Power plant flue gas desulfurization system capable of improving desulfurization efficiency

Abstract

The utility model relates to the technical field of flue gas desulfurization, in particular to a power plant flue gas desulfurization system capable of improving desulfurization efficiency, which comprises a primary absorption tower, a secondary absorption tower, a carbide slag slurry tank and a limestone slurry tank, the first spraying layer and the third spraying layer are both connected with an outlet of the carbide slag slurry tank, an outlet of the limestone slurry tank is connected with the fourth spraying layer, and a bottom outlet of the secondary absorption tower is connected with the second spraying layer. The carbide slag slurry is used as a supplementary absorbent and can assist in absorbing SO2 residual gas which is not completely absorbed by the limestone slurry, so that the desulfurization reaction is more sufficient, and the desulfurization efficiency is improved; meanwhile, CaSO3 reacts with CO2 in the flue gas to generate CaSO3, and the CaSO3 can be used as supplement of limestone, so that the usage amount of the limestone is further reduced, and the operation cost is reduced.

Description

Technical Field

[0001] This application relates to the technical field of flue gas desulfurization, and particularly to a power plant flue gas desulfurization system for improving desulfurization efficiency. Background Art

[0002] With the gradual popularization of the concept of environmental sustainable development, waste smoke and exhaust gas in industrial and other fields need to meet certain standards before being discharged. Generally, flue gas is treated using desulfurization devices. Flue gas desulfurization refers to the process of removing sulfur dioxide from the flue gas discharged from coal-fired power plants, industrial boilers, etc. using desulfurization equipment.

[0003] The most common flue gas desulfurization methods are wet flue gas desulfurization and dry flue gas desulfurization. Wet flue gas desulfurization is achieved by spraying desulfurizing agents into the flue gas, causing a chemical reaction between sulfur dioxide and the desulfurizing agent (limestone or carbide slag) to generate calcium sulfate for removal. The limestone-gypsum desulfurization process is roughly as follows: The flue gas containing SO2 enters the absorption tower under the action of an induced draft fan. The absorption tower uses a countercurrent spraying structure to evenly spray limestone slurry into the tower. SO2 contacts the limestone slurry and is converted into calcium bisulfite Ca(HSO3)2. The calcium bisulfite and the limestone slurry form a solution that accumulates at the bottom of the absorption tower. Air is introduced into the solution, and the calcium bisulfite undergoes an oxidation reaction with the air to generate calcium sulfate CaSO4. When the calcium sulfate reaches a certain saturation, it crystallizes to form gypsum dihydrate. The gypsum dihydrate slurry is finally discharged from the absorption tower for cyclic dehydration treatment. The carbide slag-gypsum desulfurization method uses carbide slag slurry mainly composed of Ca(OH)2 to contact and mix with the flue gas in the absorption tower by spraying. SO2 in the flue gas undergoes a chemical reaction with Ca(OH)2 in the slurry and the injected oxidation air to be removed. The final reaction product is gypsum, thereby achieving the purpose of purifying the flue gas.

[0004] The limestone-gypsum desulfurization method requires a large amount of limestone consumption and has a high operating cost, while the desulfurization efficiency of the carbide slag-gypsum method is relatively low. Therefore, it is necessary to study a power plant flue gas desulfurization system that saves the usage amount of limestone and has a high desulfurization efficiency. Summary of the Invention

[0005] Based on this, this application provides a power plant flue gas desulfurization system for improving desulfurization efficiency to solve the technical problems in the prior art of consuming a large amount of limestone, having a high operating cost, and low desulfurization efficiency.

[0006] The technical solution for this application to solve the above technical problems is as follows:

[0007] A flue gas desulfurization system for power plants to improve desulfurization efficiency, comprising a primary absorption tower, a secondary absorption tower, a carbide slag slurry tank and a limestone slurry tank. In the height direction, a first spray layer and a second spray layer are arranged from top to bottom in the primary absorption tower, and a third spray layer and a fourth spray layer are arranged from top to bottom in the secondary absorption tower. The flue gas outlet of the primary absorption tower is connected to the flue gas inlet of the secondary absorption tower. The first spray layer and the third spray layer are both connected to the outlet of the carbide slag slurry tank, the outlet of the limestone slurry tank is connected to the fourth spray layer, and the bottom outlet of the secondary absorption tower is connected to the second spray layer.

[0008] Preferably, the above-mentioned flue gas desulfurization system for power plants to improve desulfurization efficiency further comprises a first oxidation blower, a second oxidation blower, a first air inlet pipe and a second air inlet pipe. One end of the first air inlet pipe is connected to the outlet of the first oxidation blower, and the other end is connected to the bottom of the primary absorption tower. One end of the second air inlet pipe is connected to the outlet of the second oxidation blower, and the other end is connected to the bottom of the secondary absorption tower.

[0009] Preferably, for the above-mentioned flue gas desulfurization system for power plants to improve desulfurization efficiency, the outlet of the first oxidation blower is also connected to the second air inlet pipe.

[0010] Preferably, for the above-mentioned flue gas desulfurization system for power plants to improve desulfurization efficiency, the primary absorption tower further comprises a first slurry circulation pump. The feed end of the first slurry circulation pump is connected to the bottom outlet of the primary absorption tower, and the discharge end of the first slurry circulation pump is connected to the second spray layer.

[0011] Preferably, for the above-mentioned flue gas desulfurization system for power plants to improve desulfurization efficiency, it further comprises a filtration assembly. A gypsum slurry outlet is arranged at the discharge end of the first slurry circulation pump. The gypsum slurry outlet is connected to the filtration assembly, and the filtrate outlet of the filtration assembly is connected to at least one of the carbide slag slurry tank and the limestone slurry tank.

[0012] Preferably, for the above-mentioned flue gas desulfurization system for power plants to improve desulfurization efficiency, the secondary absorption tower further comprises a second slurry circulation pump. The feed end of the second slurry circulation pump is connected to the bottom outlet of the secondary absorption tower, and the discharge end of the second slurry circulation pump is connected to the fourth spray layer.

[0013] Preferably, for the above-mentioned flue gas desulfurization system for power plants to improve desulfurization efficiency, the discharge end of the second slurry circulation pump is also connected to the feed end of the first slurry circulation pump.

[0014] Preferably, in the power plant flue gas desulfurization system for improving desulfurization efficiency, an electric control valve is provided between the outlet of the carbide slag slurry tank and the third spray layer. A flue gas detection device is also provided at the flue gas outlet of the first absorption tower, and the flue gas detection device is electrically connected to the electric control valve.

[0015] Adopting the technical solution of the present application has at least the following beneficial effects:

[0016] The power plant flue gas desulfurization system for improving desulfurization efficiency disclosed in the present application includes a first absorption tower, a second absorption tower, a carbide slag slurry tank, and a limestone slurry tank. In the height direction, a first spray layer and a second spray layer are arranged from top to bottom in the first absorption tower, and a third spray layer and a fourth spray layer are arranged from top to bottom in the second absorption tower. The flue gas outlet of the first absorption tower is connected to the flue gas inlet of the second absorption tower. The first spray layer and the third spray layer are both connected to the outlet of the carbide slag slurry tank, the outlet of the limestone slurry tank is connected to the fourth spray layer, and the bottom outlet of the second absorption tower is connected to the second spray layer.

[0017] When the flue gas enters the absorption tower from the side air inlet of the first absorption tower, it reacts with the limestone slurry (CaCO3). Some of the flue gas may not react completely, and there will be some residual SO2 gas. At this time, the carbide slag slurry (Ca(OH)2) transported to the first spray layer can assist in absorbing the residual SO2 gas that the limestone slurry has not completely absorbed, making the desulfurization reaction more complete, thereby improving the desulfurization efficiency. At the same time, Ca(OH)2 reacts with CO2 in the flue gas to generate CaCO3, which can be used as a supplement to limestone, further reducing the usage amount of limestone, and thus reducing the operating cost. The carbide slag slurry is transported to the third spray layer of the second absorption tower to react with the SO2 that has not been completely absorbed in the first absorption tower. While absorbing SO2, the CaCO3 generated in the second absorption tower is transported to the fourth spray layer of the first absorption tower as an absorbent for the first absorption tower, improving the utilization rate of the absorbent raw materials and further reducing the operating cost. The multi-layer spray layer structure design in the first absorption tower and the second absorption tower makes the desulfurization reaction in the tower more complete, further improving the desulfurization efficiency. Description of the Drawings

[0018] Figure 1 It is a device diagram of the power plant flue gas desulfurization system for improving desulfurization efficiency of the present application.

[0019] Wherein: primary absorption tower 100, first spray layer 110, second spray layer 120, first slurry circulation pump 130, gypsum slurry outlet 140, first oxidation blower 150, first air inlet pipe 160, secondary absorption tower 200, third spray layer 210, fourth spray layer 220, second slurry circulation pump 230, second oxidation blower 240, second air inlet pipe 250, carbide slag slurry tank 300, limestone slurry tank 400, electric control valve 500, flue gas detection device 600. Detailed implementation manners

[0020] For ease of understanding the present application, the present application will be described more comprehensively below with reference to the relevant drawings. Preferred embodiments of the present application are shown in the drawings. However, the present application can be implemented in many different forms and is not limited to the embodiments described herein. On the contrary, these embodiments are provided so that the disclosure of the present application can be understood more thoroughly and comprehensively.

[0021] It should be noted that when an element is referred to as being "disposed on" another element, it can be directly on the other element or there may also be an intermediate element. When an element is considered to be "connected" to another element, it can be directly connected to the other element or there may be an intermediate element at the same time. The terms "vertical", "horizontal", "left", "right", "top", "bottom", "bottom end", "top end" and similar expressions used herein are for illustrative purposes only and do not represent the only embodiments.

[0022] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those of ordinary skill in the technical field to which this application belongs. The terms used in the description of the present application herein are only for the purpose of describing specific embodiments and are not intended to limit the present application. The term "and / or" used herein includes any and all combinations of one or more of the related listed items.

[0023] Please refer to Figure 1, in a specific embodiment of the present application, a power plant flue gas desulfurization system for improving desulfurization efficiency includes a primary absorption tower 100, a secondary absorption tower 200, a carbide slag slurry tank 300, and a limestone slurry tank 400. In the height direction, a first spray layer 110 and a second spray layer 120 are arranged from top to bottom in the primary absorption tower 100, and a third spray layer 210 and a fourth spray layer 220 are arranged from top to bottom in the secondary absorption tower 200. The flue gas outlet of the primary absorption tower 100 is connected to the flue gas inlet of the secondary absorption tower 200. The first spray layer 110 and the third spray layer 210 are both connected to the outlet of the carbide slag slurry tank 300, the outlet of the limestone slurry tank 400 is connected to the fourth spray layer 220, and the bottom outlet of the secondary absorption tower 200 is connected to the second spray layer 120.

[0024] The absorption tower adopts a countercurrent spray tower. The first spray layer 110 and the second spray layer 120 are located between the flue gas inlet and the flue gas outlet of the primary absorption tower 100, and the third spray layer 210 and the fourth spray layer 220 are located between the flue gas inlet and the flue gas outlet of the secondary absorption tower 200. The flue gas outlet of the primary absorption tower 100 is connected to the flue gas inlet of the secondary absorption tower 200. The raw flue gas enters the primary absorption tower 100 from the side air inlet of the primary absorption tower 100. The flue gas contacts the mist-like absorbent slurry countercurrently in the primary absorption tower 100. Here, the flue gas is cooled and saturated, and the SO2 in the flue gas is absorbed for the first time. The treated flue gas is discharged from the top of the primary absorption tower 100 to the demister of the primary absorption tower 100 and then discharged from the flue gas outlet, and then enters the secondary absorption tower 200 again. The SO2 in the flue gas is absorbed again, and then the liquid droplets in the flue gas are removed through a dust removal and demisting device and discharged to the chimney. After being lifted to a certain height by the chimney, it is discharged into the atmosphere.

[0025] The flue gas absorbents in this solution are carbide slag slurry and limestone slurry, which are respectively stored in the carbide slag slurry tank 300 and the limestone slurry tank 400. The carbide slag slurry is respectively transported to the first spray layer 110 and the third spray layer 210. In the primary absorption tower 100, the carbide slag slurry is sprayed out in a mist through the nozzles of the first spray layer 110, contacts the flue gas to absorb SO2 therein, and at the same time reacts with CO2 in the flue gas to form CaCO3. CaCO3, as a supplement to the absorbent, continues to react with the flue gas to absorb SO2 in the flue gas to form gypsum CaSO4, which precipitates at the bottom of the absorption tower and is finally discharged. In the secondary absorption tower 200, the carbide slag slurry is sprayed out in a mist through the nozzles of the third spray layer 210, contacts the flue gas to absorb SO2 therein, and reacts with CO2 in the flue gas to form CaCO3; at the same time, the outlet of the limestone slurry tank 400 is connected to the fourth spray layer 220 of the secondary absorption tower 200, and the limestone slurry reacts with the SO2 that has not been completely absorbed in the primary absorption tower 100 to form gypsum. The CaCO3 formed by the reaction of the carbide slag slurry with the flue gas also serves as a supplement to the absorbent, that is, the limestone slurry, and continues to react with the flue gas. Due to the limestone slurry that has not been completely reacted in the reaction pool of the secondary absorption tower 200 and the limestone formed by the reaction of the carbide slag slurry with CO2 in the flue gas, in order to utilize this part of the limestone slurry, the bottom outlet of the secondary absorption tower 200 is connected to the second spray layer 120, and the slurry in the secondary absorption tower 200 is transported to the second spray layer of the primary absorption tower 100, where the unreacted limestone slurry participates in the desulfurization of the flue gas in the primary absorption tower 100 again as an absorbent.

[0026] The carbide slag slurry in this solution can assist in absorbing the residual SO2 gas that has not been completely absorbed by the limestone slurry, making the desulfurization reaction more complete, thereby improving the desulfurization efficiency; at the same time, Ca(OH)2 reacts with CO2 in the flue gas to form CaC03, which can be used as a supplement to limestone, further reducing the consumption of limestone, and thus reducing the operating cost; the carbide slag slurry is transported to the third spray layer 210 of the secondary absorption tower 200 to react with the SO2 that has not been completely absorbed in the primary absorption tower 100. While absorbing SO2, the CaCO3 formed in the secondary absorption tower 200 is transported to the fourth spray layer 220 of the primary absorption tower 100 and serves as an absorbent for the primary absorption tower 100, improving the utilization rate of the absorbent raw materials and further reducing the operating cost; the multi-layer spray layer structure design in the primary absorption tower 100 and the secondary absorption tower 200 makes the desulfurization reaction in the tower more complete and further improves the desulfurization efficiency.

[0027] In another specific embodiment of the present application, the flue gas desulfurization system of the power plant further includes a first oxidation blower 150, a second oxidation blower 240, a first air inlet pipe 160, and a second air inlet pipe 250. One end of the first air inlet pipe 160 is connected to the outlet of the first oxidation blower 150, and the other end is connected to the bottom of the first-stage absorption tower 100. One end of the second air inlet pipe 250 is connected to the outlet of the second oxidation blower 240, and the other end is connected to the bottom of the second-stage absorption tower 200.

[0028] Since a large amount of oxidation air is required for desulfurizing the flue gas in the absorption tower to fully and rapidly oxidize calcium sulfite in the slurry pool of the absorption tower, a first oxidation blower 150 is connected to the bottom of the first-stage absorption tower 100 through the first air inlet pipe 160. The first oxidation blower 150 blows oxidation air into the slurry pool of the first-stage absorption tower 100 to react with the slurry. The oxidation air is injected into the pressure side of the stirrer blades of the first-stage absorption tower 100 and is dispersed into fine bubbles and evenly distributed in the slurry by the pressure and shear force generated by the stirrer of the first-stage absorption tower 100. Part of the sulfite ions are oxidized by the oxygen in the flue gas in the spray zone of the absorption tower, and the remaining sulfite ions are completely oxidized by the oxidation air in the reaction pool. Similarly, a second oxidation blower 240 is connected to the bottom of the second-stage absorption tower 200 through the second air inlet pipe 250. The working principle and function of the second oxidation blower 240 are the same as those of the first oxidation blower 150. Further, in order to avoid frequent startup of the second oxidation blower 240, the outlet of the first oxidation blower 150 is also connected to the second air inlet pipe 250, reducing the running time of the second oxidation blower 240, ensuring sufficient oxidation of the slurry inside the first- and second-stage absorption towers 200, and achieving the purpose of energy saving while ensuring the optimization of system operation.

[0029] Further, the first-stage absorption tower 100 further includes a first slurry circulation pump 130. The feed end of the first slurry circulation pump 130 is connected to the bottom outlet of the first-stage absorption tower 100, and the discharge end of the first slurry circulation pump 130 is connected to the second spray layer 120. Since the first reaction pool is arranged at the bottom of the first-stage absorption tower 100 and the flow direction of the flue gas is from bottom to top, in order to enable the flue gas to make countercurrent contact with the absorbent, it is necessary to transport the absorbent to the second spray layer 120. Therefore, the first-stage absorption tower 100 is provided with a first slurry circulation pump 130 for transporting the absorbent in the reaction pool of the first-stage absorption tower 100 to the second spray layer 120. The absorbent is sprayed out in a mist form through the nozzles of the second spray layer 120 and reacts with the flue gas.

[0030] Further, the flue gas desulfurization system of the power plant further includes a filtering assembly. A gypsum slurry outlet 140 is provided at the discharge end of the first slurry circulation pump 130. The gypsum slurry outlet 140 is connected to the filtering assembly, and the filtrate outlet of the filtering assembly is connected to at least one of the carbide slag slurry tank 300 and the limestone slurry tank 400.

[0031] The gypsum slurry in the primary absorption tower 100 is transported to the filtering assembly through the gypsum slurry outlet 140. After being filtered and dewatered in the filtering assembly, the gypsum is discharged, and the filtrate is transported to the carbide slag slurry tank 300 or the limestone slurry tank 400, or can also be simultaneously transported to the carbide slag slurry tank 300 and the limestone slurry tank 400 for pulping.

[0032] Further, the secondary absorption tower 200 further includes a second slurry circulation pump 230. The feed end of the second slurry circulation pump 230 is connected to the bottom outlet of the secondary absorption tower 200, and the discharge end of the second slurry circulation pump 230 is connected to the fourth spray layer 220. Since the second reaction tank is arranged at the bottom of the secondary absorption tower 200 and the flow direction of the flue gas is from bottom to top, in order to enable the flue gas to contact the absorbent in a countercurrent manner, it is necessary to transport the absorbent to the fourth spray layer 220. Therefore, the secondary absorption tower 200 is provided with a second slurry circulation pump 230 for transporting the absorbent in the reaction tank of the secondary absorption tower 200 to the fourth spray layer 220. The absorbent is sprayed out in a mist form through the nozzles of the fourth spray layer 220 and reacts with the flue gas.

[0033] Preferably, the discharge end of the second slurry circulation pump 230 is further connected to the feed end of the first slurry circulation pump 130. Since there is unreacted limestone slurry in the reaction tank of the secondary absorption tower 200, in order to utilize this part of the limestone slurry, it is necessary to connect the bottom outlet of the secondary absorption tower 200 to the second spray layer 120, that is, to connect the discharge end of the second slurry circulation pump 230 to the feed end of the first slurry circulation pump 130, so as to transport the slurry in the secondary absorption tower 200 to the second spray layer of the primary absorption tower 100, and the unreacted limestone slurry participates in the desulfurization of the flue gas in the primary absorption tower 100 as an absorbent again.

[0034] In yet another specific embodiment of the present application, an electric control valve 500 is provided between the outlet of the carbide slag slurry tank 300 and the third spray layer 210, and a flue gas detection device 600 is further provided at the flue gas outlet of the primary absorption tower 100. The flue gas detection device 600 and the electric control valve 500 are electrically connected. Specifically, the flue gas detection device 600 can detect the SO2 emission at the flue gas outlet of the primary absorption tower 100, and according to the amount of SO2 emission, feedback a signal to the electric control valve 500. The electric control valve 500 adjusts the opening degree accordingly, thereby controlling the flow rate of the carbide slag slurry in the pipeline, achieving dynamic control and saving raw materials.

[0035] The specific working process is as follows:

[0036] The absorption tower adopts a countercurrent spray tower. The flue gas from the outlet of the induced draft fan enters the primary absorption tower 100 from the side air inlet of the primary absorption tower 100. The flue gas contacts the mist-like slurry countercurrently in the primary absorption tower 100. Here, the flue gas is cooled and saturated, and the SO2 in the flue gas is absorbed for the first time. The treated flue gas is discharged from the top of the primary absorption tower 100 to the demister of the primary absorption tower 100 and then enters the secondary absorption tower 200 again. The SO2 in the flue gas is absorbed once again, and then the droplets in the flue gas are removed through the dust and mist removal device and discharged to the chimney. After being lifted to a certain height by the chimney, it is discharged into the atmosphere. Among them, during the working process of the primary absorption tower 100, the carbide slag slurry is transported to the first spray layer 110 and sprayed in a mist form through the nozzles arranged on the first spray layer 110 and countercurrent to the flue gas. In this process, the flue gas makes effective contact with the carbide slag slurry sprayed from the nozzles of the absorption tower, and the slurry that has absorbed SO2 falls into the reaction pool of the absorption tower; the first slurry circulation pump 130 continues to transport the slurry in the reaction pool to the second spray layer 120 to continue reacting with the flue gas. At the same time, the first slurry circulation pump 130 also transports the slurry from the secondary absorption tower 200 to the second spray layer 120 at the same time; to fully and rapidly oxidize the calcium sulfite in the reaction pool, an oxidation air assembly is provided. The oxidation air is injected into the reaction pool of the primary absorption tower 100 by the first oxidation fan 150. Part of the HSO3 － is oxidized by the oxygen in the flue gas in the spray area of the absorption tower, and the remaining part of HSO3 － is completely oxidized by the oxidation air in the reaction pool.

[0037] During the operation of the secondary absorption tower 200, the limestone slurry is conveyed to the fourth spray layer 220 and sprayed in a mist through the nozzles arranged on the fourth spray layer 220 and countercurrent to the flue gas. During this process, the flue gas makes effective contact with the first turbid liquid sprayed from the absorption tower nozzles, and the slurry that has absorbed SO2 falls into the reaction tank of the absorption tower. At the same time, the carbide slag slurry is conveyed to the third spray layer 210 to continue reacting with the flue gas to further absorb the SO2 that has not been completely absorbed by the limestone slurry. Similarly, the slurry that has absorbed SO2 falls into the reaction tank of the absorption tower. At this time, the reaction tank of the secondary absorption tower 200 contains unreacted limestone slurry and limestone formed by the reaction of carbide slag slurry with CO2 in the flue gas. Therefore, the slurry in the reaction tank of the secondary absorption tower 200 is simultaneously conveyed to the second spray layer 120 of the primary absorption tower 100 to react with the flue gas again as an absorbent. To fully and rapidly oxidize calcium sulfite in the reaction tank, an oxidation air assembly is provided, and the oxidation air is injected into the reaction tank of the secondary absorption tower 200 by the second oxidation blower 240. Part of HSO3 － is oxidized by the oxygen in the flue gas in the spray area of the absorption tower, and the remaining part of HSO3 － is completely oxidized by the oxidation air in the reaction tank.

[0038] During the desulfurization process of the two-stage absorption tower, the flue gas detection device 600 continuously detects the SO2 emission at the flue gas outlet of the primary absorption tower 100. According to the amount of SO2 emission, a feedback signal is sent to the electric control valve 500, and the electric control valve 500 adjusts the opening accordingly to control the flow rate of the carbide slag slurry in the pipeline, achieving the purpose of dynamic control and saving raw materials.

[0039] The above-disclosed are only the preferred embodiments of the present application. Of course, the scope of rights of the present application cannot be limited thereby. Those of ordinary skill in the art can understand all or part of the processes of implementing the above embodiments, and the equivalent changes made according to the claims of the present application still fall within the scope covered by the present application.

Claims

1. A power plant flue gas desulfurization system for improving desulfurization efficiency, characterized in that: It includes a primary absorption tower, a secondary absorption tower, a carbide slag slurry tank and a limestone slurry tank. In the height direction, the first absorption tower is provided with a first spray layer and a second spray layer from top to bottom, and the secondary absorption tower is provided with a third spray layer and a fourth spray layer from top to bottom. The smoke outlet of the first absorption tower is connected to the smoke inlet of the secondary absorption tower, the first spray layer and the third spray layer are both connected to the outlet of the carbide slag slurry tank, the outlet of the limestone slurry tank is connected to the fourth spray layer, and the bottom outlet of the secondary absorption tower is connected to the second spray layer.

2. The power plant flue gas desulfurization system for improving desulfurization efficiency according to claim 1 is characterized in that: It also includes a first oxidation fan, a second oxidation fan, a first air inlet pipe and a second air inlet pipe, one end of the first air inlet pipe is connected to the outlet of the first oxidation fan, and the other end is connected to the bottom of the first-level absorption tower, one end of the second air inlet pipe is connected to the outlet of the second oxidation fan, and the other end is connected to the bottom of the second-level absorption tower.

3. The power plant flue gas desulfurization system for improving desulfurization efficiency according to claim 2 is characterized in that: The outlet of the first oxidation blower is also connected to the second air inlet pipe.

4. The power plant flue gas desulfurization system for improving desulfurization efficiency according to claim 1, characterized in that: The primary absorption tower further comprises a first slurry circulation pump, a feed end of the first slurry circulation pump is connected to the bottom outlet of the primary absorption tower, and a discharge end of the first slurry circulation pump is connected to the second spray layer.

5. The power plant flue gas desulfurization system for improving desulfurization efficiency according to claim 4 is characterized in that: It also includes a filtering component, wherein the discharge end of the first slurry circulation pump is provided with a gypsum slurry outlet, the gypsum slurry outlet is connected to the filtering component, and the filtrate outlet of the filtering component is connected to at least one of the carbide slag slurry tank and the limestone slurry tank.

6. The power plant flue gas desulfurization system for improving desulfurization efficiency according to claim 4 is characterized in that: The secondary absorption tower also includes a second slurry circulation pump, a feed end of the second slurry circulation pump is connected to the bottom outlet of the secondary absorption tower, and a discharge end of the second slurry circulation pump is connected to the fourth spray layer.

7. The power plant flue gas desulfurization system for improving desulfurization efficiency according to claim 6, characterized in that: The discharge end of the second slurry circulation pump is also connected to the feed end of the first slurry circulation pump.

8. The power plant flue gas desulfurization system for improving desulfurization efficiency according to claim 1, characterized in that: An electric regulating valve is arranged between the outlet of the carbide slag slurry tank and the third spray layer, and a smoke detection device is also arranged at the smoke outlet of the primary absorption tower, and the smoke detection device is electrically connected to the electric regulating valve.

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