WO2016074266A1 - 一种横向极板绕流式湿式电除尘装置及湿式电除尘方法 - Google Patents

一种横向极板绕流式湿式电除尘装置及湿式电除尘方法 Download PDF

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WO2016074266A1
WO2016074266A1 PCT/CN2014/091687 CN2014091687W WO2016074266A1 WO 2016074266 A1 WO2016074266 A1 WO 2016074266A1 CN 2014091687 W CN2014091687 W CN 2014091687W WO 2016074266 A1 WO2016074266 A1 WO 2016074266A1
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flue gas
anode
dust
anode plates
plates
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PCT/CN2014/091687
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English (en)
French (fr)
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朱廷钰
王雪
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中国科学院过程工程研究所
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
    • B03C3/02—Plant or installations having external electricity supply
    • B03C3/16—Plant or installations having external electricity supply wet type

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  • the invention belongs to the technical field of wet electric dust removal and multi-contaminant removal, in particular to a device for capturing and removing pollutants such as particulate matter, SO 3 and Hg in flue gas, and particularly relates to a transverse plate flow type.
  • Wet electrostatic precipitator and electric dust removal method is a method for capturing and removing pollutants such as particulate matter, SO 3 and Hg in flue gas.
  • the wet electrostatic precipitator combines the advantages of the electrostatic precipitator and the wet precipitator. Due to the spray of atomized water, the specific resistance of the particulate matter is stabilized. Therefore, the wet electrostatic precipitator is not affected by the specific resistance, and is suitable for PM 2.5 , SO 3 and elemental substances.
  • Hg has high collection efficiency and is the preferred high-efficiency dust collector for flue gas purification after wet desulfurization and high-risk gas such as gas. It is increasingly used in flue gas and steel industry after flue gas wet desulfurization of coal-fired power station boilers. Deep purification of blast furnace gas, etc.
  • the existing wet electrostatic precipitators are usually vertical or horizontal.
  • the arrangement of the anode plates is parallel to the flow direction of the flue gas, and the flow velocity of the flue gas is very high.
  • the wet electrostatic precipitator directly washes the anode plates, it is difficult to maintain uniform water on the surface of the plates. Membrane, local dry spots and back corona phenomenon, greatly reducing the system's pollutant removal efficiency.
  • CN 103301944A discloses a wet type electrostatic precipitator, wherein the flue gas inlet and the outlet are both located at the top of the precipitator, and the inlet flue gas moves along the anode plate from the top to the bottom, the direction changes, and the other group of anode plates moves from the bottom to the top, the smoke
  • the overall baffle of the gas increases the residence time, but increases the system resistance and energy consumption.
  • no specific solution is proposed for the local dry spot and anti-corona phenomenon on the anode plate.
  • CN 103191832A discloses a compound horizontal wet electrostatic precipitator, wherein the flue gas inlet and the outlet are both located at the top of the dust collector, and the dust removing unit is two or more multi-layer structures vertically stacked, the structure can increase the dust removing area, but the same The height of the wet electrostatic precipitator and the system energy consumption have been increased, and local dry spots and back corona phenomena have not been solved.
  • the object of the present invention is to provide a transverse plate type flow type wet electric dust removing device and an electric dust removing method, which can solve the local water film unevenness, partial dry spot back corona and dust removing dead angle of the conventional wet type electrostatic precipitator anode plate. Problems such as short smoke retention time.
  • a transverse plate type flow type wet electric dust removing device comprises a casing having a cavity inside, a dust removing unit and an atomizing water sprinkling system are arranged inside the casing, and the dust removing unit comprises a plurality of rows of anode plates and a plurality of rows of cathodes a line in which the anode plate is perpendicular to the direction of flow of the flue gas.
  • a plurality of (ie, at least one) anode plates are arranged on the same section perpendicular to the flow direction of the flue gas, and the edge spacing of the adjacent two anode plates cannot be too narrow, otherwise the flow rate of the flue gas flowing through is high.
  • the distribution of local smoke in the electrostatic precipitator unit is not uniform; the spacing can not be too large, otherwise the number of anode plates on the same plane is reduced, and the effective dust removal area is reduced. Therefore, the selection pitch is 50-100 mm, for example, 55 mm, 60 mm, 65 mm, 70 mm. , 75mm, 80mm, 85mm, 90mm or 95mm.
  • the spacing between any two adjacent sections is 200-500 mm (the spacing is too small, the electric field breakdown voltage is reduced; the spacing is too large, the electric field between the plates).
  • the strength and the current density on the plates are weakened, for example 230 mm, 260 mm, 290 mm, 320 mm, 350 mm, 380 mm, 410 mm, 440 mm or 470 mm, and the cathode lines are arranged in the middle of any two adjacent sections.
  • the anode plates of any two adjacent sections are staggered so that the flue gas passes through the gap between the anode plates of the previous section to reach the vertical centerline of the anode plate of the latter section.
  • the anode plate has a plate width of 0.4 to 0.8 m, for example, 0.45 m, 0.5 m, 0.55 m, 0.60 m, 0.65 m, 0.70 m or 0.75 m, and a plate length of 5 to 10 m, for example, 6 m. 7m, 8m or 9m.
  • the cathode wire is vertical through the cathode frame at the top end and the cathode holder at the bottom end. Straight arrangement.
  • the left and right ends of the housing are respectively provided with an air inlet and an air outlet.
  • a gas guiding device is disposed in the intake port, and preferably a plurality of (at least one layer) gas distribution plates are disposed in the intake port.
  • the flue gas flows into the casing from the air inlet and is evenly dispersed after passing through the gas distribution plate.
  • the air inlet and the air outlet are each independently flared.
  • a hopper is disposed at the bottom of the casing, and a sump is disposed at the bottom end of the hopper.
  • the atomized water sprinkler system includes a spray pipe and a conical nozzle of uniform spacing.
  • the spray pipe is disposed above the anode plate, and the tapered nozzle is located on an extension of the vertical centerline of the anode plate.
  • the spray water is sprayed by the conical nozzle, flows from the top to the bottom along the anode plate, is collected by the ash hopper, and is discharged to the outside of the casing through the discharge port at the bottom end of the ash hopper.
  • the dusty flue gas flows into the casing from the air inlet, is evenly dispersed after passing through the gas guiding device, enters the dust removing unit containing the plurality of rows of anode plates, and the atomized water sprinkling system sprays the anode plate and the cathode line in the flue gas.
  • the specific resistance of the particulate matter combined with the sprayed atomized water is reduced. Since the flow direction of the flue gas is perpendicular to the transverse anode plate, the effective driving speed of the particulate matter in the electric field is the sum of the velocity of the flue gas and the velocity caused by the electric field force.
  • the flue gas can pass through the gap between the adjacent anode plates, and the flow occurs, reaching the second row of anode plates, and the particulate matter is again captured, Pushing this way until the flue gas passes through the entire dust removal unit; the atomized water forms a continuous flowing water film on the anode plate, the dust collected on the anode plate is brought into the ash hopper, and the slurry is passed through the slag outlet at the bottom end of the ash hopper. It is discharged to the outside of the casing, and the purified flue gas is discharged from the air outlet to enter the atmosphere, thereby achieving the purpose of removing dust from the flue gas.
  • the invention has the following beneficial effects:
  • the transverse plate type flow-type wet type electrostatic precipitator of the present invention adopts a lateral arrangement to display the anode plate so as to be perpendicular to the flow direction of the flue gas, and the flue gas flows around the gap of the same row of anode plates to prolong the flue gas.
  • the residence time increases the disturbance of the particles, weakens the erosion of the water film on the surface of the anode plate, avoids local dry spots and back corona, and makes various pollutants such as PM 2.5 easy to be trapped by the plates, and the traditional wet electrostatic precipitator Compared with the system stability and the capture efficiency of various pollutants such as PM2.5 in the flue gas, the efficiency is obviously improved.
  • the lateral electrode plate type flow type wet electrostatic precipitator has a particle removal efficiency of 99%, an outlet discharge concentration of less than 5 mg/m 3 , a SO 3 removal efficiency of 80%, and an outlet discharge concentration of less than 5 mg/m. 3 ; Hg 0 removal efficiency can reach 85%, and the export emission concentration is lower than 5 ⁇ g/m 3 .
  • FIG. 1 is a schematic structural view of a lateral plate type flow type wet type electrostatic precipitator according to the present invention
  • FIG. 2 is a side view of a lateral plate type flow type wet type electrostatic precipitator according to the present invention.
  • a lateral plate type flow type wet type electrostatic precipitator device comprises a casing 1 , and the left and right ends of the casing 1 are respectively provided with a flared air inlet 2 and an air outlet 3 , and the air inlet 3
  • a plurality of gas distribution plates are arranged in the port 2.
  • a hopper 7 is arranged at the bottom of the casing 1, and a slurry port is arranged at the bottom end of the ash hopper 7.
  • the dust removing unit comprises a plurality of rows of anode plates 4 and cathode wires 5 perpendicular to the flow direction of the flue gas, wherein the same cross section is arranged perpendicular to the flow direction of the flue gas
  • Multiple anode plates 4 the adjacent two anode plates 4 have an edge spacing of 80 mm, perpendicular to the flow of smoke
  • the adjacent two sections are spaced apart by 300 mm
  • the cathode line 5 is arranged in the middle of the adjacent two sections.
  • the anode plates 4 on two adjacent sections are staggered.
  • the anode plate 4 has a plate width of 0.5 m and a plate length of 8 m, and the cathode wire 5 is vertically arranged by the cathode frame of the top end and the cathode holder of the bottom end.
  • the atomized water sprinkler system 6 includes a plurality of spray pipes and tapered nozzles disposed directly above the anode plates 4, each of which is disposed on an extension of the vertical centerline of the anode plates 4.
  • the dust-containing flue gas 9 flows into the casing 1 from the air inlet 2, and is uniformly dispersed after passing through the gas guiding device.
  • the dust-containing flue gas 9 adsorbs the dust in the dust-containing flue gas 9 on the anode plate 4 under the action of the dust removing unit.
  • the atomized water sprinkling system 6 sprays the anode plate 4, and forms a water film on the surface of the anode plate 4 to purify and collect the charged dust, and the continuously flowing water film simultaneously brings the collected dust into the ash hopper 7.
  • the slurry 8 is discharged to the outside of the casing 1 through the slurry outlet at the bottom end of the ash bucket 7, and the purified flue gas 10 is discharged from the gas outlet 3 to enter the atmosphere, thereby achieving the purpose of removing dust from the flue gas.
  • the lateral electrode plate type flow type wet electrostatic precipitator has a particle removal efficiency of 99%, an outlet discharge concentration of less than 5 mg/m 3 , a SO 3 removal efficiency of 80%, and an outlet discharge concentration of less than 5 mg/m. 3 ; Hg 0 removal efficiency can reach 85%, and the export emission concentration is lower than 5 ⁇ g/m 3 .
  • edge spacing of the adjacent two anode plates 4 is controlled to be 50 mm
  • the plate width of the anode plate 4 is 0.4 m
  • the length of the plate is 5 m
  • the section spacing is 200mm.
  • the lateral electrode plate type flow type wet electrostatic precipitator has a particle removal efficiency of 99%, an outlet discharge concentration of less than 5 mg/m 3 , a SO 3 removal efficiency of 80%, and an outlet discharge concentration of less than 5 mg/m. 3 ; Hg 0 removal efficiency can reach 85%, and the export emission concentration is lower than 5 ⁇ g/m 3 .
  • edge spacing of the adjacent two anode plates 4 is controlled to be 100 mm
  • the plate width of the anode plate 4 is 0.8 m
  • the plate length is 10 m
  • the section spacing is 500mm.
  • the lateral electrode plate type flow type wet electrostatic precipitator has a particle removal efficiency of 99%, an outlet discharge concentration of less than 5 mg/m 3 , a SO 3 removal efficiency of 80%, and an outlet discharge concentration of less than 5 mg/m. 3 ; Hg 0 removal efficiency can reach 85%, and the export emission concentration is lower than 5 ⁇ g/m 3 .

Abstract

一种应用于颗粒物、ＳＯ３和Ｈｇ等多种污染物捕集脱除的横向极板绕流式湿式电除尘装置及电除尘方法，所述横向极板绕流式湿式电除尘装置包括壳体(1)，壳体(1)内设有雾化水喷淋系统(6)和若干除尘单元；所述雾化水喷淋系统(6)包括雾化水喷淋管道及间距均匀的锥形喷嘴；所述除尘单元包括多排阳极板(4)和多排阴极线(5)，其中，阳极板(4)与烟气流动方向相垂直；含尘烟气(9)通过同一排阳极板(4)的间隙后发生绕流，减弱了对阳极板(4)表面水膜的冲刷，避免了局部干斑和反电晕现象；该方法运行可靠，提高了湿式电除尘器的污染物捕集效率和系统稳定性。

Description

一种横向极板绕流式湿式电除尘装置及湿式电除尘方法 技术领域
本发明属于湿式电除尘和多污染物脱除技术领域，尤其是指一种烟气中的颗粒物、SO3和Hg等污染物的捕集脱除装置，具体涉及一种横向极板绕流式湿式电除尘装置及电除尘方法。
背景技术
湿式电除尘器综合了电除尘器和湿式除尘器的优点，由于雾化水的喷淋，使得颗粒物的比电阻稳定，因此湿式电除尘器不受比电阻影响，对PM2.5、SO3和单质Hg的捕集效率高，成为湿法脱硫后烟气净化以及煤气等高危险性气体的首选高效除尘器，越来越多的应用于燃煤电站锅炉烟气湿法脱硫后烟气以及钢铁行业高炉煤气等的深度净化。
现有湿式电除尘器通常为立式或卧式，阳极板的布置与烟气流动方向平行，烟气流速很高，通过湿式电除尘器时直接冲刷阳极板，使得极板表面难以维持均匀水膜，出现局部干斑和反电晕现象，大大降低系统的污染物脱除效率。
CN 103301944A公开了一种湿式电除尘器，烟气进口、出口均位于除尘器顶端，进口烟气沿阳极板由上向下运动后，方向变化，沿另一组阳极板由下向上运动，烟气的整体折流增加了停留时间，但提高了系统阻力和能耗，另外对于阳极板上的局部干斑、反电晕现象没有提出针对性解决办法。
CN 103191832A公开了一种复式卧式湿式电除尘器，烟气进口、出口均位于除尘器顶端，除尘单元为垂直叠加的两个或两个以上多层结构，该结构可增加除尘面积，但同样增加了湿式电除尘器的高度和系统能耗，同时未能解决局部干斑、反电晕现象。
发明内容
本发明的目的在于提供一种横向极板绕流式湿式电除尘装置和电除尘方法，以解决现有湿式电除尘器阳极板局部水膜不均匀、局部干斑反电晕和产生除尘死角，烟气停留时间短等问题。
为了实现上述目的，本发明采用了如下技术方案：
一种横向极板绕流式湿式电除尘装置，包括内部为空腔的壳体，壳体内部设有除尘单元和雾化水喷淋系统，所述除尘单元包括多排阳极板和多排阴极线，其中，阳极板与烟气流动方向相垂直。
在本发明中，在垂直于烟气流动方向的同一截面上布置多块(即至少为一块)阳极板，相邻两块阳极板的边缘间距不能过窄，否则流经的烟气流速很高，导致电除尘单元局部烟气分布不均匀；间距也不能过大，否则同一平面上阳极板的块数减少，有效除尘面积降低，因此选择间距为50～100mm，例如55mm、60mm、65mm、70mm、75mm、80mm、85mm、90mm或95mm。垂直于烟气流动方向的截面有若干个(至少为2个)，任意相邻的两个截面间距为200～500mm(间距过小，电场击穿电压降低；间距过大，极板间的电场强度和极板上的电流密度减弱)，例如230mm、260mm、290mm、320mm、350mm、380mm、410mm、440mm或470mm，阴极线布置在任意相邻的两个截面中间。
在本发明中，任意相邻的两个截面上的阳极板交错布置，使烟气通过前一截面的阳极板间的空隙，到达后一截面的阳极板竖直中心线。
在本发明中，所述阳极板的板宽为0.4～0.8m，例如0.45m、0.5m、0.55m、0.60m、0.65m、0.70m或0.75m，板长为5～10m，例如6m、7m、8m或9m。
在本发明中，所述阴极线通过顶端的阴极框架和底端的阴极固定架实现竖 直布置。
在本发明中，所述壳体左右两端分别设置有进气口和出气口。
在本发明中，进气口内布置气体导流装置，优选进气口内布置多层(至少为一层)气体分布板。烟气从进气口流入壳体，经过气体分布板后均匀分散。
在本发明中，所述进气口和出气口均独立地为喇叭形。
在本发明中，壳体底部设置灰斗，灰斗底端设置出浆口。
在本发明中，所述雾化水喷淋系统包括喷淋管道和间距均匀的锥形喷嘴。
在本发明中，喷淋管道布置在阳极板上方，锥形喷嘴位于阳极板竖直中心线的延长线上。在雾化水喷淋系统中，喷淋水由锥形喷嘴喷出，沿阳极板由上向下流动，通过灰斗收集，再通过灰斗底端的出浆口排出到壳体外部。
一种利用如上所述的横向极板绕流式湿式电除尘装置进行电除尘的方法，所述方法包括以下步骤：
含尘烟气从进气口流入壳体，经过气体导流装置后均匀分散，进入含有多排阳极板的除尘单元，雾化水喷淋系统对阳极板和阴极线进行喷淋，烟气中的颗粒物与喷淋出的雾化水结合后比电阻降低，由于烟气流动方向垂直于横向阳极板，颗粒物在电场中的有效驱进速度为烟气流速与电场力导致的速度之和，大大提高颗粒物的捕集效率；烟气经过第一排阳极板后，烟气可穿过相邻阳极板之间的间隙，发生绕流，到达第二排阳极板，再次发生颗粒物的捕集，以此类推，直到烟气穿过整个除尘单元；雾化水在阳极板上形成连续流动的水膜，将阳极板上收集的粉尘带入灰斗中，并通过灰斗底端的出浆口将浆液排出到壳体外部，净化烟气从出气口排出，进入大气环境，从而达到清除烟气中的粉尘的目的。
与已有技术方案相比，本发明具有以下有益效果：
本发明所述的横向极板绕流式湿式电除尘装置，采用横向布置方式陈列阳极板，使其与烟气流动方向垂直，烟气通过同一排阳极板的间隙后发生绕流，延长烟气停留时间，增加颗粒物的扰动，减弱对阳极板表面水膜的冲刷，避免局部干斑和反电晕现象，并且使PM2.5等多种污染物易于被极板捕集，与传统湿式电除尘器相比，系统稳定性和烟气中PM2.5等多种污染物的捕集效率明显提高。
所述横向极板绕流式湿式电除尘装置的颗粒物脱除效率可达99％，出口排放浓度低于5mg/m3；SO3脱除效率可达80％，出口排放浓度低于5mg/m3；Hg0脱除效率可达85％，出口排放浓度低于5μg/m3。
附图说明
图1为本发明所述一种横向极板绕流式湿式电除尘装置的结构示意图；
图2为本发明所述一种横向极板绕流式湿式电除尘装置的侧视图。
图中：1-壳体；2-进气口；3-出气口；4-阳极板；5-阴极线；6-雾化水喷淋系统；7-灰斗；8-浆液；9-含尘烟气；10-净化烟气。
具体实施方式
下面结合附图并通过具体实施方式来进一步说明本发明的技术方案。
实施例1
如图1所示，本发明的一种横向极板绕流式湿式电除尘装置，包括壳体1，壳体1左右两端分别设置有喇叭形的进气口2和出气口3，进气口2内布置多层气体分布板。壳体1底部设置灰斗7，灰斗7底端设置出浆口。
壳体1内部布置雾化水喷淋系统6和除尘单元，除尘单元包含垂直于烟气流动方向的若干排阳极板4和阴极线5，其中，与烟气流动方向相垂直的同一截面上布置多块阳极板4，相邻两块阳极板4的边缘间距80mm，垂直于烟气流动 方向的截面有若干个，相邻两个截面间距为300mm，阴极线5布置在所述相邻两个截面中间。相邻两个截面上的阳极板4交错布置。所述阳极板4的板宽为0.5m，板长为8m，阴极线5通过顶端的阴极框架和底端的阴极固定架实现竖直布置。所述雾化水喷淋系统6，包括若干个喷淋管道和锥形喷嘴，布置在阳极板4正上方，每个锥形喷嘴布置于所述阳极板4竖直中心线的延长线上。
一种利用如上所述的横向极板绕流式湿式电除尘装置进行电除尘的方法，所述方法包括以下步骤：
含尘烟气9从进气口2流入壳体1，经过气体导流装置后均匀分散，含尘烟气9在除尘单元的作用下，使含尘烟气9中的粉尘吸附在阳极板4上，雾化水喷淋系统6对阳极板4进行喷淋，在阳极板4面上形成水膜对带电粉尘进行净化收尘，连续流动的水膜同时将收集的粉尘带入灰斗7中，并通过灰斗7底端的出浆口将浆液8排出到壳体1外部，净化烟气10从出气口3排出，进入大气环境，从而达到清除烟气中的粉尘的目的。
所述横向极板绕流式湿式电除尘装置的颗粒物脱除效率可达99％，出口排放浓度低于5mg/m3；SO3脱除效率可达80％，出口排放浓度低于5mg/m3；Hg0脱除效率可达85％，出口排放浓度低于5μg/m3。
实施例2
其余同实施例1，除控制相邻两块阳极板4的边缘间距50mm，阳极板4的板宽为0.4m，板长为5m，垂直于烟气流动方向的截面有若干个，相邻两个截面间距为200mm。
所述横向极板绕流式湿式电除尘装置的颗粒物脱除效率可达99％，出口排放浓度低于5mg/m3；SO3脱除效率可达80％，出口排放浓度低于5mg/m3；Hg0脱除效率可达85％，出口排放浓度低于5μg/m3。
实施例3
其余同实施例1，除控制相邻两块阳极板4的边缘间距100mm，阳极板4的板宽为0.8m，板长为10m，垂直于烟气流动方向的截面有若干个，相邻两个截面间距为500mm。
所述横向极板绕流式湿式电除尘装置的颗粒物脱除效率可达99％，出口排放浓度低于5mg/m3；SO3脱除效率可达80％，出口排放浓度低于5mg/m3；Hg0脱除效率可达85％，出口排放浓度低于5μg/m3。
申请人声明，本发明通过上述实施例来说明本发明的详细方法，但本发明并不局限于上述详细方法，即不意味着本发明必须依赖上述详细方法才能实施。所属技术领域的技术人员应该明了，对本发明的任何改进，对本发明产品各原料的等效替换及辅助成分的添加、具体方式的选择等，均落在本发明的保护范围和公开范围之内。

Claims (10)

  1. 一种横向极板绕流式湿式电除尘装置，其特征在于，所述装置包括壳体，壳体内部设有除尘单元和雾化水喷淋系统，所述除尘单元包括多排阳极板和多排阴极线，其中，阳极板与烟气流动方向相垂直。
  2. 如权利要求1所述的装置，其特征在于，在垂直于烟气流动方向的同一截面上布置多块阳极板，相邻两块阳极板的边缘间距50～100mm，垂直于烟气流动方向的截面有若干个，任意相邻的两个截面间距为200～500mm，阴极线布置在任意相邻的两个截面中间。
  3. 如权利要求2所述的装置，其特征在于，任意相邻的两个截面上的阳极板交错布置。
  4. 如权利要求1-3之一所述的装置，其特征在于，所述阳极板的板宽为0.4～0.8m，板长为5～10m。
  5. 如权利要求1-4之一所述的装置，其特征在于，所述阴极线通过顶端的阴极框架和底端的阴极固定架实现竖直布置。
  6. 如权利要求1-5之一所述的装置，其特征在于，所述壳体左右两端分别设置有进气口和出气口；
    优选地，进气口内布置气体导流装置，优选进气口内布置多层气体分布板；优选地，所述进气口和出气口均独立地为喇叭形。
  7. 如权利要求1-6之一所述的装置，其特征在于，壳体底部设置灰斗，灰斗底端设置出浆口。
  8. 如权利要求1-7之一所述的装置，其特征在于，所述雾化水喷淋系统包括喷淋管道和间距均匀的锥形喷嘴。
  9. 如权利要求8所述的装置，其特征在于，喷淋管道布置在阳极板上方，锥形喷嘴位于阳极板竖直中心线的延长线上。
  10. 一种利用如权利要求1-9之一所述的横向极板绕流式湿式电除尘装置进行湿式电除尘的方法，其特征在于，所述方法包括以下步骤：
    含尘烟气从进气口流入壳体，经过气体导流装置后均匀分散，进入含有多排阳极板的除尘单元，雾化水喷淋系统对阳极板和阴极线进行喷淋，烟气经过第一排阳极板后，烟气可穿过相邻阳极板之间的间隙，发生绕流，到达第二排阳极板，再次发生颗粒物的捕集，以此类推，直到烟气穿过整个除尘单元；雾化水在阳极板上形成连续流动的水膜，将阳极板上收集的粉尘带入灰斗中，并通过灰斗底端的出浆口将浆液排出到壳体外部，净化烟气从出气口排出，进入大气环境，从而达到清除烟气中的粉尘的目的。
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