

[0045] The countercurrent contact oxidation tower disclosed in CN217868137U is additionally configured with a conventional countercurrent extraction tower for extracting the concentrated oxidation liquid discharged from the oxidation tower. The diameter of the oxidation tower is 600 mm, the height is 10 m, and the number of tower plates is 8; the diameter of the oxidation liquid separator is 300 mm, the height is 2 m; the diameter of the extraction tower is 600 mm, the height is 12 m, and the number of tower plates is 15; the hydrogenation liquid flow rate is 5 m 3 / h, the hydrogenation efficiency is 6.5 g / L, and the oxygen-containing gas is 140 Nm 3 / h. The operating pressure of the oxidation tower is 0.3 MPaG, and the operating temperature is 45-55℃. The results show that the oxidation yield of the oxidation tower is 94%, and the output of the concentrated hydrogen peroxide is 29wt%.

[0046] The above is only a preferred embodiment of the present application, and does not limit the present application in any way. Any simple modification, change, or equivalent transformation of the above embodiment according to the technical essence of the present application still falls within the protection scope of the technical solution of the present application.

Claims

1. An oxidation reaction extraction device for producing hydrogen peroxide, comprising an oxidation extraction tower (15), an oxidation liquid separator (16), an extraction tower (17) and a coalescer (19), characterized in that: The oxidation extraction tower (15) is used to perform countercurrent oxidation and parallel current extraction processes, and a hydrogenation liquid inlet (1) is provided at the top thereof for introducing the hydrogenation liquid to be oxidized from the top of the tower, an oxygen-containing gas inlet (2) is provided at the bottom thereof for introducing the oxygen-containing gas from the bottom of the tower, and a hydrogen peroxide rare product inlet (4) is provided at the middle and lower part thereof and located above the oxygen-containing gas inlet (2) for introducing the hydrogen peroxide rare product for extraction from the middle and lower part of the tower body; the oxidation liquid and the hydrogen peroxide rare product flow from top to bottom in the oxidation extraction tower (15), and the oxygen-containing gas flows from bottom to top in the oxidation extraction tower (15), thereby forming an oxidation extraction process in which the whole tower is countercurrently oxidized and the bottom of the tower is parallel current extracted; a medium-pressure tail gas outlet (3) is provided at the top of the oxidation extraction tower (15); the oxidation extraction tower (1 5) is provided with a concentrated oxidizing liquid outlet (5) at the bottom of the tower, which is connected to the oxidizing liquid separator (16) through a pipeline; the oxidizing liquid separator (16) has a water phase outlet (6) and an oil phase outlet (7); the water phase outlet (6) is used to discharge the concentrated hydrogen peroxide product after oil-water separation; the oil phase outlet (7) is connected to the bottom of the extraction tower (17) through a pipeline, and the top of the oxidizing liquid separator (16) is also provided with an oxidation tail gas outlet; the top of the extraction tower (17) is provided with an extractant inlet (9) for inputting a pure water extractant added with a stabilizer into the extraction tower (17); the bottom of the extraction tower (17) is provided with a dilute hydrogen peroxide outlet, and its through pipeline is connected to the dilute hydrogen peroxide inlet (4) at the lower middle part of the oxidation extraction tower (15).

2. The oxidation reaction extraction device for producing hydrogen peroxide as claimed in claim 1, wherein: An overflow baffle is provided inside the oxidizing liquid separator (16), the water phase outlet (6) and the oil phase outlet (7) are respectively provided on both sides of the overflow baffle, and the water phase outlet (6) is located at the bottom of the oxidizing liquid separator (16).

3. The oxidation reaction extraction device for producing hydrogen peroxide as claimed in claim 2, wherein: A hydrogen peroxide rare product pump (18) is provided on a pipeline connecting the hydrogen peroxide rare product outlet of the extraction tower (17) and the hydrogen peroxide rare product inlet (4) of the oxidation extraction tower (15).

4. The oxidation reaction extraction device for producing hydrogen peroxide as claimed in claim 3, wherein: The top of the extraction tower (17) is provided with a second oxidation tail gas outlet, which is combined with the oxidation tail gas outlet at the top of the extraction tower (17) into a low-pressure oxidation tail gas pipe (8).

5. The oxidation reaction extraction device for producing hydrogen peroxide as claimed in claim 4, wherein: The top side wall of the extraction tower (17) is provided with a raffinate outlet (10), which is connected to a coalescer (19) through a pipeline; the coalescer (19) is provided with a drain outlet (11) and a working liquid outlet (12), for respectively discharging water and working liquid generated after the raffinate is subjected to coalescence treatment.

6. The oxidation reaction extraction device for producing hydrogen peroxide according to claim 5, wherein: The invention also comprises a dehydrator (20) having a receiving chamber, and the receiving chamber is connected to the working fluid outlet (12) of the coalescer (19) through a pipeline.

7. The oxidation reaction extraction device for producing hydrogen peroxide according to claim 6, wherein: The outlet end of the low-pressure oxidation tail gas pipe (8) extends into the bottom of the accommodating cavity and is immersed below the liquid level of the working fluid; the top of the dehydrator (20) is provided with a tail gas outlet (14), and the bottom is provided with a dehydrated working fluid outlet (13).

8. The oxidation reaction extraction device for producing hydrogen peroxide as claimed in claim 7, wherein: The oxidation extraction tower (15) is a plate tower; the extraction tower (17) is also a plate tower, and a polymer material grid or a woven mesh is arranged below the tower plate, and the polymer material is at least one of polypropylene or a fluoropolymer.

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