Comprehensive utilization system for hydrogen peroxide tail gas

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By designing a comprehensive utilization system for hydrogen peroxide exhaust, the problems of complex processes, crystallization blockage and high aromatic consumption in traditional expansion refrigeration power generation processes are solved, and efficient aromatic recovery and cooling capacity are achieved, reducing VOCs emissions and energy consumption.

CN222849864UActive Publication Date: 2025-05-09PINGHU PETROCHEM

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Patent Information

Application Number: CN202421762351.1
Authority / Receiving Office: CN · China
Patent Type: Utility models(China)
Current Assignee / Owner
Filing Date: 2024-07-24
Publication Date: 2025-05-09
Estimated Expiration: 2034-07-24

AI Technical Summary

Technical Problem

In the purification treatment of hydrogen peroxide exhaust, the traditional expansion refrigeration power generation process is complex, which can easily lead to water freezing and entrained working liquid precipitation and blockage. The aromatic hydrocarbon consumption is high, and the cooling capacity cannot be effectively utilized, resulting in high VOCs emissions.

Method used

A hydrogen peroxide exhaust comprehensive utilization system is designed, including the first and second coalescence separation units and the exhaust gas treatment unit. Through the cooler, the cold box is divided into pre-cooled reheating section and condensing section, which increases the indirect heat exchange and reheating process of exhaust gas, and reduces the temperature of exhaust gas by using expansion generators and cold and heat exchange to avoid crystallization blockage, and improves the aromatic recovery efficiency through multiple coalescing and separation.

Benefits of technology

It effectively avoids crystallization blockage, reduces aromatic hydrocarbon consumption and VOCs emissions, improves the comprehensive utilization of cooling capacity, enhances power generation, and reduces energy consumption and organic gas content in waste gas.

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Abstract

The utility model provides a hydrogen peroxide tail gas comprehensive utilization system. The hydrogen peroxide tail gas comprehensive utilization system comprises a first coalescence separation unit, a second coalescence separation unit and a tail gas treatment unit, the first coalescence separation unit comprises a cooler and a primary tail gas condensate receiving tank, and the cooler is communicated with the first tail gas condensate receiving tank. By adding the processes of cold medium reheating, coalescence separation, expansion power generation, secondary coalescence separation and condensation heat exchange, multiple benefits are achieved after tail gas condensation, the problem of crystallization blockage caused by the fact that tail gas contains water is solved, more energy is recycled for power generation, aromatic hydrocarbon is further recycled, and consumption of the aromatic hydrocarbon is reduced; meanwhile, cold energy is comprehensively utilized to save water and electricity, entrainment of organic gas in waste gas is effectively reduced, the content of the organic gas entering the tail gas treatment unit is controlled from the source, the emission value of VOCs is further reduced, and the service life of a tail gas adsorption unit is prolonged.

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Description

Technical Field

[0001] The utility model relates to a system, in particular to a hydrogen peroxide tail gas comprehensive utilization system, belonging to the technical field of chemical equipment. Background Art

[0002] The production of hydrogen peroxide (hydrogen peroxide) is mostly done by the anthraquinone process. The incompletely oxidized tail gas from the oxidation system contains a mixture of heavy aromatics, nitrogen, oxygen, etc. If it is recycled, it can save raw materials, protect the environment, and reduce consumption costs.

[0003] At present, hydrogen peroxide tail gas purification treatment mostly adopts tail gas condensation and expansion refrigeration to recover heavy aromatics, and there are also expansion and power generation at the same time. Among them, the expansion refrigeration power generation process is complicated, and when the expansion temperature is too low, it is easy to cause water freezing and entrained working fluid precipitation, resulting in blockage and even damage to equipment.

[0004] The traditional hydrogen peroxide expansion refrigeration purification and power generation device consists of a cold box, a high-pressure separator, an expander, a generator, a bypass automatic thermostatic valve, a cyclone separator, etc. The aromatics consumption is high, and in the production process, the organic waste gas is generally discharged directly into the atmosphere after simple treatment, which cannot meet the emission standards. Utility Model Content

[0005] Based on the above background, the purpose of the utility model is to provide a hydrogen peroxide tail gas comprehensive utilization system that avoids crystallization blockage, reduces aromatics consumption, makes comprehensive utilization of cold energy and can reduce VOCs emissions, so as to solve the problems described in the background technology.

[0006] In order to achieve the above-mentioned utility model purpose, the utility model provides the following technical solutions:

[0007] A hydrogen peroxide tail gas comprehensive utilization system, comprising a first coalescence and separation unit, a second coalescence and separation unit and a tail gas treatment unit;

[0008] The first coalescence separation unit comprises a cooler and a primary tail gas condensate receiving tank, wherein the cooler is in communication with the first tail gas condensate receiving tank;

[0009] The second condensation separation unit comprises a cold box, a heat exchanger, a first tail gas condensate receiving tank, a second tail gas condensate receiving tank and an expansion generator, wherein the cold box is connected to the heat exchanger, the first tail gas condensate receiving tank and the second tail gas condensate receiving tank;

[0010] An expansion generator is arranged between the first tail gas condensate receiving tank and the second tail gas condensate receiving tank, and the expansion generator is communicated with the first tail gas condensate receiving tank and the second tail gas condensate receiving tank;

[0011] The heat exchanger is also communicated with the tail gas treatment unit.

[0012] Preferably, the primary tail gas condensate receiving tank is provided with a primary aromatic hydrocarbon recovery tank, and the primary aromatic hydrocarbon recovery tank is connected to the primary tail gas condensate receiving tank.

[0013] Preferably, the first tail gas condensate receiving tank is provided with a first aromatic hydrocarbon recovery tank, and the first aromatic hydrocarbon recovery tank is connected to the first tail gas condensate receiving tank.

[0014] Preferably, the second tail gas condensate receiving tank is provided with a second aromatic hydrocarbon recovery tank, and the second aromatic hydrocarbon recovery tank is connected to the second tail gas condensate receiving tank.

[0015] Preferably, the heat exchanger is provided with a cold energy recycling heat exchange device, and the cold energy recycling heat exchange device is connected to the heat exchanger.

[0016] Preferably, the cooler is provided with an oxidation tail gas inlet, and the oxidation tail gas inlet is connected to the cooler.

[0017] The system is connected to an external oxidation tower. The oxidized tail gas coming out from the top of the oxidation tower is collected and initially condensed through a cooler to remove the entrained solvent. The tail gas then enters a primary tail gas condensate receiving tank to separate the condensed solvent.

[0018] The cold box is divided into a pre-cooling and reheating section and a condensing section. Before the hydrogen peroxide tail gas that has been separated and purified after condensation enters the expander, an indirect heat exchange and reheating process of the tail gas is added. Because the separation and purification of the oxidation tail gas is carried out at high pressure and low temperature, it becomes a superheated gas for the small amount of heavy aromatics it contains after reheating, which is more conducive to the separation of aromatics.

[0019] The cooled gas enters the first tail gas condensate receiving tank for gas-liquid separation, and the solvent therein is further recovered, and the solvent recovery and utilization is increased by 30%.

[0020] Before entering the expansion generator, heat exchange is added to reduce the temperature of hydrogen peroxide tail gas entering the expander. The first tail gas condensate receiving tank is used to separate the atomized water and aromatics, further remove the liquid medium in the tail gas, and avoid the problem of ice clogging of the entrained water during the expansion and cooling process. Prevent the expander from malfunctioning and damaging the equipment.

[0021] The tail gas from the outlet of the first tail gas condensate tank enters the expansion end inlet of the expander, and the residual pressure is used to drive the expander impeller to rotate at high speed to further expand and cool the tail gas. The temperature can be controlled at 0-0.5℃.

[0022] The saturated vapor pressure of heavy aromatics is further reduced to conduct a second condensation separation of heavy aromatics in the tail gas, and the recovery effect is improved by 15%; at the same time, the power generation during the operation process is increased by 10% compared with similar devices. The temperature of the gas recovered from the second time is 0.2℃, and it is heat exchanged with the electronic grade hydrogen peroxide raw material to reduce the feed temperature. In terms of cold utilization, the effect is obvious, the comprehensive utilization of energy is improved, the economic benefits of electricity saving are considerable, and it is more conducive to the condensation and purification of heavy aromatics in the tail gas.

[0023] Compared with the prior art, the utility model has the following advantages:

[0024] 1. Reduce the consumption of heavy aromatics. Compared with the traditional process, the consumption of heavy aromatics is reduced by 30%;

[0025] 2. Avoid the problem of crystallization blockage caused by water in tail gas, and use more recovered energy for power generation. The power generation is increased by 10%;

[0026] 3. Comprehensive utilization of cooling capacity to save water and electricity, and reduce energy consumption by 5%;

[0027] 4. Reduce the entrainment of organic gas in the exhaust gas, control the organic gas content entering the tail gas treatment unit from the source, reduce VOCs emission values, and increase the life of the tail gas adsorption unit. The VOCs source emission value is reduced by 70%. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] 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.

[0029] Figure 1 It is a schematic diagram of the overall structure of the hydrogen peroxide tail gas comprehensive utilization system of the utility model.

[0030] In the figure: 1. first coalescence and separation unit; 101. cooler; 102. primary tail gas condensate receiving tank; 2. second coalescence and separation unit; 201. cold box; 202. heat exchanger; 203. first tail gas condensate receiving tank; 204. second tail gas condensate receiving tank; 205. expansion generator; 3. tail gas treatment unit; 4. primary aromatics recovery tank; 5. first aromatics recovery tank; 6. second aromatics recovery tank; 7. cold capacity recycling heat exchange device. DETAILED DESCRIPTION

[0031] 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.

[0032] 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.

[0033] 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.

[0034] like Figure 1 As shown, a hydrogen peroxide tail gas comprehensive utilization system includes a first coalescence and separation unit 1, a second coalescence and separation unit 2 and a tail gas treatment unit 3.

[0035] The first coalescence separation unit 1 comprises a cooler 101 and a primary tail gas condensate receiving tank 102. The cooler 101 is provided with an oxidized tail gas inlet, which is communicated with the cooler 101. The cooler 101 is communicated with the first tail gas condensate receiving tank 203. The primary tail gas condensate receiving tank 102 is provided with a primary aromatics recovery tank 4, which is communicated with the primary tail gas condensate receiving tank 102.

[0036] The second condensation and separation unit includes a cold box 201, a heat exchanger 202, a first tail gas condensate receiving tank 203, a second tail gas condensate receiving tank 204 and an expansion generator 205. The cold box 201 is connected to the heat exchanger 202, the first tail gas condensate receiving tank 203 and the second tail gas condensate receiving tank 204. The first tail gas condensate receiving tank 203 is provided with a first aromatic hydrocarbon recovery tank 5, and the first aromatic hydrocarbon recovery tank 5 is connected to the first tail gas condensate receiving tank 203. The second tail gas condensate receiving tank 204 is provided with a second aromatic hydrocarbon recovery tank 6, and the second aromatic hydrocarbon recovery tank 6 is connected to the second tail gas condensate receiving tank 204. The heat exchanger 202 is provided with a cold amount recycling heat exchange device 7, and the cold amount recycling heat exchange device 7 is connected to the heat exchanger 202.

[0037] An expansion generator 205 is disposed between the first tail gas condensate receiving tank 203 and the second tail gas condensate receiving tank 204 , and the expansion generator 205 is communicated with the first tail gas condensate receiving tank 203 and the second tail gas condensate receiving tank 204 .

[0038] The heat exchanger 202 is also connected to the tail gas treatment unit 3 .

[0039] The system is connected to an external oxidation tower. The oxidation tail gas coming out from the top of the oxidation tower is collected and initially condensed with the entrained solvent through a cooler 101, and then enters a primary tail gas condensate receiving tank to separate the condensed solvent.

[0040] The cold box 201 is divided into a pre-cooling and reheating section and a condensing section. Before the hydrogen peroxide tail gas separated and purified after condensation enters the expander, an indirect heat exchange and reheating process of the tail gas is added. Because the separation and purification of the oxidation tail gas is carried out at high pressure and low temperature, it becomes a superheated gas for the small amount of heavy aromatics contained in it after reheating, which is more conducive to the separation of aromatics.

[0041] The cooled gas enters the first tail gas condensate receiving tank 203 for gas-liquid separation, and the solvent therein is further recovered, and the solvent recovery and utilization is increased by 30%.

[0042] Before entering the expansion generator 205, a heat exchange is added to reduce the temperature of the hydrogen peroxide tail gas entering the expander, and the first tail gas condensate receiving tank 203 is used to separate the water and aromatic hydrocarbons in the atomized state, further removing the liquid medium in the tail gas, avoiding the problem of ice clogging of the entrained water during the expansion and cooling process, and preventing the expander from malfunctioning and damaging the equipment.

[0043] The tail gas from the outlet of the first tail gas condensate tank enters the expansion end inlet of the expander, and the residual pressure is used to drive the expander impeller to rotate at high speed to further expand and cool the tail gas. The temperature can be controlled at 0-0.5℃.

[0044] The saturated vapor pressure of heavy aromatics is further reduced to conduct a second condensation separation of heavy aromatics in the tail gas, and the recovery effect is improved by 15%; at the same time, the power generation during the operation process is increased by 10% compared with similar devices. The temperature of the gas recovered from the second time is 0.2℃, and it is heat exchanged with the electronic grade hydrogen peroxide raw material to reduce the feed temperature. In terms of cold utilization, the effect is obvious, the comprehensive utilization of energy is improved, the economic benefits of electricity saving are considerable, and it is more conducive to the condensation and purification of heavy aromatics in the tail gas.

[0045] The operation process of the hydrogen peroxide tail gas comprehensive utilization system of the utility model is as follows:

[0046] The oxidized tail gas separated by the built-in separator at the top of the oxidation tower is collected and initially condensed with the entrained solvent through the cooler 101, and enters the primary tail gas condensate receiving tank 102 to separate the condensed solvent, and the separated solvent enters the primary aromatic hydrocarbon recovery tank 4. After the tail gas after gas-liquid separation is pressure-controlled by the regulating valve, it enters the cold box 201 by utilizing the residual pressure, and performs heat exchange with the low-temperature tail gas from the expansion end of the expansion generator 205, and then the cooled gas enters the first tail gas condensate receiving tank 203 for gas-liquid separation, and further recovers the solvent therein.

[0047] The tail gas at the outlet of the first tail gas condensate receiving tank 203 enters the expansion end inlet of the expander, and the residual pressure is used to drive the expander impeller to rotate at high speed to further expand and cool the tail gas. The cooled tail gas enters the second tail gas condensate receiving tank 204 to further recover the solvent therein, and then enters the tail gas treatment unit 3 after heat exchange with the oxidized tail gas. The tail gas treatment unit 3 is used to adsorb the solvent entrained in the tail gas, and the purified oxidized tail gas is discharged to the high altitude. The expansion generator 205 has its own generator to generate electricity, and the power generation capacity of the oxidized tail gas is about 487kW·h per hour, and 3.9 millionkW·h of electricity can be recovered annually.

[0048] 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 hydrogen peroxide tail gas comprehensive utilization system, characterized in that: The hydrogen peroxide tail gas comprehensive utilization system comprises a first coalescence and separation unit (1), a second coalescence and separation unit (2) and a tail gas treatment unit (3); The first coalescence separation unit (1) comprises a cooler (101) and a primary tail gas condensate receiving tank (102), wherein the cooler (101) is in communication with the first tail gas condensate receiving tank (203); The second condensation and separation unit comprises a cold box (201), a heat exchanger (202), a first tail gas condensate receiving tank (203), a second tail gas condensate receiving tank (204) and an expansion generator (205), wherein the cold box (201) is connected to the heat exchanger (202), the first tail gas condensate receiving tank (203) and the second tail gas condensate receiving tank (204); An expansion generator (205) is disposed between the first tail gas condensate receiving tank (203) and the second tail gas condensate receiving tank (204), and the expansion generator (205) is communicated with both the first tail gas condensate receiving tank (203) and the second tail gas condensate receiving tank (204); The heat exchanger (202) is also in communication with the tail gas treatment unit (3).

2. The hydrogen peroxide tail gas comprehensive utilization system according to claim 1, characterized in that: The primary tail gas condensate receiving tank (102) is provided with a primary aromatic hydrocarbon recovery tank (4), and the primary aromatic hydrocarbon recovery tank (4) is connected to the primary tail gas condensate receiving tank (102).

3. The hydrogen peroxide tail gas comprehensive utilization system according to claim 1, characterized in that: The first tail gas condensate receiving tank (203) is provided with a first aromatic hydrocarbon recovery tank (5), and the first aromatic hydrocarbon recovery tank (5) is connected to the first tail gas condensate receiving tank (203).

4. The hydrogen peroxide tail gas comprehensive utilization system according to claim 1, characterized in that: The second tail gas condensate receiving tank (204) is provided with a second aromatic hydrocarbon recovery tank (6), and the second aromatic hydrocarbon recovery tank (6) is connected to the second tail gas condensate receiving tank (204).

5. The hydrogen peroxide tail gas comprehensive utilization system according to claim 1, characterized in that: The heat exchanger (202) is provided with a cold energy recycling heat exchange device (7), and the cold energy recycling heat exchange device (7) is connected to the heat exchanger (202).

6. The hydrogen peroxide tail gas comprehensive utilization system according to claim 1, characterized in that: The cooler (101) is provided with an oxidation tail gas inlet, and the oxidation tail gas inlet is in communication with the cooler (101).