Carbon-reduced tail gas recovery device and hydrogen peroxide production system

Abstract

The utility model provides a carbon-reduced tail gas recovery device and a hydrogen peroxide production system, and relates to the technical field of batteries. The tail gas recovery device comprises a nitrogen making machine, an air compressor, an activated carbon adsorption tank, a gas storage tank and a first control pipeline, an inlet of the activated carbon adsorption tank is communicated with an outlet of the gas storage tank, an outlet of the activated carbon adsorption tank is communicated with an inlet of the air compressor through the first control pipeline, and an outlet of the air compressor is communicated with an inlet of the nitrogen making machine; and the first control pipeline at least can be switched between a connected state and a disconnected state. When the tail gas discharged by the hydrogen peroxide production system is used as the nitrogen-making raw material gas, only trace trimethylbenzene and other impurities need to be removed at the inlet of the air compressor, and then the tail gas is compressed and enters the nitrogen making machine, so that the device has the advantages of less pollution, low energy consumption, carbon and emission reduction and low cost.

Description

Technical Field

[0001] The present application relates to the technical field of batteries, and particularly to a tail gas recovery device for carbon reduction and a hydrogen peroxide production system. Background Art

[0002] How to reduce carbon emissions is one of the means for enterprises to enhance product competitiveness. Then, how to reduce carbon emissions during the production process of hydrogen peroxide is one of the research directions of enterprises. Content of the Utility Model

[0003] In view of this, the purpose of the present application is to overcome the deficiencies in the prior art, and provide a tail gas recovery device for carbon reduction and a hydrogen peroxide production system, aiming to solve the problem of relatively large carbon emissions during the production process of hydrogen peroxide in the prior art.

[0004] The present application provides the following technical solutions:

[0005] In a first aspect, an embodiment of the present application provides a tail gas recovery device for carbon reduction. The tail gas recovery device for carbon reduction includes a nitrogen generator, an air compressor, an activated carbon adsorption tank, a gas storage tank, and a first control pipeline. The inlet of the activated carbon adsorption tank is communicated with the outlet of the gas storage tank, the outlet of the activated carbon adsorption tank is communicated with the inlet of the air compressor through the first control pipeline, and the outlet of the air compressor is communicated with the inlet of the nitrogen generator; wherein, the first control pipeline can at least switch between a connected state and a disconnected state.

[0006] In one of the embodiments of the first aspect, the number of the activated carbon adsorption tanks is multiple, and the multiple activated carbon adsorption tanks are arranged in parallel;

[0007] The tail gas recovery device for carbon reduction further includes a second control pipeline, and the outlet of the air compressor is further communicated with the outlet of the activated carbon adsorption tank through the second control pipeline;

[0008] wherein, the second control pipeline can at least switch between a connected state and a disconnected state.

[0009] In one of the embodiments of the first aspect, the tail gas recovery device for carbon reduction further includes a gas-gas heat exchanger. The gas-gas heat exchanger has a cold medium inlet, a cold medium outlet, a hot medium inlet, and a hot medium outlet. The outlet of the activated carbon adsorption tank is communicated with the cold medium inlet through the first control pipeline, the cold medium outlet is communicated with the inlet of the air compressor, and the inlet of the activated carbon adsorption tank is communicated with the hot medium inlet.

[0010] In one embodiment of the first aspect, the tail gas recovery device for carbon reduction further includes a gas-liquid separator and a third control pipeline. The gas-liquid separator has a gas-liquid mixture inlet. The inlet of the activated carbon adsorption tank is communicated with the heat medium inlet through the third control pipeline. The heat medium outlet is communicated with the gas-liquid mixture inlet. The third control pipeline can at least switch between a connected state and a disconnected state.

[0011] In one embodiment of the first aspect, the tail gas recovery device for carbon reduction further includes a gas-liquid condenser. The gas-liquid condenser has a gas phase inlet. The gas-liquid separator also has a gas outlet. The gas phase inlet is communicated with the gas outlet.

[0012] In one embodiment of the first aspect, the tail gas recovery device for carbon reduction further includes a storage tank. The gas-liquid separator also has a liquid outlet. The gas-liquid condenser also has a condensate outlet. The storage tank is respectively communicated with the condensate outlet and the liquid outlet.

[0013] In one embodiment of the first aspect, the tail gas recovery device for carbon reduction further includes:

[0014] A fourth control pipeline. The outlet of the activated carbon adsorption tank is also communicated with the cold medium inlet of the gas-gas heat exchanger through the fourth control pipeline. Wherein, the fourth control pipeline can at least switch between a connected state and a disconnected state.

[0015] In one embodiment of the first aspect, the first control pipeline includes:

[0016] A first switch valve, a first main pipeline and a first branch pipeline. The outlet of the activated carbon adsorption tank is sequentially communicated with the cold medium inlet through the first branch pipeline and the first main pipeline. The first switch valve is installed on the first branch pipeline;

[0017] The second control pipeline includes:

[0018] A second switch valve, a second main pipeline and a second branch pipeline. The outlet of the air compressor is sequentially communicated with the outlet of the activated carbon adsorption tank through the second main pipeline and the second branch pipeline. The second switch valve is installed on the second branch pipeline; The diameter of the second main pipeline is smaller than the diameter of the outlet of the air compressor;

[0019] The third control pipeline includes:

[0020] A third switch valve, a third main pipeline and a third branch pipeline. The inlet of the activated carbon adsorption tank is sequentially communicated with the heat medium inlet through the third branch pipeline and the third main pipeline. The third switch valve is installed on the third branch pipeline;

[0021] The fourth control pipeline includes:

[0022] A fourth switching valve and a fourth main pipeline. The first main pipeline is connected to the second main pipeline through the fourth main pipeline. The fourth switching valve is installed on the fourth main pipeline, and a seventh switching valve is installed on the second main pipeline. In the gas flow direction in the second main pipeline, the connection between the fourth main pipeline and the second main pipeline is located downstream of the seventh switching valve, and the diameter of the fourth main pipeline is smaller than that of the first main pipeline.

[0023] In one embodiment of the first aspect, the carbon-reducing tail gas recovery device further includes an intake control pipeline. The intake control pipeline includes a main intake pipeline, a branch intake pipeline, a fifth switching valve, and a sixth switching valve. The main intake pipeline is communicated with the inlet of the corresponding activated carbon adsorption tank through the branch intake pipeline. The fifth switching valve and the sixth switching valve are arranged at intervals in the extending direction of the branch intake pipeline. The sixth switching valve is located between the fifth switching valve and the corresponding activated carbon adsorption tank, and the third main pipeline is connected to the branch intake pipeline through a third branch pipeline. The connection between the third branch pipeline and the branch intake pipeline is located between the fifth switching valve and the sixth switching valve.

[0024] In a second aspect, an embodiment of the present application further provides a hydrogen peroxide production system, including an oxidation tower, an expansion refrigeration generator, a tail gas treatment system, and the carbon-reducing tail gas recovery device according to any one of the above embodiments. The oxidation tower, the expansion refrigeration generator, the tail gas treatment system, and the carbon-reducing tail gas recovery device are connected in sequence.

[0025] The embodiments of the present application have the following advantages:

[0026] The present application provides a carbon-reducing tail gas recovery device. The parallel use and circulating reflux design of the activated carbon adsorption tanks reduce the burden on the activated carbon, may extend its service life, and reduce carbon emissions. In addition, when using the tail gas discharged from the hydrogen peroxide production system as the raw material gas for nitrogen production, it only needs to remove trace impurities such as trimethylbenzene at the inlet of the air compressor and then be compressed into the nitrogen generator. Its advantages are less pollution, low energy consumption, carbon reduction and emission reduction, and low cost. It should be noted that although the operation of directly recovering nitrogen in the tail gas itself does not reduce carbon emissions, it indirectly promotes the reduction of carbon emissions by improving efficiency, promoting resource recycling, reducing waste emissions, and optimizing the production process, which is in line with the sustainable development goal.

[0027] In addition, the present application also relates to a hydrogen peroxide production system. Since the carbon-reducing tail gas recovery device has the above technical effects, the hydrogen peroxide production system including the carbon-reducing tail gas recovery device should have the same technical effects, which will not be elaborated here. Description of the Drawings

[0028] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings required for the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of the present application, and therefore should not be regarded as a limitation of the scope. For those of ordinary skill in the art, without creative efforts, other related drawings can also be obtained based on these drawings.

[0029] Figure 1 Fig. shows a schematic structural diagram of a hydrogen peroxide production system provided by an embodiment of the present application.

[0030] Main element symbol description:

[0031] 100 - Hydrogen peroxide production system; 110 - Tail gas treatment system; 120 - Expansion refrigeration generator; 130 - Oxidation tower; 200 - Gas storage tank; 300 - First activated carbon adsorption tank; 400 - Second activated carbon adsorption tank; 500 - Intake air control pipeline; 510 - Sixth switching valve; 520 - Branch intake pipeline; 530 - Fifth switching valve; 540 - Main intake pipeline; 600 - Third control pipeline; 610 - Third switching valve; 620 - Third branch pipeline; 630 - Third main pipeline; 640 - Low point drain port; 650 - Eighth switching valve; 700 - First control pipeline; 710 - First main pipeline; 720 - First switching valve; 730 - First branch pipeline; 800 - Fourth control pipeline; 810 - Fourth switching valve; 820 - Fourth main pipeline; 900 - Second control pipeline; 910 - Second main pipeline; 920 - Seventh switching valve; 930 - Second switching valve; 940 - Second branch pipeline; 1000 - Gas - gas heat exchanger; 1100 - Silencer; 1200 - Gas - liquid condenser; 1300 - Gas - liquid separator; 1400 - Air compressor; 1500 - Buffer tank; 1600 - Nitrogen generator; 1700 - Storage tank. Detailed Embodiments

[0032] The embodiments of the present application will be described in detail below. The examples of the embodiments are shown in the drawings, where the same or similar reference numerals represent the same or similar elements or elements with the same or similar functions throughout. The embodiments described below by referring to the drawings are exemplary and are only used to explain the present application and should not be construed as a limitation of the present application.

[0033] It should be noted that when an element is referred to as "fixed to" another element, it can be directly on the other element or there may also be an intermediate element. When an element is considered to be "connected" to another element, it can be directly connected to the other element or there may be an intermediate element at the same time. On the contrary, when an element is referred to as being "directly on" another element, there is no intermediate element. The terms "vertical", "horizontal", "left", "right" and similar expressions used herein are for illustrative purposes only.

[0034] In this application, unless otherwise clearly specified and defined, terms such as "installed", "connected", "joined", "fixed", etc. shall be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or integrated; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the internal communication of two elements or the interaction relationship between two elements. For those of ordinary skill in the art, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0035] In addition, in the description of this application, the meaning of "a plurality of" is two or more, unless otherwise clearly specifically defined.

[0036] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those skilled in the technical field to which this application belongs. The terms used in the specification of the template herein are only for the purpose of describing specific embodiments and are not intended to limit this application. The term "and / or" used herein includes any and all combinations of one or more of the related listed items.

[0037] In the related art, the components in the tail gas discharged from the hydrogen peroxide production system are mainly: 3%-6% oxygen, about 94% nitrogen, 40 mg / m of mesitylene 3 , and other organic gases are negligible. It can be seen that the direct emission of the tail gas is a waste, is not conducive to reducing carbon emissions, and pollutes the environment.

[0038] Obviously, the nitrogen content in the tail gas is high, and the characteristics of the tail gas can be fully utilized to prepare nitrogen, so as to improve the utilization value of the tail gas. Compared with preparing nitrogen using air as a raw material, it can reduce the consumption of air, has low energy consumption, and can reduce the carbon emissions during the production process of hydrogen peroxide.

[0039] Such as Figure 1As shown in the figure, to solve the above technical problems, an embodiment of the present application provides a tail gas recovery device for carbon reduction. The tail gas recovery device for carbon reduction includes a nitrogen generator 1600, an air compressor 1400, a nitrogen generator 1600, an activated carbon adsorption tank, a first control pipeline 700, and a gas storage tank 200. The inlet of the activated carbon adsorption tank is connected to the outlet of the gas storage tank 200, the outlet of the activated carbon adsorption tank is connected to the inlet of the air compressor 1400 through the first control pipeline 700, and the outlet of the air compressor 1400 is connected to the inlet of the nitrogen generator 1600; wherein, the first control pipeline 700 can at least switch between a connected state and a disconnected state.

[0040] Among them, the gas storage tank 200 is used to receive and store the tail gas discharged from the hydrogen peroxide production system 100, and then supply gas to the activated carbon adsorption tank by means of the gas storage tank 200. Moreover, through the transfer of the tail gas by the gas storage tank 200, the stability of the air flow entering the activated carbon adsorption tank can be maintained.

[0041] The first control pipeline 700 connects the outlet of the activated carbon adsorption tank to the inlet of the air compressor 1400, ensuring that the purified gas directly enters the compression link and reducing the possibility of secondary pollution.

[0042] The activated carbon adsorption tank is used to adsorb trimethylbenzene in the tail gas and gradually reach a saturated state to improve the purity of nitrogen in the tail gas; at this time, if the activated carbon adsorption tank is in a saturated state, high-temperature gas is introduced into the activated carbon adsorption tank, and then the activated carbon in the activated carbon adsorption tank is purged at high temperature to make the trimethylbenzene separate from the activated carbon and regenerate the activated carbon.

[0043] In other words, the switching ability of the first control pipeline 700 provides flexibility for the system. During the production process, according to actual needs, the gas flow direction can be adjusted and the process flow can be optimized. For example, before the adsorption tank reaches saturation, it can be switched to a standby tank, or when needed, high-temperature gas can be refluxed to assist in the regeneration of the activated carbon, reducing the downtime and energy consumption.

[0044] Applying the tail gas recovery device for carbon reduction provided by the present application, the circulating reflux design of the activated carbon adsorption tank reduces the burden on the activated carbon, may extend its service life, and reduces carbon emissions. In addition, when using the tail gas discharged from the hydrogen peroxide production system 100 as the raw material gas for nitrogen production, it only needs to remove trace impurities such as trimethylbenzene at the inlet of the air compressor 1400 and then be compressed into the nitrogen generator 1600. Its advantages are less pollution, low energy consumption, carbon reduction and emission reduction, and low cost. It should be noted that although the operation of directly recovering nitrogen in the tail gas itself does not reduce carbon emissions, it indirectly promotes the reduction of carbon emissions by improving efficiency, promoting resource recycling, reducing waste emissions, and optimizing the production process, meeting the sustainable development goals.

[0045] In some embodiments, the number of activated carbon adsorption tanks is multiple, and the multiple activated carbon adsorption tanks are arranged in parallel;

[0046] The tail gas recovery device for carbon reduction further includes a second control pipeline 900. The outlet of the air compressor 1400 is also communicated with the outlet of the activated carbon adsorption tank through the second control pipeline 900. Among them, the second control pipeline 900 can at least switch between a connected state and a disconnected state.

[0047] In this embodiment, it aims to increase the adsorption surface area and adsorption rate by introducing multiple activated carbon adsorption tanks arranged in parallel and a flexible control pipeline design.

[0048] In this application, two activated carbon adsorption tanks are set as an example. Of course, in other embodiments, the number of activated carbon adsorption tanks can also be set to three, four, five, etc., which is not specifically limited here.

[0049] For multiple activated carbon adsorption tanks arranged in parallel, compared with the traditional single-tank or series design, the two parts in the multi-tank parallel arrangement work alternately, which can increase the adsorption surface area and adsorption rate, and effectively improve the adsorption efficiency of impurities, water vapor, organic gases, etc. in the air. And when one part is working, the other part is purged with hot gas to remove the trimethylbenzene adsorbed on the activated carbon, realizing the regeneration of the activated carbon.

[0050] Obviously, the second control pipeline 900 is used to connect the outlet of the air compressor 1400 and the outlet of the activated carbon adsorption tank. That is to say, in this application, two activated carbon adsorption tanks are set as an example, which are divided into a first activated carbon adsorption tank 300 and a second activated carbon adsorption tank 400. When the first activated carbon adsorption tank 300 gradually reaches the saturated state of adsorbing trimethylbenzene, it is switched to the second activated carbon adsorption tank 400 to connect the air compressor 1400, so as to use the second activated carbon adsorption tank 400 to continue adsorbing trimethylbenzene in the tail gas. At this time, control the second control pipeline 900 to connect the outlet of the air compressor 1400 and the first activated carbon adsorption tank 300, so as to introduce the high-temperature gas formed by the compression of the air compressor 1400 into the first activated carbon adsorption tank 300, and then realize the high-temperature purging of the activated carbon in the first activated carbon adsorption tank 300, so that the trimethylbenzene is separated from the activated carbon, realizing the regeneration of the activated carbon and reducing the energy consumption of the direct regeneration of the activated carbon.

[0051] In other words, the switching cooperation of the first control pipeline 700 and the second control pipeline 900 provides flexibility for the system. During the production process, according to actual needs, the gas flow direction can be adjusted to optimize the process flow, such as switching to the standby tank before the adsorption tank reaches saturation, or performing high-temperature gas reflux through the second control pipeline 900 when needed to assist the regeneration of the activated carbon, reducing the downtime and energy consumption.

[0052] In other words, by recycling and optimizing the gas flow direction, the activated carbon in the activated carbon adsorption tank for regeneration is purged with the high-temperature gas generated by the air compressor 1400, reducing the energy consumption for directly heating the regenerated activated carbon and decreasing the consumption of clean nitrogen for backwashing the activated carbon regeneration; moreover, the parallel use and cyclic reflux design of the activated carbon alleviate the burden on the activated carbon, potentially extending its service life, reducing the replacement frequency and cost. Additionally, when the oxidation tail gas is used as the raw material gas for nitrogen production, it only needs to be compressed into the nitrogen generator 1600 after removing trace amounts of trimethylbenzene at the inlet of the air compressor 1400. Its advantages are less pollution, low energy consumption, carbon emission reduction, low cost, and theoretically higher nitrogen purity, without consuming external pure air for nitrogen production.

[0053] As Figure 1 shown, in some embodiments, the tail gas recovery device for carbon emission reduction further includes a gas-gas heat exchanger 1000. The gas-gas heat exchanger 1000 has a cold medium inlet, a cold medium outlet, a hot medium inlet, and a hot medium outlet. The outlet of the activated carbon adsorption tank is connected to the cold medium inlet through a first control pipeline 700. The cold medium outlet is connected to the inlet of the air compressor 1400, and the inlet of the activated carbon adsorption tank is connected to the hot medium inlet.

[0054] In these embodiments, the energy efficiency and operating performance of the tail gas recovery device for carbon emission reduction are further optimized by integrating the gas-gas heat exchanger 1000. The specific improvement points and advantages are as follows:

[0055] The gas-gas heat exchanger 1000 is designed with a cold medium inlet, a cold medium outlet, a hot medium inlet, and a hot medium outlet, such that the low-temperature gas discharged from the outlet of the first activated carbon adsorption tank 300 directly enters the cold medium inlet of the gas-gas heat exchanger 1000, while the purging high-temperature gas discharged from the outlet of the second activated carbon adsorption tank 400 enters the gas-gas heat exchanger 1000 through the hot medium inlet. Such a design can effectively recover the heat in the purging high-temperature gas and transfer it to the low-temperature gas to raise the low-temperature gas, facilitating the compression of the gas by the air compressor 1400; additionally, since the temperature of the high-temperature gas is reduced by using the gas-gas heat exchanger 1000, it can be discharged, reducing the thermal pollution to the external environment, reducing energy consumption, and also reducing greenhouse gas emissions, playing a positive role in environmental protection and having the function of energy conservation.

[0056] In other words, the preheating process of the low-temperature gas reduces the energy required for direct heating. Especially in winter or low-temperature environments, the preheating effect significantly reduces the load on the air compressor 1400 because the temperature rise requirement during the compression process is reduced, thereby saving power consumption.

[0057] Moreover, the introduction of the gas-gas heat exchanger 1000 can significantly reduce the overall energy consumption of the system operation through the efficient recovery and utilization of thermal energy, meeting the requirements of modern industrial green production. Obviously, although additional investment in the gas-gas heat exchanger 1000 may be required initially, in the long run, due to the improvement of energy efficiency and the reduction of maintenance costs, the overall operating cost will be greatly reduced, bringing better economic benefits to the enterprise.

[0058] In summary, this design of the carbon reduction tail gas recovery device integrated with the gas-gas heat exchanger 1000 not only improves the energy efficiency and economy of the system, but also contributes to environmental protection, which is an important technological progress for realizing sustainable industrial production.

[0059] Exemplarily, the gas-gas heat exchanger 1000 can be any of the following: 1. Shell and tube heat exchanger: This is one of the most common types of heat exchangers, consisting of a shell, tube bundle, tube sheet, and head. The gas flows inside the tubes, while the other gas flows in the shell side outside the tubes, and heat transfer occurs through the tube wall. The shell and tube heat exchanger has a strong structure and can withstand high pressure and temperature, being suitable for high-temperature and high-pressure working conditions. 2. Finned heat exchanger: In this type of heat exchanger, the heat transfer surface is added with fin structures to increase the heat transfer area and improve the heat transfer efficiency. The fins can be continuous or intermittent, and the material is usually selected as a metal with good thermal conductivity. The finned heat exchanger is suitable for situations that require high heat transfer efficiency or when the processed fluid has a phase change, but its structure is complex, the cost is relatively high, and the pipeline is prone to blockage. 3. Plate heat exchanger: It is composed of a series of thin metal plates stacked together, forming narrow flow channels between the plates, and the two gases flow alternately on both sides of the plates. The plate heat exchanger has the advantages of high heat transfer efficiency, small volume, light weight, convenient disassembly, cleaning, etc., and is suitable for occasions with strict requirements for heat transfer efficiency and space. 4. Hybrid heat exchanger: It combines the characteristics of two or more of the above heat exchangers, with a more flexible design to adapt to specific process requirements. 5. Tube heat exchanger: It includes various types such as fixed tube sheet type, floating head type, U-tube type, etc., and each design has its specific application scenarios. For example, the floating head heat exchanger can effectively reduce the stress problem caused by thermal expansion and is suitable for situations where the medium pressure or temperature fluctuates greatly. 6. Plate-fin heat exchanger: This heat exchanger combines the characteristics of plate type and fin type, has very high heat transfer efficiency, is especially suitable for heat transfer between gases, and is commonly found in air compressors, refrigeration systems, etc. 7. Spiral tube heat exchanger: One or two fluids flow inside the winding tubes, and the other fluid flows outside the tubes or in the cavity of the winding tubes. This design is suitable for situations with a small processing capacity or when precise temperature control is required, and is not specifically limited here. The specific application type can be selected according to the actual scenario.

[0060] As Figure 1As shown, in some embodiments, the tail gas recovery device for carbon reduction further includes a gas-liquid separator 1300 and a third control pipeline 600. The gas-liquid separator 1300 has a gas-liquid mixture inlet, a heat medium outlet, and the gas-liquid mixture inlet is connected. The inlet of the activated carbon adsorption tank is connected to the heat medium inlet through the third control pipeline 600, and the third control pipeline 600 can at least switch between a connected state and a disconnected state.

[0061] In these embodiments, the tail gas recovery device for carbon reduction further improves the system function through the design of adding the gas-liquid separator 1300 and the third control pipeline 600. The main improvement points are as follows:

[0062] The introduction of the gas-liquid separator 1300 aims to separate the liquid droplets liquefied after cooling in the high-temperature gas from the heat medium. Since the high-temperature gas purges the activated carbon, the liquid contains trimethylbenzene. By immediately performing gas-liquid separation after the heat medium leaves the heat exchange process, the coalescence, recovery of trimethylbenzene, and reduction of the three wastes emissions can be achieved.

[0063] The third control pipeline 600 is used to connect the outlet of the activated carbon adsorption tank to the heat medium inlet. The heat medium outlet is connected to the gas-liquid mixture inlet of the gas-liquid separator 1300 and can be switched between a connected state and a disconnected state as needed. This design gives the system flexibility in operation. When it is not necessary to purge and regenerate the activated carbon, the connection can be disconnected, which is convenient for operation and management. That is to say, through the switching of the third control pipeline 600, the on-demand use of the gas-liquid separator 1300 can be realized.

[0064] Exemplarily, the gas-liquid separator 1300 is set as a cyclone separator; of course, in other embodiments, the gas-liquid separator 1300 can also be set as a gravity settling separator, a multi-tube separator, a fiber membrane separator, an electrostatic separator, a filter separator, a centrifugal separator, a combined separator, etc., which are not specifically limited herein.

[0065] As Figure 1 shown, in some embodiments, the tail gas recovery device for carbon reduction further includes a gas-liquid condenser 1200. The gas-liquid condenser 1200 has a gas phase inlet, and the gas-liquid separator 1300 also has a gas outlet, and the gas phase inlet is connected to the gas outlet.

[0066] In this embodiment, the gas separated by the gas-liquid separator 1300 is further cooled by the gas-liquid condenser 1200 to recover the residual trimethylbenzene, further reducing the emissions of pollutants and the recovery amount of trimethylbenzene.

[0067] Optionally, the gas-liquid condenser 1200 also has a gas phase outlet, and a silencer 1100 is connected to the gas phase outlet to reduce the noise generated by the venting.

[0068] Exemplarily, the gas-liquid condenser 1200 can be a water-cooled condenser, an air-cooled condenser, an evaporative condenser, a shell-and-tube condenser, etc., which are not specifically limited herein as long as the gas can be condensed.

[0069] As Figure 1 shown, in some embodiments, the tail gas recovery device for carbon reduction further includes a storage tank 1700. The gas-liquid separator 1300 further has a liquid outlet, and the gas-liquid condenser 1200 further has a condensate outlet. The storage tank 1700 is respectively communicated with the condensate outlet and the liquid outlet.

[0070] In this embodiment, the condensate outlet and the liquid outlet are respectively communicated with the storage tank 1700 through a buffer tank 1500, so as to be able to collect and store trimethylbenzene for recycling and squeezing the remaining value of the tail gas.

[0071] In some embodiments, the tail gas recovery device for carbon reduction further includes a fourth control pipeline 800. The outlet of the activated carbon adsorption tank is also communicated with the cold medium inlet of the gas-gas heat exchanger 1000 through the fourth control pipeline 800, that is, the outlet of the activated carbon adsorption tank is communicated with the outlets of the other activated carbon adsorption tanks through the fourth control pipeline 800; wherein, the fourth control pipeline 800 can at least switch between a connected state and a disconnected state.

[0072] That is to say, the connection state between the activated carbon adsorption tanks can be controlled through the fourth control pipeline 800. The gas discharged from the outlet of the activated carbon adsorption tank is a low-temperature gas, roughly at 2°C. Exemplarily, in the present application, there is a first activated carbon adsorption tank 300 and a second activated carbon adsorption tank 400. After the first activated carbon adsorption tank 300 is regenerated by high-temperature purging, the first activated carbon adsorption tank 300 cannot be put into use immediately due to its high temperature and needs to be cooled by a lower-temperature gas, which is called cold blowing. Therefore, by controlling the fourth control pipeline 800 to be in a connected state, the low-temperature gas discharged from the outlet of the second activated carbon adsorption tank 400 can enter through the outlet of the first activated carbon adsorption tank 300 to cold blow the activated carbon in the first activated carbon adsorption tank 300 until the temperature drops to about 2°C, that is, the regeneration and standby are completed, improving the regeneration efficiency of the activated carbon adsorption tank, reducing the usage amount of the activated carbon adsorption tank, and thus reducing the cost.

[0073] As Figure 1 shown, in some embodiments, the first control pipeline 700 includes a first switching valve 720, a first main pipeline 710 and a first branch pipeline 730. The outlet of the activated carbon adsorption tank is sequentially communicated with the cold medium inlet through the first branch pipeline 730 and the first main pipeline 710, and the first branch pipeline 730 is provided with a first switching valve 720;

[0074] In this embodiment, one end of the first main pipeline 710 is communicated with the cold medium inlet, and the other end of the first main pipeline 710 is respectively communicated with the outlets of the corresponding activated carbon adsorption tanks through a plurality of first branch pipelines 730, so that all the activated carbon adsorption tanks are connected in parallel to the first main pipeline 710, and the connection state between the outlet of the corresponding activated carbon adsorption tank and the first main pipeline 710 can be controlled through the first switching valve 720 on the first branch pipeline 730. Among them, when the first activated carbon adsorption tank 300 needs to be regenerated by high-temperature purging, the first switching valve 720 connected to the first activated carbon adsorption tank 300 is closed to cut off the connection between the outlet of the first activated carbon adsorption tank 300 and the first main pipeline 710, and the first switching valve 720 connected to the second activated carbon adsorption tank 400 is opened to communicate the outlet of the second activated carbon adsorption tank 400 with the first main pipeline 710, realizing the alternate use of the first activated carbon adsorption tank 300 and the second activated carbon adsorption tank 400.

[0075] In some embodiments, the second control pipeline 900 includes a second switching valve 930, a second main pipeline 910 and a second branch pipeline 940. The outlet of the air compressor 1400 is sequentially communicated with the outlets of the activated carbon adsorption tanks through the second main pipeline 910 and the second branch pipeline 940, and the second switching valve 930 is installed on the second branch pipeline 940; the diameter of the second main pipeline 910 is smaller than the diameter of the outlet of the air compressor 1400.

[0076] As Figure 1 shown, in this embodiment, one end of the second main pipeline 910 is communicated with the outlet of the air compressor 1400, and the other end of the second main pipeline 910 is respectively communicated with the outlets of the corresponding activated carbon adsorption tanks through a plurality of first branch pipelines 730, so that all the activated carbon adsorption tanks are connected in parallel to the second main pipeline 910, and the connection state between the outlet of the corresponding activated carbon adsorption tank and the second main pipeline 910 can be controlled through the second switching valve 930 on the second branch pipeline 940. Among them, when the first activated carbon adsorption tank 300 needs to be regenerated by high-temperature purging, the first switching valve 720 connected to the first activated carbon adsorption tank 300 is closed to cut off the connection between the outlet of the first activated carbon adsorption tank 300 and the first main pipeline 710, and the first switching valve 720 connected to the second activated carbon adsorption tank 400 is opened to communicate the outlet of the second activated carbon adsorption tank 400 with the first main pipeline 710, realizing the alternate use of the first activated carbon adsorption tank 300 and the second activated carbon adsorption tank 400; at the same time, the second switching valve 930 connected to the first activated carbon adsorption tank 300 is opened, and the second switching valve 930 connected to the second activated carbon adsorption tank 400 is closed, so that high-temperature gas flows into the first activated carbon adsorption tank 300 to purge the activated carbon at high temperature.

[0077] In this embodiment, the diameter of the second main pipeline 910 is set much smaller than the diameter of the outlet of the air compressor 1400. The reason is that the gas consumption required for hot purging the activated carbon in the activated carbon adsorption tank is small and will not cause fluctuations in the main process parameters.

[0078] As Figure 1 shown, in some embodiments, the third control pipeline 600 includes a third switching valve 610, a third main pipeline 630, and a third branch pipeline 620. The inlet of the activated carbon adsorption tank is communicated with the hot medium inlet through the third branch pipeline 620 and the third main pipeline 630 in sequence, and the third switching valve 610 is installed on the third branch pipeline 620.

[0079] In this embodiment, one end of the third main pipeline 630 is communicated with the hot medium inlet, and the other end of the third main pipeline 630 is communicated with the inlets of the corresponding activated carbon adsorption tanks through a plurality of third branch pipelines 620, so that the inlets of all the activated carbon adsorption tanks are connected in parallel to the third main pipeline 630, and the connection state between the inlet of the corresponding activated carbon adsorption tank and the third main pipeline 630 can be controlled by the third switching valve 610 on the third branch pipeline 620.

[0080] Among them, when the first activated carbon adsorption tank 300 needs to be regenerated by high-temperature purging, the first switching valve 720 connected to the first activated carbon adsorption tank 300 is closed to cut off the connection between the outlet of the first activated carbon adsorption tank 300 and the first main pipeline 710, and the first switching valve 720 connected to the second activated carbon adsorption tank 400 is opened to connect the outlet of the second activated carbon adsorption tank 400 and the first main pipeline 710, so as to realize the alternating use of the first activated carbon adsorption tank 300 and the second activated carbon adsorption tank 400; at the same time, the second switching valve 930 connected to the first activated carbon adsorption tank 300 is opened, and the second switching valve 930 connected to the second activated carbon adsorption tank 400 is closed, so that the high-temperature gas flows into the first activated carbon adsorption tank 300 for high-temperature purging of the activated carbon. At this time, the third switching valve 610 connected to the first activated carbon adsorption tank 300 is opened, and the third switching valve 610 connected to the second activated carbon adsorption tank 400 is closed, so that the high-temperature gas discharged from the inlet of the first activated carbon adsorption tank 300 can be cooled by the gas-gas heat exchanger 1000 and then discharged, and the low-temperature gas discharged from the outlet of the second activated carbon adsorption tank 400 can be heated, which is beneficial to the subsequent compression of the gas by the air compressor 1400.

[0081] On the basis of the above embodiments, the fourth control pipeline 800 includes a fourth switching valve 810 and a fourth main pipeline 820. The first main pipeline 710 is connected to the second main pipeline 910 through the fourth main pipeline 820. The fourth main pipeline 820 is equipped with a fourth switching valve 810, and the second main pipeline 910 is equipped with a seventh switching valve 920; in the gas flow direction in the second main pipeline 910, the connection between the fourth main pipeline 820 and the second main pipeline 910 is located downstream of the seventh switching valve 920, and the diameter of the fourth main pipeline 820 is smaller than the diameter of the first main pipeline 710.

[0082] In this embodiment, the fourth main pipeline 820 and the second main pipeline 910 share the second branch pipeline 940, reducing pipeline installation and cost. For example, when the first activated carbon adsorption tank 300 needs to be cooled by cold blowing, the fourth switching valve 810 and the second switching valve 930 connected to the first activated carbon adsorption tank 300 are opened, and the second switching valve 930 and the seventh switching valve 920 connected to the second activated carbon adsorption tank 400 are closed, so that the low-temperature gas discharged from the outlet of the second activated carbon adsorption tank 400 can flow into the first activated carbon adsorption tank 300 for cold blowing.

[0083] In this embodiment, the diameter of the fourth main pipeline 820 is set to be much smaller than that of the first main pipeline 710. The reason is that the gas consumption required for cold purging the activated carbon in the activated carbon adsorption tank is small and will not cause fluctuations in the main process parameters.

[0084] As Figure 1 shown, in some embodiments, the tail gas recovery device for carbon reduction further includes an intake control pipeline 500. The intake control pipeline 500 includes a main intake pipeline 540, a branch intake pipeline 520, a fifth switching valve 530, and a sixth switching valve 510. The main intake pipeline 540 is connected to the inlet of the corresponding activated carbon adsorption tank through the branch intake pipeline 520. The branch intake pipeline 520 is provided with a fifth switching valve 530 and the sixth switching valve 510 at intervals in its extending direction. The sixth switching valve 510 is located between the fifth switching valve 530 and the corresponding activated carbon adsorption tank, and the third main pipeline 630 is connected to the branch intake pipeline 520 through a third branch pipeline 620. The connection between the third branch pipeline 620 and the branch intake pipeline 520 is located between the fifth switching valve 530 and the sixth switching valve 510.

[0085] In this embodiment, the inlets of all the activated carbon adsorption tanks are connected in parallel to the main intake pipeline 540. That is to say, opening the fifth switching valve 530 and the sixth switching valve 510 connected to the inlet of the corresponding activated carbon adsorption tank can realize the intake of the activated carbon adsorption tank.

[0086] Exemplarily, when purging the first activated carbon adsorption tank 300 with high-temperature gas, the sixth switch valve 510 and the third switch valve 610 connected to the first activated carbon adsorption tank 300 are opened, and the fifth switch valve 530 connected to the first activated carbon adsorption tank 300 is closed; the sixth switch valve 510 and the fifth switch valve 530 connected to the second activated carbon adsorption tank 400 are opened, and the third switch valve 610 connected to the second activated carbon adsorption tank 400 is closed, so that the high-temperature gas discharged from the first activated carbon adsorption tank 300 can be introduced into the gas-gas heat exchanger 1000.

[0087] As Figure 1 shown, in some embodiments, a low-point drain port 640 is provided on the third main pipeline 630, and the low-point drain port 640 is connected to an eighth switch valve 650, so that impurities in the third main pipeline 630 can be discharged.

[0088] In the above embodiments, the air pressure requirement for purging the activated carbon in the activated carbon adsorption tank by cold purge is small. The fourth main pipeline 820 is set as a reducing pipe. In the direction close to the activated carbon adsorption tank, the diameter of the fourth main pipeline 820 gradually increases to reduce pressure by reducing the diameter;

[0089] The air pressure requirement for purging the activated carbon in the activated carbon adsorption tank by hot purge is small. The second main pipeline 910 is set as a reducing pipe. In the direction close to the activated carbon adsorption tank, the diameter of the second main pipeline 910 gradually increases to reduce pressure by reducing the diameter.

[0090] As Figure 1 shown, in some embodiments, the embodiment of the present application further provides a hydrogen peroxide production system, including an oxidation tower 130, an expansion refrigeration generator 120, a tail gas treatment system 110, and a tail gas recovery device for carbon reduction as described in any one of the above embodiments. The oxidation tower 130, the expansion refrigeration generator 120, the tail gas treatment system 110, and the tail gas recovery device for carbon reduction are connected in sequence.

[0091] Since the above-mentioned tail gas recovery device for carbon reduction has the above technical effects, the hydrogen peroxide production system 100 including the tail gas recovery device for carbon reduction should have the same technical effects, which will not be elaborated here.

[0092] Exemplarily, the tail gas port of the hydrogen peroxide production system 100 is communicated with the inlet of the activated carbon adsorption tank for direct recovery and treatment.

[0093] The tail gas of the hydrogen peroxide production system 100 comes out from the upper part of the oxidation tower 130 and then passes through the expansion refrigeration generator 120, where its kinetic energy decreases and is converted into potential energy to drive the operation of the expansion refrigeration generator 120, thereby driving the expansion refrigeration generator 120 to generate electricity. During the power generation process, due to the reduction of the energy of the tail gas itself, the temperature drops. After expansion refrigeration, the temperature of the oxidized tail gas drops from about 50 degrees to about 2 degrees. The tail gas at about 2 degrees is then processed by the tail gas treatment system 110 and discharged into the above-mentioned tail gas recovery device for carbon reduction to produce nitrogen using the nitrogen in the tail gas.

[0094] Obviously, the tail gas processed by the tail gas treatment system 110 flows through the activated carbon adsorption tank, the air compressor 1400, and the nitrogen generator 1600 in sequence. Furthermore, the activated carbon adsorption tank is used to remove the impurity gases in the tail gas to increase the nitrogen content in the tail gas entering the air compressor 1400. Then, the nitrogen generator 1600 partially produces nitrogen using the nitrogen in the tail gas, which can improve the residual value of the utilization of the tail gas, reduce the carbon emission, and reduce the consumption of using air as a raw material for nitrogen production.

[0095] In all the examples shown and described here, any specific value should be construed as merely exemplary, not as a limitation. Therefore, other examples of the exemplary embodiments may have different values.

[0096] It should be noted that similar reference numerals and letters denote similar items in the following figures. Therefore, once an item is defined in one figure, it does not need to be further defined and explained in subsequent figures.

[0097] The above-described embodiments merely represent several implementation manners of the present application. The description is relatively specific and detailed, but it should not be construed as a limitation of the scope of the present application. It should be pointed out that for those of ordinary skill in the art, without departing from the concept of the present application, several modifications and improvements can still be made, and these all belong to the protection scope of the present application.

Claims

1. A tail gas recovery device for reducing carbon, characterized in that: The tail gas recovery device comprises a nitrogen generator (1600), an air compressor (1400), an activated carbon adsorption tank, a gas storage tank (200) and a first control pipeline (700); the inlet of the activated carbon adsorption tank is connected to the outlet of the gas storage tank (200); the outlet of the activated carbon adsorption tank is connected to the inlet of the air compressor (1400) through the first control pipeline (700); the outlet of the air compressor (1400) is connected to the inlet of the nitrogen generator (1600); wherein the first control pipeline (700) can at least switch between a connected state and a disconnected state.

2. The carbon reduction tail gas recovery device according to claim 1, characterized in that: The number of the activated carbon adsorption tanks is multiple, and the multiple activated carbon adsorption tanks are arranged in parallel; The tail gas recovery device further comprises a second control pipeline (900), and the outlet of the air compressor (1400) is also connected to the outlet of the activated carbon adsorption tank through the second control pipeline (900); The second control pipeline (900) is at least switchable between a connected state and a disconnected state.

3. The carbon reduction tail gas recovery device according to claim 2, characterized in that: The exhaust gas recovery device also includes an air-to-air heat exchanger (1000), the air-to-air heat exchanger (1000) having a cold medium inlet, a cold medium outlet, a hot medium inlet and a hot medium outlet, the outlet of the activated carbon adsorption tank being connected to the cold medium inlet via the first control pipeline (700), the cold medium outlet being connected to the inlet of the air compressor (1400), and the inlet of the activated carbon adsorption tank being connected to the hot medium inlet.

4. The carbon reduction tail gas recovery device according to claim 3, characterized in that: The tail gas recovery device also includes a gas-liquid separator (1300) and a third control pipeline (600), wherein the gas-liquid separator (1300) has a gas-liquid mixture inlet, the inlet of the activated carbon adsorption tank is connected to the heat medium inlet through the third control pipeline (600), the heat medium outlet is connected to the gas-liquid mixture inlet, and the third control pipeline (600) can at least switch between a connected state and a disconnected state.

5. The carbon reduction tail gas recovery device according to claim 4, characterized in that: The tail gas recovery device further comprises a gas-liquid condenser (1200), wherein the gas-liquid condenser (1200) has a gas phase inlet, and the gas-liquid separator (1300) further comprises a gas outlet, wherein the gas phase inlet is connected to the gas outlet.

6. The carbon reduction tail gas recovery device according to claim 5, characterized in that: The tail gas recovery device also includes a storage tank (1700), the gas-liquid separator (1300) also has a liquid outlet, the gas-liquid condenser (1200) also has a condensate outlet, and the storage tank (1700) is connected to the condensate outlet and the liquid outlet respectively.

7. The carbon reduction tail gas recovery device according to any one of claims 4 to 6, characterized in that: The tail gas recovery device also includes: A fourth control pipeline (800), wherein the outlet of the activated carbon adsorption tank is also connected to the cold medium inlet of the gas-to-gas heat exchanger (1000) through the fourth control pipeline (800); wherein the fourth control pipeline (800) is capable of at least switching between a connected state and a disconnected state.

8. The carbon reduction tail gas recovery device according to claim 7, characterized in that: The first control pipeline (700) comprises: a first switch valve (720), a first main pipeline (710) and a first branch pipeline (730), wherein the outlet of the activated carbon adsorption tank is connected to the cold medium inlet via the first branch pipeline (730) and the first main pipeline (710) in sequence, and the first switch valve (720) is installed in the first branch pipeline (730); The second control pipeline (900) comprises: a second switch valve (930), a second main pipeline (910) and a second branch pipeline (940); the outlet of the air compressor (1400) is connected to the outlet of the activated carbon adsorption tank through the second main pipeline (910) and the second branch pipeline (940) in sequence; the second switch valve (930) is installed in the second branch pipeline (940); the diameter of the second main pipeline (910) is smaller than the diameter of the outlet of the air compressor (1400); The third control pipeline (600) comprises: a third switch valve (610), a third main pipeline (630) and a third branch pipeline (620), wherein the inlet of the activated carbon adsorption tank is connected to the heat medium inlet via the third branch pipeline (620) and the third main pipeline (630) in sequence, and the third switch valve (610) is installed in the third branch pipeline (620); The fourth control pipeline (800) comprises: A fourth switch valve (810) and a fourth main pipeline (820), the first main pipeline (710) is connected to the second main pipeline (910) through the fourth main pipeline (820), the fourth main pipeline (820) is installed with the fourth switch valve (810), and the second main pipeline (910) is installed with the seventh switch valve (920); in the gas flow direction in the second main pipeline (910), the connection between the fourth main pipeline (820) and the second main pipeline (910) is located downstream of the seventh switch valve (920), and the diameter of the fourth main pipeline (820) is smaller than the diameter of the first main pipeline (710).

9. The carbon reduction tail gas recovery device according to claim 8, characterized in that: The exhaust gas recovery device further comprises an intake control pipeline (500), the intake control pipeline (500) comprising a main intake pipeline (540), a branch intake pipeline (520), a fifth switch valve (530) and a sixth switch valve (510), the main intake pipeline (540) being connected to the inlet of the corresponding activated carbon adsorption tank via the branch intake pipeline (520), the fifth switch valve (530) and the sixth switch valve (510) being arranged at intervals in the extension direction of the branch intake pipeline (520), the sixth switch valve (510) being located between the fifth switch valve (530) and the corresponding activated carbon adsorption tank, and the third main pipeline (630) being connected to the branch intake pipeline (520) via a third branch pipeline (620), the connection between the third branch pipeline (620) and the branch intake pipeline (520) being located between the fifth switch valve (530) and the sixth switch valve (510).

10. A hydrogen peroxide production system, characterized in that: The hydrogen peroxide production system (100) comprises an oxidation tower (130), an expansion refrigeration generator (120), a tail gas treatment system (110) and a tail gas recovery device for reducing carbon as described in any one of claims 1 to 9, and the oxidation tower (130), the expansion refrigeration generator (120), the tail gas treatment system (110) and the tail gas recovery device for reducing carbon are connected in sequence.

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