A modular energy-saving tank for multi-stage carbon capture and storage

Abstract

The present invention relates to the technical field of waste gas purification, and specifically to a modular energy-saving tank body for multi-stage carbon capture and storage, comprising a heat recovery tank, an absorption tank, a regeneration circulation 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 component; the regeneration channel is arranged in the heat recovery tank; the circulation component is connected between the regeneration channel and the absorption tank; the carbon storage tank is connected to the compression cooling system; by recycling the heat and pressure of high-temperature and high-pressure exhaust gas, utilizing the waste heat of the exhaust gas to achieve amine liquid regeneration, utilizing the exhaust gas pressure to achieve amine liquid flow circulation, thereby saving energy consumption in the carbon capture process; and solving the problem that the amine liquid regeneration process requires a large amount of heat energy to consume, resulting in high carbon capture costs.

Description

Technical Field

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

[0002] Multi-stage carbon capture and storage technology is a carbon management technology that optimizes processes and improves efficiency in stages. It aims to capture carbon dioxide from industrial emission sources or energy production and reduce its entry into the atmosphere through long-term storage. Multi-stage carbon capture technology usually includes three core links: capture, transportation and storage. During the transportation process, modular tanks are required as intermediate storage units to store carbon dioxide compressed into liquid or supercritical states.

[0003] Carbon capture and storage technology is currently mostly used in the energy industry, heavy industry and transportation and shipping. Ships, as the main carrier of global trade, account for 2.89% of the global carbon emissions. In order to reduce carbon emissions from ships, carbon capture and storage technology has developed rapidly in this field. At present, ship carbon capture technology mainly separates carbon dioxide from ship exhaust gas through chemical adsorption, and then compresses and cools the carbon dioxide gas to liquefy the carbon dioxide gas. After liquefaction, it is stored in a tank for preservation and the tank is unloaded after docking. When capturing carbon dioxide by chemical adsorption, it mainly uses amine liquid to react with carbon dioxide, and the exhaust gas is passed into an absorption tower. The carbon dioxide in the exhaust gas reacts with the amine liquid to form carbonate, and the non-acidic gas will be discharged directly. When the non-acidic gas is discharged, it will carry the amine liquid with it to escape, causing environmental pollution and loss of amine liquid, thereby leading to increased costs. The existing technology has proposed good solutions to this problem, such as patent publication number CN113499680B, which describes a device system and method for preventing amine escape in a carbon dioxide amine capture process. Through the swirl effect of the dual impellers in the cyclone separation device, amine-containing droplets in the airflow collide, condense, and adhere to and are removed under the action of centrifugal force, thereby preventing the amine droplets from escaping. The device has a simple structure, is easy to operate and control, and has low processing costs.

[0004] Although the existing technology has solved the problem of increased processing costs caused by the escape of amine liquid during the carbon dioxide capture process, the following problems still exist: the carbon dioxide capture and storage process requires the exhaust gas to be cooled from 300 degrees Celsius to 40-60 degrees Celsius to prevent the high-temperature exhaust gas from damaging the adsorbent. The cooled exhaust gas is passed into the absorption tower to contact the amine liquid. The carbon dioxide in the exhaust gas reacts with the amine liquid to produce carbonate, which needs to be heated to above 120 degrees Celsius to decompose and release the carbon dioxide gas and regenerate the amine liquid. The regenerated amine liquid is returned to the absorption tower for reuse, and finally the carbon dioxide gas is compressed, cooled and liquefied for storage. A large amount of heat energy is consumed in the process of amine liquid regeneration, which leads to increased costs.

[0005] In view of the above situation, in order to overcome the above technical problems, the present invention designs a modular energy-saving tank 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 requires 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 exhaust gas discharged by the ship will swirl through the outer surface of the regeneration channel. On the one hand, it can extend the residence time of the exhaust gas in the heat recovery tank, provide sufficient heat energy for amine liquid regeneration, reduce energy consumption, and the exhaust gas temperature of the amine liquid introduced can be reduced to a suitable temperature to avoid damage to the amine liquid. On the other hand, the particulate matter in the exhaust gas is separated to avoid pollution of the amine liquid, thereby reducing the cost of amine liquid replacement; and a circulation component is provided. When the exhaust gas flows from the heat recovery tank to the absorption tank, the circulation component will be driven to rotate, so that the amine liquid that has absorbed carbon dioxide is automatically pumped into the regeneration channel for regeneration reaction, and the regenerated and separated amine liquid will be atomized back into the absorption tank under the swirl force of the exhaust 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; comprising a compression cooling system, 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 comprises 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 connected to the absorption tank, and the upper part of the regeneration channel is connected to the compression cooling system, after the exhaust gas enters the heat recovery tank, it swirls and descends through the outer surface of the regeneration channel, and 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, and after the exhaust gas flows out of the heat recovery tank, it passes through the circulation component and enters the absorption tank and drives the circulation component to rotate, and the circulation component rotates to pump the amine liquid in the absorption tank into the regeneration channel; the carbon storage tank is connected to the compression cooling system, and the separated carbon dioxide gas is liquefied by the compression cooling system and stored in the carbon storage tank.

[0009] Preferably, the heat recovery tank includes a recovery shell, an air inlet channel and swirl blades; the recovery shell 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 shell; the swirl blade circumferential array is arranged between the recovery shell and the regeneration channel.

[0010] In the above scheme, since the high-temperature exhaust gas in the existing technology needs to be cooled before entering the absorption tower to react with the amine liquid to prevent the absorbent from being damaged by excessive temperature, the heat in the high-temperature exhaust gas will be wasted. Here, the discharged high-temperature exhaust gas is passed into the recovery shell. The high-temperature exhaust gas entering the recovery shell transfers heat to the regeneration channel to help the amine liquid to regenerate. After the high-temperature exhaust gas enters the recovery shell, it will swirl under the guidance of the swirl blades. The high-temperature exhaust gas can extend the time in the recovery shell through the swirl, so that it can fully contact the regeneration channel to transfer heat. At the same time, the particulate matter in the exhaust gas can be separated through the swirl, so that the particulate matter content in the exhaust gas entering the absorption tank is reduced, avoiding pollution of the amine liquid.

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

[0012] In the above scheme, the exhaust gas after cyclone cooling and separation of solid particles will enter the lower part of the absorption shell from the reaction gas channel, and the exhaust gas will be directly introduced into the amine liquid to ensure sufficient contact for reaction. The amine liquid after the reaction (i.e., rich amine liquid) enters the regeneration channel from the rich amine liquid channel. Since the regeneration channel is heated by the discharged exhaust gas, the rich amine liquid can be decomposed into carbon dioxide gas and lean amine liquid (i.e., amine liquid that does not contain carbonates). The decomposed lean amine liquid will return to the lower part of the absorption shell from the lower part of the regeneration channel to form a cycle, saving amine liquid loss.

[0013] Preferably, the rich amine liquid channel passes through the lower middle portion of the recovery shell and is connected to the regeneration channel.

[0014] In the above scheme, since the rich amine liquid enters the middle layer of the regeneration channel through the rich amine liquid channel, the reaction temperature of the rich amine liquid can be controlled at about 120 degrees Celsius, ensuring the optimal amine liquid regeneration temperature, thereby avoiding the amine liquid from volatilizing and being carried away by carbon dioxide and escaping due to excessive temperature. The temperature decreases as it goes down, which can ensure that the separated lean amine liquid 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 atomizing assembly; the main channel is arranged in the center of the recovery shell; the pressure reducing valve is arranged in the main channel and connected to the rich amine liquid channel; the corrugated demister is arranged at the upper part of the main channel; and the atomizing assembly is arranged at the lower part of the main channel.

[0016] In the above scheme, the rich amine liquid after entering the main channel will decompose the carbon dioxide gas again at the regeneration temperature. At this time, the lean amine liquid will return to the absorption shell through the atomization component. The carbon dioxide gas will rise and filter the amine liquid droplets it carries through the corrugated demister to prevent the amine liquid from escaping. Since the rich amine liquid entering the main channel will first pass through the recovery shell, the rich amine liquid will be preheated in the recovery shell. The preheated rich amine liquid will lower the boiling point through the pressure reducing valve to achieve flash evaporation, quickly separating the carbon dioxide and amine liquid. Flash evaporation can further reduce energy consumption on the one hand, and on the other hand, it can reduce the temperature of the amine liquid returning to the absorption shell.

[0017] Preferably, the atomization assembly includes an atomizing disk, a sealed bearing and a driving vane; the atomizing disk is rotatably installed below the main channel, and a plurality of atomization holes are opened on the atomizing disk; the sealed bearing is connected between the atomizing disk and the absorption shell; the driving vane is connected to the atomizing disk.

[0018] In the above scheme, the amine liquid after flash separation reaches the atomizing disk position, and the atomizing hole can slow down the falling speed of the amine liquid, thereby ensuring that the amine liquid can be retained in the lower part of the main channel for a period of time, thereby completely separating the carbon dioxide in the amine liquid. The driving vanes will rotate the atomizing disk under the driving force of the high-pressure exhaust gas. The rotation of the atomizing disk will enable the lean amine liquid to be evenly sprayed downward while being atomized. The spray coverage effect can fully contact with the carbon dioxide that has not been completely absorbed and mixed in the exhaust gas, thereby capturing this part of the carbon dioxide and improving the capture efficiency.

[0019] Preferably, the upper end of the rich amine liquid channel located between the main channel and the recovery shell is a semi-annular structure.

[0020] In the above scheme, the amine liquid enters the semi-annular structure at the upper end of the rich amine liquid channel, which can extend the heat exchange time, thereby achieving the purpose of preheating the rich amine liquid to the saturation temperature, allowing 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 component includes a driving chamber, a driving impeller, a circulation chamber, a circulating impeller and a connecting shaft; the driving chamber is connected to the reaction gas channel; the driving impeller is rotatably installed in the driving chamber; the circulation chamber is connected to the rich amine liquid channel; the circulating impeller is rotatably installed in the circulation chamber; the connecting shaft is connected between the driving impeller and the circulating impeller.

[0022] In the above scheme, the high-pressure exhaust gas will enter the reaction gas channel after heat recovery from the recovery shell. The high-pressure exhaust gas entering the reaction gas channel will pass through the driving chamber to rotate the driving impeller. At this time, the driving 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 shell into the main channel. The circulation component converts the pressure of the high-pressure exhaust gas into driving force, thereby realizing autonomous circulation. There is no need for an external hydraulic pump to achieve circulation, which further saves energy consumption.

[0023] Compared with the prior art, the present invention has the following beneficial effects:

[0024] 1. Compared with the existing modular tank for carbon capture and storage, the present invention sets the regeneration channel in the recovery shell and sets swirl blades between the regeneration channel and the recovery shell. After the high-temperature exhaust gas enters the recovery shell, it will swirl under the guidance of the swirl blades. The high-temperature exhaust gas can extend the time in the recovery shell through the swirl, so that it can fully contact the regeneration channel to transfer heat. Under the action of heat, it can help the amine liquid to regenerate, and no external heat source is required for amine liquid regeneration, thereby saving energy loss in the carbon capture and storage process and reducing costs; and the solid particles in the exhaust gas can be separated through the exhaust swirl process, thereby preventing the solid particles from entering the amine liquid. The exhaust gas has high cleanliness and will not cause pollution to the amine liquid. At the same time, the exhaust gas temperature can be controlled at a temperature suitable for absorption through the heat transfer process, ensuring that the amine liquid will not be damaged, further reducing the cost of amine liquid loss.

[0025] 2. The present invention sets a circulation component. After the heat is recovered from the recovery shell, the high-pressure exhaust gas will enter the reaction gas channel. The high-pressure exhaust gas entering the reaction gas channel will pass through the driving chamber to rotate the driving impeller. At this time, the driving 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 shell into the regeneration channel. The circulation component is used to convert the pressure of the high-pressure exhaust gas into the driving force for the rich amine liquid to flow to the regeneration channel, thereby realizing autonomous circulation. There is no need for an external hydraulic pump to control the system to realize the capture cycle, thereby ensuring that the carbon dioxide capture process can be maintained normal and autonomous without energy drive, further saving energy consumption.

[0026] 3. The present invention provides an atomizing assembly, and the atomizing holes on the surface of the atomizing disk can slow down the falling speed of the amine liquid, thereby ensuring that the amine liquid can be retained in the lower part of the main channel for a period of time, thereby completely separating the carbon dioxide in the amine liquid. The driving vanes will rotate the atomizing disk under the driving force of the high-pressure exhaust gas. The rotation of the atomizing disk will enable the lean amine liquid to be evenly sprayed downward while being atomized. The spray coverage effect can fully contact the carbon dioxide that has not been completely absorbed and mixed in the exhaust 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 is a brief introduction to the drawings required for use in the specific embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

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

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

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

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

[0032] Figure 5 for Figure 4 A magnified view of the structure at center A;

[0033] Figure 6 Schematic diagram of the flow direction of tail gas and rich amine liquid during the working process of the present invention;

[0034] Figure 7 for Figure 6 A magnified view of the structure at point B in the middle;

[0035] Figure 8 Schematic diagram of the flow 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 shell; 22. Air inlet channel; 23. Swirl blade; 3. Absorption tank; 31. Absorption shell; 32. Exhaust gas channel; 33. Reaction gas channel; 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 disk; 41411. Atomization hole; 4142. Sealed bearing; 4143. Drive rotor; 42. Circulation assembly; 421. Drive chamber; 422. Drive impeller; 423. Circulation chamber; 424. Circulation impeller; 425. Connecting shaft; 5. Carbon storage tank. DETAILED DESCRIPTION

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

[0038] See also Figures 1 to 8 The present invention provides a modular energy-saving tank for multi-stage carbon capture and storage. The technical solution is as follows:

[0039] As a specific embodiment of the present invention, refer to Figure 1 、 Figure 2 、 Figure 6 and Figure 8 , a modular energy-saving tank body for multi-stage carbon capture and storage; comprising a compression cooling system 1, 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 comprises a regeneration channel 41 and a circulation component 42; the regeneration channel 41 is arranged in the heat recovery tank 2, and the lower part of the regeneration channel 41 is connected to the absorption tank 3, and the upper part of the regeneration channel 41 is connected to the compression The cooling system 1 is connected, and the exhaust gas enters the heat recovery tank 2 and then swirls down and flows through the outer surface of the regeneration channel 41. 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. After the exhaust gas flows out of the heat recovery tank 2, it passes through the circulation component 42 and enters the absorption tank 3 while driving the circulation component 42 to rotate. The circulation component 42 rotates to pump 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.

[0040] As a specific embodiment of the present invention, refer to Figure 2 、 Figure 3 、 Figure 4 and Figure 6The heat recovery tank 2 includes a recovery shell 21, an air inlet channel 22 and swirl blades 23; the recovery shell 21 is connected to the upper part of the absorption tank 3; the air inlet channel 22 is tangentially connected to the upper outer wall of the recovery shell 21; the swirl blades 23 are arranged in a circular array between the recovery shell 21 and the regeneration channel 41. Since the high-temperature exhaust gas in the prior art needs to be cooled before entering the absorption tower to react with the amine liquid to prevent the absorbent from being damaged by excessive temperature, the heat in the high-temperature exhaust gas will be wasted. Here, the discharged high-temperature exhaust gas is passed into the recovery shell 21. The high-temperature exhaust gas entering the recovery shell 21 transfers heat to the regeneration channel 41 to help the amine liquid to regenerate. After the high-temperature exhaust gas enters the recovery shell 21, it will swirl under the guidance of the swirl blades 23. The high-temperature exhaust gas can extend the time in the recovery shell 21 through the swirl, so that it can fully contact the regeneration channel 41 to transfer heat. At the same time, the particulate matter in the exhaust gas can be separated through the swirl, so that the particulate matter content in the exhaust gas entering the absorption tank 3 is reduced, avoiding pollution to the amine liquid. In order to prevent the accumulation of solid particulate matter after long-term use, the recovery shell 21 needs to be disassembled regularly to clean the solid particulate matter on its inner wall.

[0041] As a specific embodiment of the present invention, refer to Figure 2 、 Figure 3 、 Figure 4 、 Figure 6 and Figure 8 The absorption tank 3 includes 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, and a demister is provided at the outlet of the exhaust gas channel 32 to ensure that the amine liquid carried by the exhaust gas after separation of carbon dioxide can be filtered out, thereby reducing the loss of amine liquid; 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 outlet position of the reaction gas channel 33 is set to a downward bending structure, so that the exhaust gas passes into the bottom of the filled amine liquid, so that the exhaust gas and the amine liquid are fully in contact; the rich amine liquid channel 34 is connected between the regeneration channel 41 and the absorption shell 31. When filling the amine liquid, the amine liquid submerges the reaction gas channel 33 and the rich amine liquid channel 34 to ensure normal circulation. The tail gas after cyclone cooling and separation of solid particles will enter the lower part of the absorption shell 31 from the reaction gas channel 33, and the tail gas will be directly introduced into the amine liquid to ensure sufficient contact for reaction. The amine liquid after the reaction (i.e., rich amine liquid) enters the regeneration channel 41 from the rich amine liquid channel 34. Since the regeneration channel 41 is heated by the discharged tail gas, the rich amine liquid can be decomposed into carbon dioxide gas and lean amine liquid (i.e., amine liquid that does not contain carbonates). The decomposed lean amine liquid will return to the lower part of the absorption shell 31 from the lower part of the regeneration channel 41 to form a cycle, saving amine liquid loss.

[0042] As a specific embodiment of the present invention, refer to Figure 3 and Figure 4 The rich amine liquid channel 34 passes through the middle and lower part of the recovery shell 21 and is connected to the regeneration channel 41. As the exhaust gas swirls downward, 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 of the middle layer of the regeneration channel 41 to about 120 degrees Celsius. Since the rich amine liquid enters 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 degrees Celsius to ensure the optimal amine liquid regeneration temperature, thereby preventing the amine liquid from being carried away by carbon dioxide after volatilization due to excessive temperature. The temperature decreases as the temperature 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 lowest layer is controlled at about 60 degrees Celsius, ensuring that the lean amine liquid returning to the absorption shell 31 is at an appropriate temperature while fully separating the carbon dioxide while waiting to return to the absorption shell 31.

[0043] As a specific embodiment of the present invention, refer 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 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; the atomizing assembly 414 is arranged at the lower part of the main channel 411. After entering the main channel 411, the rich amine liquid will decompose the carbon dioxide gas again at the regeneration temperature. At this time, the lean amine liquid will return to the absorption shell 31 through the atomization component 414. The carbon dioxide gas will rise and filter the amine liquid droplets carried by it through the corrugated demister 413 to prevent the amine liquid from escaping. Since the rich amine liquid entering the main channel 411 will first pass through the recovery shell 21, the rich amine liquid will be preheated in the recovery shell 21. The preheated rich amine liquid will reduce the boiling point through the pressure reducing valve 412 to achieve flash evaporation, and quickly separate the carbon dioxide and amine liquid. Flash evaporation can further reduce energy consumption on the one hand, and on the other hand, it can reduce the temperature of the amine liquid returned to the absorption shell 31.

[0044] As a specific embodiment of the present invention, refer to Figure 4 and Figure 5The atomization assembly 414 includes an atomization disk 4141, a sealing bearing 4142 and a driving vane 4143; the atomization disk 4141 is rotatably installed below the main channel 411, and a plurality of atomization holes 41411 are opened on the atomization disk 4141, and the aperture of the atomization hole 41411 first decreases and then increases along the axial direction; the sealing bearing 4142 is connected between the atomization disk 4141 and the absorption shell 31; the driving vane 4143 is connected to the atomization disk 4141. The amine liquid after flash separation reaches the position of the atomizing disk 4141. Since the structure of the atomizing hole 41411 can reduce the amount of amine liquid falling per unit time, it can ensure that the amine liquid can be retained in the lower part of the main channel 411 for a period of time, thereby separating all the carbon dioxide in the amine liquid. In addition, the structure of the atomizing hole 41411 can make the lean amine liquid disperse into smaller droplets under pressure changes when it is discharged, and the driving blade 4143 will rotate the atomizing disk 4141 under the driving force of the high-pressure exhaust gas. The rotation of the atomizing disk 4141 will enable the lean amine liquid to be sprayed downward evenly while being atomized. The spraying and covering effect can fully contact with the carbon dioxide that has not been completely absorbed and mixed in the exhaust gas, thereby capturing this part of the carbon dioxide and improving 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, located between the main channel 411 and the recovery shell 21, is a semi-annular structure. The rich amine liquid entering the semi-annular structure at the upper end of the rich amine liquid channel 34 prolongs the heat exchange time, thereby preheating the rich amine liquid to the saturation temperature. This allows the flash evaporation process to proceed smoothly, thereby improving 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 8The circulation component 42 includes 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 installed in the driving chamber 421; the circulation chamber 423 is connected to the rich amine liquid channel 34; the circulating impeller 424 is rotatably installed in the circulation chamber 423; the connecting shaft 425 is connected between the driving impeller 422 and the circulating impeller 424. After the high-pressure exhaust gas is heat recovered from the recovery shell 21, it will enter the reaction gas channel 33. The high-pressure exhaust gas entering the reaction gas channel 33 will pass through the driving chamber 421 to drive the impeller 422 to rotate. At this time, the driving 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 shell 31 into the main channel 411. The circulation component 42 converts the pressure of the high-pressure exhaust gas into driving force, thereby realizing autonomous circulation. There is no need for an external hydraulic pump to achieve circulation, which further saves energy consumption.

[0047] Working process: The high-temperature and high-pressure exhaust gas discharged from the ship is introduced into the heat recovery tank 2, and the high-temperature and high-pressure exhaust gas performs a swirling downward motion between the recovery shell 21 and the regeneration channel 41 to transfer heat to the regeneration channel 41. After cooling, the high-temperature and high-pressure exhaust gas enters the absorption shell 31 to react with the amine liquid and drive the circulation component 42 to rotate. The reacted amine liquid (hereinafter referred to as rich amine liquid) will be drawn into the regeneration channel 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 then stored in the carbon storage tank 5, while the lean amine liquid will flow back to the absorption shell 31.

[0048] Specifically, the high-temperature and high-pressure exhaust gas discharged from the ship is introduced into the recovery shell 21 through the air inlet channel 22 tangentially connected to the recovery shell 21. At this time, the high-temperature and high-pressure exhaust gas will undergo a swirling downward motion under the guidance of the swirl blades 23. The high-temperature exhaust gas can prolong the time in the recovery shell 21 through the swirl flow, thereby fully contacting and transferring heat with the regeneration channel 41. At the same time, the swirl flow can separate particulate matter in the exhaust gas, thereby reducing the particulate matter content in the exhaust gas entering the absorption tank 3 and avoiding contamination of the amine liquid.

[0049] The tail gas reaching the bottom of the recovery shell 21 will enter the reaction gas channel 33, and then enter the absorption shell 31 through the reaction gas channel 33, where it will come into contact with and react with the amine liquid in the absorption shell 31. The amine liquid in the absorption shell 31 absorbs carbon dioxide in the tail gas. The tail gas passing through the reaction gas channel 33 will flow through the drive chamber 421, causing the driving impeller 422 to rotate. At this time, the driving impeller 422 will drive the circulation impeller 424 to rotate, so that the rich amine liquid channel 34 can draw the amine liquid in the absorption shell 31 that has absorbed carbon dioxide into the main channel 411, thereby realizing autonomous circulation.

[0050] The rich amine liquid enters the semi-annular structure at the upper end of the rich amine liquid channel 34 to extend the heat exchange time, thereby achieving the purpose of preheating the rich amine liquid to the saturation temperature. The rich amine liquid that reaches the saturation temperature can be flashed through the pressure reducing valve 412 to quickly separate the carbon dioxide and the 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 after compression cooling, it will be converted from gaseous carbon dioxide into liquid carbon dioxide and stored in the carbon storage tank 5. The separated lean amine liquid will reach the lower part of the main channel 411 under the action of gravity. And accumulate, because the high-temperature and high-pressure exhaust gas swirling in the main channel 411 will continuously supply heat to the main channel 411 and drive the atomizing disk 4141 to rotate by driving the rotor blades 4143, the lean amine liquid will be refined into fine droplets through the atomizing holes 41411 on the atomizing disk 4141 and evenly sprayed back into the absorption shell 31, thereby realizing the recycling of the amine liquid, and the evenly sprayed lean amine liquid can fully contact with the carbon dioxide that has not been completely absorbed and mixed in the exhaust gas, thereby capturing this part of the carbon dioxide and improving the capture efficiency.

[0051] The basic principles, main features, and advantages of the present invention are shown and described above. It should be understood by those skilled in the art that the present invention is not limited to the foregoing embodiments. The foregoing embodiments and descriptions are merely illustrative of the principles of the present invention. Various changes and modifications may be made to the present invention without departing from the spirit and scope of the present invention. Such changes and modifications are intended to fall within the scope of the present invention as claimed, which 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 includes 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) includes 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) includes 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), and the lower part of the regeneration channel (41) is connected to the absorption tank (3), and the tail gas enters the regeneration circulation system (42). After the shell (21) is collected, the swirl flow descends and flows through the outer surface of the regeneration channel (41). 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). After the tail gas flows out of the heat recovery tank (2), it passes through the circulation component (42) and enters the absorption tank (3). At the same time, the circulation component (42) is driven to rotate. The circulation component (42) rotates to pump 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); The heat recovery tank (2) further comprises an air inlet channel (22) and swirl blades (23); the air inlet channel (22) is tangentially connected to the upper outer wall of the recovery shell (21); the swirl blades (23) are arranged in a circumferential array between the recovery shell (21) and the regeneration channel (41); 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).

2. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 1, characterized in that: 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).

3. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 1, characterized in that: 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).

4. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 3, characterized in that: The atomizing assembly (414) comprises an atomizing disc (4141), a sealing bearing (4142) and a driving vane (4143); the atomizing disc (4141) is rotatably mounted below the main channel (411), and a plurality of atomizing holes (41411) are provided on the atomizing disc (4141); the sealing bearing (4142) is connected between the atomizing disc (4141) and the absorption shell (31); and the driving vane (4143) is connected to the atomizing disc (4141).

5. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 3, characterized in that: 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.

6. The modular energy-saving tank for multi-stage carbon capture and storage according to claim 1, characterized in that: The circulation assembly (42) includes 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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