Modularized energy-saving tank for multi-stage carbon capture and storage

Abstract

The invention relates to the technical field of waste gas purification, in particular to a multi-stage carbon capture and storage modular energy-saving tank which comprises a heat recovery tank, an absorption tank, a regeneration cycle system and a carbon storage tank. The heat recovery tank is arranged above the absorption tank; the regeneration circulation system comprises a regeneration channel and a circulation assembly; the regeneration channel is arranged in the heat recovery tank; the circulating assembly is connected between the regeneration channel and the absorption tank; the carbon storage tank is connected with the compression cooling system; heat and pressure of high-temperature and high-pressure tail gas are recycled, tail gas waste heat is utilized to realize amine liquid regeneration, tail gas pressure is utilized to realize amine liquid flow circulation, and energy consumption in the carbon capture process is reduced; the problem of high carbon capture cost caused by consumption of a large amount of heat energy in the amine liquid regeneration process is solved.

Description

Technical Field

[0001] The present invention relates to the technical field of waste gas purification, and particularly relates to a modular energy-saving tank body for multi-stage carbon capture and storage. Background Art

[0002] The multi-stage carbon capture and storage technology is a carbon management technology that optimizes the process in stages and improves efficiency, aiming to capture carbon dioxide from industrial emission sources or energy production and reduce its entry into the atmosphere through long-term sequestration; the multi-stage carbon capture technology generally includes three core links: capture, transportation, and sequestration. During the transportation process, a modular tank body is required as an intermediate storage unit to store the compressed liquid or supercritical carbon dioxide.

[0003] The carbon capture and storage technology is currently mostly used in the energy industry, heavy industry, and transportation and shipping fields. As the main carrier of global trade, ships account for 2.89% of the global total carbon emissions. In order to reduce the carbon emissions of ships, the carbon capture and storage technology has developed rapidly in this field. Currently, the ship carbon capture technology mainly separates carbon dioxide from ship exhaust gas through chemical adsorption method, and then compresses and cools the carbon dioxide gas to make it liquefy. After liquefaction, it is stored in the tank body for preservation, and the tank body is unloaded after docking; when the chemical adsorption method is used to capture carbon dioxide, amine liquid is mainly used to react with carbon dioxide, and the exhaust gas is introduced into the absorption tower. The carbon dioxide in the exhaust gas reacts with the amine liquid to form carbonate, and the non-acidic gas will be directly discharged. When the non-acidic gas is discharged, it will carry the amine liquid to escape, causing environmental pollution and loss of amine liquid, thus resulting in an increase in cost. The prior art has proposed good solutions to this problem, such as a device system and method for preventing amine escape in the carbon dioxide amine method capture process with the patent publication number of CN113499680B; through the double impeller swirling action in the cyclone separator, the amine-containing liquid droplets in the airflow collide and coagulate and adhere to be removed under the action of centrifugal force, thus preventing the escape of amine liquid droplets, with simple structure, easy operation and regulation, and low treatment cost.

[0004] Although the prior art has solved the problem of increased treatment cost caused by amine liquid escape during the carbon dioxide capture process, there are still the following problems: during the carbon dioxide capture and storage process, the exhaust gas needs to be cooled from 300 degrees Celsius to 40 - 60 degrees Celsius to avoid damage to the adsorbent by high-temperature exhaust gas. After the cooled exhaust gas is introduced into the absorption tower and contacts with the amine liquid, the carbon dioxide in the exhaust gas reacts with the amine liquid to produce carbonate, and then it needs to be heated to above 120 degrees Celsius to decompose and release the carbon dioxide gas again and regenerate the amine liquid, and the regenerated amine liquid is returned to the absorption tower for reuse. Finally, the carbon dioxide gas is compressed, cooled, and liquefied for storage. A large amount of heat energy is consumed during the regeneration process of the amine liquid, thus resulting in an increase in cost.

[0005] In view of the above situation, in order to overcome the above technical problems, the present invention designs a modular energy-saving tank body for multi-stage carbon capture and storage. Summary of the Invention

[0006] The present invention provides a modular energy-saving tank body for multi-stage carbon capture and storage, which solves the problem that the amine liquid regeneration process consumes a large amount of heat energy, resulting in high carbon capture costs. By arranging the regeneration channel in the heat recovery tank, the high-temperature and high-pressure tail gas discharged from the ship will flow through the outer surface of the regeneration channel in a swirling manner. On the one hand, it can extend the residence time of the tail gas in the heat recovery tank, provide sufficient heat energy for amine liquid regeneration, reduce energy consumption, and the temperature of the tail gas introduced into the amine liquid can be reduced to an appropriate temperature to avoid damage to the amine liquid. On the other hand, the particulate matter in the tail gas is separated to avoid polluting the amine liquid and reducing the cost caused by amine liquid replacement; and a circulation component is provided. When the tail gas flows from the heat recovery tank to the absorption tank, it will drive the circulation component to rotate, so as to automatically pump the amine liquid that has absorbed carbon dioxide into the regeneration channel for regeneration reaction, and the regenerated and separated amine liquid will be atomized back into the absorption tank under the swirling force of the tail gas and its own gravity to further capture the carbon dioxide that has not been completely absorbed by the amine liquid.

[0007] To achieve the above object, the present invention provides the following technical solutions:

[0008] A modular energy-saving tank body for multi-stage carbon capture and storage; including a compression and cooling system, and further including a heat recovery tank, an absorption tank, a regeneration circulation system and a carbon storage tank; the absorption tank is fixedly installed on the ground; the heat recovery tank is arranged above the absorption tank; the regeneration circulation system includes a regeneration channel and a circulation component; the regeneration channel is arranged in the heat recovery tank, and the lower part of the regeneration channel is communicated with the absorption tank, and the upper part of the regeneration channel is connected with the compression and cooling system. After the tail gas enters the heat recovery tank, it swirls and descends through the outer surface of the regeneration channel. The amine liquid enters the middle part of the regeneration channel and then enters the absorption tank from the bottom of the regeneration channel; the circulation component is connected between the regeneration channel and the absorption tank. After the tail gas flows out of the heat recovery tank, it passes through the circulation component and enters the absorption tank while driving the circulation component to rotate. The rotation of the circulation component pumps the amine liquid in the absorption tank into the regeneration channel; the carbon storage tank is connected with the compression and cooling system, and the separated carbon dioxide gas is liquefied by the compression and cooling system and stored in the carbon storage tank.

[0009] Preferably, the heat recovery tank includes a recovery housing, an air inlet channel and swirling vanes; the recovery housing is connected to the upper part of the absorption tank; the air inlet channel is tangentially connected to the upper outer wall of the recovery housing; the swirling vanes are arranged in a circumferential array between the recovery housing and the regeneration channel.

[0010] In the above solution, since the high-temperature tail gas in the prior art needs to be cooled down before entering the absorption tower to react with the amine solution to prevent damage to the absorbent due to excessive temperature, the heat in the high-temperature tail gas will be wasted. Here, the discharged high-temperature tail gas is introduced into the recovery housing, and the high-temperature tail gas entering the recovery housing transfers heat to the regeneration channel to help regenerate the amine solution. Moreover, after the high-temperature tail gas enters the recovery housing, it will swirl under the guiding action of the swirl vanes. The swirling of the high-temperature tail gas can extend the residence time in the recovery housing, so as to fully contact the regeneration channel to transfer heat. At the same time, the swirling can separate the particulate matter in the tail gas, reducing the content of particulate matter in the tail gas entering the absorption tank and avoiding contamination of the amine solution.

[0011] Preferably, the absorption tank includes an absorption housing, an exhaust gas channel, a reaction air duct, and a rich amine solution channel; the absorption housing is connected to the lower part of the recovery housing, and the lower part of the absorption housing is filled with amine solution; the exhaust gas channel is connected to the upper part of the absorption housing; the reaction air duct connects the lower part of the recovery housing and the lower part of the absorption housing; the rich amine solution channel is connected between the regeneration channel and the absorption housing.

[0012] In the above solution, the tail gas after swirling cooling and separation of solid particulate matter will enter the lower part of the absorption housing from the reaction air duct, and the tail gas will be directly introduced into the amine solution to ensure sufficient contact for reaction. The reacted amine solution (i.e., rich amine solution) enters the regeneration channel from the rich amine solution channel. Since the regeneration channel is heated by the discharged tail gas, the rich amine solution can be decomposed back into carbon dioxide gas and lean amine solution (i.e., amine solution without carbonate). The decomposed lean amine solution will return to the lower part of the absorption housing from the lower part of the regeneration channel to form a cycle, saving amine solution loss.

[0013] Preferably, the rich amine solution channel penetrates through the middle and lower parts of the recovery housing and is connected to the regeneration channel.

[0014] In the above solution, since the rich amine solution enters from the middle layer of the regeneration channel through the rich amine solution channel, the reaction temperature of the rich amine solution can be controlled at about 120 °C, ensuring the best amine solution regeneration temperature, thus avoiding the escape of the amine solution carried by carbon dioxide due to volatilization caused by excessive temperature. Moreover, the temperature is lower towards the bottom, ensuring that the separated lean amine solution accumulated at the bottom of the main channel will not volatilize and escape.

[0015] Preferably, the regeneration channel includes a main channel, a pressure reducing valve, a corrugated demister, and an atomization assembly; the main channel is arranged at the center of the recovery housing; the pressure reducing valve is arranged in the main channel and is connected to the rich amine solution channel; the corrugated demister is arranged at the upper part of the main channel; the atomization assembly is arranged at the lower part of the main channel.

[0016] In the above solution, the rich amine solution entering the main channel will decompose carbon dioxide gas again at the regeneration temperature. At this time, the lean amine solution will return to the absorption housing through the atomization assembly. The carbon dioxide gas will move upward and filter out the carried amine liquid droplets through the corrugated demister to avoid amine liquid escape. Since the rich amine solution entering the main channel will first pass through the recovery housing, the rich amine solution will be preheated in the recovery housing. The preheated rich amine solution will reduce the boiling point through a pressure reducing valve to achieve flash evaporation, quickly separating carbon dioxide and amine liquid. Flash evaporation can, on the one hand, further reduce energy consumption, and on the other hand, reduce the temperature of the amine liquid returning to the absorption housing.

[0017] Preferably, the atomization assembly includes an atomization disk, a sealed bearing, and a driving rotor. The atomization disk is rotatably installed below the main channel, and a plurality of atomization holes are formed in the atomization disk. The sealed bearing is connected between the atomization disk and the absorption housing. The driving rotor is connected to the atomization disk.

[0018] In the above solution, the amine liquid after flash separation reaches the position of the atomization disk. The falling speed of the amine liquid can be slowed down through the atomization holes, so as to ensure that the amine liquid can stay in the lower part of the main channel for a period of time, thereby separating all the carbon dioxide in the amine liquid. The driving rotor will cause the atomization disk to rotate under the driving force of the high-pressure tail gas. The rotation of the atomization disk will enable the lean amine liquid to be evenly sprayed downward while being atomized. Through the spraying coverage effect, it can fully contact the carbon dioxide that has not been completely absorbed and mixed in the waste gas, thereby capturing this part of carbon dioxide and improving the capture efficiency.

[0019] Preferably, the upper part of the rich amine liquid channel located between the main channel and the recovery housing is a semi-circular structure.

[0020] In the above solution, the amine liquid entering the semi-circular structure at the upper end of the rich amine liquid channel can extend the heat exchange time, so as to preheat the rich amine liquid to the saturation temperature, enabling the flash evaporation process to proceed smoothly, thereby improving the separation efficiency and reducing the carbon content in the regenerated amine liquid.

[0021] Preferably, the circulation assembly includes a driving chamber, a driving impeller, a circulation chamber, a circulation impeller, and a connecting shaft. The driving chamber is connected to the reaction air duct. The driving impeller is rotatably installed in the driving chamber. The circulation chamber is connected to the rich amine liquid channel. The circulation impeller is rotatably installed in the circulation chamber. The connecting shaft is connected between the driving impeller and the circulation impeller.

[0022] In the above solution, after the high-pressure tail gas recovers heat from the recovery housing, it will enter the reaction air duct. The high-pressure tail gas entering the reaction air duct will pass through the drive cavity to make the drive impeller rotate. At this time, the drive impeller will drive the circulation impeller to rotate, so that the rich amine liquid channel can suck the amine liquid that has absorbed carbon dioxide in the absorption housing into the main channel. The circulation component converts the pressure of the high-pressure tail gas into a driving force, thereby realizing autonomous circulation without an external hydraulic pump to achieve circulation, further saving energy consumption.

[0023] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0024] 1. Compared with the existing modular tank for carbon capture and storage, in the present invention, the regeneration channel is arranged in the recovery housing, and swirl vanes are arranged between the regeneration channel and the recovery housing. After the high-temperature tail gas enters the recovery housing, it will swirl under the guiding action of the swirl vanes. The high-temperature tail gas can extend the time in the recovery housing through swirling, so as to fully contact and transfer heat with the regeneration channel. Under the action of heat, it can help the amine liquid to be regenerated without an external heat source for amine liquid regeneration, thereby saving energy loss in the carbon capture and storage process to reduce costs; and through the process of tail gas swirling, solid particles in the tail gas can be separated, so as to prevent solid particles from entering the amine liquid. The tail gas has high cleanliness and will not pollute the amine liquid. At the same time, through the heat transfer process, the temperature of the tail gas can be controlled at a suitable absorption temperature to ensure that it will not damage the amine liquid, further reducing the cost of amine liquid loss.

[0025] 2. In the present invention, by setting a circulation component, after the high-pressure tail gas recovers heat from the recovery housing, it will enter the reaction air duct. The high-pressure tail gas entering the reaction air duct will pass through the drive cavity to make the drive impeller rotate. At this time, the drive impeller will drive the circulation impeller to rotate, so that the rich amine liquid channel can actively suck the amine liquid that has absorbed carbon dioxide in the absorption housing into the regeneration channel. The circulation component is used to convert the pressure of the high-pressure tail gas into the driving force for the rich amine liquid to flow to the regeneration channel, thereby realizing autonomous circulation work without an external hydraulic pump to regulate the system to achieve capture circulation, so as to ensure that the carbon dioxide capture process can be carried out normally autonomously without energy drive, further saving energy consumption.

[0026] 3. The present invention slows down the falling speed of the amine solution through the atomization holes on the surface of the atomization disk by setting up the atomization component, so as to ensure that the amine solution can stay in the lower part of the main channel for a period of time, thereby separating all the carbon dioxide in the amine solution. The driving rotor will make the atomization disk rotate under the driving force of the high-pressure tail gas. The rotation of the atomization disk will enable the lean amine solution to be evenly sprayed downward while atomizing. Through the spraying coverage effect, it can fully contact with the carbon dioxide that has not been completely absorbed and mixed in the waste gas, thereby capturing this part of the carbon dioxide and improving the capture efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] In order to more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the following will briefly introduce the drawings required for the description of the specific embodiments or the prior art. Obviously, the drawings in the following description are some embodiments of the present invention. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0028] Figure 1 is the overall structure diagram of the present invention;

[0029] Figure 2 is the schematic diagram of the internal structure of the heat recovery tank of the present invention;

[0030] Figure 3 is the cross-sectional view of the recovery housing and the absorption housing of the present invention;

[0031] Figure 4 is the cross-sectional view of the regeneration channel of the present invention;

[0032] Figure 5 is Figure 4 the enlarged view of the structure at A in

[0033] Figure 6 is the schematic diagram of the flow directions of the tail gas and the rich amine solution during the working process of the present invention;

[0034] Figure 7 is Figure 6 the enlarged view of the structure at B in

[0035] Figure 8 is the schematic diagram of the flow directions of carbon dioxide, lean amine solution and rich amine solution during the working process of the present invention;

[0036] In the figure: 1. Compression cooling system; 2. Heat recovery tank; 21. Recovery housing; 22. Intake channel; 23. Swirl vane; 3. Absorption tank; 31. Absorption housing; 32. Exhaust gas channel; 33. Reaction air duct; 34. Rich amine liquid channel; 4. Regeneration circulation system; 41. Regeneration channel; 411. Main channel; 412. Pressure reducing valve; 413. Corrugated demister; 414. Atomization assembly; 4141. Atomization disc; 41411. Atomization holes; 4142. Sealing bearing; 4143. Driving rotor; 42. Circulation assembly; 421. Driving cavity; 422. Driving impeller; 423. Circulation cavity; 424. Circulation impeller; 425. Connecting shaft; 5. Carbon storage tank. Detailed implementation manners

[0037] In order to better understand the above technical solution, the above technical solution will be described in detail below in conjunction with the accompanying drawings of the specification and specific implementation manners.

[0038] Please refer to Figures 1 to 8 , the present invention provides a modular energy-saving tank body for multi-stage carbon capture and storage, and the technical solution is as follows:

[0039] As a specific implementation manner of the present invention, referring to Figure 1 , Figure 2 , Figure 6 and Figure 8 , a modular energy-saving tank body for multi-stage carbon capture and storage; including a compression cooling system 1, and further including a heat recovery tank 2, an absorption tank 3, a regeneration circulation system 4 and a carbon storage tank 5; the absorption tank 3 is fixedly installed on the ground; the heat recovery tank 2 is arranged above the absorption tank 3; the absorption tank 3 is arranged below the heat recovery tank 2; the regeneration circulation system 4 includes a regeneration channel 41 and a circulation assembly 42; the regeneration channel 41 is arranged in the heat recovery tank 2, and the lower part of the regeneration channel 41 is communicated with the absorption tank 3, and the upper part of the regeneration channel 41 is connected with the compression cooling system 1. After the tail gas enters the heat recovery tank 2, it swirls and descends and flows through the outer surface of the regeneration channel 41. The amine liquid enters the middle part of the regeneration channel 41 and then enters the absorption tank 3 from the bottom of the regeneration channel 41; the circulation assembly 42 is connected between the regeneration channel 41 and the absorption tank 3. After the tail gas flows out of the heat recovery tank 2, it enters the absorption tank 3 through the circulation assembly 42 and drives the circulation assembly 42 to rotate at the same time. The rotation of the circulation assembly 42 pumps the amine liquid in the absorption tank 3 into the regeneration channel 41; the carbon storage tank 5 is connected with the compression cooling system 1.

[0040] As a specific implementation manner of the present invention, referring to Figure 2 , Figure 3 , Figure 4 and Figure 6, the heat recovery tank 2 includes a recovery housing 21, an intake passage 22, and a swirl vane 23; the recovery housing 21 is connected to the upper part of the absorption tank 3; the intake passage 22 is tangentially connected to the upper outer wall of the recovery housing 21; the swirl vanes 23 are arranged in a circumferential array between the recovery housing 21 and the regeneration passage 41. In the prior art, the high-temperature tail gas needs to be cooled before entering the absorption tower to react with the amine solution to prevent damage to the absorbent due to excessive temperature. However, the heat in the high-temperature tail gas will be wasted. Here, the discharged high-temperature tail gas is introduced into the recovery housing 21. The high-temperature tail gas entering the recovery housing 21 transfers heat to the regeneration passage 41 to help regenerate the amine solution. And after the high-temperature tail gas enters the recovery housing 21, it will swirl under the guiding action of the swirl vanes 23. The swirling of the high-temperature tail gas can extend the time in the recovery housing 21, so as to fully contact the regeneration passage 41 to transfer heat. At the same time, the swirling can separate the particulate matter in the tail gas, reducing the content of particulate matter in the tail gas entering the absorption tank 3 and avoiding pollution to the amine solution. In order to prevent the accumulation of solid particulate matter during long-term use, it is necessary to regularly disassemble the recovery housing 21 to clean the solid particulate matter on its inner wall.

[0041] As a specific embodiment of the present invention, referring to Figure 2 , Figure 3 , Figure 4 , Figure 6 and Figure 8 , the absorption tank 3 includes an absorption housing 31, an exhaust gas passage 32, a reaction air passage 33, and a rich amine liquid passage 34; the absorption housing 31 is connected to the lower part of the recovery housing 21, and the lower part of the absorption housing 31 is filled with amine liquid; the exhaust gas passage 32 is connected to the upper part of the absorption housing 31, and a demister is arranged at the outlet position of the exhaust gas passage 32, which can ensure that the amine liquid entrained when the tail gas after separating carbon dioxide is discharged can be filtered out, reducing amine liquid loss; the reaction air passage 33 connects the lower part of the recovery housing 21 and the lower part of the absorption housing 31, and the outlet position of the reaction air passage 33 is set to be bent downward, so that the tail gas is introduced to the bottom of the filled amine liquid, ensuring full contact between the tail gas and the amine liquid; the rich amine liquid passage 34 is connected between the regeneration passage 41 and the absorption housing 31. When filling the amine liquid, the amine liquid is filled to cover the reaction air passage 33 and the rich amine liquid passage 34 to ensure normal circulation. The tail gas after swirling cooling and separating solid particulate matter will enter the lower part of the absorption housing 31 from the reaction air passage 33, and the tail gas will be directly introduced into the amine liquid to ensure full contact for reaction. The reacted amine liquid (i.e., rich amine liquid) enters the regeneration passage 41 from the rich amine liquid passage 34. Since the regeneration passage 41 is heated by the discharged tail gas, the rich amine liquid can be decomposed back into carbon dioxide gas and lean amine liquid (i.e., amine liquid without carbonate). The decomposed lean amine liquid will return to the lower part of the absorption housing 31 from the lower part of the regeneration passage 41 to form a cycle, saving amine liquid loss.

[0042] As a specific embodiment of the present invention, referring to Figure 3 and Figure 4 , the rich amine liquid channel 34 penetrates through the middle and lower parts of the recovery housing 21 and is connected to the regeneration channel 41. During the downward swirling of the tail gas, the heat will gradually decrease. In actual use, the thermal conductivity of the material of the regeneration channel 41 can be selected to control the temperature in the middle layer of the regeneration channel 41 at about 120 °C. Since the rich amine liquid enters from the middle layer of the regeneration channel 41 through the rich amine liquid channel 34, the reaction temperature of the rich amine liquid is controlled at about 120 °C to ensure the best amine liquid regeneration temperature, thereby avoiding the escape of the amine liquid carried by carbon dioxide after volatilization due to too high temperature. Moreover, the temperature decreases as it goes down, which can ensure that the separated lean amine liquid accumulated at the bottom of the main channel 411 will not volatilize and escape. The temperature of the lowermost layer is controlled at about 60 °C, which can ensure that the temperature of the lean amine liquid returning to the absorption housing 31 is appropriate and can fully separate carbon dioxide during the waiting process of returning to the absorption housing 31.

[0043] As a specific embodiment of the present invention, referring to Figure 4 and Figure 8 , the regeneration channel 41 includes a main channel 411, a pressure reducing valve 412, a corrugated demister 413 and an atomization assembly 414; the main channel 411 is arranged at the center of the recovery housing 21; the pressure reducing valve 412 is arranged in the main channel 411 and is connected to the rich amine liquid channel 34; the corrugated demister 413 is arranged at the upper part of the main channel 411; the atomization assembly 414 is arranged at the lower part of the main channel 411. After the rich amine liquid enters the main channel 411, it will decompose carbon dioxide gas again at the regeneration temperature. At this time, the lean amine liquid will return to the absorption housing 31 through the atomization assembly 414. The carbon dioxide gas moves upward and filters out the carried amine liquid droplets through the corrugated demister 413 to avoid the escape of the amine liquid; since the rich amine liquid entering the main channel 411 will first pass through the recovery housing 21, the rich amine liquid will be preheated in the recovery housing 21. The preheated rich amine liquid will reduce the boiling point through the pressure reducing valve 412 to achieve flash evaporation, quickly separating carbon dioxide and amine liquid. Moreover, flash evaporation can further reduce energy consumption on the one hand and reduce the temperature of the amine liquid returning to the absorption housing 31 on the other hand.

[0044] As a specific embodiment of the present invention, referring to Figure 4 and Figure 5, the atomization assembly 414 includes an atomization disk 4141, a sealed bearing 4142, and a driving impeller 4143; the atomization disk 4141 is rotatably installed below the main channel 411, and a plurality of atomization holes 41411 are formed in the atomization disk 4141. The aperture of the atomization holes 41411 first becomes smaller and then larger along the axial direction; the sealed bearing 4142 is connected between the atomization disk 4141 and the absorption housing 31; the driving impeller 4143 is connected to the atomization disk 4141. The amine liquid after flash separation reaches the position of the atomization disk 4141. Since the structure of the atomization holes 41411 can reduce the amount of amine liquid falling per unit time, it is ensured that the amine liquid can stay in the lower part of the main channel 411 for a period of time, so that all the carbon dioxide in the amine liquid can be separated. Moreover, the structure of the atomization holes 41411 can make the lean amine liquid disperse into smaller droplets under the pressure change when discharged. The driving impeller 4143 will cause the atomization disk 4141 to rotate under the driving force of the high-pressure tail gas. The rotation of the atomization disk 4141 will enable the lean amine liquid to be evenly sprayed downward while being atomized. Through the spraying coverage effect, it can fully contact with the carbon dioxide that has not been completely absorbed and mixed in the waste gas, so as to capture this part of carbon dioxide and improve the capture efficiency.

[0045] As a specific embodiment of the present invention, refer to Figure 3 and Figure 4 , the upper end of the rich amine liquid channel 34 in the part between the main channel 411 and the recovery housing 21 is a semi-circular structure. The rich amine liquid entering the semi-circular structure at the upper end of the rich amine liquid channel 34 can extend the heat exchange time, so as to achieve the purpose of preheating the rich amine liquid to the saturation temperature, enabling the flash separation process to proceed smoothly, thereby improving the separation efficiency and reducing the carbon content in the regenerated amine liquid.

[0046] As a specific embodiment of the present invention, refer to Figure 6 、 Figure 7 and Figure 8, the circulation component 42 includes a drive chamber 421, a drive impeller 422, a circulation chamber 423, a circulation impeller 424 and a connecting shaft 425; the drive chamber 421 is connected to the reaction air passage 33; the drive impeller 422 is rotatably installed in the drive chamber 421; the circulation chamber 423 is connected to the rich amine liquid passage 34; the circulation impeller 424 is rotatably installed in the circulation chamber 423; the connecting shaft 425 is connected between the drive impeller 422 and the circulation impeller 424. After the high-pressure tail gas recovers heat from the recovery housing 21, it will enter the reaction air passage 33. The high-pressure tail gas entering the reaction air passage 33 will pass through the drive chamber 421 to cause the drive impeller 422 to rotate. At this time, the drive impeller 422 will drive the circulation impeller 424 to rotate, so that the rich amine liquid passage 34 can suck the amine liquid that has absorbed carbon dioxide in the absorption housing 31 into the main passage 411. The circulation component 42 converts the pressure of the high-pressure tail gas into a driving force, thereby realizing autonomous circulation without an external hydraulic pump to achieve circulation, further saving energy consumption.

[0047] Working process: The high-temperature and high-pressure tail gas discharged from the ship is introduced into the heat recovery tank 2. The high-temperature and high-pressure tail gas performs a swirling downward movement between the recovery housing 21 and the regeneration passage 41 to transfer heat to the regeneration passage 41. After the high-temperature and high-pressure tail gas cools down, it enters the absorption housing 31 to react with the amine liquid and drive the circulation component 42 to rotate. The reacted amine liquid (hereinafter collectively referred to as rich amine liquid) will be sucked into the regeneration passage 41 under the rotation of the circulation component 42 for amine liquid regeneration reaction. At this time, the rich amine liquid will be decomposed into carbon dioxide and lean amine liquid. The carbon dioxide is compressed and cooled by the compression cooling system and stored in the carbon storage tank 5, while the lean amine liquid will flow back to the absorption housing 31.

[0048] Specifically, the high-temperature and high-pressure tail gas discharged from the ship is introduced into the recovery housing 21 through the intake passage 22 tangentially connected to the recovery housing 21. At this time, the high-temperature and high-pressure tail gas will perform a swirling downward movement under the guiding action of the swirling blades 23. The high-temperature tail gas can extend the time in the recovery housing 21 through swirling, so as to fully contact and transfer heat with the regeneration passage 41. At the same time, the particulate matter in the tail gas can be separated through swirling, reducing the particulate matter content in the tail gas entering the absorption tank 3 and avoiding polluting the amine liquid.

[0049] The tail gas reaching the bottom of the recovery housing 21 will enter the reaction air duct 33, and pass through the reaction air duct 33 into the absorption housing 31, contact the amine liquid in the absorption housing 31 and react. The amine liquid in the absorption housing 31 absorbs carbon dioxide in the tail gas. The tail gas passing through the reaction air duct 33 will flow through the drive chamber 421 to make the drive impeller 422 rotate. At this time, the drive impeller 422 will drive the circulation impeller 424 to rotate, so that the rich amine liquid channel 34 can suck the amine liquid that has absorbed carbon dioxide in the absorption housing 31 into the main channel 411 to achieve autonomous circulation;

[0050] The rich amine liquid entering the semi-circular structure at the upper end of the rich amine liquid channel 34 can extend the heat exchange time, so as to achieve the purpose of preheating the rich amine liquid to the saturation temperature. The rich amine liquid reaching the saturation temperature can achieve flash evaporation through the pressure reducing valve 412 to quickly separate carbon dioxide and amine liquid. At this time, the separated carbon dioxide will enter the compression cooling system 1 from the upper part of the main channel 411, and change from gaseous carbon dioxide to liquid carbon dioxide through compression cooling and be stored in the carbon storage tank 5. The separated lean amine liquid will accumulate at the lower part of the main channel 411 under the action of gravity. Since the swirling high-temperature and high-pressure tail gas in the main channel 411 continuously heats the main channel 411 and drives the atomizing disc 4141 to rotate through the driving rotor 4143, at this time, the lean amine liquid will be refined into fine droplets through the atomizing holes 41411 on the atomizing disc 4141 and evenly sprayed back into the absorption housing 31, so as to realize the recycling of amine liquid, and the evenly sprayed lean amine liquid can fully contact the carbon dioxide that has not been completely absorbed and mixed in the waste gas, so as to capture this part of carbon dioxide and improve the capture efficiency.

[0051] The above shows and describes the basic principles, main features and advantages of the present invention. Those skilled in the art should understand that the present invention is not limited by the above embodiments. What is described in the above embodiments and the specification only illustrates the principle of the present invention. Without departing from the spirit and scope of the present invention, the present invention will have various changes and improvements, and these changes and improvements all fall within the scope of the present invention claimed. The scope of the present invention claimed is defined by the appended claims and their equivalents.

Claims

1. A modular energy-saving tank for multi-stage carbon capture and storage; comprising a compression cooling system (1), characterized in that: The invention also comprises a heat recovery tank (2), an absorption tank (3), a regeneration circulation system (4) and a carbon storage tank (5); the heat recovery tank (2) comprises a recovery shell (21); the absorption tank (3) is fixedly arranged on the ground; the recovery shell (21) is arranged above the absorption tank (3); the regeneration circulation system (4) comprises a regeneration channel (41) and a circulation component (42); the regeneration channel (41) is arranged in the recovery shell (21); the upper part of the regeneration channel (41) is connected to the compression cooling system (1); the lower part of the regeneration channel (41) is connected to the absorption tank (3); the tail gas enters the recovery shell (41) and enters the regeneration circulation system (42); After the shell (21) is collected, the swirl flow descends through the outer surface of the regeneration channel (41), and the amine liquid enters the middle of the regeneration channel (41) and then enters the absorption tank (3) from the bottom of the regeneration channel (41); the circulation component (42) is connected between the regeneration channel (41) and the absorption tank (3), and the tail gas flows out of the heat recovery tank (2) and enters the absorption tank (3) through the circulation component (42) and drives the circulation component (42) to rotate. The circulation component (42) rotates to draw the amine liquid in the absorption tank (3) into the regeneration channel (41); the carbon storage tank (5) is connected to the compression cooling system (1).

2. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 1 is characterized by: The heat recovery tank (2) further comprises an air intake channel (22) and swirl blades (23); the air intake channel (22) is tangentially connected to the upper outer wall of the recovery shell (21); and the swirl blades (23) are arranged in a circumferential array between the recovery shell (21) and the regeneration channel (41).

3. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 2 is characterized by: The absorption tank (3) comprises an absorption shell (31), an exhaust gas channel (32), a reaction gas channel (33) and a rich amine liquid channel (34); the absorption shell (31) is connected to the lower part of the recovery shell (21), and the lower part of the absorption shell (31) is filled with amine liquid; the exhaust gas channel (32) is connected to the upper part of the absorption shell (31); the reaction gas channel (33) connects the lower part of the recovery shell (21) with the lower part of the absorption shell (31); and the rich amine liquid channel (34) is connected between the regeneration channel (41) and the absorption shell (31).

4. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 3 is characterized by: The rich amine liquid channel (34) passes through the lower middle portion of the recovery shell (21) and is connected to the regeneration channel (41).

5. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 3 is characterized by: The regeneration channel (41) comprises a main channel (411), a pressure reducing valve (412), a corrugated demister (413) and an atomizing assembly (414); the main channel (411) is arranged at the center of the recovery shell (21); the pressure reducing valve (412) is arranged in the main channel (411) and connected to the rich amine liquid channel (34); the corrugated demister (413) is arranged at the upper part of the main channel (411); and the atomizing assembly (414) is arranged at the lower part of the main channel (411).

6. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 5 is characterized by: The atomizing assembly (414) comprises an atomizing disk (4141), a sealing bearing (4142) and a driving rotor (4143); the atomizing disk (4141) is rotatably mounted below the main channel (411), and a plurality of atomizing holes (41411) are provided on the atomizing disk (4141); the sealing bearing (4142) is connected between the atomizing disk (4141) and the absorption shell (31); and the driving rotor (4143) is connected to the atomizing disk (4141).

7. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 5 is characterized by: The upper end of the rich amine liquid channel (34) located between the main channel (411) and the recovery shell (21) is a semi-annular structure.

8. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 3 is characterized by: The circulation component (42) comprises a driving chamber (421), a driving impeller (422), a circulation chamber (423), a circulating impeller (424) and a connecting shaft (425); the driving chamber (421) is connected to the reaction gas channel (33); the driving impeller (422) is rotatably mounted in the driving chamber (421); the circulation chamber (423) is connected to the rich amine liquid channel (34); the circulating impeller (424) is rotatably mounted in the circulation chamber (423); and the connecting shaft (425) is connected between the driving impeller (422) and the circulating impeller (424).

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