Greenhouse gas circulating treatment system for ship power device

Abstract

The invention provides a greenhouse gas circulation treatment system for a ship power device, and belongs to the technical field of carbon circulation of ship power devices. The problems that CO2 cannot be treated in time after being captured by an existing ship carbon capture system, the size of the device is large, and desorption energy consumption is high are solved. The device comprises a ship power device, a booster fan and a carbon circulation system, an inlet of the booster fan is connected with an outlet of an exhaust pipe of the ship power device, and an outlet of the booster fan is connected with a waste gas inlet of a thermoelectric catalytic fuel synthesizer in the carbon circulation system. And the carbon circulation system is used for separating CO2 in the tail gas and converting the CO2 into fuel again. The device is mainly used for carbon circulation of ship power devices.

Description

Technical Field

[0001] The present invention belongs to the technical field of carbon cycle of ship power plants, and particularly relates to a greenhouse gas circulation treatment system for ship power plants. Background Art

[0002] Carrying out carbon reduction actions in the ship field has become the consensus of countries around the world. Among the existing carbon emission reduction measures, post-combustion carbon capture technology is the most effective means to achieve a large-scale carbon emission reduction in a short time, and it is also the fallback means to achieve the strategic goals of "carbon peak and carbon neutrality" in China.

[0003] In the current ship carbon capture field, the destination of the captured CO 2 has always been a hot topic of debate. At present, most of the treatment measures for the CO 2 captured during navigation are liquefied storage, and the liquefied CO 2 is transported to onshore tank trucks or pipelines after the ship docks. However, this method requires high supporting facilities in the port, and not all ports have the ability to unload CO 2 . If the captured CO 2 cannot be processed in time, the emission reduction effect of the carbon capture system will be greatly reduced.

[0004] In addition, since most of the current carbon capture systems use traditional organic amine solutions as absorbents, there is generally a problem of large device volume, which is even more of a challenge for the limited ship space. The large device volume not only needs to occupy the space for transporting goods originally, but on the other hand, it will also lead to changes in the original ship layout. At the same time, the traditional organic amine solution contains a large amount of water, which will cause a sharp increase in energy consumption during the desorption process, ultimately resulting in a reduction in capture efficiency. Summary of the Invention

[0005] In view of this, the present invention aims to propose a greenhouse gas circulation treatment system for ship power plants to solve the problems that the existing ship carbon capture system cannot process the captured CO 2 in time, has a large device volume, and has high desorption energy consumption.

[0006] To achieve the above object, the present invention adopts the following technical solutions:

[0007] A greenhouse gas circulation treatment system for ship power plants includes a ship power plant, a booster fan, and a carbon cycle system. The inlet of the booster fan is connected to the exhaust pipe outlet of the ship power plant, and the outlet of the booster fan is connected to the waste gas inlet of the thermoelectric catalytic fuel synthesizer in the carbon cycle system. The carbon cycle system is used to separate the CO 2 in the tail gas and re-convert it into fuel.

[0008] Furthermore, the fuel outlet of the carbon cycle system is connected to the fuel inlet of the fuel storage and mixing device, and the fuel outlet of the fuel storage and mixing device is connected to the ship power device.

[0009] Furthermore, the carbon cycle system includes a first high-efficiency absorption tower, a second high-efficiency absorption tower, a rich and lean liquid buffer tank, an integrated heat exchange center, and a strengthened desorption and stripping tower. The exhaust gas outlet of the thermoelectric catalytic fuel synthesizer is connected to the exhaust gas inlet of the strengthened desorption and stripping tower, the exhaust gas outlet of the strengthened desorption and stripping tower is connected to the exhaust gas inlet of the integrated heat exchange center, the exhaust gas outlet of the integrated heat exchange center is connected to the exhaust gas inlet of the first high-efficiency absorption tower, the exhaust gas outlet of the first high-efficiency absorption tower is connected to the exhaust gas inlet of the second high-efficiency absorption tower, and the exhaust gas outlet above the second high-efficiency absorption tower is placed in the atmosphere. The Co 2 outlet at the top of the strengthened desorption and stripping tower is connected to the material inlet of the thermoelectric catalytic fuel synthesizer. The rich and lean liquid buffer tank is provided with a rich liquid area and a lean liquid area. The absorbent outlet of the rich liquid area is connected to the rich liquid inlet of the integrated heat exchange center through a rich liquid transfer pump. The rich liquid outlet of the integrated heat exchange center is connected to the absorbent inlet of the strengthened desorption and stripping tower. The absorbent outlet of the strengthened desorption and stripping tower is connected to the lean liquid inlet of the integrated heat exchange center. The lean liquid outlet of the integrated heat exchange center is connected to the inlet of the lean liquid area. The outlet of the lean liquid area is connected to the absorbent inlet of the first high-efficiency absorption tower through a lean liquid transfer pump. The absorbent outlet of the first high-efficiency absorption tower is connected to the absorbent inlet of the second high-efficiency absorption tower through an inter-stage cooling pump. The absorbent outlet of the second high-efficiency absorption tower is connected to the rich liquid inlet of the rich liquid area through a rich liquid supply pump.

[0010] Furthermore, an exhaust gas heat exchanger is provided at the bottom inside the strengthened desorption and stripping tower.

[0011] Furthermore, the integrated heat exchange center includes an exhaust gas cooling module, a lean liquid cooling module, an exhaust gas heat exchange module, and a rich and lean liquid heat exchange module. The exhaust gas outlet of the exhaust gas heat exchange module is connected to the exhaust gas inlet of the exhaust gas cooling module. The rich liquid outlet of the exhaust gas heat exchange module is connected to the rich liquid inlet of the rich and lean liquid heat exchange module. The lean liquid outlet of the rich and lean liquid heat exchange module is connected to the lean liquid inlet of the lean liquid cooling module. The cooling water outlet of the lean liquid cooling module is connected to the cooling water inlet of the exhaust gas cooling module.

[0012] Furthermore, the temperature field inside the integrated heat exchange center is divided into a high-temperature area, a medium-temperature area, and a low-temperature area. The exhaust gas cooling module, the exhaust gas heat exchange module, and the pipelines form the high-temperature area. The rich and lean liquid heat exchange module and the pipelines form the medium-temperature area. The lean liquid cooling module and the pipelines form the low-temperature area.

[0013] Furthermore, heat insulation materials are filled between the high-temperature area, the medium-temperature area, and the low-temperature area inside the integrated heat exchange center.

[0014] Furthermore, the thermoelectric catalytic fuel synthesizer is loaded with a fuel synthesis catalyst.

[0015] Furthermore, the carbon cycle system uses a separation method to separate CO from the exhaust gas. 2 The absorbent is CO 2 Capture absorbent.

[0016] Furthermore, the CO 2 The capture absorbent component is composed of chain or cyclic diamine containing primary amine and tertiary amine groups in the molecule, organic solvent N-methylpyrrolidone and water, with the mass concentration of diamine being 38%-42%, the mass concentration of organic solvent being 58%-62% and the mass concentration of water being 0%-4%.

[0017] Compared with the prior art, the present invention has the following beneficial effects:

[0018] 1. The carbon cycle system of the present invention is provided with a post-combustion carbon capture device and a thermoelectric catalytic fuel synthesizer, and the outlet of the desorption tower is directly connected to the thermoelectric catalytic fuel synthesizer, without the need to add other substances or to treat CO 2 Mixed gas is dried directly with CO 2 and H 2 O catalytic conversion to synthesize fuel has three advantages: first, it saves the traditional carbon capture device to CO 2 The process of drying, liquefying, and compressing the mixed gas effectively reduces the size of the device; secondly, 2 The mixed gas directly generates fuel under the catalytic action, completing the capture of CO 2 The disposal work can be done by the port, reducing the dependence on the relevant disposal equipment; thirdly, the generated fuel can be burned again, which reduces the fuel consumption rate from the perspective of the whole process and improves the economic efficiency of shipping;

[0019] 2. The present invention effectively reduces the tower height and thus the device volume by setting a double-stage high-efficiency absorption tower in the carbon circulation system without sacrificing the removal efficiency;

[0020] 3. The present invention modularizes the heat exchange system in the carbon cycle system, integrates the original heat exchanger into the heat exchange center, and sets temperature zones and performs heat insulation treatment inside the heat exchange center to further improve the heat exchange efficiency. At the same time, it can also effectively reduce the increase in system volume caused by the dispersion of devices;

[0021] 4. The present invention further enhances the absorption effect, reduces the desorption energy consumption, and extends the service life by adopting a new absorbent in the carbon cycle system. The diamine in the water-lean absorbent has excellent absorption and desorption properties, and the organic solvent N-methylpyrrolidone can also play a role in physical absorption. Meanwhile, under the condition of a large amount of organic solvent, the diamine is more likely to decompose by heat to release CO 2 and can play a role in physical absorption. At the same time, under the condition of a large amount of organic solvent, the diamine is more likely to decompose by heat to release CO 2 . Through the dual promotion of the diamine and the organic solvent, not only can the desorption energy consumption be effectively reduced, but also the separation efficiency can be improved, the volume of the device can be further reduced, and the organic solvent is less likely to degrade, so the service life of the absorbent can be effectively extended. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] The drawings constituting a part of the present invention are used to provide a further understanding of the present invention. The schematic embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation to the present invention. In the drawings:

[0023] Figure 1 is a schematic diagram of a greenhouse gas circulation treatment system for a ship power plant according to the present invention;

[0024] Figure 2 is a schematic diagram of the integrated heat exchange center according to the present invention.

[0025] In the drawings:

[0026] 1 - ship power plant, 2 - booster fan, 3 - carbon cycle system, 4 - fuel storage and mixing device, 5 - first high-efficiency absorption tower, 6 - inter-stage cooling pump, 7 - second high-efficiency absorption tower, 8 - rich liquid supply pump, 9 - rich and lean liquid buffer tank, 10 - lean liquid transfer pump, 11 - rich liquid transfer pump, 12 - integrated heat exchange center, 13 - enhanced desorption stripper tower, 14 - thermoelectric catalytic fuel synthesizer, 15 - exhaust gas cooling module, 16 - lean liquid cooling module, 17 - exhaust gas heat exchange module, 18 - rich and lean liquid heat exchange module. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0027] The technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. It should be noted that, without conflict, the embodiments and features in the embodiments of the present invention can be combined with each other. The described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments.

[0028] Detailed Embodiment 1: Refer to Figure 1-2Description of this embodiment, a greenhouse gas recycling treatment system for a ship power plant, characterized in that: it includes a ship power plant 1, a booster fan 2, and a carbon recycling system 3. The inlet of the booster fan 2 is connected to the exhaust pipe outlet of the ship power plant 1, and the outlet of the booster fan 2 is connected to the waste gas inlet of the thermoelectric catalytic fuel synthesizer 14 in the carbon recycling system 3. The carbon recycling system 3 is used to separate the CO 2 in the tail gas and reconvert it into fuel. The fuel outlet of the carbon recycling system 3 is connected to the fuel inlet of the fuel storage and mixing device 4, and the fuel outlet of the fuel storage and mixing device 4 is connected to the ship power plant 1.

[0029] The carbon recycling system 3 includes a first high-efficiency absorption tower 5, a second high-efficiency absorption tower 7, a rich and lean liquid buffer tank 9, an integrated heat exchange center 12, and a strengthened desorption and stripping tower 13. The waste gas outlet of the thermoelectric catalytic fuel synthesizer 14 is connected to the waste gas inlet of the strengthened desorption and stripping tower 13. The waste gas outlet of the strengthened desorption and stripping tower 13 is connected to the waste gas inlet of the integrated heat exchange center 12. The waste gas outlet of the integrated heat exchange center 12 is connected to the waste gas inlet of the first high-efficiency absorption tower 5. The waste gas outlet of the first high-efficiency absorption tower 5 is connected to the waste gas inlet of the second high-efficiency absorption tower 7. The waste gas outlet above the second high-efficiency absorption tower 7 is placed in the atmosphere. The Co 2 outlet at the top of the strengthened desorption and stripping tower 13 is connected to the material inlet of the thermoelectric catalytic fuel synthesizer 14. The rich and lean liquid buffer tank 9 is provided with a rich liquid area and a lean liquid area. The absorbent outlet of the rich liquid area is connected to the rich liquid inlet of the integrated heat exchange center 12 through a rich liquid transfer pump 11. The rich liquid outlet of the integrated heat exchange center 12 is connected to the absorbent inlet of the strengthened desorption and stripping tower 13. The absorbent outlet of the strengthened desorption and stripping tower 13 is connected to the lean liquid inlet of the integrated heat exchange center 12. The lean liquid outlet of the integrated heat exchange center 12 is connected to the lean liquid area inlet. The lean liquid area outlet is connected to the absorbent inlet of the first high-efficiency absorption tower 5 through a lean liquid transfer pump 10. The absorbent outlet of the first high-efficiency absorption tower 5 is connected to the absorbent inlet of the second high-efficiency absorption tower 7 through an inter-stage cooling pump 6. The absorbent outlet of the second high-efficiency absorption tower 7 is connected to the rich liquid inlet of the rich liquid area through a rich liquid supply pump 8.

[0030] The integrated heat exchange center 12 includes a waste gas cooling module 15, a lean liquid cooling module 16, a waste gas heat exchange module 17, and a rich and lean liquid heat exchange module 18. The waste gas outlet of the waste gas heat exchange module 17 is connected to the waste gas inlet of the waste gas cooling module 15. The rich liquid outlet of the waste gas heat exchange module 17 is connected to the rich liquid inlet of the rich and lean liquid heat exchange module 18. The lean liquid outlet of the rich and lean liquid heat exchange module 18 is connected to the lean liquid inlet of the lean liquid cooling module 16. The cooling water outlet of the lean liquid cooling module 16 is connected to the cooling water inlet of the waste gas cooling module 15.

[0031] During use, the exhaust gas generated during the operation of the ship power plant 1 enters the carbon cycle system 3 after being pressurized by the booster fan 2. In the carbon cycle system 3, the exhaust gas first enters from the exhaust gas inlet of the thermoelectric catalytic fuel synthesizer 14, provides energy for the catalytic reaction of the fuel in the thermoelectric catalytic fuel synthesizer 14, and then discharges from the exhaust gas outlet of the thermoelectric catalytic fuel synthesizer 14. The exhaust gas after the initial energy utilization enters from the exhaust gas inlet of the exhaust gas heat exchanger of the enhanced desorption and stripping tower 13, provides energy for the desorption process of the absorbent in the enhanced desorption and stripping tower 13, and then discharges from the exhaust gas outlet of the exhaust gas heat exchanger of the enhanced desorption and stripping tower 13, enters the integrated heat exchange center 12 from the exhaust gas inlet of the integrated heat exchange center 12. In the integrated heat exchange center 12, the exhaust gas first enters from the exhaust gas inlet of the exhaust gas heat exchange module 17, provides energy for heating the rich absorbent solution, and then discharges from the exhaust gas outlet of the exhaust gas heat exchange module 17, enters the exhaust gas cooling module 15 from the exhaust gas inlet. In the exhaust gas cooling module 15, it is cooled by cooling water and reduced to about 40 °C, and then discharges from the exhaust gas outlet of the exhaust gas cooling module 15, enters the first high-efficiency absorption tower 5 from the exhaust gas inlet at the lower side of the first high-efficiency absorption tower 5, and contacts and reacts with the absorbent sprayed from above from bottom to top, removing the CO in the exhaust gas 2 for the first time, and then discharges from the exhaust gas outlet at the top of the first high-efficiency absorption tower 5, enters the exhaust gas inlet at the lower side of the second high-efficiency absorption tower 7, enters the interior of the second high-efficiency absorption tower 7. The exhaust gas contacts and reacts with the absorbent sprayed from above from bottom to top inside the second high-efficiency absorption tower 7 to complete the second contact and reaction, further removing CO 2 , and finally discharges from the exhaust gas outlet above the second absorption tower 7 out of the system.

[0032] In the carbon cycle system 3, the absorbent is first stored in the lean liquid area of the circulation buffer tank 9, flows out from the bottom of the lean liquid area of the circulation buffer tank 9, is transported by the lean liquid transfer pump 10, and enters the first high-efficiency absorption tower from the absorbent inlet at the upper side of the first high-efficiency absorption tower 5, sprays from top to bottom, and fully contacts and reacts with the exhaust gas from below to absorb CO in the exhaust gas 2 , and then discharges from the absorbent outlet below the first high-efficiency absorption tower 5, and continues to enter the absorbent inlet at the upper side of the second high-efficiency absorption tower 7 through the transportation of the inter-stage cooling pump 6. Since the pipelines before and after the inter-stage cooling pump 6 are not insulated, the absorbent will be physically cooled when flowing through the pipeline, reducing the temperature of the absorbent. Since the heat released by the reaction of the tail gas and the absorbent is not large, there is no need to add an additional cooling module, and the volume of the device can be further reduced. The absorbent sprays into the second high-efficiency absorption tower 7 from the absorbent inlet at the top side of the second high-efficiency absorption tower 7, makes secondary contact with the exhaust gas from below, and further removes CO in the exhaust gas 2, after completing the absorption task, the absorbent flows out from the absorbent outlet below the second high-efficiency absorption tower 7, is transported by the rich liquid supply pump 8 to the rich liquid area in the circulation buffer tank 9. There is an absorbent outlet provided below the rich liquid area of the circulation buffer tank 7. The absorbent enters the integrated heat exchange center 12 through the absorbent inlet of the integrated heat exchange center 12 by the rich liquid transfer pump 11. In the integrated heat exchange center 12, the absorbent first enters from the absorbent inlet of the waste gas heat exchange module 17, and fully utilizes the waste heat of the waste gas in the waste gas heat exchange module to achieve preliminary temperature rise. After completing the preliminary temperature rise, the absorbent leaves from the absorbent outlet of the waste gas heat exchange module 17 and enters the rich and lean liquid heat exchange module 18 through the rich liquid inlet of the rich and lean liquid heat exchange module 18. In the rich and lean liquid heat exchange module 18, it exchanges heat with the high-temperature lean liquid to achieve secondary temperature rise, so that the system heat is fully utilized. Subsequently, the absorbent leaves the integrated heat exchange center 12 from the rich liquid outlet of the rich and lean liquid heat exchange module 18. At this time, the absorbent that has undergone secondary temperature rise has initially met the conditions for releasing CO 2 . The absorbent that leaves from the rich liquid outlet of the integrated heat exchange center 12 enters the enhanced desorption stripping tower 13 through the absorbent inlet above the side of the enhanced desorption stripping tower 13. Inside the enhanced desorption stripping tower 13, it conducts full heat exchange with the mixed steam evaporating from the bottom. At this time, the absorbent that has completed three temperature rises has been able to release a part of the absorbent inside it. After the absorbent falls onto the outer surface of the waste gas heat exchanger inside the enhanced desorption stripping tower 13, the waste gas heat exchanger heats the absorbent for the fourth time. At this time, a large amount of CO can be released from the absorbent 2 . After completing the desorption reaction and releasing all the CO 2 , the absorbent flows out from the absorbent outlet below the enhanced desorption stripping tower 13 and returns to the lean liquid inlet of the integrated heat exchange center 12, enters the integrated heat exchange center 12 through the lean liquid inlet. After the absorbent enters the integrated heat exchange center 12, it enters the rich and lean liquid heat exchange module 18 through the lean liquid inlet of the rich and lean liquid heat exchange module 18. At this time, the temperature of the absorbent is about 110°C, and it can transfer energy to the lower-temperature absorbent rich liquid. After completing the heat exchange, the absorbent flows out from the lean liquid outlet of the rich and lean liquid heat exchange module 18, enters the lean liquid cooling module 15 through the lean liquid inlet of the lean liquid cooling module 15, and conducts full heat exchange with the cooling water here, reduces the temperature to 40°C, and then leaves from the lean liquid outlet of the lean liquid cooling module 15 and returns to the lean liquid area. Thus, the absorbent circulation is closed-loop.

[0033] Among them, the cooling water enters the integrated heat exchange center 12 from the cooling water inlet of the integrated heat exchange center 12, is divided and flows to the waste gas cooling module 15 and the lean liquid cooling module 16 respectively. It cools the waste gas in the waste gas cooling module 15 and cools the lean liquid in the lean liquid cooling module 16. After completing the cooling, the cooling water leaves the integrated heat exchange center 12 through the cooling water outlet of the integrated heat exchange center 12, CO2 The mixed gas exits from the mixed gas outlet at the top of the enhanced desorption stripper 13 and enters the thermoelectric catalytic fuel synthesizer 14. Inside the thermoelectric catalytic fuel synthesizer 14, CO 2 The mixed gas completes catalytic reforming under the action of a catalyst to synthesize fuel. The heat source is the energy in the waste gas. In the case of insufficient energy supply, the ship's auxiliary engine will generate electricity to supply energy for the catalytic reaction. After synthesis, the fuel exits from the material outlet on the side of the thermoelectric catalytic fuel synthesizer and enters the fuel storage and mixing device 4, and finally is transported to the ship power plant 1 for combustion. Thus, the carbon cycle part of the ship carbon cycle system completes a closed loop.

[0034] Specific Embodiment 2: Refer to Figure 1-2 To describe this embodiment, the temperature field in the integrated heat exchange center 12 is divided into a high-temperature zone, a medium-temperature zone, and a low-temperature zone. The waste gas cooling module 15, the waste gas heat exchange module 17, and the pipelines form the high-temperature zone. The rich and lean liquid heat exchange module 18 and the pipelines form the medium-temperature zone. The lean liquid cooling module 16 and the pipelines form the low-temperature zone. Heat insulation materials are filled between the high-temperature zone, the medium-temperature zone, and the low-temperature zone in the integrated heat exchange center 12 to further improve the heat exchange efficiency of the integrated heat exchange center 12.

[0035] Specific Embodiment 3: Refer to Figure 1-2 To describe this embodiment, the thermoelectric catalytic fuel synthesizer 14 is loaded with a fuel synthesis catalyst, and CO 2 The mixed gas completes catalytic reforming under the action of a catalyst to synthesize fuel. The energy supply method of the thermoelectric catalytic fuel synthesizer 14 is waste gas heat exchange. The waste gas flows through the waste gas side of the thermoelectric catalytic fuel synthesizer 14, only providing heat and not directly contacting the CO 2 mixed gas and the catalyst. When the waste gas heat exchange energy supply is insufficient, the ship's auxiliary engine will generate electricity to provide energy.

[0036] Specific Embodiment 4: Refer to Figure 1-2 To describe this embodiment, the absorbent used in the carbon cycle system 3 to separate CO 2 from the waste gas is a high-efficiency, long-life, low-energy-consumption CO 2 capture absorbent, which is composed of a chain or cyclic diamine containing primary amine and tertiary amine groups in the molecule, an organic solvent N-methylpyrrolidone, and water. The ratio is that the mass concentration of diamine is 38%-42%, the mass concentration of organic solvent is 58%-62%, and the mass concentration of water is 0%-4%.

[0037] The specific embodiments of the present invention disclosed above are only used to help illustrate the present invention. The specific embodiments do not describe all the details in detail, nor do they limit the invention to the specific embodiments described. According to the content of this specification, many modifications and variations can be made. These embodiments are selected and specifically described in this specification in order to better explain the principles and practical applications of the present invention, so that those skilled in the art can well understand and utilize the present invention.

Claims

1. A greenhouse gas circulation treatment system for a ship power plant, characterized in that: The invention comprises a ship power device (1), a booster fan (2) and a carbon circulation system (3), wherein the inlet of the booster fan (2) is connected to the outlet of the exhaust pipe of the ship power device (1), and the outlet of the booster fan (2) is connected to the exhaust gas inlet of a thermoelectric catalytic fuel synthesizer (14) in the carbon circulation system (3). The carbon circulation system (3) is used to separate CO2 in the exhaust gas and reconvert it into fuel.

2. A greenhouse gas circulation treatment system for a ship power plant according to claim 1, characterized in that: The fuel outlet of the carbon circulation system (3) is connected to the fuel inlet of the fuel storage and mixing device (4), and the fuel outlet of the fuel storage and mixing device (4) is connected to the ship power device (1).

3. A greenhouse gas circulation treatment system for a ship power plant according to claim 1, characterized in that: The carbon circulation system (3) comprises a first high-efficiency absorption tower (5), a second high-efficiency absorption tower (7), a lean-rich liquid buffer cabinet (9), an integrated heat exchange center (12) and an enhanced desorption stripping tower (13); the exhaust gas outlet of the thermoelectric catalytic fuel synthesizer (14) is connected to the exhaust gas inlet of the enhanced desorption stripping tower (13); the exhaust gas outlet of the enhanced desorption stripping tower (13) is connected to the exhaust gas inlet of the integrated heat exchange center (12); the exhaust gas outlet of the integrated heat exchange center (12) is connected to the exhaust gas inlet of the first high-efficiency absorption tower (5); the exhaust gas outlet of the first high-efficiency absorption tower (5) is connected to the exhaust gas inlet of the second high-efficiency absorption tower (7); the exhaust gas outlet above the second high-efficiency absorption tower (7) is placed in the atmosphere; the CO2 outlet at the top of the enhanced desorption stripping tower (13) is connected to the material inlet of the thermoelectric catalytic fuel synthesizer (14); A rich liquid zone and a lean liquid zone are arranged in the lean and rich liquid buffer tank (9); the absorbent outlet of the rich liquid zone is connected to the rich liquid inlet of the integrated heat exchange center (12) through a rich liquid delivery pump (11); the rich liquid outlet of the integrated heat exchange center (12) is connected to the absorbent inlet of the enhanced desorption stripping tower (13); the absorbent outlet of the enhanced desorption stripping tower (13) is connected to the lean liquid inlet of the integrated heat exchange center (12); the lean liquid outlet of the integrated heat exchange center (12) is connected to the lean liquid zone inlet; the lean liquid zone outlet is connected to the absorbent inlet of the first high-efficiency absorption tower (5) through a lean liquid delivery pump (10); the absorbent outlet of the first high-efficiency absorption tower (5) is connected to the absorbent inlet of the second high-efficiency absorption tower (7) through an interstage cooling pump (6); and the absorbent outlet of the second high-efficiency absorption tower (7) is connected to the rich liquid inlet of the rich liquid zone through a rich liquid supply pump (8).

4. A greenhouse gas circulation treatment system for a ship power plant according to claim 3, characterized in that: A waste gas heat exchanger is arranged at the bottom of the enhanced desorption stripping tower (13).

5. A greenhouse gas circulation treatment system for a ship power plant according to claim 3, characterized in that: The integrated heat exchange center (12) comprises an exhaust gas cooling module (15), a lean liquid cooling module (16), an exhaust gas heat exchange module (17) and a lean-rich liquid heat exchange module (18); the exhaust gas outlet of the exhaust gas heat exchange module (17) is connected to the exhaust gas inlet of the exhaust gas cooling module (15); the rich liquid outlet of the exhaust gas heat exchange module (17) is connected to the rich liquid inlet of the lean-rich liquid heat exchange module (18); the lean liquid outlet of the lean-rich liquid heat exchange module (18) is connected to the lean liquid inlet of the lean liquid cooling module (16); and the cooling water outlet of the lean liquid cooling module (16) is connected to the cooling water inlet of the exhaust gas cooling module (15).

6. A greenhouse gas circulation treatment system for a ship power plant according to claim 5, characterized in that: The temperature field in the integrated heat exchange center (12) is divided into a high temperature zone, a medium temperature zone and a low temperature zone. The exhaust gas cooling module (15), the exhaust gas heat exchange module (17) and the pipeline form the high temperature zone, the lean-rich liquid heat exchange module (18) and the pipeline form the medium temperature zone, and the lean liquid cooling module (16) and the pipeline form the low temperature zone.

7. A greenhouse gas circulation treatment system for a ship power plant according to claim 6, characterized in that: The high temperature zone, the medium temperature zone and the low temperature zone in the integrated heat exchange center (12) are filled with heat insulation materials.

8. A greenhouse gas circulation treatment system for a ship power plant according to claim 3, characterized in that: The thermoelectric catalytic fuel synthesizer (14) is loaded with a fuel synthesis catalyst.

9. A greenhouse gas circulation treatment system for a ship power plant according to claim 3, characterized in that: The absorbent used in the carbon cycle system (3) to separate CO2 from the exhaust gas is a CO2 capture absorbent.

10. A greenhouse gas circulation treatment system for a ship power plant according to claim 9, characterized in that: The CO2 capture absorbent component is composed of a chain or cyclic diamine containing primary amine and tertiary amine groups in the molecule, an organic solvent N-methylpyrrolidone and water, with the mass concentration of the diamine being 38%-42%, the mass concentration of the organic solvent being 58%-62%, and the mass concentration of water being 0%-4%.

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