Efficient gas-liquid countercurrent oxidation tower

Abstract

The utility model provides a high-efficiency gas-liquid countercurrent oxidation tower which comprises a tower body, an oxidized tail gas outlet pipeline and an oxidized liquid outlet pipeline are respectively arranged at the upper end and the lower end of the tower body, the oxidized tail gas outlet pipeline and the oxidized liquid outlet pipeline are both communicated with the tower body, and a gas-liquid separator and a demister are arranged at the upper end in the tower body. The gas-liquid separator and the demister are both connected with the tower body, and are both communicated with the oxidized tail gas outlet pipeline; a hydrogenated liquid inlet pipeline is arranged at the upper part of the tower body, an air inlet pipeline is arranged at the lower part of the tower body, the hydrogenated liquid inlet pipeline and the air inlet pipeline are communicated with the tower body, and a hydrogenated liquid distributor and an air distributor are arranged in the tower body. According to the utility model, the retention time of the oxidation tower on the sieve plate of the gas-liquid dispersion mass transfer assembly is increased, the contact area is increased, and the oxidation yield is improved and can reach more than 97%. And the gas-liquid separator and the demister are used for efficiently separating the oxidized tail gas, so that the problem of liquid carrying is prevented.

Description

Technical Field

[0001] The utility model relates to an oxidation tower, in particular to a high-efficiency gas-liquid countercurrent oxidation tower, belonging to the technical field of gas-liquid countercurrent oxidation towers. Background Art

[0002] There are three types of oxidation towers used in my country's hydrogen peroxide plant industry: empty towers, sieve plate towers, and improved packed towers. In order to increase the oxidation yield, we have made structural improvements to the oxidation towers or improved the working fluid system, thereby adjusting the oxidation temperature and air distribution ratio to increase the oxidation yield from 92% to 94% to 94% to 96%.

[0003] The Chinese utility model patent with announcement number CN208577436U discloses a gas-liquid countercurrent oxidation tower. The utility model relates to an oxidation tower for hydrogen peroxide production. The oxidation tower is provided with an air inlet pipeline and an air distributor at the bottom, a hydrogenation liquid inlet pipeline and a hydrogenation liquid distributor at the top, a plurality of layers of gas-liquid dispersion mass transfer components and heat extraction facilities arranged between the gas-liquid dispersion mass transfer components are arranged in the tower space, an oxidation tail gas outlet pipeline is arranged at the top of the tower, and an oxidation liquid outlet pipeline is arranged at the bottom of the tower. The gas-liquid countercurrent oxidation tower of the utility model can significantly shorten the residence time for oxidation to achieve complete oxidation, which is only 50-80% of the existing gas-liquid co-current oxidation technology, and the oxidation reaction has fewer side reactions, less decomposition of hydrogen peroxide, and the oxidation yield reaches ≥95%. However, the device can only achieve an oxidation rate of ≥95%, and does not remove liquid from the oxidized tail gas. Utility Model Content

[0004] Based on the above background, the purpose of the utility model is to provide an efficient gas-liquid countercurrent oxidation tower with an oxidation yield of ≥97% and no residual liquid in the oxidation tail gas, so as to solve the problems described in the background technology.

[0005] In order to achieve the above-mentioned utility model purpose, the utility model provides the following technical solutions:

[0006] A high-efficiency gas-liquid countercurrent oxidation tower comprises a tower body, wherein an oxidation tail gas outlet pipeline and an oxidation liquid outlet pipeline are respectively arranged at the upper and lower ends of the tower body, and the oxidation tail gas outlet pipeline and the oxidation liquid outlet pipeline are both connected to the tower body; a gas-liquid separator and a demister are arranged at the upper end of the tower body, and the gas-liquid separator and the demister are both connected to the tower body, and the gas-liquid separator and the demister are both connected to the tower body, and are connected to the oxidation tail gas outlet pipeline;

[0007] A hydrogenated liquid inlet pipeline is arranged at the upper part of the tower body, and an air inlet pipeline is arranged at the lower part of the tower body, the hydrogenated liquid inlet pipeline and the air inlet pipeline are both connected to the tower body, a hydrogenated liquid distributor and an air distributor are arranged inside the tower body, the hydrogenated liquid distributor and the air distributor are both connected to the tower body, and the hydrogenated liquid distributor and the air distributor are respectively connected to the hydrogenated liquid distributor and the air distributor;

[0008] A plurality of gas-liquid dispersion mass transfer components are arranged between the hydrogenation liquid distributor and the air distributor, a plurality of through holes are provided on the sieve plate portion of the gas-liquid dispersion mass transfer components, the gas-liquid dispersion mass transfer components are connected to the tower body, a plurality of heat exchangers are arranged inside the tower body, and the heat exchangers are connected to the tower body.

[0009] An air distributor is provided in the tower body. When the gas flows upward in countercurrent after the gas-liquid contact, the gas tends to gather in the center of the tower. In order to prevent the gas-liquid two-phase deviation and back-mixing from affecting the oxidation yield, a multi-layer porous sieve plate is installed in the tower body, which can make the gas-liquid two-phase contact more, so that the hydrogen anthraquinone molecules in the hydrogenated liquid can contact more with oxygen, improve the oxidation efficiency of the oxidation tower, and improve the oxidation yield. Since a large amount of heat is released during the oxidation reaction, and several heat exchangers are arranged inside the tower body, the heat generated by the oxidation reaction can be taken away in time by circulating cooling water, solving the hidden danger of decomposition of hydrogen peroxide due to uneven temperature. Since the air reacts with the hydrogenated liquid from bottom to top, several layers of gas-liquid dispersed mass transfer components can reduce back-mixing, make the hydrogenated liquid that is difficult to oxidize contact with fresh air to shorten the reaction time, and then completely oxidize, with an oxidation yield of ≥97%, and under the action of the gas-liquid separator and the demister, the oxidation tail gas can be discharged from the tower body in a state without residual liquid.

[0010] Preferably, the heat exchanger is provided with a circulating water return pipeline, the heat exchanger is communicated with the circulating water return pipeline, the circulating water return pipeline is provided with a regulating valve, and the regulating valve is connected to the circulating water return pipeline.

[0011] Preferably, the heat exchanger is any one of a U-shaped built-in heat exchanger, a shell and tube heat exchanger, and a half-tube heat exchanger.

[0012] Preferably, the gas-liquid dispersion mass transfer components are arranged in 2 to 18 layers.

[0013] Preferably, there are at least two heat exchangers.

[0014] Preferably, the two heat exchangers are located between a plurality of the gas-liquid dispersed mass transfer components.

[0015] Preferably, the hydrogenation liquid distributor may be any one of a tube type, a trough type and a disc type.

[0016] Preferably, the tower body can be any one of a packed tower and an empty tower.

[0017] Compared with the prior art, the utility model has the following advantages:

[0018] (1) The residence time of the sieve plate in the gas-liquid dispersion mass transfer component of the oxidation tower is increased, the contact area is increased, and the oxidation yield is improved, and the yield can reach more than 97%.

[0019] (2) The gas-liquid separator and demister can efficiently separate the oxidation tail gas and prevent the problem of liquid carryover.

[0020] (3) A heat exchanger is installed in the tower body to remove the reaction heat in time, and at the same time, the reaction temperature can be increased, so that the reaction rate is increased, thereby solving the potential safety hazard of hydrogen peroxide decomposition caused by the failure to remove the reaction heat in time.

[0021] (4) Reduce system fluctuations during the hydrogen peroxide oxidation process, especially the safety hazards caused by air compressor tripping.

[0022] (5) Expose the difficult-to-oxidize hydrogenated liquid to fresh air to increase the reaction kinetics, shorten the reaction time, and simplify the operation. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings in the following description are only embodiments of the utility model. For ordinary technicians in this field, other drawings can be obtained based on the provided drawings without paying creative work.

[0024] Figure 1 This is a schematic diagram of the overall structure of the utility model high-efficiency gas-liquid countercurrent oxidation tower;

[0025] Figure 2 It is a schematic diagram of the sieve plate structure of the utility model high-efficiency gas-liquid countercurrent oxidation tower.

[0026] In the figure: 1. tower body; 2. oxidation tail gas outlet pipeline; 3. oxidation liquid outlet pipeline; 4. gas-liquid separator; 5. demister; 6. hydrogenation liquid inlet pipeline; 7. air inlet pipeline; 8. hydrogenation liquid distributor; 9. air distributor; 10. gas-liquid dispersion mass transfer component; 11. sieve plate; 12. through hole; 13. heat exchanger; 14. circulating water return pipeline; 15. regulating valve. DETAILED DESCRIPTION

[0027] The technical solution of the utility model is further described in detail below through specific embodiments and in combination with the accompanying drawings. It should be understood that the implementation of the utility model is not limited to the following embodiments, and any form of modification and / or change made to the utility model will fall within the protection scope of the utility model.

[0028] In the present invention, unless otherwise specified, all parts and percentages are weight units, and the equipment and raw materials used can be purchased from the market or are commonly used in the field. The methods in the following embodiments, unless otherwise specified, are conventional methods in the field. The components or equipment in the following embodiments, unless otherwise specified, are universal standard parts or components known to those skilled in the art, and their structures and principles are known to those skilled in the art through technical manuals or conventional experimental methods.

[0029] The following is a detailed description of the embodiments of the present invention in conjunction with the accompanying drawings. In the following detailed description, for ease of explanation, many specific details are described to provide a comprehensive understanding of the embodiments of the present invention. However, one or more embodiments may also be implemented by those skilled in the art without these specific details.

[0030] like Figure 1 and Figure 2 As shown, a high-efficiency gas-liquid countercurrent oxidation tower includes a tower body 1, and the tower body 1 can be any one of a packed tower and an empty tower. An oxidation tail gas outlet pipeline 2 and an oxidation liquid outlet pipeline 3 are respectively arranged at the upper and lower ends of the tower body 1, and the oxidation tail gas outlet pipeline 2 and the oxidation liquid outlet pipeline 3 are both connected to the tower body 1. A gas-liquid separator 4 and a demister 5 are arranged at the upper end of the tower body 1, and the gas-liquid separator 4 and the demister 5 are both connected to the tower body 1, and the gas-liquid separator 4 and the demister 5 are both connected to the tower body 1, and the gas-liquid separator 4 and the demister 5 are both connected to the oxidation tail gas outlet pipeline 2;

[0031] A hydrogenated liquid inlet pipeline 6 is arranged at the upper part of the tower body 1, and an air intake pipeline 7 is arranged at the lower part of the tower body 1. The hydrogenated liquid inlet pipeline 6 and the air intake pipeline 7 are both communicated with the tower body 1. A hydrogenated liquid distributor 8 and an air distributor 9 are arranged inside the tower body 1. The hydrogenated liquid distributor 8 and the air distributor 9 are both connected to the tower body 1, and the hydrogenated liquid distributor 8 and the air distributor 9 are respectively connected to the hydrogenated liquid distributor 8 and the air distributor 9; the hydrogenated liquid distributor 8 can be any one of a tubular type, a trough type, and a disc type.

[0032] Several gas-liquid dispersion mass transfer components 10 are arranged between the hydrogenation liquid distributor 8 and the air distributor 9, and the gas-liquid dispersion mass transfer components 10 are arranged in 2 to 18 layers. Several through holes 12 are opened on the sieve plate 11 of the gas-liquid dispersion mass transfer component 10, and the gas-liquid dispersion mass transfer component 10 is connected to the tower body 1. Several heat exchangers 13 are arranged inside the tower body 1, and the heat exchangers 13 are connected to the tower body 1. There are at least two heat exchangers 13. The heat exchanger 13 can be any one of a U-shaped built-in heat exchanger, a shell and tube heat exchanger, and a half-tube heat exchanger. Two heat exchangers 13 are located between several gas-liquid dispersion mass transfer components 10.

[0033] An air distributor 9 is provided in the tower body 1. When the gas flows upward in countercurrent after the gas-liquid contact, the gas tends to gather toward the center of the tower. In order to prevent the gas-liquid two-phase deviation and backmixing from affecting the oxidation yield, a multi-layer porous sieve plate 11 is installed in the tower body 1, which can make the gas-liquid two-phase contact more, and then make the hydrogen anthraquinone molecules in the hydrogenated liquid contact more with oxygen, improve the oxidation efficiency of the oxidation tower, and improve the oxidation yield. Since a large amount of heat is released during the oxidation reaction, several heat exchangers 13 are arranged inside the tower body 1, so that the heat generated by the oxidation reaction can be taken away in time by circulating cooling water, and the heat exchanger 13 is provided with a circulating water return pipeline 14, the heat exchanger 13 is connected to the circulating water return pipeline 14, and the circulating water return pipeline 14 is provided with a regulating valve 15, and the regulating valve 15 is connected to the circulating water return pipeline 14. Solve the hidden danger of decomposition of hydrogen peroxide due to uneven temperature. Since the air reacts with the hydrogenated liquid from bottom to top, the several layers of gas-liquid dispersed mass transfer components 10 can reduce back mixing, so that the difficult-to-oxidize hydrogenated liquid can contact with fresh air to shorten the reaction time, thereby achieving complete oxidation, with an oxidation yield of ≥97%. Under the action of the gas-liquid separator 4 and the demister 5, the oxidized tail gas can be discharged from the tower body 1 in a state without residual liquid.

[0034] The implementation principle of the utility model of a high-efficiency gas-liquid countercurrent oxidation tower is:

[0035] An air distributor 9 is provided in the tower body 1. When the gas flows upward in countercurrent after the gas-liquid contact, the gas tends to gather toward the center of the tower. In order to prevent the gas-liquid two-phase bias and back-mixing from affecting the oxidation yield, a multi-layer porous sieve plate 11 is installed in the tower body 1, which can make the gas-liquid two-phase contact more, and then make the hydrogenanthraquinone molecules in the hydrogenated liquid contact more with oxygen, improve the oxidation efficiency of the oxidation tower, and improve the oxidation yield. Since a large amount of heat is released during the oxidation reaction, and a number of heat exchangers 13 are arranged inside the tower body 1, the heat generated by the oxidation reaction can be taken away in time by circulating cooling water, and the decomposition hidden danger of hydrogen peroxide due to uneven temperature is solved. Since the air reacts with the hydrogenated liquid from bottom to top, the gas-liquid dispersed mass transfer components 10 of several layers can reduce back-mixing, make the hydrogenated liquid that is difficult to oxidize contact with fresh air to shorten the reaction time, and then the oxidation is complete, and the oxidation yield is ≥97%, and under the action of the gas-liquid separator 4 and the demister 5, the oxidation tail gas can be discharged from the tower body 1 in a state without residual liquid.

[0036] This article uses specific examples to illustrate the principles and implementation methods of the utility model. The above examples are only used to help understand the method and core ideas of the utility model. It should be pointed out that for ordinary technicians in this technical field, without departing from the principles of the utility model, the utility model can also be improved and modified, and these improvements and modifications also fall within the scope of protection of the claims of the utility model.

Claims

1. A high-efficiency gas-liquid countercurrent oxidation tower, characterized in that: The high-efficiency gas-liquid countercurrent oxidation tower comprises a tower body (1), wherein an oxidation tail gas outlet pipeline (2) and an oxidation liquid outlet pipeline (3) are respectively arranged at the upper and lower ends of the tower body (1), and the oxidation tail gas outlet pipeline (2) and the oxidation liquid outlet pipeline (3) are both connected to the tower body (1); a gas-liquid separator (4) and a demister (5) are arranged at the upper end of the tower body (1), and the gas-liquid separator (4) and the demister (5) are both connected to the tower body (1), and the gas-liquid separator (4) and the demister (5) are both connected to the tower body (1); A hydrogenated liquid inlet pipeline (6) is arranged at the upper part of the tower body (1), and an air inlet pipeline (7) is arranged at the lower part of the tower body (1); the hydrogenated liquid inlet pipeline (6) and the air inlet pipeline (7) are both in communication with the tower body (1); a hydrogenated liquid distributor (8) and an air distributor (9) are arranged inside the tower body (1), and the hydrogenated liquid distributor (8) and the air distributor (9) are both connected to the tower body (1); A plurality of gas-liquid dispersion mass transfer components (10) are arranged between the hydrogenation liquid distributor (8) and the air distributor (9); a plurality of through holes (12) are provided on the sieve plate (11) of the gas-liquid dispersion mass transfer components (10); the gas-liquid dispersion mass transfer components (10) are connected to the tower body (1); a plurality of heat exchangers (13) are arranged inside the tower body (1); and the heat exchangers (13) are connected to the tower body (1).

2. The high-efficiency gas-liquid countercurrent oxidation tower according to claim 1 is characterized in that: The heat exchanger (13) is provided with a circulating water return pipeline (14), the heat exchanger (13) is in communication with the circulating water return pipeline (14), the circulating water return pipeline (14) is provided with a regulating valve (15), and the regulating valve (15) is connected to the circulating water return pipeline (14).

3. The high-efficiency gas-liquid countercurrent oxidation tower according to claim 1 is characterized in that: The heat exchanger (13) is any one of a U-shaped built-in heat exchanger, a shell-and-tube heat exchanger, and a half-tube heat exchanger.

4. The high-efficiency gas-liquid countercurrent oxidation tower according to claim 1 is characterized in that: The gas-liquid dispersion mass transfer component (10) is arranged in 2 to 18 layers.

5. The high-efficiency gas-liquid countercurrent oxidation tower according to claim 3 is characterized in that: The number of the heat exchangers (13) is at least two.

6. The high-efficiency gas-liquid countercurrent oxidation tower according to claim 5 is characterized in that: The two heat exchangers (13) are located between the plurality of gas-liquid dispersed mass transfer components (10).

7. The high-efficiency gas-liquid countercurrent oxidation tower according to claim 6 is characterized in that: The hydrogenation liquid distributor (8) may be any one of a tube type, a trough type and a disc type.

8. The high-efficiency gas-liquid countercurrent oxidation tower according to claim 7 is characterized in that: The tower body (1) may be any one of a packed tower and an empty tower.

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