An integrated dual tray for a wet flue gas desulfurization absorber

Abstract

The application discloses an integrated double tray for a wet flue gas desulfurization absorption tower, and relates to the technical field of flue gas desulfurization; it comprises a tray body; a slurry pool, a desulfurization reaction zone, a flue gas demisting zone and a flue gas outlet are sequentially arranged in the absorption tower from bottom to top; the desulfurization reaction zone comprises a flue gas inlet and a spraying layer from bottom to top; the flue gas inlet is arranged on the side wall of the absorption tower; the tray body is located between the flue gas inlet and the spraying layer; the upper surface of the bottom of the first layer of tray is a first liquid accumulation layer, and the upper surface of the bottom of the second layer of tray is a second liquid accumulation layer. The upper surface of the top of the first layer of tray is tightly attached to the lower surface of the bottom of the second layer of tray, the two layers of trays are closely stacked, the secondary flow deviation of flue gas can be avoided, the rectification effect is continuously stable, the double-layer plate surface is stacked to form a continuous bubbling liquid layer, the gas-liquid contact time is prolonged, and the desulfurization reaction of high-sulfur flue gas is strengthened.

Description

Technical Field

[0001] This invention relates to the field of flue gas desulfurization technology, and more specifically, it is an integrated double-pallet system for wet flue gas desulfurization absorption towers, which is particularly suitable for gas-liquid mass transfer enhancement and multi-pollutant synergistic removal in countercurrent spray absorption towers in industries such as coal-fired power plants, steel, and coking. Background Technology

[0002] Limestone-gypsum wet flue gas desulfurization (WFGD) has become the mainstream flue gas purification technology in industries such as coal-fired power plants, steel, and coking due to its high desulfurization efficiency, mature technology, and the resource utilization of by-products. Its core equipment is a counter-current spray desulfurization absorption tower. SO2-containing flue gas flows upward from the bottom of the tower and comes into counter-current contact with limestone slurry sprayed from top to bottom. SO2 absorption and chemical reaction are completed through gas-liquid two-phase mass transfer, thus achieving flue gas purification. However, the problems commonly found in the desulfurization process, such as uneven distribution of flue gas flow field, easy deviation and short-circuiting of flue gas, insufficient gas-liquid contact area, and low mass transfer efficiency, directly or indirectly affect the desulfurization efficiency.

[0003] Existing technologies mostly improve desulfurization efficiency by increasing the liquid-to-gas ratio and the number of spray layers. However, this leads to increased energy consumption and operating costs. Furthermore, desulfurization stability is poor when the unit load fluctuates or the flue gas dust content is high, making it difficult to meet the latest ultra-low emission control requirements. This is especially true for applications burning high-sulfur coal or treating high-sulfur flue gas (SO2 concentration ≥ 10000 mg / Nm³). 3 Even as high as 12500 mg / Nm 3 Under the above operating conditions, the limitations of traditional desulfurization technology are drastically amplified: on the one hand, in order to achieve 35mg / Nm³, 3 To meet ultra-low emission limits, the theoretical desulfurization efficiency needs to reach over 99.5%, which requires a liquid-to-gas ratio generally exceeding 15 L / Nm³. 3 The number of spray layers can be as high as 5-6, which leads to a significant increase in the power consumption of the circulating pump, slurry preparation and operation and maintenance costs. On the other hand, the absorption reaction of high concentration SO2 is violent, and the local pH value fluctuates greatly. It is easy to form serious scaling on the tray, spray layer and tower wall, which further deteriorates the uniformity of the flow field, causes gas-liquid short circuit, and the actual desulfurization efficiency is far lower than the design value, and there is even a risk of exceeding the emission standards.

[0004] To optimize airflow distribution and enhance gas-liquid mass transfer efficiency within the tower, porous trays have gradually become one of the core internal components of absorption towers. Currently, there are three mainstream structures: single-layer, double-layer, and multi-layer, each with its own advantages and disadvantages. Single-layer trays are simple in structure, have low resistance, and low maintenance costs, but they only provide preliminary rectification and mass transfer, and are prone to problems such as flue gas deviation, scaling and pore blockage, resulting in poor performance under low load. Multi-layer trays with three or more layers offer better mass transfer and desulfurization effects, but their system resistance, energy consumption, and cost are higher, and they carry a greater risk of scaling, thus limiting their engineering application in the short term. Double-layer trays offer outstanding overall performance, providing two-stage rectification... While improving airflow distribution and resistance with controllable costs, double-layer trays are the mainstream solution for ultra-low emission projects. However, existing double-layer trays are mostly simple stacked designs without integrated optimization, which cannot match the non-uniform flow field inside the tower. Furthermore, the lack of coordinated design between the upper and lower trays leads to problems such as secondary airflow deviation and frequent slurry blockage on the tray surface. This makes it impossible to achieve efficient, low-resistance, and stable gradient gas-liquid mass transfer enhancement and desulfurization effect improvement. It also lacks the ability to actively intercept and capture fine dust, gypsum slurry droplets, and SO3 aerosols carried in the flue gas, making it difficult to meet the requirements for coordinated control of multiple pollutants.

[0005] Therefore, it is necessary to develop an integrated dual-pallet system for wet flue gas desulfurization that can achieve deep enhancement of gas-liquid mass transfer, improve desulfurization efficiency to over 99.5%, and simultaneously possess efficient synergistic capture capabilities for fine particulate matter, gypsum droplets, and SO3 acid mist, thereby completing integrated synergy of "desulfurization-dust removal-mist removal" within the desulfurization tower and reducing or even replacing the load of subsequent wet electrostatic precipitators. Summary of the Invention

[0006] The purpose of this invention is to overcome the shortcomings of the above-mentioned background technology and provide an integrated dual-pallet system for wet flue gas desulfurization absorption towers, which solves the problems of uneven flue gas flow field distribution, easy flue gas deflection and short circuit, insufficient gas-liquid contact area, and low mass transfer efficiency in existing wet desulfurization technologies.

[0007] To achieve the above objectives, the technical solution of the present invention is as follows: an integrated double-pallet system for a wet flue gas desulfurization absorption tower, comprising a pallet body disposed within the absorption tower; the absorption tower is provided with a slurry pool, a desulfurization reaction zone, a flue gas demisting zone, and a flue gas outlet arranged sequentially from bottom to top; the desulfurization reaction zone includes a flue gas inlet and a spray layer from bottom to top; the flue gas inlet is disposed on the side wall of the absorption tower; characterized in that: The tray body is located between the flue gas inlet and the spray layer. The tray body includes a first tray and a second tray. The top surface of the first tray is in close contact with the bottom surface of the second tray. The first tray has a plurality of first channels spaced apart. The second tray has a plurality of second channels spaced apart. The first channels and the second channels correspond one-to-one. The bottom upper surface of the first layer tray is the first liquid accumulation layer, and the bottom upper surface of the second layer tray is the second liquid accumulation layer.

[0008] In the above technical solution, both the first and second trays are divided into a central area, an intermediate ring area, and an edge ring area from the center towards the tower wall. The diameter of the first and second channels in the central area is larger than the diameter of the first and second channels in the intermediate ring area. The diameter of the first and second channels in the intermediate ring area is larger than the diameter of the first and second channels in the edge ring area.

[0009] In the above technical solution, the diameter of the first channel gradually decreases from bottom to top; the diameter of the second channel gradually increases from bottom to top.

[0010] In the above technical solution, the diameter of the top of the first channel is the same as the diameter of the bottom of the second channel, and the diameter of the bottom of the first channel is the same as the diameter of the top of the second channel.

[0011] In the above technical solution, the tray body is tilted at an angle of 1°-4°, and the slurry forms a continuously flowing tilted liquid film on the upper surface of the tray body.

[0012] In the above technical solution, multiple spraying devices are arranged at intervals from bottom to top in the spraying layer; a mechanical demister is arranged in the flue gas demisting zone; flushing pipes are arranged above and below the mechanical demister; and the slurry tank is connected to the spraying device through a circulating pump.

[0013] In the above technical solution, the vertical distance from the lower surface of the first layer tray to the flue gas inlet is 400-1200mm, and the vertical distance from the upper surface of the second layer tray to the spray device in the lowest layer of the spray layer is 1000-1500mm. The center area, middle ring area, and edge ring area of ​​the first and second layer trays are divided into three equal parts by radius.

[0014] In the above technical solution, the diameter of the bottom of the first channel is 39-41mm in the central area, 33-35mm in the middle ring area, and 27-29mm in the edge ring area; the diameter of the top of the first channel is 30-32mm in the central area, 25-27mm in the middle ring area, and 19-21mm in the edge ring area. The diameter of the bottom of the second channel is 30-32 mm in the central area, 25-27 mm in the middle ring area, and 19-21 mm in the edge ring area. The diameter of the top of the second channel is 39-41 mm in the central area, 33-35 mm in the middle ring area, and 27-29 mm in the edge ring area.

[0015] In the above technical solution, the central area of ​​the first and second trays and the rectangular area from the central area to the side near the flue gas inlet are combined into a high-speed zone, and the remaining parts of the first and second trays are low-speed zones; the opening ratio of the first and second channels in the high-speed zone is less than that of the first and second channels in the low-speed zone.

[0016] Compared with the prior art, the present invention has the following advantages: 1) The present invention tightly attaches the top surface of the first layer tray to the bottom surface of the second layer tray. The two layers of trays are tightly stacked to prevent secondary flow of flue gas and ensure continuous and stable rectification effect. The double-layer plate surface is stacked to form a continuous bubbling liquid layer, which prolongs the gas-liquid contact time and enhances the desulfurization reaction of high sulfur flue gas. At the same time, the first and second liquid layers are used to achieve dust classification and collection, which can also reduce the space occupied in the tower and effectively reduce the equipment infrastructure cost.

[0017] 2) The present invention is in close contact with the top surface of the first tray and the bottom surface of the second tray, dividing the tray into a central area, an intermediate ring area and an edge ring area. The aperture of the first channel and the second channel gradually decreases from the center of the tray to the tower wall. The flow resistance of each area of ​​the tray is adjusted by the aperture difference. The resistance difference brought by the aperture of the first channel and the second channel is used to guide the high-speed central flue gas and throttle and constrain the stagnant airflow on the wall, thereby correcting the defects in cross-sectional velocity distribution.

[0018] 3) In this invention, the top surface of the first tray and the bottom surface of the second tray are in close contact. The tray is divided into a central area, an intermediate ring area, and an edge ring area. The diameters of the first and second channels gradually decrease from the center of the tray towards the tower wall. The diameter of the first channel gradually decreases from bottom to top, while the diameter of the second channel gradually increases from bottom to top. There are no straight sections of trumpet-shaped conical channels. The first channel narrows from bottom to top to form a throttling and acceleration effect. The flue gas impacts the sprayed slurry upward to form a bubbling layer, which strengthens the gas-liquid contact. The resistance difference brought by the partitioned aperture guides the high-speed flue gas in the center and constrains the airflow along the edge wall, avoiding short-circuit flow of flue gas and achieving initial uniform distribution of flue gas, improving the flow field inside the tower and enhancing the desulfurization stability. The cross-section of the second channel gradually expands from bottom to top. The expansion effect reduces the flue gas velocity and achieves secondary fine uniform distribution of the rectified flue gas in the lower layer. The zoned variable diameter creates differentiated flow resistance, diverting excess airflow in the center and confining flue gas adhering to the edge walls. The airflow is cut and dispersed through the channels to form fine bubbles, generating a uniform bubbling turbulence zone above the plate surface. A stable second liquid layer remains on the upper surface of the second channel, where bubbles turbulent and continuously renew the liquid film, expanding the gas-liquid contact area and reducing SO2 mass transfer resistance. This allows the flue gas to fully complete the deep mass transfer reaction, achieving integrated flue gas deceleration, fine rectification, bubble refinement, and efficient desulfurization. The opening directions of the first and second channels are completely opposite, forming a reverse convection structure. This causes the first tray to increase the flue gas velocity, strengthen gas-liquid turbulence, and perform primary dispersion and rectification of the flue gas. The second tray reduces the flue gas velocity, stabilizes the upper flue gas flow field, and prolongs the gas-liquid two-phase contact reaction time.

[0019] 4) The tray body of the present invention is generally set with a slight inclination in the same direction, and the upper and lower surfaces of the tray body cooperate and regulate the flow of the medium in both directions. This design has multiple advantages in optimizing the flue gas flow field and improving the reliability of equipment operation. The inclined surface of the lower surface of the tray body can divert and redirect the deflected flue gas, disperse the vortex formed in the tower bottom and tower wall areas, and guide the flue gas to converge in the middle of the tray body, eliminating the dead angle of low-speed airflow stagnation from the source. Meanwhile, under its own weight, the slurry on the upper surface of the tray body flows from the high end to the low end, forming a differentiated liquid film distribution. The slurry flow rate is fast and the liquid film is thin at the high end of the tray body, resulting in lower resistance to flue gas passage; while the slurry converges and the liquid film is thicker at the low end of the tray body, resulting in relatively greater resistance to flue gas passage. Utilizing the natural resistance difference of the tray surface, the flue gas will spontaneously diffuse towards the high-end area with lower resistance, achieving a secondary uniform distribution in the lateral direction, effectively suppressing flue gas deviation and local short-circuiting problems. In addition, the continuously flowing slurry will not stand still on the plate surface, completely avoiding the accumulation, blockage and scaling of slurry and solid impurities, and ensuring the long-term stable operation of the equipment.

[0020] 5) This invention possesses significant synergistic dust removal capabilities; the upward-flowing flue gas sequentially passes through the first and second trays; in the first tray, the high-speed flue gas is throttled and accelerated through the inverted trumpet-shaped first channel with gradually decreasing aperture from bottom to top, impacting the first liquid accumulation layer of the first tray to form a strongly turbulent bubbling zone. The fine dust, gypsum slurry droplets, and SO3 aerosols carried in the flue gas collide, wet, and condense with the slurry film, and are initially captured and enter the slurry circulation; in the second tray, the flue gas is expanded and decelerated through the upright trumpet-shaped second channel with gradually increasing aperture from bottom to top, forming uniform and dense bubbles in the stable second liquid accumulation layer of the second tray. The remaining fine particles fully contact the inclined liquid film during the bubble disturbance process and are captured by secondary washing; the plate surface liquid layers of the two trays synergistically constitute a dust removal path of "graded interception and step-by-step washing", significantly improving the capture efficiency of PM2.5 and smaller fine particles.

[0021] 6) The continuously flowing inclined liquid film on the upper surface of the tray body of the present invention can effectively remove the captured solid particles, prevent dust and scale buildup on the tray surface, and ensure long-term stable operation.

[0022] 7) The first and second channels of the present invention adopt a smooth conical inclined surface structure, and there are no right angles, sharp corners or other areas that are prone to material accumulation on the inner wall of the channel, thus completely eliminating dead corners for material accumulation from the structure. For flue gas media containing dust and solid impurities, the continuous and smooth conical surface can greatly reduce the adhesion and retention of impurities, effectively reduce the probability of channel blockage, and ensure smooth medium flow. The overall hole shape transition is gentle, the medium flow resistance is small, further improving the flow stability and extending the effective service life of the channel.

[0023] 8) The pallet body of the present invention can also serve as a maintenance support platform. When inspecting the internal components of the tower, there is no need to drain the slurry of the tower body or set up an additional temporary maintenance frame. Maintenance personnel can directly carry out internal component inspection and replacement work based on the pallet body surface, shortening maintenance time, optimizing the convenience of equipment operation and maintenance, and reducing operation and maintenance costs.

[0024] In summary, this invention can simultaneously achieve efficient desulfurization and deep dust removal within the absorption tower, realizing integrated synergy of "desulfurization-dust removal-mist removal". Attached Figure Description

[0025] Figure 1 This is a schematic diagram of the structure of Example 1.

[0026] Figure 2 This is a schematic diagram of the tray body in Example 1.

[0027] Figure 3 This is a schematic diagram of the lower surface of the first tray in Example 2.

[0028] Figure 4 This is a schematic diagram of the upper surface of the first layer tray in Example 2.

[0029] Figure 5 This is a schematic diagram of the lower surface of the second tray in Example 2.

[0030] Figure 6 This is a schematic diagram of the upper surface of the second layer tray in Example 2.

[0031] Figure 7 This is a schematic diagram of the tray body in Example 2.

[0032] Figure 8 This is a schematic diagram of the tray body in Example 3.

[0033] Figure 9 This is a schematic diagram of a split-type dual-tray design in the prior art.

[0034] Figure 10 This is a schematic diagram of the structure of Example 4.

[0035] Figure 11 This is a schematic diagram of a continuous bubbling liquid layer in the tray body.

[0036] Figure 12 This is a schematic diagram of the tray body in Example 6.

[0037] Among them, 100-tray body, 110-first layer tray, 111-first channel, 120-second layer tray, 121-second channel, 131-first liquid accumulation layer, 132-second liquid accumulation layer, 140-continuous bubbling liquid layer, 200-absorption tower, 210-slurry pool, 211-circulating pump, 220-desulfurization reaction zone, 221-flue gas inlet, 222-spray layer, 2221-spray device, 230-flue gas demisting zone, 231-mechanical demister, 232-flushing pipeline, 240-flue gas outlet, A-central zone, B-intermediate ring zone, C-edge ring zone, D-high speed zone, E-low speed zone. Detailed Implementation

[0038] The embodiments of the present invention will be described in detail below with reference to the accompanying drawings, but these descriptions are not intended to limit the invention and are merely illustrative. The advantages of the present invention will become clearer and easier to understand through this description.

[0039] like Figure 1 As shown, an integrated double-pallet system for a wet flue gas desulfurization absorption tower includes a pallet body 100 disposed within an absorption tower 200; the absorption tower 200 is provided with, from bottom to top, a slurry pool 210, a desulfurization reaction zone 220, a flue gas demisting zone 230, and a flue gas outlet 240; the desulfurization reaction zone 220 includes, from bottom to top, a flue gas inlet 221 and a spray layer 222; the flue gas inlet 221 is disposed on the side wall of the absorption tower 200; characterized in that: The tray body 100 is located between the flue gas inlet 221 and the spray layer 222. The tray body 100 includes a first tray 110 and a second tray 120. The top upper surface of the first tray 110 is in close contact with the bottom lower surface of the second tray 120. The first tray 110 has a plurality of first channels 111 spaced apart. The second tray 120 has a plurality of second channels 121 spaced apart. The first channels 111 and the second channels 121 correspond one-to-one. The bottom upper surface of the first layer tray 110 is the first liquid accumulation layer 131, and the bottom upper surface of the second layer tray 120 is the second liquid accumulation layer 132.

[0040] The pallet body 100 is made of high-strength corrosion-resistant alloy plate. The entire pallet body 100 has reliable load-bearing capacity and is fixedly installed inside the absorption tower 200. When the equipment inside the tower is under maintenance, there is no need to drain the slurry at the bottom of the tower or set up temporary maintenance scaffolding on site. Maintenance personnel can stand directly on the pallet body 100 and perform maintenance and disassembly on the internal components such as spray pipes and nozzles of the tower nearby, which shortens the on-site maintenance construction cycle and reduces maintenance costs.

[0041] like Figures 2-5 As shown, both the first layer tray 110 and the second layer tray 120 are divided into a central area A, an intermediate ring area B, and an edge ring area C from the center towards the tower wall. The first layer tray 110 and the second layer tray 120 adopt concentric circular gradient irregular openings. The diameter of the first channel 111 and the second channel 121 in the central area A is larger than the diameter of the first channel 111 and the second channel 121 in the intermediate ring area B. The diameter of the first channel 111 and the second channel 121 in the intermediate ring area B is larger than the diameter of the first channel 111 and the second channel 121 in the edge ring area C.

[0042] like Figure 6 As shown, the first channel 111 and the second channel 121 form a trumpet-shaped channel without a straight section. The diameter of the first channel 111 gradually decreases from bottom to top, forming an inverted trumpet-shaped hole; the diameter of the second channel 121 gradually increases from bottom to top, forming a positive trumpet-shaped hole. During operation, the gradient opening adapts to the gas-liquid load of each zone, balances the degree of slurry disturbance on the board surface, makes the liquid holding thickness uniform throughout the entire area, avoids the problems of slurry accumulation and blockage of holes and local dry board leakage, ensures consistent bubbling intensity throughout the board surface, reduces ineffective slurry spraying, and achieves a decrease in the liquid-gas ratio of the system and energy-saving long-term operation.

[0043] Both the first channel 111 and the second channel 121 are designed with a smooth conical inclined surface structure, with no right angles or sharp corners on the inner wall of the channel, eliminating dead corners for material accumulation from the structural source. For the complex flue gas conditions containing dust and solid impurities within the absorption tower 200, the continuous smooth conical inner wall reduces the adhesion and retention of dust and impurities, effectively avoiding channel blockage and ensuring stable flue gas flow. At the same time, the overall diameter transition of the channel is gentle, resulting in less resistance to flue gas flow, further improving the stability of flue gas flow within the tower and extending the long-term service life of the tray channels.

[0044] The diameter of the top of the first channel 111 is the same as the diameter of the bottom of the second channel 121, and the diameter of the bottom of the first channel 111 is the same as the diameter of the top of the second channel 121.

[0045] like Figure 1 As shown, the tray body 100 is inclined at an angle of 1°-4°, forming a continuously flowing inclined liquid film on the upper surface of the tray body 100. The inclined surface of the lower surface of the tray body 100 can divert and redirect the deflected flue gas in the tower, disperse the vortex between the tower wall and the bottom of the tray, and guide the flue gas to converge towards the middle of the tray body 100, eliminating dead zones where the airflow stagnates at low speeds. The slurry on the upper surface of the tray body 100 flows from the high end to the low end by its own weight, forming a differentiated liquid film of varying thickness. Relying on the difference in flue gas flow resistance on the tray body 100, the flue gas is driven to redistribute laterally, further suppressing flue gas deflection and short-circuiting problems. At the same time, the slurry always maintains a dynamic flow state, avoiding the accumulation of slurry and impurities on the tray body 100, effectively preventing equipment scaling and blockage, and ensuring the long-term continuous and stable operation of the desulfurization tower.

[0046] The spray layer 222 is provided with multiple spray devices 2221 at intervals from bottom to top. The superposition of multiple sprays ensures sufficient spray intensity, allowing the desulfurization slurry to evenly cover the entire flow section of the tower body and meet the desulfurization reaction requirements under different loads. The multi-layer spray devices 2221 work together to achieve a single spray layer coverage of up to 180%, and the overall stacked coverage of the entire tower can reach up to 320%. This ensures that the desulfurization slurry fully and evenly covers the entire flue gas flow section of the absorption tower, leaving no blank spray areas. The multi-layer spray devices 2221 can flexibly match the unit's 30%-110% full-load variable operating conditions. Under low-load conditions, some spray layers can be started and stopped as needed to adapt to the operating conditions, while under high-load conditions, all spray layers can be opened to ensure the spray liquid volume, maintaining a stable and sufficient spray intensity at all times. This effectively avoids the problems of flue gas escape and insufficient gas-liquid contact. In conjunction with the 100mm rectifier mass transfer structure of the tray body, it fills in the gas-liquid contact blind spots, eliminates flue gas short-circuit escape, further consolidates the foundation of the desulfurization reaction, and ensures stable ultra-low emissions of flue gas under all operating conditions of the unit.

[0047] A mechanical demister 231 is installed within the flue gas demisting zone 230 to ensure effective demisting. Flushing pipes 232 are installed above and below the mechanical demister 231, enabling comprehensive cleaning and timely removal of liquid and scale buildup on the demister 231's plates. This ensures long-term stable operation of the mechanical demister 231, effectively improving overall demisting efficiency and achieving compliant flue gas emissions. Slurry droplets and fine dust entrained in the flue gas easily adhere to the surface of the mechanical demister 231, and long-term accumulation can cause channel blockage, reduced demisting capacity, and lead to liquid and particulate matter exceeding standards in the flue gas. The bidirectional flushing system thoroughly removes deposits from both sides of the blades, completely eliminating cleaning blind spots and ensuring stable demisting performance. It effectively removes liquid droplets and solid impurities from the flue gas, ensuring clean exhaust gas that meets environmental emission standards. Simultaneously, it prevents demister blockage and failure, extending equipment operating cycles and reducing maintenance workload.

[0048] The slurry tank 210 is connected to the spraying device 2221 via a circulating pump 211.

[0049] Flue gas enters the absorption tower 200 through flue gas inlet 221, and after passing through tray body 100, multi-layer spray device 2221 and mechanical demister 231 to remove pollutants, it is discharged from flue gas outlet 240.

[0050] The vertical distance from the lower surface of the first layer tray 110 to the flue gas inlet 221 is 400-1200mm, and the vertical distance from the upper surface of the second layer tray 120 to the lowest spray device 2221 in the spray layer 222 is 1000-1500mm.

[0051] Both the first-layer tray 110 and the second-layer tray 120 are divided into three equal-width central areas A, intermediate ring areas B, and edge ring areas C, based on the center of the circle and the effective opening radius. The central area A extends from the center to 1 / 3 of the radius, the intermediate ring area B is between 1 / 3 and 2 / 3 of the radius, and the edge ring area C extends from 2 / 3 of the radius to the outer edge of the tray. The three ring areas are of equal width.

[0052] The aperture at the bottom of the first channel 111 is 39-41 mm in the central region A, 33-35 mm in the middle ring region B, and 27-29 mm in the edge ring region C. The aperture at the top of the first channel 111 is 30-32 mm in the central region A, 25-27 mm in the middle ring region B, and 19-21 mm in the edge ring region C. During operation, the gradually narrowing channel has a throttling and speed-up effect, enhances flue gas disturbance, and the flue gas impacts the sprayed slurry upward to form a primary bubbling layer, optimizing the gas-liquid contact effect. At the same time, the zoned gradient aperture creates differentiated flow resistance, guides the high-speed flue gas in the center, blocks the airflow adhering to the wall, avoids flue gas short-circuiting and deflection, achieves initial uniform distribution of flue gas, and regulates the flow field inside the tower.

[0053] The aperture of the second channel 121 at the bottom is 30-32 mm in the central region A, 25-27 mm in the middle ring region B, and 19-21 mm in the edge ring region C. The aperture of the second channel 121 at the top is 39-41 mm in the central region A, 33-35 mm in the middle ring region B, and 27-29 mm in the edge ring region C. During operation, the gradually expanding channel has a capacity-expanding and decelerating effect, refining and breaking up the upward flue gas to form fine bubbles. A stable liquid layer is left on the plate surface, and the bubble disturbance continuously renews the liquid film and expands the gas-liquid contact area. At the same time, the zoned gradient aperture creates differentiated flow resistance, guiding the excess airflow in the center and binding the airflow adhering to the edge wall, achieving secondary fine and uniform distribution of flue gas and realizing deep gas-liquid mass transfer desulfurization.

[0054] The central area of ​​the first tray 110 and the second tray 120 and the rectangular area from the central area to the side near the flue gas inlet 221 are merged into a high-speed zone D, and the remaining part of the first tray 110 and the second tray 120 is a low-speed zone E; the opening ratio of the first channel 111 and the second channel 121 in the high-speed zone D is less than the opening ratio of the first channel 111 and the second channel 121 in the low-speed zone E.

[0055] Example 1

[0056] like Figure 1 and Figure 2 As shown in this embodiment, an integrated double-pallet system for a wet flue gas desulfurization absorption tower includes a pallet body 100 disposed within an absorption tower 200. The absorption tower 200 contains, from bottom to top, a slurry pool 210, a desulfurization reaction zone 220, a flue gas demisting zone 230, and a flue gas outlet 240. The desulfurization reaction zone 220 includes, from bottom to top, a flue gas inlet 221 and a spray layer 222. The flue gas inlet 221 is disposed on the side wall of the absorption tower 200. The pallet body 100 is located between the flue gas inlet 221 and the spray layer 222. The pallet body 100 includes a first pallet 110 and a second pallet 120. The top upper surface of the first pallet 110 is in close contact with the bottom lower surface of the second pallet 120. Multiple first channels 111 are spaced apart on the first pallet 110. Multiple second channels 121 are spaced apart on the second pallet 120. The first channels 111 and the second channels 121 correspond one-to-one. The spray layer 222 is equipped with multiple spray devices 2221 arranged at intervals from bottom to top; the flue gas demisting zone 230 is equipped with a mechanical demister 231; flushing pipes 232 are provided above and below the mechanical demister 231; the slurry tank 210 is connected to the spray devices 2221 via a circulating pump 211. The flue gas enters the absorption tower 200 through the flue gas inlet 221, and passes through the tray body 100, the multiple spray devices 2221, and the mechanical demister 231 in sequence to remove pollutants before being discharged from the flue gas outlet 240. The vertical distance from the lower surface of the first tray 110 to the upper edge of the flue gas inlet 221 is 400-1200mm, and the vertical distance from the upper surface of the second tray 120 to the lower edge of the lowest spray device 2221 in the spray layer 222 is 1000-1500mm.

[0057] like Figure 11 As shown, in this embodiment, the tray body 100 is a compact, gapless double-layer tray structure. The first layer tray 110 and the second layer tray 120 are tightly stacked and integrally set between the flue gas inlet and the lowest spray device 2221. The structure of this embodiment can prevent secondary flow deviation of flue gas and ensure continuous and stable rectification effect. The double-layer plates of the first layer tray 110 and the second layer tray 120 are stacked to form a continuous bubbling liquid layer 140, which prolongs the gas-liquid contact time, enhances the desulfurization reaction of high-sulfur flue gas, and achieves dust classification and collection by relying on the double-layer liquid film. It can also reduce the space occupied in the tower and effectively reduce the equipment infrastructure cost.

[0058] Example 2

[0059] like Figure 1 , Figures 3-7 As shown, in this embodiment, based on embodiment 1, the first layer tray 110 and the second layer tray 120 adopt concentric circular gradient irregular openings. The first layer tray 110 and the second layer tray 120 are divided into a central area A, an intermediate ring area B, and an edge ring area C from the center to the tower wall. The central area A, the intermediate ring area B, and the edge ring area C of the first layer tray 110 and the second layer tray 120 are divided into three equal parts according to the radius.

[0060] The diameters of the first channel 111 and the second channel 121 in the central area A are larger than the diameters of the first channel 111 and the second channel 121 in the intermediate ring area B; the diameters of the first channel 111 and the second channel 121 in the intermediate ring area B are larger than the diameters of the first channel 111 and the second channel 121 in the edge ring area C.

[0061] The diameters of the first channel 111 and the second channel 121 gradually decrease from the center of the tray to the tower wall, and the flow resistance in each zone is adjusted by the difference in diameter.

[0062] The diameter of the bottom of the first channel 111 is 39-41 mm in the central area A, 33-35 mm in the middle ring area B, and 27-29 mm in the edge ring area C. The diameter of the top of the first channel 111 is 30-32 mm in the central area A, 25-27 mm in the middle ring area B, and 19-21 mm in the edge ring area C. The diameter of the bottom of the second channel 121 is 30-32 mm in the central area A, 25-27 mm in the middle ring area B, and 19-21 mm in the edge ring area C. The diameter of the top of the second channel 121 is 39-41 mm in the central area A, 33-35 mm in the middle ring area B, and 27-29 mm in the edge ring area C.

[0063] In this embodiment, the central area A, the middle ring area B, and the edge ring area C have equal ring widths, which can match the gas-liquid load distribution patterns in different areas of the plate. This balances the degree of slurry disturbance caused by airflow in each area, resulting in a uniform and stable liquid holding thickness across the entire tray. This prevents localized slurry accumulation and clumping, as well as channel blockage, and also prevents localized dry burning and smoke leakage due to insufficient liquid. It significantly reduces the rate of gypsum scaling and extends the tray maintenance cycle. The uniform liquid holding environment ensures consistent bubbling intensity in each area, allowing for simultaneous mass transfer across the entire plate. This avoids problems of excessive or insufficient localized reactions, stabilizing desulfurization efficiency while reducing ineffective slurry spraying losses. This also helps lower the system's liquid-to-gas ratio, resulting in energy savings and reduced consumption.

[0064] The structure of this embodiment can be adapted to the inherent flow field characteristics inside the tower, balance the flue gas velocity in the cross section, eliminate flue gas short circuit and wall retention, keep the liquid layer in the entire tray consistent with the bubbling reaction state, reduce the increase in system resistance, and simultaneously improve desulfurization and dust removal performance.

[0065] Example 3

[0066] like Figure 1 , Figures 3-6 , Figure 8 As shown, in this embodiment, based on embodiment 1, the first channel 111 and the second channel 121 are optimized into a horn-shaped conical channel without straight sections. The diameter of the first channel 111 gradually decreases from bottom to top, forming an inverted horn-shaped hole; the diameter of the second channel 121 gradually increases from bottom to top, forming a positive horn-shaped hole; the diameter at the top of the first channel 111 is the same as the diameter at the bottom of the second channel 121, and the diameter at the bottom of the first channel 111 is the same as the diameter at the top of the second channel 121.

[0067] In this embodiment, the inlet and outlet diameters of the first channel 111 and the second channel 121 are the same, only the channel contraction directions are opposite: the inverted funnel-shaped hole of the first channel 111, which is wider at the bottom and narrower at the top, increases the flue gas velocity by throttling, thereby enhancing the gas-liquid turbulence disturbance and the ability to capture large dust particles; the positive funnel-shaped hole of the second channel 121, which is narrower at the bottom and wider at the top, extends the gas-liquid reaction time by expanding the volume and slowing down, thus refining the flue gas bubbles and enhancing the adsorption effect of fine dust particles; the structure of this embodiment weakens the influence of the flue gas boundary layer by using a fluid control method of first accelerating and then decelerating the flue gas, thereby enhancing the gas-liquid mass transfer efficiency and achieving graded removal of coarse and fine dust, with only a slight increase in system flow resistance, which can simultaneously improve desulfurization and synergistic dust removal performance.

[0068] Example 4

[0069] exist Figure 2 and 10As shown, in this embodiment, based on embodiment 1, the pallet body 100 is tilted at an angle of 1°-4°, and the pallet body 100 forms a unidirectional overall slightly tilted structure; the slurry forms a continuously flowing tilted liquid film on the upper surface of the pallet body 100.

[0070] The inclined lower surface of the tray body 100 directly diverts and redirects the eccentric flue gas within the tower, breaking up the vortex at the bottom of the tower wall and tray body 100, guiding the flue gas to converge towards the center of the tray body 100, and eliminating the dead zone of low-speed stagnation near the wall. Simultaneously, the slurry on the upper surface of the tray body 100 relies on self-redirecting flow to form a naturally zoned inclined liquid film: the slurry at the high end of the tray body 100 has a fast flow rate, a thin liquid film, and low airflow resistance; while the slurry at the low end of the tray body 100 converges, has a thick liquid film, and high airflow resistance. This difference in resistance on the tray body 100 surface achieves secondary lateral flow equalization of the flue gas, further suppressing flue gas deviation and short-circuiting problems. At the same time, the directional flow of the slurry prevents impurities from accumulating on the plate surface and clogging the channels. The inclined structure of the tray body 100 helps optimize the flue gas flow field within the tower, serving both airflow rectification and automatic unclogging functions, resulting in extremely low system pressure drop increase.

[0071] Example 5

[0072] like Figures 2-6 , Figure 8 , Figure 10 As shown, this embodiment is based on the compact, gapless double-layer tray structure of embodiment 1, and incorporates the technical solutions of embodiments 2-4. The first layer tray 110 and the second layer tray 120 adopt concentric circular gradient irregular openings to balance the flue gas flow field. The first channel 111 and the second channel 121 are non-straight section horn cone channels and horn channels with equal diameters in opposite directions to achieve graded control of flue gas acceleration followed by deceleration. The tray body 100 is combined with a unidirectional micro-tilted structure to complete the secondary rectification of airflow and slurry self-cleaning and anti-clogging.

[0073] This embodiment adopts integrated dual-tray technology. The tray body 100 is a compact, gapless double-layer tray structure. The upper and lower trays adopt a combination structure of concentric circle gradient irregular openings, reverse trumpet-shaped channels and unidirectional micro-inclination, to construct a desulfurization coupling system with gradient resistance, graded flow velocity and progressively enhanced mass transfer. The structure is simple, easy to operate, and has low operating and maintenance costs, which greatly improves the overall desulfurization efficiency.

[0074] The technical solution of this embodiment enhances gas-liquid mass transfer while possessing significant synergistic dust removal capabilities; the upward flue gas passes sequentially through the first tray 110 and the second tray 120: First tray 110: High-speed flue gas is accelerated by throttling and impacts the first liquid accumulation layer 131 on the plate surface to form a strongly turbulent continuous bubbling liquid layer 140. Fine dust, gypsum slurry droplets and SO3 aerosols carried in the flue gas collide, wet and coagulate with the slurry film, and large-diameter particles are initially captured and enter the slurry circulation.

[0075] Second tray 120: Flue gas expands and slows down, forming uniform and dense bubbles within the stable second liquid accumulation layer 132. Residual fine particles come into full contact with the liquid film during bubble agitation and are captured by secondary washing.

[0076] Graded interception and step-by-step washing: The plate area and liquid layer of the two-layer tray work together to form a dust removal path of "coarse capture + fine capture", which has a significantly higher capture efficiency for PM2.5 and smaller fine particles than single-layer trays or conventional split double-layer trays.

[0077] Self-cleaning and anti-clogging: The continuously flowing inclined liquid film on the upper surface of the tray can effectively remove the captured solid particles, prevent dust and scale buildup on the tray, and ensure long-term stable operation.

[0078] In summary, the four design features of this embodiment work together to sequentially achieve macroscopic airflow stabilization, cross-sectional flow field uniformity, microscopic gas-liquid mass transfer enhancement, and long-term stable operation of the device, forming a complete flow field control system. This system synergistically improves desulfurization and dust removal performance while addressing the shortcomings of traditional tray-type flue gas flow deviation, insufficient purification efficiency, easy accumulation of scale and clogging of holes, and high operation and maintenance costs. High-efficiency desulfurization and deep dust removal can be completed simultaneously within the desulfurization tower, achieving integrated "desulfurization-dust removal" and saving investment and operating costs.

[0079] The newly revised Ambient Air Quality Standard (GB 3095-2026), implemented in March 2026, tightened the secondary limit for annual average PM2.5 concentration to 25 μg / m³. 3 The "Emission Standard of Air Pollutants for Thermal Power Plants and Boilers" (GB 13223) was also revised to tighten the particulate matter limit for boilers with a capacity of 65 t / h and above to 5 mg / m³. 3 The sulfur dioxide emission limit has been lowered from 100 mg / m³ in the previous stage. 3 (50mg / m² in key areas) 3 The concentration was uniformly reduced to 35 mg / m³. 3 In some key areas, "near-zero emissions" have been piloted, requiring sulfur dioxide emissions to be ≤20mg / Nm³. 3 .

[0080] Existing split-type dual tray technology (such as...) Figure 9 As shown, ultra-low emissions can be achieved under normal sulfur conditions, but when faced with ultra-high sulfur (such as SO2 ≥ 10000 mg / Nm³), the emission level is significantly reduced. 3 Even 12500mg / Nm 3When operating under ultra-high sulfur conditions, bottlenecks such as insufficient desulfurization efficiency, scaling and blockage, and a sharp increase in energy consumption exist. This invention addresses this "ultra-high sulfur dilemma" by implementing a series of structural optimizations, thereby achieving a stable desulfurization efficiency of over 99% and synergistic removal of multiple pollutants even under ultra-high sulfur conditions. To more clearly illustrate the advantages of this invention, a standard dry flue gas flow rate of 1,160,000 Nm³ is used. 3 / h, inlet SO2 concentration 12500 mg / Nm 3 (Standard conditions, dry basis, 6% O2), inlet flue gas dust concentration: 60 mg / Nm³ 3 Dry basis liquid-to-gas ratio 25 L / Nm 3 The wet desulfurization absorption towers under different technical schemes were compared at an average flue gas temperature of 55℃. The comparison results are shown in the table below: Table 1 Comparison Results

[0081] As shown in Table 1, the outstanding advantages of using Example 5 of the present invention for ultra-high sulfur conditions are: Tests have shown that even with an inlet SO2 concentration as high as 12500 mg / Nm³, [the following conditions are observed]. 3 Even under extreme high-sulfur conditions, it can still operate stably; the desulfurization efficiency jumps to 99.84%, and the outlet SO2 concentration is stably controlled at 35.0 mg / Nm³. 3 The following parameters fully meet or even exceed national ultra-low emission limits. Compared with split-type dual-pallet technology, this invention does not experience problems such as duct blockage, liquid layer failure, or a sharp drop in desulfurization efficiency under ultra-high sulfur conditions. The system pressure drop increase is less than 5% after more than 90 days of continuous operation, significantly superior to existing technologies. Simultaneously, by utilizing the continuous bubbling liquid layer and graded interception structure of the dual-pallet system, it achieves synergistic and deep removal of fine dust, gypsum slurry droplets, and SO3 aerosols from the flue gas. The measured dust removal efficiency reaches as high as 93.3%, with the outlet dust concentration as low as 4 mg / Nm³. 3 It is far superior to the current national standard (5mg / m³). 3 It also completely solves the "gypsum rain" problem; this synergistic dust removal function is especially suitable for areas with strict control requirements for PM2.5 and condensable particulate matter; under high sulfur conditions, the minimum liquid-to-gas ratio required for the system to achieve standard operation is reduced from the conventional 25 L / Nm³. 3 Reduced to 14 L / Nm 3 The slurry circulation spray volume is reduced by more than 20%, effectively reducing the power consumption and operating costs of the circulation pump. The total pressure drop within the entire tower is only 590 Pa, which avoids a significant increase in system resistance while efficiently purifying flue gas, achieving excellent comprehensive performance of "high desulfurization efficiency, high dust removal efficiency, low energy consumption, and low resistance loss"; meeting the requirements of the newly revised "Ambient Air Quality Standard" (GB 3095-2026) in March 2026.

[0082] When the technical solutions of embodiments 2-4 of the present invention are adopted, they are superior to the existing split-type double-pallet technical solutions in terms of desulfurization efficiency, outlet SO2 concentration, dust removal efficiency, and outlet flue dust concentration.

[0083] Although the technical solution of Embodiment 1 of the present invention is the same as that of the split-type double-pallet technical solution in the prior art in terms of desulfurization efficiency, outlet SO2 concentration, dust removal efficiency, and outlet flue dust concentration, the compact gapless double-layer pallet structure of Embodiment 1 of the present invention can accumulate slurry to form a liquid accumulation layer. Relying on the liquid accumulation structure, two or more spraying systems can be constructed inside a single tower, eliminating the need for multi-tower series arrangement and effectively reducing project infrastructure investment. Compared with the split-type double-pallet of the prior art, it can reduce the space occupied inside the tower and effectively reduce equipment infrastructure costs.

[0084] Example 6 In a single-sided flue gas desulfurization tower, the biased flow of flue gas also leads to a severe "wall-adhering flow" phenomenon—a large amount of flue gas passes through the tower wall at high speed, forming a flue gas corridor, while the gas-liquid contact in the central area of ​​the absorption tower 200 is insufficient. The concentric gradient irregular opening technology of the first tray 110 and the second tray 120, which divides the first tray 110 and the second tray 120 from the center to the tower wall into a central area A, an intermediate ring area B, and an edge ring area C, and divides the central area A, the intermediate ring area B, and the edge ring area C of the first tray 110 and the second tray 120 into three equal parts by radius, can solve the problem of insufficient gas-liquid contact in the central area of ​​the absorption tower 200. However, this solution divides the first tray 110 and the second tray 120 into three areas. If only the problem of insufficient gas-liquid contact in the central area of ​​the absorption tower 200 is addressed, the processing difficulty is relatively high and it is not economical.

[0085] like Figure 12 As shown, in this embodiment, based on embodiment 1, the first layer tray 110 and the second layer tray 120 are improved into non-uniformly perforated trays; the central region and the rectangular region from the central region to the side near the flue gas inlet 221 are merged into the high-speed zone D, and the remaining part of the first layer tray 110 and the second layer tray 120 is the low-speed zone E; the opening ratio of the first channel 111 and the second channel 121 in the high-speed zone D is less than the opening ratio of the first channel 111 and the second channel 121 in the low-speed zone E.

[0086] The diameter (usually φ30mm-φ50mm) and spacing of the first channel 111 and the second channel 121 are adjusted by reverse calculation based on the opening ratio, and the opening direction of the first channel 111 and the second channel 121 is usually designed to be vertically downward or with a guide angle.

[0087] This embodiment increases the flow resistance in the sidewall region by setting a smaller opening ratio or even a partially non-open area in the high-speed zone D, forcing the flue gas to divert to the central region of the tower. This not only eliminates the flue gas corridor but also significantly reduces the negative impact of the 200-degree sidewall effect on the desulfurization efficiency, resulting in more thorough and uniform gas-liquid contact across the entire cross-section of the tower.

[0088] When flue gas enters the absorption tower 200 from the flue gas inlet 221, due to inertia and sudden change in flow direction, the flow velocity on the inlet side of the absorption tower 200 is usually much higher than that on the opposite side (i.e., "flue gas deflection").

[0089] The flue gas in the high-speed zone D has high kinetic energy and high velocity. If the opening ratio in this zone is also large, the flue gas will "pass through quickly", resulting in a short gas-liquid contact time on this side and squeezing the passage space of the flue gas in the low-speed zone. In this embodiment, the opening ratio is set to be small, which means that the tray body 100 provides greater local resistance in this zone, which can "hold back" the high-speed flue gas and force some of the flue gas to be diverted to the low-speed zone E.

[0090] The flue gas kinetic energy is small in the low-speed zone E; in this embodiment, the opening ratio is set to be large, which means that the local resistance is small, which facilitates the smooth passage of flue gas coming from the high-speed zone.

[0091] This embodiment utilizes the resistance differences in different areas of the tray body 100 to artificially create a "resistance balance," making the flue gas flow distribution across the entire tower cross section tend to be uniform.

[0092] Based on CFD (Computational Fluid Dynamics) simulations, the conventional uniform opening ratio is typically between 25% and 40% (for the spray tower tray). In this embodiment, the non-uniform variable opening ratio is as follows: the opening ratio in the high-speed zone D is reduced by 3%-5% compared to the design center value (for example, if the design center value is 30%, this zone is set to 25%-27%); the opening ratio in the low-speed zone E is increased by 3%-5% compared to the design center value (for example, set to 33%-35%). This can economically solve the problem of insufficient gas-liquid contact in the central area of ​​the absorption tower 200.

[0093] Improved gas-liquid contact efficiency: After the flue gas is evenly distributed, the slurry spray coverage is more uniform, avoiding "short circuits" and "dead zones", resulting in higher desulfurization efficiency under the same circulating slurry volume.

[0094] Reduce energy consumption: After the uniformity of energy distribution is improved, in order to achieve the same emission values ​​(e.g., SO2 ≤ 20 mg / m³), 3 This eliminates the need to excessively increase the frequency of the slurry circulation pump 211, thereby reducing power consumption; it also prevents localized corrosion / wear by avoiding long-term scouring of the tower wall or localized demisters by high-speed flue gas.

[0095] All other unspecified parts belong to the prior art.

Claims

1. An integrated double-tray system for a wet flue gas desulfurization absorption tower, comprising a tray body (100) disposed within an absorption tower (200); wherein the absorption tower (200) is provided with, from bottom to top, a slurry pool (210), a desulfurization reaction zone (220), a flue gas demisting zone (230), and a flue gas outlet (240); wherein the desulfurization reaction zone (220) comprises, from bottom to top, a flue gas inlet (221) and a spray layer (222); wherein the flue gas inlet (221) is disposed on the side wall of the absorption tower (200); characterized in that: The tray body (100) is located between the flue gas inlet (221) and the spray layer (222). The tray body (100) includes a first tray (110) and a second tray (120). The upper top surface of the first tray (110) is in close contact with the lower bottom surface of the second tray (120). The first tray (110) has a plurality of first channels (111) spaced apart. The second tray (120) has a plurality of second channels (121) spaced apart. The first channels (111) and the second channels (121) correspond one-to-one. The bottom upper surface of the first tray (110) is a first liquid accumulation layer (131), and the bottom upper surface of the second tray (120) is a second liquid accumulation layer (132); The first tray (110) and the second tray (120) are both divided into a central area (A), an intermediate ring area (B), and an edge ring area (C) from the center towards the tower wall. The diameter of the first channel (111) and the second channel (121) in the central area (A) is larger than the diameter of the first channel (111) and the second channel (121) in the intermediate ring area (B). The diameter of the first channel (111) and the second channel (121) in the intermediate ring area (B) is larger than the diameter of the first channel (111) and the second channel (121) in the edge ring area (C). The diameter of the first channel (111) gradually decreases from bottom to top; the diameter of the second channel (121) gradually increases from bottom to top. The tray body (100) is tilted.

2. The integrated double-pallet system for a wet flue gas desulfurization absorption tower according to claim 1, characterized in that: The diameter of the top of the first channel (111) is the same as the diameter of the bottom of the second channel (121), and the diameter of the bottom of the first channel (111) is the same as the diameter of the top of the second channel (121).

3. The integrated double-pallet system for a wet flue gas desulfurization absorption tower according to claim 1, characterized in that: The tilt angle of the tray body (100) is 1°-4°, and the slurry forms a continuously flowing tilted liquid film on the upper surface of the tray body (100).

4. The integrated double-pallet system for a wet flue gas desulfurization absorption tower according to claim 1, characterized in that: The spray layer (222) is provided with multiple spray devices (2221) spaced from bottom to top; the flue gas demisting zone (230) is provided with a mechanical demister (231); the mechanical demister (231) is provided with flushing pipes (232) above and below; the slurry tank (210) is connected to the spray device (2221) through a circulating pump (211).

5. An integrated dual-pallet system for a wet flue gas desulfurization absorption tower according to claim 4, characterized in that: The vertical distance from the lower surface of the first layer tray (110) to the flue gas inlet (221) is 400-1200mm, and the vertical distance from the upper surface of the second layer tray (120) to the lowest spray device (2221) in the spray layer (222) is 1000-1500mm. The central area (A), middle ring area (B), and edge ring area (C) of the first layer tray (110) and the second layer tray (120) are all divided into three equal parts by radius.

6. The integrated double-pallet system for a wet flue gas desulfurization absorption tower according to claim 2, characterized in that: The diameter of the bottom of the first channel (111) is 39-41 mm in the central area (A), 33-35 mm in the middle ring area (B), and 27-29 mm in the edge ring area (C). The diameter of the top of the first channel (111) is 30-32 mm in the central area (A), 25-27 mm in the middle ring area (B), and 19-21 mm in the edge ring area (C). The diameter of the bottom of the second channel (121) is 30-32 mm in the central area (A), 25-27 mm in the middle ring area (B), and 19-21 mm in the edge ring area (C). The diameter of the top of the second channel (121) is 39-41 mm in the central area (A), 33-35 mm in the middle ring area (B), and 27-29 mm in the edge ring area (C).

7. The integrated double-pallet system for a wet flue gas desulfurization absorption tower according to claim 1, characterized in that: The central area of ​​the first tray (110) and the second tray (120) and the rectangular area from the central area to the side near the flue gas inlet (221) are merged into a high-speed zone (D), and the remaining part of the first tray (110) and the second tray (120) is a low-speed zone (E); the opening ratio of the first channel (111) and the second channel (121) in the high-speed zone (D) is less than the opening ratio of the first channel (111) and the second channel (121) in the low-speed zone (E).

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