A ship flue gas denitrification, desulfurization and decarbonization system

Abstract

The present application relates to a ship flue gas denitration, desulfurization and decarbonization system, which includes a denitration mechanism, a desulfurization mechanism, a decarbonization mechanism and a carbon dioxide preparation mechanism, wherein the flue gas input end of the denitration mechanism is used to receive ship flue gas, the flue gas output end of the denitration mechanism is connected to the flue gas input end of the desulfurization mechanism, the flue gas output end of the desulfurization mechanism is connected to the flue gas input end of the decarbonization mechanism, the decarbonization mechanism is provided with a solid amine to be reacted for reacting with the desulfurized flue gas to generate decarbonized flue gas, the solid amine to be reacted generates saturated solid amine after reacting with the desulfurized flue gas, the carbon dioxide preparation mechanism is used to heat the saturated solid amine to generate carbon dioxide and the solid amine to be reacted, and the solid amine output end of the carbon dioxide preparation mechanism transports the solid amine to be reacted to the decarbonization mechanism. By optimizing the recycling of solid amine, the space occupation and equipment size requirements are reduced, and the efficiency and compactness of ship flue gas treatment are improved.

Description

Technical Field

[0001] The invention relates to the technical field of ship flue gas denitration, desulfurization and decarbonization, and in particular to a ship flue gas denitration, desulfurization and decarbonization system. Background Art

[0002] At present, traditional ship flue gas treatment systems usually use seawater desulfurization and alcohol amine solution decarbonization. Seawater desulfurization uses the alkaline components in seawater to react with sulfur dioxide in flue gas to generate harmless sulfates, thereby effectively removing sulfur dioxide in flue gas. Alcohol amine solution is also widely used in decarbonization. Alcohol amine solution reacts with carbon dioxide in flue gas to form a reversible amine-carbon dioxide complex, thereby effectively removing carbon dioxide in flue gas.

[0003] However, since the chemical reaction rate of the alcohol amine solution is affected by the gas velocity, in order to improve the decarbonization efficiency, it is usually necessary to reduce the flue gas velocity, which often leads to the decarbonization tower being too large and unable to meet the application scenario of limited space such as ships. In the design process of ships, especially when designing the flue gas treatment system, due to the limitations of space, weight and installation location, it is usually necessary to avoid using equipment that is too large or takes up too much space. Summary of the invention

[0004] In order to solve the problem that the flue gas treatment equipment in the traditional ship flue gas treatment system is too large due to the use of alcohol amine solution, the present application provides a ship flue gas denitrification, desulfurization and decarbonization system.

[0005] A ship flue gas denitration, desulfurization and decarbonization system, the ship flue gas denitration, desulfurization and decarbonization system comprising a denitration mechanism, a desulfurization mechanism, a decarbonization mechanism and a carbon dioxide preparation mechanism, the flue gas input end of the denitration mechanism is used to receive ship flue gas, the denitration mechanism is provided with a reducing agent for reacting with the ship flue gas to generate denitrified flue gas, the flue gas output end of the denitration mechanism is connected to the flue gas input end of the desulfurization mechanism, the desulfurization mechanism is provided with seawater for reacting with the denitrified flue gas to generate desulfurized flue gas, the flue gas output end of the desulfurization mechanism is connected to the flue gas input end of the decarbonization mechanism, the decarbonization mechanism is provided with a reducing agent for reacting with the desulfurized flue gas to generate desulfurized flue gas, The solid amine to be reacted should be used to generate decarbonized flue gas. The flue gas output end of the decarbonization mechanism discharges decarbonized flue gas. The solid amine to be reacted generates saturated solid amine after reacting with the desulfurized flue gas. The solid amine output end of the decarbonization mechanism transports the saturated solid amine to the solid amine input end of the carbon dioxide production mechanism. The carbon dioxide production mechanism is used to heat the saturated solid amine to generate carbon dioxide and solid amine to be reacted. The carbon dioxide output end of the carbon dioxide production mechanism outputs carbon dioxide. The solid amine output end of the carbon dioxide production mechanism transports the solid amine to be reacted into the decarbonization mechanism to react with the desulfurized flue gas again.

[0006] By adopting the above technical solution, the functions of denitration, desulfurization and decarbonization are integrated, and the multi-stage reaction of solid amine and flue gas and the recycling technology of solid amine are adopted. Specifically, the denitration mechanism removes nitrogen oxides by reacting with the reducing agent, the desulfurization mechanism uses seawater to remove sulfur dioxide, and the decarbonization mechanism uses solid amine to remove carbon dioxide and generate saturated solid amine, and then the solid amine is heated and recovered by the carbon dioxide preparation mechanism, carbon dioxide is released and the solid amine is regenerated. This system can not only effectively denitrify, desulfurize and decarbonize, but also reduce the space occupied and equipment size requirements by optimizing the recycling of solid amine, and improve the efficiency and compactness of ship flue gas treatment.

[0007] Preferably, the denitrification mechanism includes a denitrification tower, in which a denitrification filler layer is provided, a flue gas input end of the denitrification tower is used to receive ship flue gas and is located below the denitrification filler layer, a reducing agent input end of the denitrification tower is used to receive the reducing agent and is located above the denitrification filler layer, the reducing agent flows from top to bottom based on the filler surface of the denitrification filler layer to react with the ship flue gas passing through the denitrification filler layer from bottom to top, thereby generating the denitrification flue gas, which is transported to the desulfurization mechanism through the flue gas output end of the denitrification tower.

[0008] By adopting the above technical solution, the contact area between the flue gas and the reducing agent can be effectively increased, and the efficiency of the denitration reaction can be improved. By allowing the reducing agent to flow from top to bottom based on the surface of the filler and fully reacting with the flue gas passing through the filler layer from bottom to top, it can promote the efficient removal of nitrogen oxides in the flue gas, reduce harmful gas emissions, and thus improve the denitration effect of the ship's flue gas treatment system. This design can ensure the treatment efficiency of the denitration tower, reduce the concentration of NOx in the flue gas, meet environmental emission standards, and optimize the spatial layout and equipment configuration of the system.

[0009] Preferably, the denitrification mechanism also includes a denitrification liquid level sensor assembly, a denitrification regulating valve and a denitrification circulation pump. A denitrification conical component is provided below the flue gas input end of the denitrification tower. The bottom of the denitrification conical component is connected to one end of the denitrification regulating valve, and the other end of the denitrification regulating valve is used for discharging into the sea. The first conducting end of the denitrification liquid level sensor assembly is located between the top of the denitrification conical component and the bottom of the denitrification packing layer, and the second conducting end of the denitrification liquid level sensor assembly is located at the bottom of the denitrification conical component. The denitrification liquid level sensor assembly is electrically connected to the denitrification regulating valve, one end of the denitrification circulation pump is connected to the bottom of the denitrification conical component, and the other end of the denitrification circulation pump is located above the denitrification packing layer.

[0010] By adopting the above technical solution, accurate liquid level control and flow regulation of reducing agent can be achieved inside the denitration tower. The use of liquid level sensor and regulating valve can monitor the liquid level of the denitration tower in real time, avoid excessive or insufficient reducing agent, and thus ensure the stability and efficiency of the denitration reaction. By using a denitration circulation pump, the uniform distribution of reducing agent in the tower can be ensured, and the appropriate fluidity can be maintained, which can further optimize the reaction process and improve the reliability and processing capacity of the denitration system.

[0011] Preferably, the desulfurization mechanism includes a desulfurization tower, a desulfurization regulating valve and a desulfurization liquid level sensor assembly. A desulfurization packing layer is provided in the desulfurization tower. The flue gas input end of the desulfurization tower is used to receive denitrification flue gas and is located below the desulfurization packing layer. The seawater input end of the desulfurization tower is used to receive seawater and is located above the desulfurization packing layer. The seawater output end of the desulfurization tower is connected to one end of the desulfurization regulating valve, and the other end of the desulfurization regulating valve is used to discharge into the sea. The first conducting end of the desulfurization liquid level sensor assembly is located at the top of the desulfurization packing layer, and the second conducting end of the desulfurization liquid level sensor assembly is located at the bottom of the desulfurization tower. The desulfurization liquid level sensor assembly is electrically connected to the desulfurization regulating valve. The denitrification flue gas forms bubbles flowing from bottom to top in the seawater to react with seawater, thereby generating the desulfurized flue gas, and the desulfurized flue gas is transported to the decarbonization mechanism through the flue gas output end of the desulfurization tower.

[0012] By adopting the above technical solution, the flow of seawater can be effectively controlled and the seawater level in the desulfurization tower can be monitored in real time to ensure the continuous stability of the desulfurization reaction. By adjusting the seawater flow and level, the absorption process of sulfur dioxide can be optimized to ensure the effective removal of sulfur dioxide in the flue gas. In addition, the contact between seawater and flue gas optimizes the reaction efficiency. Through the bottom-up bubble flow, the surface area of ​​the gas-liquid reaction is enhanced, the desulfurization capacity of the desulfurization tower is significantly improved, and the emission of sulfur dioxide is reduced, which meets the environmental emission requirements.

[0013] Preferably, the decarbonization mechanism includes a dehydration tower, a decarbonization tower and a dust filter tower, the flue gas input end of the dehydration tower is used to receive the desulfurized flue gas, the dehydration tower is used to dehydrate the desulfurized flue gas to generate dehydrated flue gas, the flue gas output end of the dehydration tower is connected to the flue gas input end of the decarbonization tower for receiving the dehydrated flue gas, the decarbonization tower is provided with a bed layer for filling the solid amine to be reacted, the flue gas input end of the decarbonization tower is located below the bed layer, the dehydrated flue gas flows from bottom to top, thereby passing through the bed layer to react with the solid amine to be reacted to generate the decarbonized flue gas, and is transported to the dust filter tower through the flue gas output end of the decarbonization tower for dust removal, and then the decarbonized flue gas after dust removal is discharged into the atmosphere through the flue gas output end of the dust filter tower.

[0014] By adopting the above technical solution, it is possible to effectively remove moisture from flue gas, reduce flue gas humidity, and prevent moisture from affecting the subsequent decarbonization process. The dehydration tower can maintain appropriate humidity when the flue gas enters the decarbonization tower through dehydration treatment, thereby improving the reaction efficiency of solid amines in the decarbonization process. At the same time, the dust filter tower can remove dust impurities in the flue gas, protect subsequent equipment from clogging, improve the stability and long-term operation capacity of the decarbonization system, and ensure that the decarbonized flue gas meets the emission standards.

[0015] Preferably, the decarbonization mechanism also includes a temperature control component, which includes a water-cooling control valve and a plurality of water-cooling coils, wherein the plurality of water-cooling coils are sequentially arranged in the bed layer from top to bottom, and one end of each of the water-cooling coils is connected to one end of the water-cooling control valve, and the other end of the water-cooling control valve is used to discharge seawater, and the other end of the water-cooling control valve is used to receive seawater.

[0016] By adopting the above technical solution, the temperature in the decarbonization tower can be effectively controlled to avoid the effect of too high or too low temperature on the efficiency of the decarbonization reaction. The water cooling system can stabilize the temperature in the decarbonization tower by adjusting the water flow of the water cooling coil, ensuring that the reaction process of the solid amine is always in the optimal reaction temperature range, thereby improving the removal efficiency of carbon dioxide. This design can reduce energy waste while ensuring the reaction rate, improve the energy efficiency of the overall system, and optimize the ship flue gas treatment process.

[0017] Preferably, the carbon dioxide preparation mechanism includes a transition conveying screw, a heating and decomposing conveying screw, a decomposing gas dust removing tower and a dryer. The solid amine input end of the transition conveying screw is connected to the bottom of the decarbonization tower for receiving the saturated solid amine, and the saturated solid amine is conveyed to the heating and decomposing conveying screw through the solid amine output end of the transition conveying screw. The solid amine output end of the heating and decomposing conveying screw is connected to the solid amine input end of the decarbonization tower. The heating and decomposing conveying screw is used to heat and decompose the saturated solid amine to generate decomposed carbon dioxide, and the carbon dioxide is conveyed to the decomposing gas dust removing tower through the carbon dioxide output end of the heating and decomposing conveying screw. The carbon dioxide output end of the decomposing gas dust removing tower is connected to a carbon dioxide compressor, and the other end of the carbon dioxide compressor is connected to the carbon dioxide input end of the dryer. The dryer is used to dry the decomposed carbon dioxide and convert it into carbon dioxide-containing waste gas and dehydrated carbon dioxide. The first output end of the dryer is used to output carbon dioxide-containing waste gas, and the second output end of the dryer is used to output dehydrated carbon dioxide. The second output end of the dryer is connected to the backblowing input end of the decomposing gas dust removing tower for backblowing and dust removal of the decomposed carbon dioxide.

[0018] By adopting the above technical solution, saturated solid amine can be efficiently heated and resolved to generate high-purity carbon dioxide. By using the transition conveying screw to deliver the saturated solid amine to the heating and resolution conveying screw, the continuous delivery and heating resolution of the solid amine can be achieved, ensuring the efficient release of carbon dioxide. At the same time, the analytical gas dust removal tower can remove dust particles generated during the resolution process, ensure the purity of carbon dioxide, and improve the preparation efficiency. The dryer can effectively remove moisture by drying carbon dioxide, further improve the quality of carbon dioxide, facilitate subsequent use or discharge, and optimize the preparation process of carbon dioxide.

[0019] Preferably, a flue gas booster induced draft fan and a flue gas heat exchanger are provided between the flue gas input end of the denitrification mechanism and the ship engine for conveying ship exhaust gas, the flue gas input end of the flue gas booster induced draft fan is used to receive ship flue gas, the flue gas output end of the flue gas booster induced draft fan is connected to the flue gas input end of the flue gas heat exchanger, the flue gas output end of the flue gas heat exchanger is connected to the flue gas input end of the denitrification mechanism through a bent pipe, the flue gas input end of the flue gas booster induced draft fan is connected to the first output end of the dryer, and the seawater input end of the flue gas booster induced draft fan is connected to the first output end of the dryer. The end and the seawater output end of the flue gas booster induced draft fan are used to introduce flowing seawater to exchange heat with the ship's flue gas, the heat transfer oil input end of the flue gas heat exchanger is connected to the heat transfer oil output end of the heating and decomposition conveying screw, and the heat transfer oil output end of the flue gas heat exchanger is connected to the heat transfer oil input end of the heating and decomposition conveying screw, so that the heat transfer oil circulates between the flue gas heat exchanger and the heating and decomposition conveying screw, and exchanges heat with the ship's flue gas in the flue gas heat exchanger, and the saturated solid amine is heated and decomposed in the heating and decomposition conveying screw.

[0020] By adopting the above technical solutions, the fluidity of flue gas can be effectively improved, and the flue gas temperature can be reduced through the heat exchanger to facilitate the subsequent denitration, desulfurization and decarbonization treatment. The flue gas booster induced draft fan can increase the pressure and flow of flue gas to ensure that the flue gas can smoothly enter the denitration tower; the flue gas heat exchanger recovers part of the heat energy by exchanging heat with the ship's flue gas, thereby providing energy for the subsequent heating and analysis process, optimizing energy utilization, and ensuring the energy efficiency of the system.

[0021] Preferably, the decarbonization mechanism also includes a solid amine feeding bin and a solid amine unloading bin, a feeding control valve and a unloading control valve, the output end of the solid amine feeding bin is connected to the solid amine input end of the decarbonization tower by means of a feeding control valve, the solid amine input end of the decarbonization tower is located above the bed layer, so that the solid amine feeding bin can transport the solid amine to be reacted into the bed layer through the solid amine input end of the decarbonization tower, and the output end of the solid amine feeding bin is connected to the solid amine unloading bin by means of a unloading control valve.

[0022] By adopting the above technical solution, accurate feeding and unloading control of solid amine can be achieved. Through the feeding control valve and the unloading control valve, the smooth addition and recovery of solid amine can be ensured, and the waste or excessive use of solid amine during the transportation process can be avoided, thereby improving the efficiency and stability of the decarbonization process. This design can also automatically adjust the flow rate of solid amine according to actual needs, ensure the smooth progress of the reaction process, and improve the operating efficiency and reliability of the overall decarbonization system.

[0023] Preferably, the solid amine output end of the heating and decomposition conveying screw is connected to a solid amine buffer silo, and the output end of the solid amine buffer silo is merged into the output end of the solid amine feeding silo for conveying the solid amine to be reacted.

[0024] By adopting the above technical solution, the heating and decomposition conveying screw is connected to the solid amine buffer silo, and the output end of the solid amine buffer silo is merged with the output end of the solid amine feeding silo, so as to realize the continuous and efficient conveying of the solid amine to be reacted. This design effectively reduces the stagnation time of the material, ensures the stable feeding during the reaction process, thereby improving the production efficiency and optimizing the material conveying management.

[0025] In summary, the present application includes at least one of the following beneficial technical effects:

[0026] The present invention integrates denitration, desulfurization and decarbonization functions, and adopts a multi-stage reaction of solid amine and flue gas and a recycling technology of solid amine. Specifically, nitrogen oxides are removed by the reaction of the denitration mechanism with the reducing agent, the desulfurization mechanism uses seawater to remove sulfur dioxide, the decarbonization mechanism uses solid amine to remove carbon dioxide and generate saturated solid amine, and then the solid amine is heated and recovered by the carbon dioxide preparation mechanism, carbon dioxide is released and the solid amine is regenerated. The system can not only effectively denitrate, desulfurize and decarbonize, but also reduce the space occupied and equipment size requirements by optimizing the recycling of solid amine, thereby improving the efficiency and compactness of ship flue gas treatment. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 It is a structural flow chart of a ship flue gas denitrification, desulfurization and decarbonization system in one embodiment of the present application.

[0028] Figure 2 It is a schematic diagram of the specific structure of a denitrification mechanism, a desulfurization mechanism, a decarbonization mechanism and a carbon dioxide production mechanism in a ship flue gas denitrification, desulfurization and decarbonization system in one embodiment of the present application;

[0029] Figure 3 It is a schematic diagram of the specific structure of a flue gas booster induced draft fan and a flue gas heat exchanger in a ship flue gas denitration, desulfurization and decarbonization system in one embodiment of the present application;

[0030] Figure 4 This is a partial structural schematic diagram of a denitration mechanism in a ship flue gas denitration, desulfurization and decarbonization system in one embodiment of the present application;

[0031] Figure 5 This is a partial structural schematic diagram of a desulfurization mechanism in a ship flue gas denitration, desulfurization and decarbonization system in one embodiment of the present application;

[0032] Figure 6 It is a partial structural schematic diagram of a decarbonization mechanism in a ship flue gas denitrification, desulfurization and decarbonization system in one embodiment of the present application.

[0033] Description of reference numerals:

[0034] 1. Denitration mechanism; 11. Denitration tower; 12. Denitration packing layer; 13. Denitration liquid level sensor component; 14. Denitration regulating valve; 15. Denitration circulation pump; 16. Denitration cone component; 2. Desulfurization mechanism; 21. Desulfurization tower; 22. Desulfurization packing layer; 23. Desulfurization regulating valve; 24. Desulfurization liquid level sensor component; 3. Decarbonization mechanism; 31. Dehydration tower; 32. Decarbonization tower; 33. Dust filter tower; 34. Temperature control component; 34 1. Water-cooled coil; 342. Water-cooled control valve; 35. Bed layer; 4. Carbon dioxide preparation mechanism; 41. Transition conveying screw; 42. Heating and decomposing conveying screw; 43. Decomposition gas dust removal tower; 44. Dryer; 5. Flue gas booster induced draft fan; 6. Flue gas heat exchanger; 71. Solid amine feeding silo; 72. Solid amine unloading silo; 73. Feeding control valve; 74. Unloading control valve; 75. Solid amine buffer silo; 8. Bending pipe. DETAILED DESCRIPTION

[0035] The present application is further described in detail below in conjunction with the accompanying drawings.

[0036] In one embodiment, if Figure 1As shown, the present application discloses a ship flue gas denitration, desulfurization and decarbonization system, which specifically includes a denitration mechanism 1, a desulfurization mechanism 2, a decarbonization mechanism 3 and a carbon dioxide preparation mechanism 4. The flue gas input end of the denitration mechanism 1 is used to receive the ship flue gas. The denitration mechanism 1 is provided with a reducing agent for reacting with the ship flue gas to generate denitrified flue gas. The flue gas output end of the denitration mechanism 1 is connected to the flue gas input end of the desulfurization mechanism 2. The desulfurization mechanism 2 is provided with seawater for reacting with the denitrified flue gas to generate desulfurized flue gas. The flue gas output end of the desulfurization mechanism 2 is connected to the flue gas input end of the decarbonization mechanism 3. The decarbonization mechanism 3 is provided with a reducing agent for reacting with the desulfurized flue gas to generate desulfurized flue gas. The flue gas of the decarbonization mechanism 3 reacts to generate the solid amine to be reacted for the decarbonized flue gas. The flue gas output end of the decarbonization mechanism 3 discharges the decarbonized flue gas. The solid amine to be reacted generates saturated solid amine after reacting with the desulfurized flue gas. The solid amine output end of the decarbonization mechanism 3 transports the saturated solid amine to the solid amine input end of the carbon dioxide preparation mechanism 4. The carbon dioxide preparation mechanism 4 is used to heat the saturated solid amine to generate carbon dioxide and the solid amine to be reacted. The carbon dioxide output end of the carbon dioxide preparation mechanism 4 outputs carbon dioxide. The solid amine output end of the carbon dioxide preparation mechanism 4 transports the solid amine to be reacted to the decarbonization mechanism 3 to react with the desulfurized flue gas again.

[0037] In this embodiment, each module is interconnected through flue gas flow and control signals to achieve efficient pollutant removal and carbon dioxide recovery. First, the flue gas input end of the denitrification mechanism 1 receives high-temperature flue gas discharged from the ship engine, and the flue gas enters the denitrification tower 11 after passing through the flue gas booster fan. The flue gas entering the denitrification tower 11 reacts with the reducing agent located in the tower to generate denitrified flue gas after nitrogen oxides are removed. The flue gas output end of the denitrification tower 11 transports the denitrified flue gas to the desulfurization mechanism 2, and enters the desulfurization tower 21 through the connected pipeline. The seawater in the desulfurization mechanism 2 absorbs sulfur dioxide in the flue gas through the reaction with the denitrified flue gas to generate desulfurized flue gas. The desulfurized flue gas flows out through the flue gas output end of the desulfurization tower 21 and enters the decarbonization mechanism 3. In the decarbonization mechanism 3, the solid amine to be reacted reacts with the desulfurized flue gas, absorbs carbon dioxide in the flue gas, and generates decarbonized flue gas and saturated solid amine. The flue gas output end of the decarbonization tower 32 discharges the decarbonized flue gas into the atmosphere, and the saturated solid amine is transported to the carbon dioxide preparation mechanism 4 through the solid amine output end of the decarbonization mechanism 3. In the carbon dioxide preparation mechanism 4, the saturated solid amine is heated and resolved to generate carbon dioxide and restore the absorption capacity of the solid amine to be reacted. The generated carbon dioxide is discharged through the carbon dioxide output end of the carbon dioxide preparation mechanism 4, and the solid amine is sent back to the decarbonization mechanism 3 through the solid amine output end to continue to react with the desulfurized flue gas. The temperature control and heating analysis process in the carbon dioxide preparation mechanism 4 is a cyclic process, which ensures that the solid amine can be efficiently regenerated, and the carbon dioxide can also be effectively recovered and purified. The port connection design and control logic between each module ensure the continuous operation and high efficiency of the system, and can stably achieve the goals of denitration, desulfurization, decarbonization and carbon dioxide recovery. The control system works together with components such as liquid level sensors, regulating valves and pumps to accurately control the reaction conditions, flow rates and liquid levels of each module to ensure the smooth progress of each process, while minimizing space occupancy and improving the overall efficiency of the system.

[0038] In summary, the system integrates denitration, desulfurization and decarbonization functions, and adopts a multi-stage reaction of solid amines with flue gas and solid amine recycling technology. Specifically, the denitration mechanism 1 reacts with the reducing agent to remove nitrogen oxides, the desulfurization mechanism 2 uses seawater to remove sulfur dioxide, and the decarbonization mechanism 3 uses solid amines to remove carbon dioxide and generate saturated solid amines, which are then heated and recovered by the carbon dioxide preparation mechanism 4 to release carbon dioxide and achieve the regeneration of solid amines. This system can not only effectively denitrify, desulfurize and decarbonize, but also reduce the space occupied and equipment size requirements by optimizing the recycling of solid amines, thereby improving the efficiency and compactness of ship flue gas treatment.

[0039] Further, such as Figure 2-Figure 4As shown, the denitrification mechanism 1 includes a denitrification tower 11, in which a denitrification packing layer 12 is provided. The flue gas input end of the denitrification tower 11 is used to receive the ship flue gas and is located below the denitrification packing layer 12. The reducing agent input end of the denitrification tower 11 is used to receive the reducing agent and is located above the denitrification packing layer 12. The reducing agent flows from top to bottom based on the packing surface of the denitrification packing layer 12 to react with the ship flue gas passing through the denitrification packing layer 12 from bottom to top, thereby generating denitrification flue gas, which is transported to the desulfurization mechanism 2 through the flue gas output end of the denitrification tower 11.

[0040] In this embodiment, the denitrification mechanism 1 realizes efficient denitrification treatment of flue gas through precise port connection and flow path. First, the flue gas input end of the denitrification tower 11 receives high-temperature flue gas from the ship engine, and the flue gas enters the denitrification tower 11 through the supercharging effect of the flue gas booster fan. In the denitrification tower 11, the flue gas passes through the denitrification packing layer 12 from the bottom, and the reducing agent enters from the top of the tower through the reducing agent input end and flows from top to bottom based on the surface of the denitrification packing layer 12. The flue gas and the reducing agent are fully contacted in the packing layer, react to remove nitrogen oxides (NOx) in the flue gas, and generate denitrification flue gas. This reaction process can effectively reduce the concentration of NOx in the flue gas and improve the denitrification efficiency. The generated denitrification flue gas flows out through the flue gas output end of the denitrification tower 11 and is smoothly transported to the subsequent desulfurization mechanism 2 for further treatment. In this process, the direction of flue gas flow, the flow mode of the reducing agent, and the optimized conditions of the reaction are precisely controlled to ensure that the reaction efficiency inside the denitrification tower 11 is maximized. At the same time, the design of the packing layer provides a large gas-liquid contact surface, allowing the reductant to fully react with the NOx in the flue gas, improving the reaction rate and the overall processing capacity of the system. Through this precise port connection and control strategy, the system can efficiently perform denitrification treatment and meet the environmental protection requirements of ship flue gas emissions.

[0041] In summary, the contact area between the flue gas and the reducing agent can be effectively enhanced, and the efficiency of the denitration reaction can be improved. By allowing the reducing agent to flow from top to bottom based on the surface of the packing and fully reacting with the flue gas passing through the packing layer from bottom to top, it can promote the efficient removal of nitrogen oxides in the flue gas, reduce harmful gas emissions, and thus improve the denitration effect of the ship's flue gas treatment system. This design can ensure the treatment efficiency of the denitration tower 11, reduce the concentration of NOx in the flue gas, meet environmental emission standards, and optimize the spatial layout and equipment configuration of the system.

[0042] Further, such as Figure 2-Figure 4As shown, the denitrification mechanism 1 also includes a denitrification liquid level sensor component 13, a denitrification regulating valve 14 and a denitrification circulating pump 15. A denitrification conical component 16 is provided below the flue gas input end of the denitrification tower 11. The bottom of the denitrification conical component 16 is connected to one end of the denitrification regulating valve 14. The other end of the denitrification regulating valve 14 is used for discharging into the sea. The first conducting end of the denitrification liquid level sensor component 13 is located between the top of the denitrification conical component 16 and the bottom of the denitrification packing layer 12. The second conducting end of the denitrification liquid level sensor component 13 is located at the bottom of the denitrification conical component 16. The denitrification liquid level sensor component 13 is electrically connected to the regulating valve. One end of the denitrification circulating pump 15 is connected to the bottom of the denitrification conical component 16. The other end of the denitrification circulating pump 15 is located above the denitrification packing layer 12.

[0043] In this embodiment, the denitrification mechanism 1 works in coordination through multiple control components to ensure the stability and efficiency of the system. A denitrification conical component 16 is provided below the flue gas input end of the denitrification tower 11, and its function is to guide the incoming flue gas into the packing layer in the tower and improve the contact efficiency between the flue gas and the reducing agent by changing the airflow distribution. The bottom of the denitrification conical component 16 is connected to one end of the denitrification regulating valve 14, and the other end of the regulating valve is connected to the sea discharge system for controlling the discharge and treatment of residual reducing agent. Through this design, the regulating valve can adjust the flow of the reducing agent according to the needs of the system, ensure the stable supply of the reducing agent during the reaction process, and avoid affecting the denitrification effect due to excessive or insufficient reducing agent. The denitrification liquid level sensor component 13 ensures that the liquid level in the tower is within a predetermined range by real-time monitoring of the liquid level changes in the denitrification conical component 16, thereby avoiding the adverse effects of excessive or low liquid levels on the reaction process. The first conducting end of the liquid level sensor is located between the top of the denitration cone 16 and the bottom of the denitration packing layer 12, and is used to sense the change of the liquid level in the tower in real time. The second conducting end is located at the bottom of the denitration cone 16 and is electrically connected to the denitration regulating valve 14 to form a closed-loop control system to ensure that the change of the liquid level can directly affect the opening and closing of the regulating valve, thereby automatically adjusting the liquid level. One end of the denitration circulation pump 15 is connected to the bottom of the denitration cone 16, and is used to transport the reacted reducing agent to the denitration packing layer 12 above the tower to ensure the circulation of the reducing agent in the tower and optimize the reaction efficiency. The other end of the circulation pump is located above the denitration packing layer 12 to ensure that the reducing agent can be evenly distributed in the packing layer and fully react with the flue gas. Through this series of port connections and control logic, the system can accurately adjust the flow and liquid level of the flue gas and the reducing agent, optimize the conditions of the denitration reaction, ensure that the nitrogen oxides in the flue gas are efficiently removed, and maintain the stable operation of the equipment.

[0044] In summary, accurate liquid level control and flow regulation of the reducing agent can be achieved inside the denitration tower 11. The use of the liquid level sensor in conjunction with the regulating valve can monitor the liquid level of the denitration tower 11 in real time, avoiding excess or insufficient reducing agent, thereby ensuring the stability and efficiency of the denitration reaction. By using the denitration circulation pump 15, the uniform distribution of the reducing agent in the tower can be ensured, and the appropriate fluidity can be maintained, further optimizing the reaction process and improving the reliability and processing capacity of the denitration system.

[0045] Further, such as Figure 2-Figure 5 As shown, the desulfurization mechanism 2 includes a desulfurization tower 21, a desulfurization regulating valve 23 and a desulfurization liquid level sensor component 24. A desulfurization packing layer 22 is provided in the desulfurization tower 21. The flue gas input end of the desulfurization tower 21 is used to receive denitrification flue gas and is located below the desulfurization packing layer 22. The seawater input end of the desulfurization tower 21 is used to receive seawater and is located above the desulfurization packing layer 22. The seawater output end of the desulfurization tower 21 is connected to one end of the desulfurization regulating valve 23, and the other end of the desulfurization regulating valve 23 is used to discharge into the sea. The first conducting end of the desulfurization liquid level sensor component 24 is located at the top of the desulfurization packing layer 22, and the second conducting end of the desulfurization liquid level sensor component 24 is located at the bottom of the desulfurization tower 21. The desulfurization liquid level sensor component 24 is electrically connected to the desulfurization regulating valve 23. The denitrification flue gas forms bubbles flowing from bottom to top in the seawater to react with the seawater, thereby generating desulfurized flue gas, and the desulfurized flue gas is transported to the decarbonization mechanism 3 through the flue gas output end of the desulfurization tower 21.

[0046] In this embodiment, the desulfurization mechanism 2 cooperates with each other through the port connection and control logic of each module to ensure that the sulfur dioxide in the flue gas is effectively removed. The flue gas input end of the desulfurization tower 21 receives the denitrified flue gas from the denitrification mechanism 1. The flue gas first enters the desulfurization tower 21 and flows through the desulfurization packing layer 22 located in the tower. The purpose of the packing layer design is to provide a larger gas-liquid contact area to ensure that the sulfur dioxide in the flue gas fully reacts with the seawater. The seawater input end of the desulfurization tower 21 is used to receive seawater from the outside and enter the tower through the top of the packing layer, where it reacts with the flue gas to remove the sulfur dioxide in the flue gas. The reacted seawater flows to the input end of the desulfurization regulating valve 23, and the other end of the regulating valve is connected to the sea discharge system for controlling the discharge of seawater. The flow and liquid level of seawater are monitored in real time by the desulfurization liquid level sensor component 24 to ensure that the seawater level in the tower is maintained in an appropriate range to avoid too low or too high liquid levels affecting the reaction efficiency. The first conducting end of the liquid level sensor is located at the top of the desulfurization packing layer 22 to sense the liquid level at the top of the desulfurization packing layer 22, while the second conducting end is located at the bottom of the desulfurization tower 21 and is connected to the desulfurization regulating valve 23 through an electrical signal. When the liquid level sensor detects a change in the liquid level, it can automatically adjust the opening and closing of the desulfurization regulating valve 23, accurately control the seawater flow rate, and ensure that the amount of seawater in the desulfurization process is appropriate to avoid excess or insufficiency. As seawater reacts with flue gas, sulfur dioxide in the denitrification flue gas is absorbed and converted into harmless sulfates, and the generated desulfurized flue gas is discharged through the flue gas output end of the desulfurization tower 21 and enters the subsequent decarbonization mechanism 3 for further processing. Through this series of port connections and control logic, the desulfurization system can ensure the effective removal of sulfur dioxide in the flue gas under stable liquid level control and precise seawater flow regulation to meet the ship flue gas emission standards.

[0047] In summary, the flow of seawater can be effectively controlled and the seawater level in the desulfurization tower 21 can be monitored in real time to ensure the continuous stability of the desulfurization reaction. By adjusting the seawater flow and level, the absorption process of sulfur dioxide can be optimized to ensure the effective removal of sulfur dioxide in the flue gas. In addition, the contact mode between seawater and flue gas optimizes the reaction efficiency, and the surface area of ​​the gas-liquid reaction is enhanced through the bottom-up bubble flow, which significantly improves the desulfurization capacity of the desulfurization tower 21, reduces sulfur dioxide emissions, and meets environmental emission requirements.

[0048] Further, such as Figure 2-Figure 6As shown, the decarbonization mechanism 3 includes a dehydration tower 31, a decarbonization tower 32 and a dust filter tower 33. The flue gas input end of the dehydration tower 31 is used to receive the desulfurized flue gas. The dehydration tower 31 is used to dehydrate the desulfurized flue gas to generate dehydrated flue gas. The flue gas output end of the dehydration tower 31 is connected to the flue gas input end of the decarbonization tower 32 for receiving the dehydrated flue gas. A bed 35 for filling the solid amine to be reacted is provided in the decarbonization tower 32. The flue gas input end of the decarbonization tower 32 is located below the bed 35. The dehydrated flue gas flows from bottom to top, thereby reacting with the solid amine to be reacted through the bed 35 to generate decarbonized flue gas, and is transported to the dust filter tower 33 through the flue gas output end of the decarbonization tower 32 for dust removal, and then the decarbonized flue gas after dust removal is discharged into the atmosphere through the flue gas output end of the dust filter tower 33.

[0049] In this embodiment, the decarbonization mechanism 3 ensures that the carbon dioxide in the flue gas after desulfurization is effectively removed through the precise connection and coordinated work of multiple modules. First, the flue gas input end of the dehydration tower 31 receives the desulfurized flue gas from the desulfurization mechanism 2 and transmits it to the dehydration tower 31 for dehydration. The dehydration tower 31 effectively reduces the moisture content in the flue gas through the internal physical process to generate dehydrated flue gas, and the humidity of the flue gas at this time is significantly reduced. The flue gas output end of the dehydration tower 31 is connected to the flue gas input end of the decarbonization tower 32, and the dehydrated flue gas is introduced into the decarbonization tower 32 for further treatment. The bed 35 in the decarbonization tower 32 is used to fill the solid amine to be reacted. The flue gas enters the tower from the flue gas input end of the decarbonization tower 32, flows along the bottom of the bed 35, reacts with the solid amine in the bed 35, absorbs the carbon dioxide in the flue gas, and generates decarbonized flue gas. The solid amine releases heat during the reaction with the carbon dioxide in the flue gas, and at the same time, carbon dioxide is generated by the reaction and the solid amine is converted into saturated solid amine. The flue gas after the reaction in the bed 35 flows to the flue gas output end of the decarbonization tower 32, and enters the dust filter tower 33 through this port. In the dust filter tower 33, the solid amine dust in the flue gas is effectively filtered to ensure the cleanliness of the decarbonized flue gas. The flue gas after dust filtration is discharged through the flue gas output end of the dust filter tower 33, and finally the decarbonized flue gas after dust removal is discharged into the atmosphere to meet the emission standards. During the whole process, the flue gas flows from the dehydration tower 31 to the decarbonization tower 32, and then to the dust filter tower 33. The flow direction and reaction of each module are precisely controlled to ensure the efficiency of carbon dioxide removal and the cleanliness of the final flue gas. The connection of each port ensures the smooth flow of the airflow and the efficient progress of each reaction. At the same time, the connection between the control logics also ensures the stable operation and optimization of the entire system.

[0050] In summary, it is possible to effectively remove moisture from flue gas, reduce flue gas humidity, and prevent moisture from affecting the subsequent decarbonization process. The dehydration tower 31 can maintain a suitable humidity when the flue gas enters the decarbonization tower 32 through dehydration treatment, thereby improving the reaction efficiency of solid amines in the decarbonization process. At the same time, the dust filter tower 33 can remove dust impurities in the flue gas, protect subsequent equipment from clogging, improve the stability and long-term operation capability of the decarbonization system, and ensure that the decarbonized flue gas meets the emission standards.

[0051] Further, such as Figure 2-Figure 6 As shown, the decarbonization mechanism 3 also includes a temperature control component 34, which includes a water-cooling control valve 342 and a plurality of water-cooling coils 341. The plurality of water-cooling coils 341 are arranged in sequence from top to bottom in the bed layer 35, and one end of each water-cooling coil 341 is connected to one end connected to the water-cooling control valve 342, and the other end of the water-cooling control valve 342 is used to discharge seawater, and the other end of the water-cooling control valve 342 is used to receive seawater.

[0052] In this embodiment, the temperature control component 34 ensures that the temperature in the decarbonization tower 32 is maintained in the optimal range through a series of precise connections and controls to ensure the efficiency of solid amine absorbing carbon dioxide. The temperature control component 34 includes a plurality of water-cooled coils 341 and a water-cooled control valve 342, and these water-cooled coils 341 are arranged in sequence from top to bottom in the bed 35 of the decarbonization tower 32. One end of each water-cooled coil 341 is connected to one end of the water-cooled control valve 342, and the other end of the water-cooled control valve 342 is connected to the sea discharge system for discharging cooled seawater. The other end of the water-cooled control valve 342 is used to receive fresh seawater to maintain the circulation of the cooling system. In this way, the seawater in the water-cooled coil 341 can effectively absorb the reaction heat in the decarbonization tower 32, and the temperature in the tower is kept below 120 degrees Celsius by the adjustment of the water-cooled control valve 342, thereby ensuring that the solid amine can efficiently absorb carbon dioxide, while avoiding excessive temperature affecting the reaction efficiency and the stability of the reactant. Through this design, the system can not only maintain a stable reaction temperature, but also reduce the decrease in reaction efficiency due to temperature fluctuations, ensure the continuity and stability of the decarbonization process, and at the same time ensure the effective flow of cooling water and the rational use of energy.

[0053] In summary, the temperature in the decarbonization tower 32 can be effectively controlled to prevent the temperature from being too high or too low, which may affect the efficiency of the decarbonization reaction. The water cooling system can stabilize the temperature in the decarbonization tower 32 by adjusting the water flow of the water cooling coil 341, ensuring that the reaction process of the solid amine is always within the optimal reaction temperature range, thereby improving the removal efficiency of carbon dioxide. While ensuring the reaction rate, this design can also reduce energy waste, improve the energy efficiency of the overall system, and optimize the treatment process of ship flue gas.

[0054] Further, such as Figure 2As shown, the carbon dioxide preparation mechanism 4 includes a transition conveying screw 41, a heating and decomposing conveying screw 42, a decomposing gas dust removal tower 43 and a dryer 44. The solid amine input end of the transition conveying screw 41 is connected to the bottom of the decarbonization tower 32 to receive saturated solid amine, and the saturated solid amine is conveyed to the heating and decomposing conveying screw 42 through the solid amine output end of the transition conveying screw 41. The solid amine output end of the heating and decomposing conveying screw 42 is connected to the solid amine input end of the decarbonization tower 32. The heating and decomposing conveying screw 42 is used to heat and decompose the saturated solid amine to generate decomposed carbon dioxide, and the heating and decomposing conveying screw 42 is used to heat and decompose the saturated solid amine to generate decomposed carbon dioxide. The carbon dioxide output end is transported to the desorption gas dust removal tower 43, the carbon dioxide output end of the desorption gas dust removal tower 43 is connected to a carbon dioxide compressor, the other end of the carbon dioxide compressor is connected to the carbon dioxide input end of the dryer 44, the dryer 44 is used to dry the desorbed carbon dioxide, and then convert it into carbon dioxide-containing waste gas and dehydrated carbon dioxide, the first output end of the dryer 44 is used to output the carbon dioxide-containing waste gas, the second output end of the dryer 44 is used to output dehydrated carbon dioxide, the second output end of the dryer 44 is connected to the back-blowing input end of the desorption gas dust removal tower 43, so as to back-blow and remove dust from the desorbed carbon dioxide.

[0055] In this embodiment, through precise port connection and control logic, the heating and parsing process of saturated solid amine is ensured to proceed smoothly, thereby efficiently recovering and purifying carbon dioxide. First, the solid amine input end of the transition conveying screw 41 is connected to the bottom of the decarbonization tower 32 to receive the saturated solid amine from the decarbonization tower 32. Through the solid amine output end of the transition conveying screw 41, the saturated solid amine is transported to the heating and parsing conveying screw 42 for further processing. The solid amine output end of the heating and parsing conveying screw 42 is connected to the solid amine input end of the decarbonization tower 32 to ensure the continuous supply of solid amine and form a closed loop. The heating and parsing conveying screw 42 parses the saturated solid amine through the heating process, releases carbon dioxide, and transports the generated carbon dioxide to the parsing gas dedust tower 43 through the carbon dioxide output end of the heating and parsing conveying screw 42. In the parsing gas dedust tower 43, carbon dioxide is subjected to dust removal treatment, and after removing impurities therein, the carbon dioxide output end of the parsing gas dedust tower 43 is connected to the carbon dioxide compressor, and carbon dioxide is compressed to a high pressure state for subsequent drying treatment. The other end of the carbon dioxide compressor is connected to the carbon dioxide input end of the dryer 44. The compressed carbon dioxide enters the dryer 44 for further processing. The carbon dioxide is thoroughly dried in the dryer 44 to remove moisture and other impurities. The dried carbon dioxide is divided into two parts. The first output end of the dryer 44 is used to output the waste gas containing carbon dioxide, and the second output end of the dryer 44 is used to output the purified dehydrated carbon dioxide. This part of carbon dioxide will be connected to the backflush input end of the analytical gas dust removal tower 43 through the second output end of the dryer 44, so as to backflush the analyzed carbon dioxide to remove dust and remove residual trace solid impurities. The coordinated effect of this series of modules ensures the efficient recovery and purification of carbon dioxide, optimizes the energy efficiency and resource utilization of the entire system, and ensures that the solid amine in the decarbonization process can be effectively regenerated and continue to play its decarbonization role.

[0056] In summary, saturated solid amine can be efficiently heated and resolved to generate high-purity carbon dioxide. By using the transition conveying screw 41 to deliver the saturated solid amine to the heating and resolution conveying screw 42, the continuous delivery and heating resolution of the solid amine can be achieved, ensuring the efficient release of carbon dioxide. At the same time, the analytical gas dust removal tower 43 can remove the dust particles generated during the analysis process, ensure the purity of carbon dioxide, and improve the preparation efficiency. The dryer 44 can effectively remove moisture by drying carbon dioxide, further improve the quality of carbon dioxide, facilitate subsequent use or discharge, and optimize the preparation process of carbon dioxide.

[0057] Further, such as Figure 3As shown, a flue gas booster induced draft fan 5 and a flue gas heat exchanger 6 are provided between the flue gas input end of the denitrification mechanism 1 and the ship engine for conveying ship exhaust gas, the flue gas input end of the flue gas booster induced draft fan 5 is used to receive ship flue gas, the flue gas output end of the flue gas booster induced draft fan 5 is connected to the flue gas input end of the flue gas heat exchanger 6, the flue gas output end of the flue gas heat exchanger 6 is connected to the flue gas input end of the denitrification mechanism 1 through a bent pipe 8, the flue gas input end of the flue gas booster induced draft fan 5 is connected to the first output end of the dryer 44, and the seawater of the flue gas booster induced draft fan 5 The input end and the seawater output end of the flue gas booster induced draft fan 5 are used to introduce flowing seawater to exchange heat with the ship's flue gas. The heat transfer oil input end of the flue gas heat exchanger 6 is connected to the heat transfer oil output end of the heating and decomposition conveying screw 42, and the heat transfer oil output end of the flue gas heat exchanger 6 is connected to the heat transfer oil input end of the heating and decomposition conveying screw 42, so that the heat transfer oil circulates between the flue gas heat exchanger 6 and the heating and decomposition conveying screw 42, and exchanges heat with the ship's flue gas in the flue gas heat exchanger 6, and heats and decomposes the saturated solid amine in the heating and decomposition conveying screw 42.

[0058] In this embodiment, the denitrification mechanism 1 and other modules form a closed-loop system through precise port connection and control logic to ensure efficient treatment of ship exhaust gas and recovery of carbon dioxide. First, the flue gas input end of the flue gas booster induced draft fan 5 receives the flue gas discharged from the ship engine, and the flue gas is sent to the flue gas input end of the flue gas heat exchanger 6 through the flue gas output end of the flue gas booster induced draft fan 5 after being pressurized. In the flue gas heat exchanger 6, the flue gas exchanges heat with the heat transfer oil, the temperature of the flue gas is appropriately reduced, and the flue gas output end of the flue gas heat exchanger 6 is connected to the flue gas input end of the denitrification mechanism 1 through a bent pipe 8, and enters the denitrification tower 11 for denitrification treatment. In this way, through the linkage of the flue gas booster induced draft fan 5 and the flue gas heat exchanger 6, not only is it ensured that the flow rate and pressure of the flue gas are suitable for the requirements of the denitrification reaction, but also the heat is effectively recovered and transferred, thereby improving the energy efficiency of the system. The flue gas input end of the flue gas booster induced draft fan 5 is connected to the first output end of the dryer 44, so that the boosted flue gas enters the dryer 44, further processes the moisture in the gas, and ensures that the dryness of the flue gas is suitable for the subsequent decarbonization treatment. At the same time, the seawater input end of the flue gas booster induced draft fan 5 is connected to its seawater output end, which is used to pass flowing seawater, and the flue gas is preheated or cooled by seawater, thereby optimizing the subsequent flue gas treatment process. Next, the heat transfer oil input end of the flue gas heat exchanger 6 is connected to the heat transfer oil output end of the heating and analysis conveying screw 42, and the heat transfer oil circulates between the flue gas heat exchanger 6 and the heating and analysis conveying screw 42, ensuring that the heat transfer oil exchanges heat with the flue gas in the heat exchanger, thereby providing a stable heat source for the saturated solid amine in the heating and analysis process. In the heating and analysis conveying screw 42, the saturated solid amine is heated and analyzed by the circulating heat transfer oil to release carbon dioxide, while ensuring that the solid amine can be effectively recovered and regenerated. Through the connection between this series of modules and precise control logic, the entire system can efficiently and stably carry out denitrification, decarbonization and carbon dioxide recovery processes, achieving environmentally friendly treatment and energy optimization of flue gas.

[0059] In summary, the fluidity of flue gas can be effectively improved, and the flue gas temperature can be reduced through the heat exchanger for subsequent denitration, desulfurization and decarbonization treatment. The flue gas booster induced draft fan 5 can increase the pressure and flow of the flue gas, ensuring that the flue gas can smoothly enter the denitration tower 11; the flue gas heat exchanger 6 recovers part of the heat energy by exchanging heat with the ship's flue gas, thereby providing energy for the subsequent heating and analysis process, optimizing energy utilization, and ensuring the energy efficiency of the system.

[0060] Further, such as Figure 2As shown, the decarbonization mechanism 3 also includes a solid amine feeding bin 71 and a solid amine unloading bin 72, a feeding control valve 73 and a unloading control valve 74. The output end of the solid amine feeding bin 71 is connected to the solid amine input end of the decarbonization tower 32 by means of a feeding control valve 73. The solid amine input end of the decarbonization tower 32 is located above the bed 35, so that the solid amine feeding bin 71 can transport the solid amine to be reacted to the bed 35 through the solid amine input end of the decarbonization tower 32. The output end of the solid amine feeding bin 71 is connected to the solid amine unloading bin 72 by means of a unloading control valve 74.

[0061] In this embodiment, the precise connection between the solid amine charging bin 71 and the decarbonization tower 32 and the solid amine unloading bin 72 ensures the continuous supply and recovery of solid amine to maintain the efficient operation of the decarbonization process. The output end of the solid amine charging bin 71 is connected to the solid amine input end of the decarbonization tower 32 through a charging control valve 73. The function of the charging control valve 73 is to adjust the flow of solid amine to ensure that the solid amine is transported to the solid amine input end of the decarbonization tower 32 at an appropriate speed and amount. This input end is located above the bed 35 of the decarbonization tower 32. Through this port, the solid amine to be reacted is transported to the bed 35 of the decarbonization tower 32 to react with the carbon dioxide in the flue gas. The solid amine in the bed 35 contacts the flue gas, absorbs carbon dioxide and generates saturated solid amine. The output end of the solid amine charging bin 71 is also connected to the solid amine unloading bin 72 through a discharge control valve 74, and the discharge control valve 74 is used to adjust the unloading process of the solid amine. Through the precise adjustment of the control valve, the discharge amount of solid amine is ensured to match the system demand, avoiding excessive or insufficient solid amine, thereby ensuring stable operation of the system. In this process, the feeding control valve 73 and the discharge control valve 74 maintain the reasonable supply and recovery of solid amine by real-time monitoring and adjusting the flow, ensuring that the reaction in the decarbonization tower 32 continues, carbon dioxide is effectively removed, and solid amine can be regenerated. This design of port connection and control logic improves the flexibility and efficiency of the decarbonization process, while ensuring the reasonable use and conservation of solid amine.

[0062] In summary, accurate feeding and unloading control of solid amine can be achieved. Through the feeding control valve 73 and the unloading control valve 74, the smooth addition and recovery of solid amine can be ensured, and the waste or excessive use of solid amine during the transportation process can be avoided, thereby improving the efficiency and stability of the decarbonization process. This design can also automatically adjust the flow rate of solid amine according to actual needs, ensure the smooth progress of the reaction process, and improve the operating efficiency and reliability of the overall decarbonization system.

[0063] Further, such as Figure 2 As shown, the solid amine output end of the heating and decomposition conveying screw 42 is connected to the solid amine buffer silo 75, and the output end of the solid amine buffer silo 75 is merged into the output end of the solid amine feeding silo 71 for conveying the solid amine to be reacted.

[0064] In this embodiment, the solid amine output end of the heating and decomposition conveying screw 42 is connected to the solid amine buffer silo 75 so that the resolved solid amine can be transported to the buffer silo for temporary storage and buffering. The function of the solid amine buffer silo 75 is to store and stably transport solid amine, ensuring that the system can continuously supply enough solid amine for reaction when needed. In the buffer silo, solid amine can be effectively stored to avoid affecting the subsequent decarbonization reaction due to unstable supply. The output end of the solid amine buffer silo 75 is connected to the output end of the solid amine feeding silo 71 to form a continuous feeding system. The connection of this port ensures that when the amount of solid amine in the buffer silo reaches a predetermined level, the solid amine can smoothly flow into the solid amine feeding silo 71 and be transported to the reaction bed 35 of the decarbonization tower 32 through the feeding silo for the absorption reaction of carbon dioxide. Through this design, the combination between the solid amine buffer silo 75 and the feeding silo can balance the supply and demand of solid amine, ensure the uninterrupted supply of solid amine in the decarbonization tower 32, and avoid the situation of excessive or insufficient solid amine. In the control logic, the coordination of the buffer silo and the feeding silo realizes the effective management and scheduling of solid amines, thereby optimizing the efficiency and stability of the decarbonization process, ensuring the continuous operation of the system and efficient removal of carbon dioxide.

[0065] In summary, accurate feeding and unloading control of solid amine can be achieved. Through the feeding control valve 73 and the unloading control valve 74, the smooth addition and recovery of solid amine can be ensured, and the waste or excessive use of solid amine during the transportation process can be avoided, thereby improving the efficiency and stability of the decarbonization process. This design can also automatically adjust the flow rate of solid amine according to actual needs, ensure the smooth progress of the reaction process, and improve the operating efficiency and reliability of the overall decarbonization system.

[0066] Specifically, the high-temperature flue gas exhausted from the engine is pressurized by the flue gas booster fan and then enters the flue gas heat exchanger 6. The flue gas heat exchanger 6 heats the heat transfer oil and provides a heat source heating medium for the downstream equipment; the cooled flue gas enters the wet reduction denitrification tower 11, in which the reducing agent is sprayed from the top of the tower into the packing layer to complete the contact and reaction process with the flue gas (because the residual temperature of the flue gas after heat exchange is still more than 100 degrees, denitrification requires a certain reaction temperature to proceed, and the denitrification structure must be placed at the front end of the desulfurization; the reducing agent forms steam and liquid phases at a certain temperature to accelerate the denitrification reaction rate. In order to prevent the reducing agent solution from taking away a large amount of heat, a bubbling tower is not used, and a packed tower is used here to complete denitrification). There is a reagent circulation pump at the bottom of the tower to circulate the residual reagent in the reaction, and a denitrification regulating valve 14 is provided at the bottom of the tower to control The liquid level in the tower is controlled, and the reacted reagents are discharged into the sea; then the denitrified flue gas enters the seawater desulfurization bubbling tower, i.e., the desulfurization tower 21, and seawater continuously flows into the bubbling tower to ensure that the liquid level in the tower submerges the filler, and the sulfur-containing flue gas is dispersed in the seawater phase and fully contacts and reacts in the filler layer (compared with the traditional seawater desulfurization tower 21, the flue gas is the continuous phase and the seawater is the dispersed phase; now the continuous phase is seawater, which is equivalent to increasing the amount of desulfurizer and improving the desulfurization efficiency). A desulfurization regulating valve 23 is provided at the bottom of the tower to control the liquid level in the tower, and the desulfurized seawater is discharged into the sea; the desulfurized flue gas enters the dehydration tower 31 for condensing the flue gas, and the flue gas is condensed and dehydrated to reduce the water content of the gas to 0.1%; since the solid amine absorbent has a certain absorption effect on water, deep dehydration is required before entering the decarbonization, and a demister is provided at the top of the seawater desulfurization bubbling tower, but deep dehydration is not possible. The flue gas after physical deep dehydration enters the decarbonization tower 32 through the flue gas booster fan. The tower is filled with a large amount of solid amine powder for absorbing carbon dioxide. The flue gas containing carbon dioxide flows through the bed 35 containing solid absorbent, i.e., solid amine, where carbon dioxide is absorbed. The solid amine powder saturated with absorption flows from top to bottom, and the gas passes through the bed 35 from bottom to top. The reaction of solid amine with carbon dioxide in the flue gas will generate heat. Generally, the reaction is controlled below 120 degrees Celsius, which can not only ensure the reaction of solid amine absorbing carbon dioxide but also ensure that water exists in the form of water vapor and is discharged from the decarbonization tower 32 along with the decarbonization flue gas. The decarbonization tower 32 is provided with a seawater cooling spiral tube to control the temperature, i.e., a temperature control unit; the flue gas after decarbonization enters the dust filter tower 33 to filter out the solid amine dust in the flue gas, and then the flue gas is discharged into the atmosphere. The bottom of the dust filter tower 33 is provided with a fan and a sealing valve to prevent flue gas from flowing through.The gas discharged from the bottom of the decarbonization tower 32 first passes through the fan and the sealing valve, and then enters the conveying screw. The conveying screw conveys the solid amine powder to the heating and decomposition conveying screw 42. There is high-temperature heat transfer oil in the external jacket of this equipment. The saturated solid amine powder is heated and decomposed to precipitate carbon dioxide during the transportation process. The gaseous carbon dioxide enters the decomposition gas dedust tower 43 for dust removal. The dedusted carbon dioxide is boosted by the decomposition carbon dioxide compressor and enters the activated carbon + molecular sieve adsorption dryer 44 to further remove impurity gases and moisture. These impurities also contain carbon dioxide and will return to the front end of the upstream flue gas booster fan; a part of the purified carbon dioxide high-pressure gas returns to the decomposition gas dedust tower 43 to backflush the filter element and can increase the concentration of gaseous carbon dioxide in the upstream equipment. A high-purity, high-pressure carbon dioxide gas returns to the bottom of the decarbonization tower 32 for gas sealing to dilute and replace the trace flue gas components entrained in the solid amine (since the solid amine is a powder and is compacted more tightly by gravity, it will not entrain too much flue gas). The solid amine that has been heated and analyzed enters the solid amine buffer silo 75 from the fan and the sealing valve at the bottom. The bottom of the solid amine buffer silo 75 is a sealing valve and a pneumatic conveying device. When the sealing valve is opened and the pneumatic conveying device is turned on, the analyzed solid amine can be transported back to the decarbonization tower 32. The gas source used for pneumatic conveying can be pressurized flue gas or compressed air, and can be switched by operating the valve; the present application also adds a solid amine feeding silo 71 and a waste solid amine unloading silo 72 to facilitate the loading and unloading operations of the adsorbent.

[0067] Those skilled in the art can clearly understand that for the convenience and simplicity of description, only the division of the above-mentioned functional units and modules is used as an example. In actual applications, the above-mentioned functions can be distributed and completed by different functional units and modules as needed, that is, the internal structure of the device can be divided into different functional units or modules to complete all or part of the functions described above.

[0068] The embodiments described above are only used to illustrate the technical solutions of the present application, rather than to limit them. Although the present application has been described in detail with reference to the aforementioned embodiments, a person skilled in the art should understand that the technical solutions described in the aforementioned embodiments may still be modified, or some of the technical features may be replaced by equivalents. Such modifications or replacements do not deviate the essence of the corresponding technical solutions from the spirit and scope of the technical solutions of the embodiments of the present application, and should all be included in the protection scope of the present application.

Claims

1. A ship flue gas denitrification, desulfurization and decarbonization system, characterized in that: The ship flue gas denitration, desulfurization and decarbonization system comprises a denitration mechanism (1), a desulfurization mechanism (2), a decarbonization mechanism (3) and a carbon dioxide production mechanism (4); the flue gas input end of the denitration mechanism (1) is used to receive ship flue gas; the denitration mechanism (1) is provided with a reducing agent for reacting with the ship flue gas to generate denitrified flue gas; the flue gas output end of the denitration mechanism (1) is connected to the flue gas input end of the desulfurization mechanism (2); the desulfurization mechanism (2) is provided with seawater for reacting with the denitrified flue gas to generate desulfurized flue gas; the flue gas output end of the desulfurization mechanism (2) is connected to the flue gas input end of the decarbonization mechanism (3); the decarbonization mechanism (3) is provided with a reducing agent for reacting with the desulfurized flue gas to generate desulfurized flue gas; The solid amine to be reacted should be used to generate decarbonized flue gas. The flue gas output end of the decarbonization mechanism (3) discharges decarbonized flue gas. The solid amine to be reacted generates saturated solid amine after reacting with the desulfurized flue gas. The solid amine output end of the decarbonization mechanism (3) transports the saturated solid amine to the solid amine input end of the carbon dioxide production mechanism (4). The carbon dioxide production mechanism (4) is used to heat the saturated solid amine to generate carbon dioxide and the solid amine to be reacted. The carbon dioxide output end of the carbon dioxide production mechanism (4) outputs carbon dioxide. The solid amine output end of the carbon dioxide production mechanism (4) transports the solid amine to be reacted into the decarbonization mechanism (3) to react with the desulfurized flue gas again.

2. A ship flue gas denitrification, desulfurization and decarbonization system according to claim 1, characterized in that The denitrification mechanism (1) comprises a denitrification tower (11), wherein a denitrification packing layer (12) is provided in the denitrification tower (11), a flue gas input end of the denitrification tower (11) is used to receive ship flue gas and is located below the denitrification packing layer (12), and a reducing agent input end of the denitrification tower (11) is used to receive the reducing agent and is located above the denitrification packing layer (12), the reducing agent flows from top to bottom based on the packing surface of the denitrification packing layer (12) to react with the ship flue gas passing through the denitrification packing layer (12) from bottom to top, thereby generating the denitrification flue gas, which is transported to the desulfurization mechanism (2) through the flue gas output end of the denitrification tower (11).

3. A ship flue gas denitration, desulfurization and decarbonization system according to claim 2, characterized in that: The denitration mechanism (1) further comprises a denitration liquid level sensor assembly (13), a denitration regulating valve (14) and a denitration circulation pump (15); a denitration conical component (16) is provided below the flue gas input end of the denitration tower (11); the bottom of the denitration conical component (16) is connected to one end of the denitration regulating valve (14); the other end of the denitration regulating valve (14) is used for discharging into the sea; the first conduction end of the denitration liquid level sensor assembly (13) is located at the denitration conical component The denitrification liquid level sensor component (13) is located between the top of the denitrification conical component (16) and the bottom of the denitrification filling layer (12), the second conductive end of the denitrification liquid level sensor component (13) is located at the bottom of the denitrification conical component (16), the denitrification liquid level sensor component (13) is electrically connected to the denitrification regulating valve (14), one end of the denitrification circulation pump (15) is connected to the bottom of the denitrification conical component (16), and the other end of the denitrification circulation pump (15) is located above the denitrification filling layer (12).

4. A ship flue gas denitration, desulfurization and decarbonization system according to claim 1, characterized in that: The desulfurization mechanism (2) comprises a desulfurization tower (21), a desulfurization regulating valve (23) and a desulfurization liquid level sensor component (24); a desulfurization packing layer (22) is provided in the desulfurization tower (21); a flue gas input end of the desulfurization tower (21) is used to receive denitrified flue gas and is located below the desulfurization packing layer (22); a seawater input end of the desulfurization tower (21) is used to receive seawater and is located above the desulfurization packing layer (22); a seawater output end of the desulfurization tower (21) is connected to one end of the desulfurization regulating valve (23); and the desulfurization regulating valve (23) is connected to the desulfurization packing layer (22). ) is used for discharging into the sea, the first conducting end of the desulfurization liquid level sensor component (24) is located at the top of the desulfurization packing layer (22), the second conducting end of the desulfurization liquid level sensor component (24) is located at the bottom of the desulfurization tower (21), the desulfurization liquid level sensor component (24) is electrically connected to the desulfurization regulating valve (23), the denitrification flue gas forms bubbles flowing from bottom to top in the seawater to react with the seawater, thereby generating the desulfurization flue gas, and the desulfurization flue gas is transported to the decarbonization mechanism (3) through the flue gas output end of the desulfurization tower (21).

5. A ship flue gas denitration, desulfurization and decarbonization system according to claim 1, characterized in that: The decarbonization mechanism (3) comprises a dehydration tower (31), a decarbonization tower (32) and a dust filtering tower (33); the flue gas input end of the dehydration tower (31) is used to receive the desulfurized flue gas; the dehydration tower (31) is used to dehydrate the desulfurized flue gas to generate dehydrated flue gas; the flue gas output end of the dehydration tower (31) is connected to the flue gas input end of the decarbonization tower (32) to receive the dehydrated flue gas; the decarbonization tower (32) is provided with a filter for filling the solid to be reacted. The flue gas input end of the decarbonization tower (32) is located below the bed layer (35), and the dehydrated flue gas flows from bottom to top, thereby passing through the bed layer (35) to react with the solid amine to be reacted to generate the decarbonized flue gas, and is transported to the dust filter tower (33) through the flue gas output end of the decarbonization tower (32) for dust removal, and then the decarbonized flue gas after dust removal is discharged into the atmosphere through the flue gas output end of the dust filter tower (33).

6. A ship flue gas denitration, desulfurization and decarbonization system according to claim 5, characterized in that: The decarbonization mechanism (3) further comprises a temperature control component (34), wherein the temperature control component (34) comprises a water cooling control valve (342) and a plurality of water cooling coils (341), wherein the plurality of water cooling coils (341) are sequentially arranged from top to bottom in the bed layer (35), wherein one end of each of the water cooling coils (341) is connected to one end connected to the water cooling control valve (342), and the other end of the water cooling control valve (342) is used to discharge seawater, and the other end of the water cooling control valve (342) is used to receive seawater.

7. A ship flue gas denitration, desulfurization and decarbonization system according to claim 5, characterized in that: The carbon dioxide preparation mechanism (4) comprises a transition conveying screw (41), a heating and decomposing conveying screw (42), a decomposing gas dust removal tower (43) and a dryer (44). The solid amine input end of the transition conveying screw (41) is connected to the bottom of the decarbonization tower (32) for receiving the saturated solid amine, and the saturated solid amine is conveyed to the heating and decomposing conveying screw (42) through the solid amine output end of the transition conveying screw (41). The solid amine output end of the heating and decomposing conveying screw (42) is connected to the solid amine input end of the decarbonization tower (32). The heating and decomposing conveying screw (42) is used to heat and decompose the saturated solid amine to generate decomposed carbon dioxide, and the heating and decomposing conveying screw (42) is used to heat and decompose the saturated solid amine to generate decomposed carbon dioxide. The carbon dioxide output end of the desorption gas dedust tower (43) is transported to the desorption gas dedust tower (43), and the carbon dioxide output end of the desorption gas dedust tower (43) is connected to a carbon dioxide compressor, and the other end of the carbon dioxide compressor is connected to the carbon dioxide input end of the dryer (44). The dryer (44) is used to dry the desorbed carbon dioxide and then convert it into carbon dioxide-containing waste gas and dehydrated carbon dioxide. The first output end of the dryer (44) is used to output the carbon dioxide-containing waste gas, and the second output end of the dryer (44) is used to output the dehydrated carbon dioxide. The second output end of the dryer (44) is connected to the back-blowing input end of the desorption gas dedust tower (43) for back-blowing and dust removal of the desorbed carbon dioxide.

8. A ship flue gas denitration, desulfurization and decarbonization system according to claim 7, characterized in that: A smoke booster induced draft fan (5) and a smoke heat exchanger (6) are provided between the smoke input end of the denitrification mechanism (1) and the ship engine for conveying ship exhaust gas. The smoke input end of the smoke booster induced draft fan (5) is used to receive ship smoke. The smoke output end of the smoke booster induced draft fan (5) is connected to the smoke input end of the smoke heat exchanger (6). The smoke output end of the smoke heat exchanger (6) is connected to the smoke input end of the denitrification mechanism (1) via a bent pipe (8). The smoke input end of the smoke booster induced draft fan (5) is connected to the first output end of the dryer (44). The seawater output end of the smoke booster induced draft fan (5) is connected to the seawater output end of ... The inlet end and the seawater output end of the flue gas booster induced draft fan (5) are used to introduce flowing seawater to exchange heat with the ship's flue gas. The heat transfer oil input end of the flue gas heat exchanger (6) is connected to the heat transfer oil output end of the heating and decomposition conveying screw (42). The heat transfer oil output end of the flue gas heat exchanger (6) is connected to the heat transfer oil input end of the heating and decomposition conveying screw (42), so that the heat transfer oil circulates between the flue gas heat exchanger (6) and the heating and decomposition conveying screw (42), exchanges heat with the ship's flue gas in the flue gas heat exchanger (6), and performs heating and decomposition of the saturated solid amine in the heating and decomposition conveying screw (42).

9. A ship flue gas denitration, desulfurization and decarbonization system according to claim 7, characterized in that: The decarbonization mechanism (3) further comprises a solid amine feeding bin (71) and a solid amine unloading bin (72), a feeding control valve (73) and a unloading control valve (74); the output end of the solid amine feeding bin (71) is connected to the solid amine input end of the decarbonization tower (32) by means of a feeding control valve (73); the solid amine input end of the decarbonization tower (32) is located above the bed (35) so that the solid amine feeding bin (71) can transport the solid amine to be reacted into the bed (35) through the solid amine input end of the decarbonization tower (32); and the output end of the solid amine feeding bin (71) and the solid amine unloading bin (72) are connected by means of a unloading control valve (74).

10. A ship flue gas denitration, desulfurization and decarbonization system according to claim 9, characterized in that: The solid amine output end of the heating and decomposition conveying screw (42) is connected to a solid amine buffer silo (75), and the output end of the solid amine buffer silo (75) is merged into the output end of the solid amine feeding silo (71) for conveying the solid amine to be reacted.

Images