A carbon dioxide capture system suitable for use with a shipboard emission source

Abstract

The application discloses a carbon dioxide capture system suitable for a ship emission source, and relates to the technical field of flue gas purification and greenhouse gas emission reduction, comprising an absorption system for absorbing carbon dioxide in flue gas by using an organic solution amine liquid, a washing system for washing organic amines in flue gas by using washing water, a regeneration system for heating rich liquid to separate and regenerate amine liquid and carbon dioxide, a heat exchange system for removing heat generated in the carbon dioxide capture system, and an amine purification system for removing salts in the amine liquid which cannot be regenerated. The carbon dioxide capture system adopts a modular and small-sized design, so that the overall height of the equipment is reduced, the floor area is reduced, and thus the arrangement and installation on the ship are facilitated, the carbon dioxide emission of the shipping industry is reduced, and a flexible market supplement scheme is provided for realizing the carbon neutralization target.

Description

Technical Field

[0001] This invention belongs to the field of flue gas purification and greenhouse gas emission reduction technology, and particularly relates to a carbon dioxide capture system suitable for ship emission sources. Background Technology

[0002] As a key link in international trade, the global shipping industry plays an irreplaceable role in promoting economic globalization. However, its environmental impact is becoming increasingly prominent. Ships emit large amounts of greenhouse gases during operation, with carbon dioxide emissions being particularly significant and a major contributor to global warming.

[0003] Shipborne carbon capture technology, which directly separates and captures carbon dioxide from ship exhaust, is a key pathway for the shipping industry's low-carbon transformation, providing a solution compatible with existing power systems and possessing the potential for large-scale emission reduction. Equipping ships with this system can reduce carbon emissions by 75%–80%, and it is expected to complement green fuels in the future, helping the shipping industry achieve its carbon neutrality goals. Currently, the mainstream shipborne carbon capture method is chemical absorption, and China has already achieved the world's first ship-to-ship liquid carbon dioxide unloading operation.

[0004] However, shipboard carbon capture technology faces severe challenges due to the unique operating conditions of ships. First, shipboard space is limited; traditional carbon capture systems have large footprints and excessively tall towers, making them difficult to install on vessels. Second, ships experience dynamic conditions such as rolling and tilting during navigation, placing higher demands on the stability and adaptability of the equipment. Third, carbon capture systems consume a significant amount of energy, impacting the ship's economics and operating costs. Finally, issues such as equipment corrosion and maintenance in the marine environment also require special consideration.

[0005] In the prior art, Chinese patent CN121177955B discloses a marine exhaust gas treatment system, specifically involving a shipborne biphase absorbent carbon capture system based on a centrifugal phase separation-coalescing-heat exchanger integrated unit. This technology combines a centrifugal phase separator, a heat exchanger, and a mixer. The lean and rich liquids flowing from the bottom of the absorption tower undergo heat exchange and centrifugal phase separation in the integrated unit. This technology aims to reduce the need for reheating, temperature rise, and centrifugal separation after the phase separator, effectively improving the efficiency of the phase separation process. Combining the phase separator and centrifugal heat exchanger effectively reduces equipment size and floor space. Chinese patent CN223586875U, through a continuous batch design and the combination of chemical absorbents, aims to solve the problems of swaying and tipping of shipborne carbon capture equipment in windy and wave environments, achieving efficient carbon dioxide capture and improving equipment stability and capture rate.

[0006] Although the aforementioned existing technologies have solved some of the problems of shipborne carbon capture to a certain extent, the following shortcomings still exist: While the supergravity technology and centrifugal technology can reduce the size of the equipment, they are technically complex, require large investments, and have high maintenance costs; While membrane separation technology has low energy consumption, its capture efficiency and product gas purity need to be improved; and although the traditional chemical absorption method is technically mature, the problems of large equipment footprint and excessively tall towers remain prominent.

[0007] Therefore, how to improve carbon capture efficiency while reducing the overall system footprint and the size and height of the core equipment tower remains a pressing technical challenge. Summary of the Invention

[0008] The technical problem to be solved by the present invention is to provide a carbon dioxide capture system and device suitable for ship emission sources, which improves carbon capture efficiency while reducing the overall system footprint and the size and height of the core equipment tower, and solves the problems of large equipment volume, excessive tower height and large footprint faced by existing shipborne carbon capture technologies.

[0009] To address the aforementioned technical problems, the present invention provides a carbon dioxide capture system suitable for ship emission sources, comprising:

[0010] An absorption subsystem is used to absorb carbon dioxide from flue gas using amine liquid. The absorption subsystem includes an absorption tower and an absorption scrubbing tower, which are arranged in sections.

[0011] A regeneration subsystem is used to heat the rich liquor to separate and regenerate the amine liquid and carbon dioxide. The regeneration subsystem includes a regeneration tower, a reboiler, and a lean liquor tank. The outlet of the reboiler is connected to the lean liquor tank, and the gas phase outlet of the lean liquor tank is connected to the regeneration tower.

[0012] The heat exchange subsystem is used to remove the heat generated by the reaction.

[0013] Furthermore, the absorption subsystem also includes a rich liquid tank, the lower part of the absorption tower is connected to the rich liquid tank, the lower part of the absorption scrubbing tower is connected to the rich liquid tank, and the upper part of the absorption tower is connected to the lower part of the absorption scrubbing tower.

[0014] Furthermore, the liquid at the bottom of the absorption tower flows into the rich liquid tank, and the liquid level at the bottom of the absorption tower is ≤1 meter. The liquid at the bottom of the absorption and washing tower flows into the rich liquid tank, and the liquid level at the bottom of the absorption and washing tower is ≤1 meter.

[0015] Furthermore, the lower parts of the absorption tower and the absorption washing tower are respectively provided with packing sections. The amine inlet of the absorption tower and the amine inlet of the absorption section of the absorption washing tower are independently connected to the amine supply pipeline. The distribution ratio of the amount of amine entering the absorption tower to the amount of amine entering the absorption section of the absorption washing tower can be dynamically adjusted.

[0016] Furthermore, the liquid at the bottom of the regeneration tower flows into the lean liquid tank, the liquid level at the bottom of the regeneration tower is ≤1 meter, the gas-liquid mixture after regeneration by the reboiler flows into the lean liquid tank, the condensate at the bottom of the regeneration tower enters the lean liquid tank, and the gas in the lean liquid tank enters the regeneration tower.

[0017] Furthermore, the gas-liquid mixture at the reboiler outlet first enters the lean liquid tank to complete gas-liquid separation. The separated gas phase is returned to the regeneration tower, and the liquid phase is returned to the absorption subsystem for recycling as lean liquid.

[0018] Furthermore, the absorption subsystem also includes an induced draft fan and a rich liquid pump, the induced draft fan being connected to the lower part of the absorption tower.

[0019] Furthermore, it also includes a washing subsystem for washing organic amine liquid in flue gas with washing water, comprising an upper part of an absorption washing tower, a washing water tank, and a washing water pump connected in sequence.

[0020] Furthermore, the heat exchange subsystem includes a washing water cooler, a lean liquid cooler, a lean-rich liquid heat exchanger, and a regeneration gas cooler.

[0021] Furthermore, it also includes an amine purification subsystem, which employs an ion exchange device to remove non-renewable salts from the amine solution.

[0022] This invention provides a carbon dioxide capture system and device suitable for ship emission sources. It adopts a modular and miniaturized design, and through a combination of technologies such as segmented design, bottom liquid level control, and reboiler outlet optimization, the overall height of the equipment is reduced and the footprint is minimized. While reducing the height of the tower equipment and the footprint, carbon capture efficiency is improved and system energy consumption is reduced. It is easy to flexibly arrange and install on ships and has good adaptability to ship operating conditions. It provides a flexible and efficient market supplement solution for the shipping industry to reduce carbon dioxide emissions and achieve carbon neutrality.

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

[0024] (1) This invention employs a segmented design for the absorption tower, arranging the packing material of the absorption tower separately in the lower sections of both the absorption tower and the absorption scrubbing tower. A lean liquid feed method is used, allowing the amine solution to contact the flue gas more fully, significantly improving the carbon dioxide absorption efficiency. Approximately 80% or more of the CO2 in the flue gas is absorbed by the lean liquid, achieving a capture rate ≥75%, and the product gas has a CO2 dry basis content greater than 99.5%. By dynamically adjusting the amine solution distribution ratio entering the absorption sections of the absorption tower and the absorption scrubbing tower, the absorption process can be optimized, ensuring high-efficiency capture performance under different operating conditions.

[0025] (2) This invention, through segmented design and the setting of independent storage tanks (rich liquid tank and lean liquid tank), controls the bottom liquid level of each tower to ≤1 meter, effectively reducing the overall height of the tower equipment. Compared with traditional integrated tower equipment, the height is reduced by 30-40%. This design maximizes space utilization while enhancing the flexibility of equipment layout, making the device suitable for ships and adapting to the installation requirements of limited space on ships.

[0026] (3) The present invention adopts a segmented design for the regeneration tower and sets up a lean liquid tank to separate the bottom liquid storage section and the packing section, which also reduces the height of the tower equipment. The liquid level at the bottom of the regeneration tower is ≤1 meter. This design further improves the space utilization and layout flexibility, and enhances the adaptability of the device to the limited space of the ship.

[0027] (4) This invention innovatively optimizes the processing path of the gas-liquid mixture at the reboiler outlet, preventing it from being directly returned to the regeneration tower. Instead, it first introduces the mixture into a lean liquid tank, where gas-liquid separation is completed. Only the separated gaseous component is sent to the regeneration tower for subsequent processes. This design effectively reduces the operating load of the regeneration tower, decreases the gas velocity and pressure drop within the tower, and alleviates the hydrodynamic load on the trays or packing. Simultaneously, the heat carried by the liquid component can be more fully recovered and utilized on the lean liquid side, reducing ineffective heat cycle losses. This helps reduce the energy consumption of amine regeneration and effectively improves the overall energy efficiency of the carbon dioxide capture system.

[0028] (5) Through modular and miniaturized system design, this invention significantly reduces the footprint of the entire carbon dioxide capture device and the overall height of the equipment, facilitating flexible layout and installation on ships. The device can operate stably within 50-110% of its rated production capacity, exhibiting good load adaptability and operational flexibility, and can meet the carbon capture requirements of ships under different operating conditions. Compared with existing technologies that use supergravity or centrifugal technologies, this invention is based on a mature chemical absorption process, with high technical reliability and lower equipment investment and maintenance costs, providing a flexible, efficient, and economical market supplement for the shipping industry to reduce carbon dioxide emissions and achieve carbon neutrality. Attached Figure Description

[0029] Figure 1 This is a schematic diagram of a preferred embodiment of the present invention.

[0030] Figure label:

[0031] 1. Exhaust fan; 2. Absorption tower; 3. Absorption and scrubbing tower; 4. Regeneration tower; 5. Scrub water pump; 6. Scrub water cooler; 7. Scrub water tank; 8. Rich solution pump; 9. Lean solution cooler; 10. Make-up pump; 11. Amine preparation tank; 12. Amine purification system; 13. Rich solution tank; 14. Rich and lean solution heat exchanger; 15. Lean solution tank; 16. Lean solution pump; 17. Reboiler; 18. Regeneration gas cooler; 19. Condensate pump; 20. Gas-liquid separator. Detailed Implementation

[0032] The present invention will be further described below with reference to specific embodiments. It should be understood that these embodiments are for illustrative purposes only and are not intended to limit the scope of the invention. Furthermore, it should be understood that after reading the teachings of this invention, those skilled in the art can make various alterations or modifications to the invention, and these equivalent forms also fall within the scope defined by the appended claims.

[0033] In the accompanying drawings, components with the same structure are indicated by the same numerical designation, and components with similar structures or functions are indicated by similar numerical designations. The dimensions and thicknesses of each component shown in the drawings are arbitrary, and the present invention does not limit the dimensions and thicknesses of each component. To make the illustrations clearer, the thickness of some components has been appropriately exaggerated in the drawings.

[0034] like Figure 1 As shown, this embodiment provides a carbon dioxide capture system and apparatus suitable for ship emission sources, including an absorption subsystem, a scrubbing subsystem, a regeneration subsystem, a heat exchange subsystem, and an amine purification subsystem. The absorption subsystem uses an organic amine solution to absorb carbon dioxide from flue gas. The regeneration subsystem heats the rich solution to separate and regenerate the amine solution and carbon dioxide, with the carbon dioxide entering downstream processes as a product. The amine solution is recycled as an absorbent. The heat exchange subsystem removes the heat generated by the reaction in the carbon dioxide capture system. The amine purification subsystem removes non-regenerable salts from the amine solution. The heat exchange and amine purification subsystems can improve the absorption rate of carbon dioxide in the amine solution.

[0035] The absorption subsystem is used to absorb carbon dioxide from flue gas using amine liquid, and includes an induced draft fan 1, an absorption tower 2, the lower part of an absorption scrubbing tower 3, a rich liquid tank 13, etc., connected in sequence; the scrubbing subsystem is used to scrub the organic amine liquid in the flue gas using scrubbing water, and includes the upper part of the absorption scrubbing tower 3, a scrubbing water tank 7, a scrubbing water pump 5, etc., connected in sequence; the regeneration subsystem is used to separate regenerated amine liquid and carbon dioxide, and includes a regeneration tower 4, a reboiler 17, a lean liquid tank 15, a gas-liquid separator 20, etc.; the heat exchange subsystem is used to remove the heat generated by the reaction in the carbon dioxide capture system; and the amine purification subsystem 12 is used to remove non-regenerable salts from the amine liquid.

[0036] The heat exchange subsystem includes a wash water cooler 6, a lean liquid cooler 9, a lean-rich liquid heat exchanger 14, and a regeneration gas cooler 18. The amine purification subsystem 12 uses ion exchange equipment to remove non-regenerable salts from the amine solution; this system is an existing complete set of equipment. All equipment is connected by pipelines.

[0037] The specific connections are as follows: the induced draft fan 1 is connected in sequence to the absorption tower 2, the absorption scrubbing tower 3, and the regeneration tower 4. The lower part of the absorption tower 2 is connected to the rich liquid tank 13, the lower part of the absorption scrubbing tower 3 is connected to the rich liquid tank 13, and the upper part of the absorption tower 2 is connected to the lower part of the absorption scrubbing tower 3; the upper part of the absorption scrubbing tower is connected in sequence to the washing water pump 5, the washing water cooler 6, and the washing water tank 7.

[0038] The regeneration tower 4 is connected to the lean liquid tank 15 and the reboiler 17. The lean liquid pump 16, the lean and rich liquid heat exchanger 14, and the lean liquid cooler 9 are connected in sequence. The outlet of the lean liquid cooler 9 is connected to the inlet of the amine purification subsystem 12, the inlet of the makeup pump 10, the amine liquid inlet of the absorption tower 2, and the amine liquid inlet of the absorption washing tower 3, respectively. The outlet of the amine purification subsystem 12 is connected to the amine mixing tank 11.

[0039] The process of capturing carbon dioxide using the above-mentioned carbon dioxide capture system includes the following steps:

[0040] (1) Absorption process

[0041] To maximize space utilization and reduce the height of the main tower equipment, the absorption tower is divided into two sections: the lower part of absorption tower 2 and absorption scrubbing tower 3. The amine liquid absorption of carbon dioxide mainly occurs in the lower part of absorption tower 2 and absorption scrubbing tower 3, while the upper part of absorption scrubbing tower 3 mainly serves to scrub the amine liquid entrained in the gas and prevent the amine from volatilizing and polluting the air.

[0042] The amine solution, mainly replenished from the amine mixing tank 11 and the reusable amine solution after desorption from the lean solution tank 15, passes through the lean solution pump 16, the lean and rich solution heat exchanger 14, and the lean solution cooler 9. A portion then passes through the amine purification subsystem 12 to remove impurities from the solution. The remaining amine solution is divided into two parts: two-thirds enter from the upper part of the absorption tower 2, and one-third enters from the lower absorption section of the absorption scrubbing tower 3. The lean solution comes into countercurrent contact with the flue gas entering the absorption tower from the lower part of the absorption tower 2. A portion of the CO2 in the flue gas is absorbed by the lean solution. Then, the flue gas enters the lower absorption section of the absorption scrubbing tower 3, where another portion of the CO2 is absorbed again by the lean solution. At this point, approximately 80% or more of the CO2 in the flue gas has been absorbed by the lean solution.

[0043] The rich liquor after CO2 absorption flows out from the bottom of absorption tower 2 and the bottom of absorption scrubbing tower 3 to the rich liquor tank 13. After being pressurized by the rich liquor pump 8, it enters the lean and rich liquor heat exchanger 14. The flue gas after CO2 absorption, carrying some rich liquor, continues to rise in absorption scrubbing tower 3 to the upper part of the tower, forming the scrubbing section. Demineralized water enters from the upper part of absorption scrubbing tower 3 and comes into countercurrent contact with the rising flue gas. After the amines in the flue gas are washed away, it is discharged from the top of the absorption scrubbing tower. The scrubbing water after amine removal is pressurized by scrubbing water pump 5 and enters scrubbing water cooler 6. After being cooled to 40°C by heat exchange with circulating cooling water, it enters the upper part of absorption scrubbing tower 3 for further scrubbing.

[0044] (2) Regeneration process

[0045] The rich amine solution from the rich solution tank 13 is pressurized by the rich solution pump 8 and sent to the lean-rich solution heat exchanger 14 for preheating, and then enters the regeneration tower 4 from the top. In the regeneration tower, the rich amine solution is heated and desorbed from CO2, thus regenerating the amine solution. The heat required for regeneration is provided by the reboiler 17, which uses steam to indirectly heat the rich amine solution.

[0046] The gas-liquid mixture at the reboiler outlet does not return directly to the regeneration tower. Instead, it first enters the lean liquid tank 15 for gas-liquid separation: the separated gas phase returns to the regeneration tower, while the liquid phase is recycled back to the absorption system as lean liquid. The CO2 gas discharged from the top of the regeneration tower is cooled to 40°C by the regeneration gas cooler 18, and then enters the gas-liquid separator 20 for preliminary gas-liquid separation. The separated gas phase is sent out as product gas, while the liquid phase is returned to the regeneration tower via the condensate pump 19, achieving condensate recovery.

[0047] Taking a 1.8-ton / hour carbon dioxide capture device for ship exhaust as an example, the normal processing capacity of the carbon dioxide capture device is approximately 25,000 Nm³ / h (wet basis), with a capture rate of ≥75%. The flue gas comes from ship exhaust, and the flue gas analysis data is shown in Table 1.

[0048] Table 1. Flue gas analysis data entering the collection device

[0049]

[0050] Under the premise of ensuring the quantity and quality of raw gas, the unit operates stably within the range of 50% to 110% of its rated production capacity, and the maximum design load of the unit is 110% of the normal capacity.

[0051] CO2 gas production: 916 Nm³ / h (dry basis), CO2 dry basis content greater than 99.5%.

[0052] Other technical specifications are shown in Table 2.

[0053] Table 2 Technical Specifications of the Collection Device

[0054]

[0055] After passing through the capture device, the ship exhaust gas can achieve a CO2 concentration of ≥99.5% (dry basis) in the carbon dioxide product gas, which reduces the height of the tower equipment (see Table 3 for details), and the equipment occupies a small area and has a flexible form.

[0056] Table 3 Tower Equipment Dimensions

[0057]

[0058] As can be seen from the above embodiments, the carbon dioxide capture system and device for ship emission sources provided in this application have the following significant advantages:

[0059] (1) Significantly reduced tower height: By segmenting the design and setting up independent storage tanks (rich liquid tank and lean liquid tank), the bottom liquid level of each tower is controlled at ≤1 meter, effectively reducing the overall height of the tower equipment. The height of the absorption tower and the absorption washing tower is 6000mm, and the height of the regeneration tower is 5000mm. Compared with the traditional integrated tower equipment, the height is reduced by 30-40%, which greatly improves the flexibility of equipment layout and the utilization rate of ship space.

[0060] (2) Significantly reduced footprint: The modular and miniaturized design significantly reduces the footprint of the entire device, making the arrangement of each piece of equipment more compact and facilitating flexible layout and installation within the limited space of a ship. Improved overall system thermal efficiency and operational economy: After gas-liquid separation is completed in the lean liquid tank, the heat carried by the liquid phase components can be more fully recovered and utilized on the lean liquid side, reducing ineffective heat cycle losses and helping to reduce amine regeneration energy consumption, effectively improving the overall energy efficiency of the carbon dioxide capture system. After the design optimization of this invention, the amine regeneration energy consumption is: steam consumption ≤ 1.2t / tCO2, a reduction of approximately 20% or more, improving the operational economy of the shipborne carbon capture device.

[0061] (3) High capture efficiency: After passing through the capture device, the ship's exhaust gas can achieve a CO2 concentration of ≥99.5% (dry basis) and a capture rate of ≥75%. While reducing the equipment height and floor space, it maintains high CO2 capture performance. More than 80% of the CO2 in the flue gas is absorbed by lean liquid, and the capture efficiency reaches the advanced level of the shipborne carbon capture industry.

[0062] The segmentation of the absorption tower and absorption scrubbing tower in this invention can be adjusted according to actual space requirements; the ratio of lean liquor allocated to the absorption tower and absorption scrubbing tower can be optimized according to specific operating conditions; the diameter and height of each tower can be adjusted accordingly based on the processing scale; the type and concentration of amine solution can be selected based on the flue gas composition; and the type and arrangement of heat exchangers can be optimized based on thermodynamic calculations.

[0063] Those skilled in the art should understand that the scope of protection of this invention is not limited to the specific embodiments described above. Based on the inventive concept, those skilled in the art can make various changes and modifications, all of which fall within the scope of protection of this invention.

Claims

1. A carbon dioxide capture system suitable for ship emission sources, characterized in that, include: An absorption subsystem is used to absorb carbon dioxide in flue gas using amine liquid. The absorption subsystem includes an absorption tower (2) and an absorption scrubbing tower (3), which are arranged in sections. The regeneration subsystem is used to heat the rich liquid to separate the regenerated amine liquid and carbon dioxide. The regeneration subsystem includes a regeneration tower (4), a reboiler (17) and a lean liquid tank (15). The outlet of the reboiler (17) is connected to the lean liquid tank (15), and the gas phase outlet of the lean liquid tank (15) is connected to the regeneration tower (4). The heat exchange subsystem is used to remove the heat generated by the reaction.

2. The carbon dioxide capture system for ship emission sources as described in claim 1, characterized in that, The absorption subsystem also includes a rich liquid tank (13), the lower part of the absorption tower (2) is connected to the rich liquid tank (13), the lower part of the absorption washing tower (3) is connected to the rich liquid tank (13), and the upper part of the absorption tower (2) is connected to the lower part of the absorption washing tower (3).

3. The carbon dioxide capture system for ship emission sources as described in claim 2, characterized in that, The liquid at the bottom of the absorption tower (2) flows into the rich liquid tank (13), and the liquid level at the bottom of the absorption tower (2) is ≤1 meter. The liquid at the bottom of the absorption and washing tower (3) flows into the rich liquid tank (13), and the liquid level at the bottom of the absorption and washing tower (3) is ≤1 meter.

4. A carbon dioxide capture system suitable for ship emission sources as described in claim 1, characterized in that, The lower parts of the absorption tower (2) and the absorption washing tower (3) are respectively provided with packing sections. The amine liquid inlet of the absorption tower (2) and the amine liquid inlet of the absorption section of the absorption washing tower (3) are respectively independently connected to the amine liquid supply pipeline. The distribution ratio of the amount of amine liquid entering the absorption tower (2) to the amount of amine liquid entering the absorption section of the absorption washing tower (3) can be dynamically adjusted.

5. The carbon dioxide capture system for ship emission sources as described in claim 1, characterized in that, The liquid at the bottom of the regeneration tower (4) flows into the lean liquid tank (15). The liquid level at the bottom of the regeneration tower (4) is ≤1 meter. The gas-liquid mixture after regeneration by the reboiler (17) flows into the lean liquid tank (15). The condensate at the bottom of the regeneration tower (4) enters the lean liquid tank (15). The gas in the lean liquid tank (15) enters the regeneration tower (4).

6. The carbon dioxide capture system for ship emission sources as described in claim 5, characterized in that, The gas-liquid mixture at the outlet of the reboiler (17) first enters the lean liquid tank (15) to complete the gas-liquid separation. The separated gas phase is returned to the regeneration tower (4), and the liquid phase is returned to the absorption system as lean liquid for recycling.

7. The carbon dioxide capture system for ship emission sources as described in claim 1, characterized in that, The absorption subsystem also includes an induced draft fan (1) and a rich liquid pump (8), wherein the induced draft fan (1) is connected to the lower part of the absorption tower (2).

8. The carbon dioxide capture system for ship emission sources as described in claim 1, characterized in that, The heat exchange subsystem includes a wash water cooler (6), a lean liquid cooler (9), a lean and rich liquid heat exchanger (14), and a regenerated gas cooler (18).

9. The carbon dioxide capture system for ship emission sources as described in any one of claims 1-8, characterized in that, It also includes a washing subsystem, which is used to wash the organic amine liquid in the flue gas with washing water, including the upper part of the absorption washing tower (3), the washing water tank (7), and the washing water pump (5) connected in sequence.

10. The carbon dioxide capture system for ship emission sources as described in any one of claims 1-8, characterized in that, It also includes an amine purification subsystem (12), which employs an ion exchange device to remove non-renewable salts from the amine solution.

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