Hydrogenated tail gas recovery system of anthraquinone process hydrogen peroxide production device

Abstract

The utility model provides a hydrogenated tail gas recovery system of an anthraquinone process hydrogen peroxide production device, which comprises a hydrogenation tower, a first gas-liquid separation tank connected with the hydrogenation tower through a pipeline, a purification tower connected with the first gas-liquid separation tank through a pipeline, a cooler connected with the purification tower through a pipeline, and a second gas-liquid separation tank connected with the cooler through a pipeline, the second gas-liquid separation tank is connected with a compressor through a pipeline, one side of the compressor is connected with a third gas-liquid separation tank, the third gas-liquid separation tank is connected with a temperature swing adsorption tower through a pipeline, the temperature swing adsorption tower is respectively connected with a heater and a gas buffer tank through pipelines, and the gas buffer tank is connected with a liquid collection pool through a pipeline. According to the hydrogenated tail gas recovery system of the anthraquinone process hydrogen peroxide production device, hydrogen in the hydrogenated tail gas is purified and then is recycled as a reaction raw material, so that the waste of the hydrogen is avoided.

Description

Technical Field

[0001] The utility model relates to the field of hydrogen peroxide, in particular to a hydrogenation tail gas recovery system of an anthraquinone method hydrogen peroxide production device. Background Art

[0002] Hydrogen peroxide is an aqueous solution of hydrogen peroxide, commonly used for sterilization and disinfection. Hydrogen peroxide solution is an explosive chemical.

[0003] According to the data of a 200,000 tons / year 27.5% hydrogen peroxide production unit, the unit hydrogen consumption is about 200Nm3 / t, while the theoretical unit hydrogen consumption is about 180Nm3 / t. There are many reasons for excessive hydrogen consumption, such as hydrogen peroxide refining loss, by-product generation, etc. However, the most important reason is that the hydrogenated tail gas is not recycled but directly vented. If the hydrogenated tail gas of the anthraquinone method hydrogen peroxide production unit can be reasonably utilized, the hydrogen consumption will be greatly reduced, reducing production costs for the enterprise.

[0004] The patent application with publication number CN202310718971 proposed in the prior art directly recycles the hydrogenated tail gas after gas-liquid separation through the system. However, since the hydrogenated tail gas contains anthraquinone, a solid that is easy to precipitate, it is very easy to cause pipe blockage, affecting stable operation. In addition, the hydrogen content in the hydrogenated tail gas is about 75% v / v, which is far from the requirement that the hydrogen content in the hydrogenation step of the anthraquinone method hydrogen peroxide production device is ≥99% v / v, which is easy to cause adverse effects such as increased by-products and difficult to control hydrogenation.

[0005] Therefore, it is necessary to provide a hydrogenation tail gas recovery system for an anthraquinone method hydrogen peroxide production device to solve the above technical problems. Utility Model Content

[0006] The utility model provides a hydrogenation tail gas recovery system for an anthraquinone method hydrogen peroxide production device, which solves the problem that the hydrogenation tail gas contains anthraquinone, which is a solid that is easy to precipitate, which easily causes pipe blockage and affects stable operation, and also causes adverse effects such as increased by-products and difficult control of hydrogenation.

[0007] In order to solve the above technical problems, the utility model provides a hydrogenation tail gas recovery system of an anthraquinone method hydrogen peroxide production device, comprising:

[0008] A hydrogenation tower, wherein the hydrogenation tower is connected to a first gas-liquid separation tank through a pipeline, the first gas-liquid separation tank is connected to a purification tower through a pipeline, the purification tower is connected to a cooler through a pipeline, the cooler is connected to a second gas-liquid separation tank through a pipeline, the second gas-liquid separation tank is connected to a compressor through a pipeline, one side of the compressor is connected to a third gas-liquid separation tank, the third gas-liquid separation tank is connected to a temperature-variable adsorption tower through a pipeline, the temperature-variable adsorption tower is respectively connected to a heater and a gas buffer tank through pipelines, and the gas buffer tank is connected to a liquid collecting tank through a pipeline.

[0009] Preferably, the third gas-liquid separation tank, the second gas-liquid separation tank and the purification tower are all connected to the liquid collecting tank through pipelines.

[0010] Preferably, a disassembly groove is provided on the surface of the temperature-swing adsorption tower.

[0011] Preferably, a disassembly cover is provided inside the disassembly groove.

[0012] Preferably, sealing components are provided on both sides of the inner wall of the disassembly groove, and the sealing component includes a sealing groove, and a sealing block is provided inside the sealing groove, and the sealing block is connected to the disassembly cover.

[0013] Preferably, a fixing assembly is provided between the temperature-variable adsorption tower and the disassembly cover, and the fixing assembly includes two fixing rings, and a fixing bolt is provided between the two fixing rings.

[0014] Preferably, the two fixing rings and the fixing bolt act to fix the disassembly cover and the temperature-variable adsorption tower.

[0015] Compared with the related art, the hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device provided by the utility model has the following beneficial effects:

[0016] The utility model provides a hydrogenation tail gas recovery system for an anthraquinone method hydrogen peroxide production device, which purifies the hydrogen in the hydrogenation tail gas and recycles it as a reaction raw material, thereby avoiding hydrogen waste;

[0017] The newly added purification tower equipment removes easily precipitated solids such as anthraquinone and hydroanthraquinone carried in the hydrogenation tail gas, so that the subsequent equipment can operate stably and avoid pipe blockage;

[0018] The purity of hydrogen has been improved by adding temperature swing adsorption related equipment, meeting the purity requirements of hydrogen for hydrogenation operations, and can be used directly as a reaction raw material;

[0019] Use chilled water as the cooler refrigerant to achieve better gas-liquid separation effect. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1A schematic structural diagram of a first embodiment of a hydrogenation tail gas recovery system of an anthraquinone method hydrogen peroxide production device provided by the utility model;

[0021] Figure 2 A schematic structural diagram of a second embodiment of a hydrogenation tail gas recovery system of an anthraquinone method hydrogen peroxide production device provided by the utility model;

[0022] Figure 3 for Figure 2 An enlarged schematic diagram of part A is shown;

[0023] Figure 4 for Figure 2 A three-dimensional schematic diagram of the overall device shown.

[0024] Numbers in the figure: 1, hydrogenation tower, 2, first gas-liquid separation tank, 3, purification tower, 4, cooler, 5, second gas-liquid separation tank, 6, compressor, 7, liquid collecting tank, 8, third gas-liquid separation tank, 9, temperature swing adsorption tower, 10, heater, 11, gas buffer tank,

[0025] 12. Disassembly slot, 13. Disassembly cover,

[0026] 14. Sealing assembly, 141. Sealing groove, 142. Sealing block,

[0027] 15. fixing assembly, 151. fixing ring, 152. fixing bolt. DETAILED DESCRIPTION

[0028] The utility model is further described below in conjunction with the accompanying drawings and implementation modes.

[0029] First embodiment

[0030] Please refer to Figure 1 ,in, Figure 1 The present invention provides a schematic structural diagram of a first embodiment of a hydrogenation tail gas recovery system for an anthraquinone method hydrogen peroxide production device. A hydrogenation tail gas recovery system for an anthraquinone method hydrogen peroxide production device comprises:

[0031] A hydrogenation tower 1, wherein the hydrogenation tower 1 is connected to a first gas-liquid separation tank 2 through a pipeline, the first gas-liquid separation tank 2 is connected to a purification tower 3 through a pipeline, the purification tower 3 is connected to a cooler 4 through a pipeline, the cooler 4 is connected to a second gas-liquid separation tank 5 through a pipeline, the second gas-liquid separation tank 5 is connected to a compressor 6 through a pipeline, one side of the compressor 6 is connected to a third gas-liquid separation tank 8, the third gas-liquid separation tank 8 is connected to a temperature-variable adsorption tower 9 through a pipeline, the temperature-variable adsorption tower 9 is respectively connected to a heater 10 and a gas buffer tank 11 through pipelines, and the gas buffer tank 11 is connected to a liquid collecting tank 7 through a pipeline.

[0032] The third gas-liquid separation tank 8 , the second gas-liquid separation tank 5 and the purification tower 3 are all connected to the liquid collecting tank 7 through pipelines.

[0033] The connection method is as follows: the hydrogen inlet pipe is connected to the upper part of the hydrogenation tower 1, the bottom of the hydrogenation tower 1 is connected to the top of the first gas-liquid separation tank 2, the upper part of the first gas-liquid separation tank 2 is connected to the upper part of the purification tower 3 through a pipeline, the pipeline extends inside the purification tower 3 to the lower part of the purification tower 3, the bottom of the first gas-liquid separation tank 2 discharges the hydrogenated liquid to the downstream process through a pipeline, the heavy aromatics feed pipeline is connected to the upper part of the purification tower 3, the lower part of the purification tower 3 is connected to the liquid collecting tank 7 through a pipeline, the lower part of the purification tower 3 is connected to the upper heat medium inlet of the cooler 4, the lower heat medium outlet of the cooler 4 is connected to the top of the second gas-liquid separation tank 5, the middle part of the second gas-liquid separation tank 5 is connected to the air inlet of the compressor 6, and the bottom of the second gas-liquid separation tank 5 is connected to the liquid collecting tank 7 through a pipeline. The air outlet of the compressor 6 is connected to the middle part of the third gas-liquid separation tank 8 through a pipeline, the bottom of the third gas-liquid separation tank 8 is connected to the liquid collecting tank 7 through a pipeline, the middle part of the third gas-liquid separation tank 8 is connected to the bottom of the temperature swing adsorption tower 9 through a pipeline, a bypass at the top of the temperature swing adsorption tower 9 is connected to the middle part of the gas buffer tank 11, another bypass at the top of the temperature swing adsorption tower 9 is connected to the refrigerant outlet at the top of the heater 10, the bottom of the heater 10 is connected to the refrigerant inlet pipeline, the regenerated gas enters the heater 10 through the pipeline, the bottom of the temperature swing adsorption tower 9 is connected to another bypass, the material goes to the torch through the pipeline, the top of the gas buffer tank 11 is connected to the hydrogen pipeline entering the hydrogenation tower 1, and the bottom of the gas buffer tank 11 is connected to the liquid collecting tank 7 through a pipeline.

[0034] The working principle is that the hydrogenated liquid in the hydrogenation tower enters the first gas-liquid separation tank 2, and gas-liquid separation is carried out in the first gas-liquid separation tank 2. The hydrogenated liquid goes to the downstream process through the bottom pipeline of the first gas-liquid separation tank 2, and the hydrogenated tail gas enters the lower part of the purification tower 3 through the pipeline. An appropriate amount of heavy aromatic hydrocarbons is added to the purification tower 3 to absorb anthraquinone, hydroanthraquinone and other easily precipitated solids entrained in the hydrogenated tail gas. When the content of anthraquinone and hydroanthraquinone in the heavy aromatic hydrocarbons reaches a certain level, they are gradually discharged to the liquid collecting pool, and heavy aromatic hydrocarbons are added to maintain the liquid level in the purification tower 3. The hydrogenated tail gas that has been removed by the purification tower 3 is cooled by the cooler 4 to remove the liquid entrained in the hydrogenated tail gas. The cooler 4 uses chilled water for cooling, and the chilled water temperature is 7-11°C. The hydrogenated tail gas cooled by the cooler 4 enters the second gas-liquid separation tank 5 to separate the gas and liquid phases. To prevent liquid from entering the compressor 6 and damaging the equipment, the second gas-liquid separation tank 5 separates the liquid phase and enters the liquid collecting pool 7. The hydrogenated tail gas in the second gas-liquid separation tank 5 is pressurized by the compressor 6 and enters the third gas-liquid separation tank 8. The gas-liquid separation is further performed in the third gas-liquid separation tank 8. The liquid phase is separated from the third gas-liquid separation tank 8 and enters the liquid collecting pool 7. The high-pressure hydrogenated tail gas in the third gas-liquid separation tank 8 enters the temperature swing adsorption tower 9. The temperature swing adsorption tower 9 is filled with a temperature swing adsorbent, which selectively adsorbs impurities in the hydrogenated tail gas under low temperature and high pressure conditions to improve the purity of hydrogen. The hydrogenated tail gas with improved purity enters the gas buffer tank 11. The liquid phase is separated from the gas buffer tank 11 and enters the liquid collecting pool 7. The purified hydrogenated tail gas in the gas buffer tank 11 is depressurized by a pressure reducing valve and then merged into the hydrogen pipeline and enters the hydrogenation tower 1 for recycling.

[0035] The valves on the connecting pipelines of the heater 10, the flare tube and the adsorption tower are in a closed state when the temperature swing adsorption tower 9 is working normally for adsorption. When the temperature swing adsorption tower 9 is saturated with adsorption, the valves on the connecting pipelines of the temperature swing adsorption tower and the third gas-liquid separation tank 8 and the gas buffer tank 11 are closed, and the valves on the connecting pipelines of the heater 10, the flare tube and the adsorption tower are opened. The regenerated gas heated by the heater 10 is used to enter the temperature swing adsorption tower 9 for desorption operation to clean the impurities adsorbed by the adsorbent. The regenerated gas and the cleaned impurities are directly sent to the flare, and higher purity raw hydrogen can be used as the regeneration gas.

[0036] Since the main component of the liquid in the liquid collecting pool 7 is heavy aromatic hydrocarbons, after a certain liquid level solution is accumulated, it can be used as a raw material for configuring the working liquid.

[0037] Main control parameters: gas phase pressure of the first gas-liquid separation tank is 0.2-0.5Mpa, the liquid level of the purification tower is related to the gas phase pressure of the first gas-liquid separation tank to ensure that the gas overflows with a pressure of at least 0.1-0.5Mpa, the compressor outlet pressure is 2-3Mpa, the hydrogenated tail gas purified in the gas buffer tank has an output pressure of 0.2-0.5Mpa after passing through the pressure reducing valve, the normal working pressure of the temperature swing adsorption tower is 2-3Mpa, and the working temperature is 10-20℃, and the working pressure of the temperature swing adsorption tower during desorption is 0.01-0.05Mpa and the working temperature is 20-40℃.

[0038] Compared with the related art, the hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device provided by the utility model has the following beneficial effects:

[0039] The utility model provides a hydrogenation tail gas recovery system for an anthraquinone method hydrogen peroxide production device, which purifies the hydrogen in the hydrogenation tail gas and recycles it as a reaction raw material, thereby avoiding hydrogen waste;

[0040] The newly added purification tower equipment removes easily precipitated solids such as anthraquinone and hydroanthraquinone carried in the hydrogenation tail gas, so that the subsequent equipment can operate stably and avoid pipe blockage;

[0041] The purity of hydrogen has been improved by adding temperature swing adsorption related equipment, meeting the purity requirements of hydrogen for hydrogenation operations, and can be used directly as a reaction raw material;

[0042] Use chilled water as the cooler refrigerant to achieve better gas-liquid separation effect.

[0043] Second embodiment

[0044] Please refer to Figure 2 , Figure 3 and Figure 4 Based on the hydrogenation tail gas recovery system of an anthraquinone method hydrogen peroxide production device provided in the first embodiment of the present application, the second embodiment of the present application proposes another hydrogenation tail gas recovery system of an anthraquinone method hydrogen peroxide production device. The second embodiment is only a preferred embodiment of the first embodiment, and the implementation of the second embodiment will not affect the independent implementation of the first embodiment.

[0045] Specifically, the difference of the hydrogenated tail gas recovery system of the anthraquinone method hydrogen peroxide production device provided in the second embodiment of the present application is that, in the hydrogenated tail gas recovery system of the anthraquinone method hydrogen peroxide production device, a disassembly groove 12 is provided on the surface of the temperature variable adsorption tower 9.

[0046] A disassembly cover 13 is disposed inside the disassembly groove 12 .

[0047] Sealing components 14 are disposed on both sides of the inner wall of the disassembly groove 12 . The sealing component 14 includes a sealing groove 141 . A sealing block 142 is disposed inside the sealing groove 141 . The sealing block 142 is connected to the disassembly cover 13 .

[0048] The use of the sealing groove 141 and the sealing block 142 facilitates sealing of the gap when the disassembly groove 12 is connected to the disassembly cover 13 .

[0049] A fixing assembly 15 is disposed between the temperature-swing adsorption tower 9 and the disassembly cover 13 . The fixing assembly 15 includes two fixing rings 151 . A fixing bolt 152 is disposed between the two fixing rings 151 .

[0050] The two fixing rings 151 and the fixing bolts 152 are used to fix the disassembly cover 13 and the temperature swing adsorption tower 9 .

[0051] The working principle of the hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device provided by the utility model is as follows:

[0052] During use, when disassembling the components inside the temperature-variable adsorption tower 9, first take out the fixing bolt 152 between the two sets of fixing rings 151. After the fixing bolt 152 is taken out, pull the disassembly cover 13 to move to the outside of the disassembly groove 12. When the disassembly cover 13 moves to the outside of the disassembly groove 12, it drives the sealing block 142 to separate from the sealing groove 141.

[0053] Compared with the related art, the hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device provided by the utility model has the following beneficial effects:

[0054] The utility model provides a hydrogenation tail gas recovery system of an anthraquinone method hydrogen peroxide production device. A disassembly groove 12, a disassembly cover 13, a sealing component 14 and a fixing component 15 are arranged on the surface of a temperature-swing adsorption tower 9 for use in conjunction with each other, so as to facilitate disassembly and replacement of components inside the temperature-swing adsorption tower 9.

[0055] The above description is only an embodiment of the present invention, and does not limit the patent scope of the present invention. Any equivalent structure or equivalent process transformation made by using the contents of the specification and drawings of the present invention, or directly or indirectly applied in other related technical fields, are also included in the patent protection scope of the present invention.

Claims

1. A hydrogenation tail gas recovery system for an anthraquinone process hydrogen peroxide production device, characterized in that: include: A hydrogenation tower, wherein the hydrogenation tower is connected to a first gas-liquid separation tank through a pipeline, the first gas-liquid separation tank is connected to a purification tower through a pipeline, the purification tower is connected to a cooler through a pipeline, the cooler is connected to a second gas-liquid separation tank through a pipeline, the second gas-liquid separation tank is connected to a compressor through a pipeline, one side of the compressor is connected to a third gas-liquid separation tank, the third gas-liquid separation tank is connected to a temperature-variable adsorption tower through a pipeline, the temperature-variable adsorption tower is respectively connected to a heater and a gas buffer tank through pipelines, and the gas buffer tank is connected to a liquid collecting tank through a pipeline.

2. The hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device according to claim 1, characterized in that: The third gas-liquid separation tank, the second gas-liquid separation tank and the purification tower are all connected to the liquid collecting tank through pipelines.

3. The hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device according to claim 1, characterized in that: A disassembly groove is provided on the surface of the temperature-swing adsorption tower.

4. The hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device according to claim 3, characterized in that: A disassembly cover is arranged inside the disassembly groove.

5. The hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device according to claim 4, characterized in that: Sealing components are arranged on both sides of the inner wall of the disassembly groove. The sealing component comprises a sealing groove. A sealing block is arranged inside the sealing groove. The sealing block is connected to the disassembly cover.

6. The hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device according to claim 4, characterized in that: A fixing assembly is arranged between the temperature-variable adsorption tower and the disassembly cover, and the fixing assembly comprises two fixing rings, and a fixing bolt is arranged between the two fixing rings.

7. The hydrogenation tail gas recovery system of the anthraquinone method hydrogen peroxide production device according to claim 6, characterized in that: The two fixing rings and the fixing bolt act to fix the disassembly cover and the temperature-variable adsorption tower.

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