Device and method for utilizing oxidized tail gas in hydrogen peroxide production

Abstract

The invention discloses an oxidation tail gas utilization device and method for producing hydrogen peroxide. The oxidation tail gas utilization device comprises an oxidation tower, an oxidation tail gas treatment procedure, unit operation equipment, an oxygen content online measurement assembly and an analysis treatment unit. After most of solvents such as aromatic hydrocarbon are cooled in the oxidation tail gas leaving from the top of the oxidation tower through a tail gas treatment process, one part of the oxidation tail gas is emptied or further treated, and the other part of the oxidation tail gas is sent to the top of unit operation equipment such as a working liquid tank, an extraction tower or a purification tower through judgment of an analysis treatment unit to replace a method of directly introducing fresh nitrogen. And safe operation of equipment in a system operation process is met. Operation parameters are analyzed and measured through the oxygen content on-line measurement assembly, the gas content on-line measurement assembly and the like, analysis data are transmitted to the analysis processing unit, and then output signals are transmitted to pipelines of oxidized tail gas and fresh nitrogen to control the proportion and flow of the oxidized tail gas and the fresh nitrogen, so that the use amount of the fresh nitrogen is reduced.

Description

Technical Field

[0001] The present invention relates to a method for utilizing industrial tail gas, and particularly to a device and method for utilizing the oxidation tail gas in the production of hydrogen peroxide. Background Art

[0002] At present, the anthraquinone process is mainly used for the preparation of hydrogen peroxide at home and abroad. In this process, alkyl anthraquinone (AQ, mainly 2-alkyl anthraquinone) is used as a carrier, and a suitable solvent for dissolving anthraquinone and anthrahydroquinone respectively and a substance for adjusting the pH of the solution are selected to jointly form a working solution. The whole preparation process generally includes processes such as hydrogenation, oxidation, extraction, and post-treatment. In the hydrogenation process, anthraquinone is hydrogenated to anthrahydroquinone under the action of a catalyst, and the working solution also becomes a hydrogenated solution. Then, the hydrogenated solution is oxidized to an oxidation solution containing H2O2 and anthraquinone by a gas containing oxygen in the oxidation process. The gas containing oxygen can be pure oxygen or oxygen-enriched air. In industrial practice, compressed air is mostly selected for cost reduction and safety considerations. In the oxidation process, the hydrogenated solution and air react in a co-current or counter-current contact manner. Since the oxygen content in the air is only about 21%, the reaction pressure in the oxidation tower is 0.18 - 0.6 MPa, and the reaction temperature is 40 - 55 °C, the oxygen content in the oxidation tail gas coming out from the top of the oxidation tower is between 3% and 10%.

[0003] In this process, the working solution tank, the extraction tower, and the purification tower have a gas phase space at the top. The working solution entering the working solution tank from the post-treatment process, as well as the liquid phase entering the extraction tower and the purification tower, will inevitably release a certain amount of oxygen. When the oxygen in the top gas phase space reaches a certain amount, it will form an explosive mixture gas with the aromatic hydrocarbon gas volatilized from the working solution, posing a safety hazard. To ensure safety, a certain amount of nitrogen is intermittently or continuously introduced in industry to dilute the oxygen concentration, so as to control the oxygen concentration below a certain amount. In particular, nitrogen is continuously introduced at the top of the extraction tower and the purification tower. At the same time, nitrogen is introduced to ensure a slightly positive pressure in the tank or at the top of the tower to prevent external air from entering the tank or the tower. At present, the price of nitrogen in industry is about 1 yuan / Nm 3 , taking a production device with an annual output of 200,000 tons of hydrogen peroxide (concentration calculated as 27.5%) as an example, its nitrogen demand is about 25 Nm 3 / h, and the cost is about 2 million yuan / year. The introduction of nitrogen significantly increases the operating cost. Summary of the Invention

[0004] The object of the present invention is to provide an oxidation tail gas utilization device and method for producing hydrogen peroxide. The oxidation tail gas utilization device includes an oxidation tower, an oxidation tail gas treatment process, unit operation equipment, an oxygen content on-line measurement component, and an analysis and processing unit; the oxidation tail gas leaving the top of the oxidation tower is cooled by the tail gas treatment process for most components such as aromatic hydrocarbons. After being judged by the analysis and processing unit, another part of the treated oxidation tail gas can be connected to the top of equipment such as a working fluid tank, an extraction tower, or a purification tower, and the treated oxidation tail gas is used to replace the originally directly introduced fresh nitrogen to meet the safe operation of the unit operation equipment during the operation of the system. The oxygen content on-line measurement component measures various operating parameters of the production device, and transmits the measurement data to the analysis and processing unit to judge the current operating state. The analysis and processing unit outputs a signal to the regulating valves in the pipelines of the oxidation tail gas and fresh nitrogen to control the ratio and flow rate of the oxidation tail gas and fresh nitrogen; thus, part of the oxidation tail gas replaces the fresh nitrogen, thereby reducing costs.

[0005] In a first aspect of the present invention, there is provided an oxidation tail gas utilization device for producing hydrogen peroxide. The oxidation tail gas utilization device includes an oxidation tower 101, an oxidation tail gas treatment process, unit operation equipment 201, an oxygen content on-line measurement component, and an analysis and processing unit; The oxidation tower 101 is provided with an oxidation tail gas discharge pipeline 122 connected to the oxidation tail gas treatment process. The oxidation tail gas treatment process is provided with a gas pipeline 124. The unit operation equipment 201 is provided with a nitrogen feed pipeline 231 and an oxidation tail gas feed pipeline 221 communicated with the gas pipeline 124; regulating valves A 601 and regulating valves B 602 are respectively arranged on the oxidation tail gas feed pipeline 221 and the nitrogen feed pipeline 231; The oxygen content on-line measurement component includes an oxygen content on-line measurement component A and an oxygen content on-line measurement component B. The signal input end of the oxygen content on-line measurement component A is connected to the gas pipeline 124, and the signal output end is connected to the analysis and processing unit; the signal input end of the oxygen content on-line measurement component B is connected to the unit operation equipment 201, and the signal output end is connected to the analysis and processing unit; the signal output end of the analysis and processing unit is respectively connected to the regulating valves A 601 and regulating valves B 602.

[0006] The oxygen content 801 of the oxidation tail gas and the oxygen content 802 of the vented tail gas measured in real time by the oxygen content on-line measurement component A and the oxygen content on-line measurement component B are transmitted to the analysis and processing unit. The analysis and processing unit processes the oxygen content 801 of the oxidation tail gas and the oxygen content 802 of the vented tail gas and sends signals to the regulating valves A and B to control the opening degrees of the regulating valves A 601 and regulating valves B 602.

[0007] The unit operation equipment 201 is one or more of a working fluid tank, an extraction tower, or a purification tower.

[0008] The oxidation tail gas treatment process includes a condenser. The oxidation tail gas treatment process is mainly to remove the heavy aromatics carried in the air. The oxidation tail gas coming out of the gas pipeline 124 is vented or further treated.

[0009] Preferably, the oxidation tower is a countercurrent oxidation tower 102. The upper part of the countercurrent oxidation tower 102 is provided with a countercurrent oxidation hydrogenated liquid feed pipeline 111, the lower part is provided with a countercurrent oxidation oxidized liquid discharge pipeline 112 and a gas feed pipeline 121, and inside is provided with a tray 1012, a liquid distributor 1013 communicated with the countercurrent oxidation hydrogenated liquid feed pipeline 111, and a gas distributor 1011 communicated with the gas feed pipeline 121. The gas enters the countercurrent oxidation tower 102 through the gas feed pipeline 121 via the gas distributor 1011, and the liquid enters the countercurrent oxidation tower 102 through the countercurrent oxidation hydrogenated liquid feed pipeline 111 via the liquid distributor 1013; the generated oxidized liquid enters the oxidized liquid tank through the countercurrent oxidation oxidized liquid discharge pipeline 112, and the tail gas at the top of the tower enters the tail gas treatment process through the oxidation tail gas discharge pipeline 122.

[0010] Preferably, the oxidation tower is a co-current oxidation tower 103. The co-current oxidation tower 103 is provided with a co-current oxidation hydrogenated liquid feed pipeline 113, a gas feed pipeline 121, and a co-current oxidation oxidized liquid discharge pipeline 114. Inside the co-current oxidation tower 103 is provided with a gas distributor 1011 communicated with the gas feed pipeline 121. The gas enters the co-current oxidation tower 103 through the gas feed pipeline 121 via the gas distributor 1011, and the liquid enters the co-current oxidation tower 103 through the co-current oxidation hydrogenated liquid feed pipeline 113; the generated oxidized liquid enters the oxidized liquid tank through the co-current oxidation oxidized liquid discharge pipeline 114, and the tail gas at the top of the tower enters the tail gas treatment process through the oxidation tail gas discharge pipeline 122.

[0011] The second aspect of the present invention provides a method for utilizing the oxidation tail gas in the production of hydrogen peroxide, including the following steps: (1) The oxygen content measuring assembly A and the oxygen content measuring assembly B respectively measure the oxygen content 801 of the oxidation tail gas and the oxygen content 802 of the vented tail gas, and transmit them to the analysis and processing unit; (2) The analysis and processing unit respectively processes the oxygen content 801 of the oxidation tail gas and the oxygen content 802 of the vented tail gas to obtain an intermediate signal A901 and an intermediate signal B902; (3) The analysis and processing unit determines the output signal A911 and the output signal B912 according to the magnitudes of the intermediate signal A901 and the intermediate signal B902 according to a given method, and the output signal A911 and the output signal B912 respectively control the opening degrees of the regulating valve A601 and the regulating valve B602.

[0012] Preferably, when the oxygen content 801 of the oxidized tail gas measured by the oxygen content measuring component A is ≤ 8%, the value of the input intermediate signal A901 is adjusted to 0; when the oxygen content 801 of the oxidized tail gas > 8%, the value of the intermediate signal A901 is adjusted to 1. When the oxygen content 802 of the vented tail gas measured by the oxygen content measuring component B is ≤ 5%, the value of the intermediate signal B902 is adjusted to 0; when the oxygen content 802 of the vented tail gas > 5%, the value of the intermediate signal B902 is adjusted to 1. When the value of the intermediate signal B902 is 0: both the output signal A911 and the output signal B912 are 0. When the value of the intermediate signal B902 is 1: if the value of the intermediate signal A901 is 0, then the output signal B912 is 0 and the output signal A911 is 1; otherwise, the output signal B912 is 1 and the output signal A911 is 0. When the output signal A911 is 0, it means not to intake air from here, and the control regulating valve A601 is closed; when the output signal A911 is not 0, it means to intake air from here, and the control regulating valve A601 is opened. When the output signal B912 is 0, it means not to intake air from here, and the control regulating valve B602 is closed; when the output signal B912 is not 0, it means to intake air from here, and the control regulating valve B602 is opened.

[0013] Preferably, in the method, the intermediate signal A901 and the intermediate signal B902 are signals between 0 and 1. The analysis and processing unit adjusts the magnitudes of the output signal A911 and the output signal B912 according to the strength of the signals, so as to adjust the flow rates of the oxidized tail gas and the fresh nitrogen entering the unit operation equipment 201. The ratio of the output signal A911 to the output signal B912 is the ratio of the nitrogen flow rate to the oxidized tail gas flow rate.

[0014] Preferably, in the method, the calculation formulas of the intermediate signal A901, the intermediate signal B902, the output signal B912, and the output signal A911 are as follows: ; Among them, the value range of k1 is 6 - 20; the value range of k2 is 8 - 30; the value range of the output signal B912 is [0, 1]. If the calculated result is greater than 1, it is taken as 1.

[0015] Preferably, the value range of k1 is 8 - 20; the value range of k2 is 8 - 20; further preferably, the value range of k1 is 8 - 12; the value range of k2 is 10 - 20.

[0016] The present invention has the following beneficial effects: (1) By connecting the oxidation tail gas pipeline in the hydrogen peroxide production process to the tops of unit operation equipment such as the working fluid tank, extraction column, and purification column, and partially or completely replacing the original method of directly introducing fresh nitrogen, the present invention can significantly reduce the cost of using fresh nitrogen. (2) Under the condition of the original online oxygen content measurement component, the present invention adds an analysis and processing unit, which can automatically adjust the proportion of oxidation tail gas and fresh nitrogen introduced into the tops of unit operation equipment such as the working fluid tank, extraction column, and purification column according to the operating conditions of each section, and minimize the use of fresh nitrogen as much as possible while ensuring the safety of the unit operation equipment, thereby improving the safety, stability, and economy of the entire device. Brief Description of the Drawings

[0017] Figure 1 is a schematic diagram of the oxidation tail gas utilization device for producing hydrogen peroxide according to the present invention; Figure 2 is a schematic diagram of the oxidation tail gas utilization device for countercurrent oxidation production of hydrogen peroxide according to the present invention; Figure 3 is a schematic diagram of the oxidation tail gas utilization device for co-current oxidation production of hydrogen peroxide according to the present invention; In the figure: 101, oxidation tower; 102, countercurrent oxidation tower; 103, co-current oxidation tower; 1011, gas distributor; 1012, tray; 1013, liquid distributor; 111, countercurrent oxidation hydrogenated liquid feed pipeline; 112, countercurrent oxidation oxidized liquid discharge pipeline; 113, co-current oxidation hydrogenated liquid feed pipeline; 114, co-current oxidation oxidized liquid discharge pipeline; 121, gas feed pipeline; 122, oxidation tail gas discharge pipeline; 124, gas pipeline; 201, unit operation equipment; 221, oxidation tail gas feed pipeline; 231, nitrogen feed pipeline; 601, regulating valve A; 602, regulating valve B; 801, oxidation tail gas oxygen content signal; 802, vent tail gas oxygen content signal; 911, output signal A; 912, output signal B. Detailed Embodiments

[0018] The present invention will be further described below with reference to the accompanying drawings through specific embodiments. The following embodiments are only descriptive and cannot be used to limit the protection scope of the present invention.

[0019] Figure 1In this process, gas enters the oxidation tower 101 after being distributed by the gas distributor 1011 from the gas feed pipeline 121. After the reaction, it leaves from the top of the oxidation tower 101 through the oxidation tail gas discharge pipeline 122. The oxidation tail gas leaving the top of the oxidation tower 101 is cooled for most components such as aromatics through the tail gas treatment process. After being judged by the analysis and processing unit, a part of the treated oxidation tail gas can enter the top of the unit operation equipment 201 through the oxidation tail gas feed pipeline 221. The unit operation equipment 201 also has a nitrogen feed pipeline 231. Control valves A 601 and control valve B 602 are respectively arranged on the oxidation tail gas feed pipeline 221 and the nitrogen feed pipeline 231; The signal input end of the online oxygen content measurement component A is connected to the gas pipeline 124, and the signal output end is connected to the analysis and processing unit; the signal input end of the online oxygen content measurement component B is connected to the unit operation equipment 201, and the signal output end is connected to the analysis and processing unit; the signal output end of the analysis and processing unit is respectively connected to the control valve A 601 and the control valve B 602; The oxygen content 801 of the oxidation tail gas and the oxygen content 802 of the vent tail gas measured in real time by the online oxygen content measurement component A and the online oxygen content measurement component B are transmitted to the analysis and processing unit. The analysis and processing unit processes the signals of the oxygen content 801 of the oxidation tail gas and the oxygen content 802 of the vent tail gas and sends signals to the control valve A and the control valve B to control the opening degrees of the control valve A 601 and the control valve B 602.

[0020] Figure 2 In this process, the gas phase enters the countercurrent oxidation tower 102. The countercurrent oxidation tower 102 is provided with a tray 1012. The liquid enters the countercurrent oxidation tower 102 from the countercurrent oxidation hydrogenated liquid feed pipeline 111 through the liquid distributor 1013 at the upper part of the tower. After the gas-liquid countercurrent contact reaction in the tower, the liquid leaves the oxidation tower from the bottom through the countercurrent oxidation oxidized liquid discharge pipeline 112.

[0021] Figure 3 In this process, the gas phase enters the co-current oxidation tower 103. The liquid enters the oxidation tower from the lower part of the tower through the co-current oxidation hydrogenated liquid feed pipeline 113. After the gas-liquid co-current reaction, the liquid leaves the oxidation tower from the upper part of the tower through the co-current oxidation oxidized liquid discharge pipeline 114.

[0022] Example 1

[0023] An oxidation tail gas utilization device for producing hydrogen peroxide designed according to the present invention, as Figure 1 shown, includes an oxidation tower 101, an oxidation tail gas treatment process, a unit operation equipment 201, an online oxygen content measurement component and an analysis and processing unit; The oxidation tower 101 is provided with a gas distributor 1011 and an oxidation tail gas discharge pipeline 122 connected to the oxidation tail gas treatment process. Gas enters the oxidation tower 101 after being distributed by the gas distributor 1011 from the gas feed pipeline 121; the oxidation tail gas treatment process is provided with a gas pipeline 124, and the unit operation equipment 201 is provided with a nitrogen feed pipeline 231 and an oxidation tail gas feed pipeline 221 communicating with the gas pipeline 124; a regulating valve A601 and a regulating valve B602 are respectively arranged on the oxidation tail gas feed pipeline 221 and the nitrogen feed pipeline 231; The oxygen content on-line measurement assembly includes an oxygen content on-line measurement assembly A and an oxygen content on-line measurement assembly B. The signal input end of the oxygen content on-line measurement assembly A is connected to the gas pipeline 124, and the signal output end is connected to the analysis and processing unit; the signal input end of the oxygen content on-line measurement assembly B is connected to the unit operation equipment 201, and the signal output end is connected to the analysis and processing unit; the signal output end of the analysis and processing unit is respectively connected to the regulating valve A601 and the regulating valve B602; The oxygen content 801 of the oxidation tail gas and the oxygen content 802 of the vent tail gas measured in real time by the oxygen content on-line measurement assembly A and the oxygen content on-line measurement assembly B are transmitted to the analysis and processing unit. The analysis and processing unit processes the oxygen content 801 of the oxidation tail gas and the oxygen content 802 of the vent tail gas and sends signals to the regulating valve A601 and the regulating valve B602 to control the opening degrees of the regulating valve A601 and the regulating valve B602.

[0024] The unit operation equipment 201 is a working liquid tank; the oxidation tower is a co-current oxidation tower 103.

[0025] When the oxygen content 801 of the oxidation tail gas measured by the oxygen content measurement assembly A ≤ 8%, the value of the input intermediate signal A901 is adjusted to 0. When the oxygen content 801 of the oxidation tail gas > 8%, the value of the intermediate signal A901 is adjusted to 1; when the oxygen content 802 of the vent tail gas measured by the oxygen content measurement assembly B ≤ 5%, the value of the intermediate signal B902 is adjusted to 0. When the oxygen content 802 of the vent tail gas > 5%, the value of the intermediate signal B902 is adjusted to 1; When the value of the intermediate signal B902 is 0: both the output signal A911 and the output signal B912 are 0. At this time, there is no need to introduce nitrogen and oxidation tail gas; When the value of the intermediate signal B902 is 1: if the value of the output intermediate signal A901 is 0, the output signal B912 is 0 and 911 is 1; otherwise, the output signal 912 is 1 and the output signal A911 is 0; When the output signal A911 is 0, it means no air intake from here, and the control regulating valve A601 is closed; when the output signal A911 is not 0, it means air intake from here, and the control regulating valve A601 is opened; when the output signal B912 is 0, it means no air intake from here, and the control regulating valve B602 is closed; when the output signal B912 is not 0, it means air intake from here, and the control regulating valve B602 is opened.

[0026] The working fluid flow rate is 930 m 3 / h, the air flow rate is 31000 Nm 3 / h, the oxidation reaction temperature is 50 °C, the pressure at the top of the oxidation tower is 0.2 MPa. When the oxygen content in the vent gas from the working fluid tank is greater than 5%, in order to ensure safety, the set gas-phase flow rate into the working fluid tank is 80 Nm 3 / h.

[0027] At this time, the distribution of the gas-phase flow rate introduced under different process conditions is shown in Table 1 as follows: Table 1. Gas-phase flow rate table for Example 1

[0028] The hydrogen peroxide device can operate stably.

[0029] Example 2

[0030] Other design and operation steps are the same as those in Example 1. The difference is that the oxidation tower is a countercurrent oxidation tower 102. The liquid enters the countercurrent oxidation tower 102 from the countercurrent oxidation hydrogenated liquid feed pipeline 111 through the liquid distributor 1013 at the upper part of the tower. After the gas-liquid countercurrent contact reaction in the tower, the liquid exits the oxidation tower from the bottom through the countercurrent oxidation oxidized liquid discharge pipeline 112; The unit operation equipment 201 is an extraction tower, and the method for the analysis and processing unit to process the signals of the oxygen content 801 in the oxidation tail gas and the oxygen content 802 in the vent gas and send signals to the regulating valves A and B to control the opening degrees of the regulating valves A601 and B602 is as follows: ; Among them, the value of k1 is 6; the value of k2 is 20; the value range of the output signal B912 is [0, 1]. If the calculated result is greater than 1, it is taken as 1.

[0031] When the oxygen content in the vent gas from the extraction tower is greater than 5%, in order to ensure safety, the set gas-phase flow rate into the extraction tower is 200 Nm 3 / h.

[0032] At this time, the distribution of the gas-phase flow rate introduced under different process conditions is shown in Table 2 as follows: Table 2. Gas-phase flow rate table for Example 2

[0033] The hydrogen peroxide device can operate stably.

[0034] Example 3

[0035] Other design and operation steps are the same as those in Example 2. The difference is that the oxidation tower is a co-current oxidation tower 103. The liquid enters the oxidation tower from the lower part of the tower through the co-current oxidation hydrogenated liquid feed pipeline 113. After the gas-liquid co-current reaction occurs, the liquid exits the oxidation tower from the upper part of the tower through the co-current oxidation oxidized liquid discharge pipeline 114. The unit operation equipment 201 is a purification tower, the value of k1 is 20; the value of k2 is 8.

[0036] When the oxygen content of the vented tail gas in the purification tower is greater than 5%, in order to ensure safety, the set gas-phase flow rate into the purification tower is 200 Nm 3 / h.

[0037] The distribution of the gas-phase flow rate introduced under different process conditions at this time is shown in Table 3.

[0038] Table 3. Different gas-phase flow rates in Example 3

[0039] The hydrogen peroxide device can operate stably.

[0040] Example 4

[0041] Other design and operation steps are the same as those in Example 2. The difference is that the unit operation equipment (201) is a working fluid tank, the value of k1 is 8; the value of k2 is 30. When the oxygen content of the vented tail gas in the working fluid tank is greater than 5%, in order to ensure safety, the set gas-phase flow rate into the working fluid tank is 80 Nm 3 / h.

[0042] The distribution of the gas-phase flow rate introduced under different process conditions at this time is shown in Table 4.

[0043] Table 4. Different gas-phase flow rates in Example 4

[0044] The hydrogen peroxide device can operate stably.

[0045] Example 5

[0046] Other design and operation steps are the same as those in Example 2. The difference is that the value of k1 is 12; the value of k2 is 10.

[0047] The distribution of the gas-phase flow rate introduced under different process conditions at this time is shown in Table 5.

[0048] Table 5. Different gas phase flow rate tables for Example 5

[0049] The hydrogen peroxide device can operate stably.

Claims

1. An oxidation tail gas utilization device for producing hydrogen peroxide, the oxidation tail gas utilization device comprising an oxidation tower (101), an oxidation tail gas treatment process, a unit operation device (201), an oxygen content online measurement component and an analysis and processing unit; The oxidation tower (101) is provided with an oxidation tail gas discharge pipeline (122) connected to the oxidation tail gas treatment process, the oxidation tail gas treatment process is provided with a gas pipeline (124), and the unit operation equipment (201) is provided with a nitrogen feed pipeline (231) and an oxidation tail gas feed pipeline (221) connected to the gas pipeline (124); the oxidation tail gas feed pipeline (221) and the nitrogen feed pipeline (231) are respectively provided with a regulating valve A (601) and a regulating valve B (602); The oxygen content online measurement component comprises an oxygen content online measurement component A and an oxygen content online measurement component B. The signal input end of the oxygen content online measurement component A is connected to a gas pipeline (124), and the signal output end is connected to an analysis and processing unit; the signal input end of the oxygen content online measurement component B is connected to a unit operating device (201), and the signal output end is connected to the analysis and processing unit; the signal output end of the analysis and processing unit is respectively connected to a regulating valve A (601) and a regulating valve B (602).

2. The oxidation tail gas utilization device according to claim 1, characterized in that: The unit operation equipment (201) is one or more of a working liquid tank, an extraction tower or a purification tower.

3. The oxidation tail gas utilization device according to claim 1, characterized in that: The oxidation tower is a countercurrent oxidation tower (102), wherein a countercurrent oxidation hydrogenation liquid feed pipeline (111) is arranged at the top of the countercurrent oxidation tower (102), a countercurrent oxidation hydrogenation liquid discharge pipeline (112) and a gas feed pipeline (121) are arranged at the bottom, and a tower plate (1012) and a liquid distributor (1013) connected to the countercurrent oxidation hydrogenation liquid feed pipeline (111) and a gas distributor (1011) connected to the gas feed pipeline (121) are arranged inside.

4. The oxidation tail gas utilization device according to claim 1, characterized in that: The oxidation tower is a parallel-flow oxidation tower (103), and the parallel-flow oxidation tower (103) is provided with a parallel-flow oxidation hydrogenation liquid feed pipeline (113), a gas feed pipeline (121), and a parallel-flow oxidation oxidized liquid discharge pipeline (114). A gas distributor (1011) connected to the gas feed pipeline (121) is provided inside the parallel-flow oxidation tower (103).

5. A method for utilizing oxidized tail gas using the oxidized tail gas utilization device according to any one of claims 1 to 4, comprising the following steps: (1) The oxygen content measuring component A and the oxygen content measuring component B respectively measure the oxygen content of the oxidized tail gas (801) and the oxygen content of the vented tail gas (802), and transmit the results to the analysis and processing unit; (2) The analysis and processing unit processes the oxygen content of the oxidized tail gas (801) and the oxygen content of the vented tail gas (802) to obtain an intermediate signal A (901) and an intermediate signal B (902); (3) The analysis and processing unit determines the output signal A (911) and the output signal B (912) according to the magnitude of the intermediate signal A (901) and the intermediate signal B (902) in accordance with a given method. The output signal A (911) and the output signal B (912) respectively control the opening of the regulating valve A (601) and the regulating valve B (602).

6. The method for utilizing oxidation tail gas according to claim 5, characterized in that: When the oxygen content (801) of the oxidized tail gas measured by the oxygen content measurement component A is ≤8%, the value of the intermediate signal A (901) is adjusted to 0; when the oxygen content (801) of the oxidized tail gas is greater than 8%, the value of the intermediate signal A (901) is adjusted to 1; when the oxygen content (802) of the vented tail gas measured by the oxygen content measurement component B is ≤5%, the value of the intermediate signal B (902) is adjusted to 0; when the oxygen content (802) of the vented tail gas is greater than 5%, the value of the intermediate signal B (902) is adjusted to 1; When the value of the intermediate signal B (902) is 0: the output signal A (911) and the output signal B (912) are both 0; When the value of the intermediate signal B (902) is 1: if the value of the intermediate signal A (901) is 0, the output signal B (912) is 0 and the output signal A (911) is 1; otherwise, the output signal B (912) is 1 and the output signal A (911) is 0; When the output signal A (911) is 0, it means that air is not taken in from here, and the control regulating valve A (601) is closed; when the output signal A (911) is not 0, it means that air is taken in from here, and the control regulating valve A (601) is opened; when the output signal B (912) is 0, it means that air is not taken in from here, and the control regulating valve B602 is closed; when the output signal B (912) is not 0, it means that air is taken in from here, and the control regulating valve B (602) is opened.

7. The method for utilizing oxidation tail gas according to claim 5, characterized in that: In the method, the intermediate signal A (901) and the intermediate signal B (902) are signals between 0 and 1, and the analysis and processing unit adjusts the magnitude of the output signal A (911) and the output signal B (912) according to the strength of the signals, thereby adjusting the flow of the oxidation tail gas and the fresh nitrogen gas entering the unit operation equipment (201).

8. The method for utilizing oxidation tail gas according to claim 7, characterized in that: In the method, the calculation formulas of the intermediate signal A (901), the intermediate signal B (902), the output signal A (911), and the output signal B (912) are as follows: ； Among them, the value range of k1 is 6~20; the value range of k2 is 8~30; the value range of the output signal B (912) is [0, 1], and if the value of the calculated result is greater than 1, it is taken as 1.

9. The method for utilizing oxidation tail gas according to claim 8, characterized in that: The value range of k1 is 8~20; the value range of k2 is 8~20.

10. The method for utilizing oxidation tail gas according to claim 8, characterized in that: The value range of k1 is 8~12; the value range of k2 is 10~20.

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