WO2017028152A1 - Fine particle aggregator, and efficient integrated system for dust and mist removal - Google Patents

Abstract

Provided are an aggregator (20) for aggregating fine particles, a flue gas channel and an integrated system for dust and mist removal comprising the aggregator (20), and a method for aggregating fine particles in a flue gas and an integrated method for dust and mist removal using the aggregator (20). The aggregator (20) comprises at least one cyclone apparatus (21) comprising at least two swirl vanes (211). The swirl vanes (211) are configured to enable an airflow containing fine particles to form a swirling airflow when passing through the cyclone apparatus (21).

Description

细微颗粒聚合器及高效除尘除雾一体化***  Fine particle aggregator and high efficiency dust removal and defogging integrated system

技术领域Technical field

本发明涉及烟气净化领域，尤其涉及一种用于火力发电厂、钢铁厂、造纸厂、玻璃厂、化工厂等尾气处理***中的细微颗粒聚合器及除尘除雾一体化***。The invention relates to the field of flue gas purification, in particular to a fine particle aggregator and an integrated dust removal and defogging system for use in an exhaust gas treatment system such as a thermal power plant, a steel plant, a paper mill, a glass factory and a chemical plant.

背景技术Background technique

为实现燃煤火力发电厂的超净排放甚至近零排放，国家提出' 50355 '指标，即要求燃煤火力发电厂的烟尘排放分别小于 5mg/Nm³ （达到燃气机组标准），二氧化硫 SO₂ 的排放标准小于 35mg/Nm³ ，氮氧化物 NO_X 浓度小于 50mg/Nm³ 。In order to achieve ultra-clean emissions and even near-zero emissions of coal-fired power plants, the state has proposed the '50355' indicator, which requires that the soot emissions from coal-fired power plants are less than 5mg/Nm ³ (to meet the gas unit standards), and SO ₂ in sulfur dioxide. emission standards less than 35mg / Nm ^3, the nitrogen oxide NO _X concentration is less than 50mg / Nm ^3.

为实现烟尘浓度达到超净排放甚至近零排放标准，由于湿式电除尘器投资大、运行能耗高、体积庞大、辅助的化学药剂消耗量大同时带来新的污染物、阳极板的腐蚀等一系列问题让诸多火力发电厂望而却步。In order to achieve ultra-net emission or even near-zero emission standards for soot concentration, wet-type electrostatic precipitators have large investment, high energy consumption, large volume, large consumption of auxiliary chemicals, and new corrosion of anodes and anode plates. A series of problems have discouraged many coal-fired power plants.

然而如何实现非湿式电除尘器下达到烟尘出口排放小于 5mg/Nm³ 标准是新的技术难题。目前有少许环境治理企业提出'协同治理方案'方案，采用具有高效除尘作用的湿法脱硫***（单塔、塔内分区、设置托盘或旋汇耦合等技术、三层高效除雾器），在实现高效脱硫的同时，将进入脱硫***的粉尘高效脱除，实现脱硫*** ≥70% 的除尘效率。However, how to achieve the non-wet electrostatic precipitator to achieve the emission limit of less than 5mg/Nm ³ is a new technical problem. At present, there are a few environmental management companies that propose a 'cooperative governance program' that uses a wet desulfurization system with high-efficiency dust removal (single tower, tower internal partition, set tray or screw coupling technology, three-layer high efficiency mist eliminator). At the same time of achieving high-efficiency desulfurization, the dust entering the desulfurization system is efficiently removed, and the dedusting efficiency of the desulfurization system is ≥70%.

并陈述湿法脱硫***高效除尘功能实现的主要原因：The main reasons for the efficient dust removal function of the wet desulfurization system are stated:

（ 1 ）采用高性能的喷嘴将浆液粒径降低 30% ，提高浆液的粉尘补集能力。(1) Using a high-performance nozzle to reduce the particle size of the slurry by 30%, and improve the dust replenishment ability of the slurry.

（ 2 ）通过托盘等技术形成的液膜层，增加液膜对微细粉尘的补集能力。(2) A liquid film layer formed by a technique such as a tray increases the ability of the liquid film to replenish fine dust.

（ 3 ）吸收塔设置三层高效除雾器，将吸收塔出口烟气液滴浓度控制在 20mg/Nm³ 以下，大大降低了烟气的石膏颗粒物携带量。(3) The absorption tower is equipped with a three-layer high-efficiency mist eliminator to control the droplet concentration of the flue gas at the outlet of the absorption tower to be less than 20 mg/Nm ³ , which greatly reduces the amount of gypsum particulate matter carried by the flue gas.

从以上数据可知，当脱硫入口粉尘为 20mg/Nm³ 时，即使脱硫***实现 ≥70% 的去尘率，即进入到高效除雾器的烟尘浓度依然可以达到 6mg/Nm³ ， 然而高效除雾器只对浆液液滴具有很好的拦截去除效果，即使达到 20mg/Nm³ 的液滴浓度，这些残余液滴含有石膏等固体以及可溶性盐，按照最低 7% 固体浓度计算，新增粉尘含量为 1.4mg/Nm³, 因此出口浓度要控制在 5mg/Nm³, 必须要求高效除雾器对粉尘从 6mg/Nm³ 进一步去除到 3.6mg/Nm³ 以内，即要求高效除雾器对粉尘去尘率达到 40% 以上，这是完全不符合实际的，而且残余的 6mg/Nm³ 几乎都是小于 5 微米的细微粉尘，经研究和实验结果表明高效除雾器（三级屋顶除雾器）最多可以将粉尘从 6mg/Nm³ 降低到 5.6mg/Nm³ ，去尘效果甚微！It can be seen from the above data that when the desulfurization inlet dust is 20mg/Nm ³ , even if the desulfurization system achieves a dust removal rate of ≥70%, the concentration of soot entering the high efficiency mist eliminator can still reach 6mg/Nm ³ , but efficient demisting The device only has a good intercepting effect on the slurry droplets. Even if the droplet concentration of 20mg/Nm ³ is reached, these residual droplets contain solids such as gypsum and soluble salts. The newly added dust content is calculated according to the minimum solid concentration of 7%. 1.4mg/Nm ³ , so the outlet concentration should be controlled at 5mg/Nm ³ , and the high-efficiency mist eliminator must be required to further remove the dust from 6mg/Nm ³ to 3.6mg/Nm ³ , which requires high-efficiency mist eliminator to dust dust. The rate is over 40%, which is completely unrealistic, and the residual 6mg/Nm ^{3 is} almost all fine dust less than 5 microns. The research and experimental results show that the high efficiency mist eliminator (three-stage roof defogger) has the most The dust can be reduced from 6mg/Nm ³ to 5.6mg/Nm ³ , and the dust removal effect is very small!

另外，在 2002 年由化学工业出版社和环境科学与工程出版中心共同出版的《燃煤烟气脱硫脱销技术及工程实例》一书中讲述了一种旋流板除雾器，其利用旋流板片使气流发生旋转，夹带在旋转气流中的液滴在旋流筒内高速旋转产生离心力从而被甩向圆筒内壁上，从而实现气液分离效果，所述旋流板除雾器必须要求足够的外筒高度，且其功能是利用旋流板产生的离心力将雾滴甩到筒壁上从而实现气液分离功能。Also, in 2002 In the book "Technology and Engineering Examples of Coal-Fired Flue Gas Desulfurization and Loss", published by the Chemical Industry Press and the Environmental Science and Engineering Publishing Center, a swirling plate defogger is described, which uses a swirling plate to make the airflow. Rotation occurs, and the droplets entrained in the swirling airflow rotate at a high speed in the swirling cylinder to generate centrifugal force to be impinged on the inner wall of the cylinder, thereby achieving a gas-liquid separation effect, and the swirling plate defogger must require a sufficient outer cylinder The height, and its function is to use the centrifugal force generated by the swirling plate to smash the mist onto the wall of the cylinder to realize the gas-liquid separation function.

再次，在专利申请号 201520058549.6 （一种高效除尘除雾一体化***）中申请了一种冷凝湿膜高效除尘除雾技术，在中空的波纹板内流冷却介质，通过冷凝方式将细微粉尘和液滴进行放大，然后通过下游位置的超精细分离器对其进行去除分离。Again, in the patent application number 201520058549.6 (A high-efficiency dust removal and defogging integrated system) applied for a high-efficiency dust removal and defogging technology for condensing wet film, flowing a cooling medium in a hollow corrugated plate, amplifying fine dust and droplets by condensation, and then passing downstream The superfine separator at the location removes it.

所述冷凝湿膜离心除尘除雾技术在烟尘治理领域属于巨大的技术创新，但是对极其细微粉尘和液滴，比如粒径小于 1 微米甚至小于 0.5 微米的粉尘和液滴，即使放大后依然难以被后续的超精细分离去除分离，因此为进一步深度提高极其细微粉尘和液滴的去除，有必要对所述冷凝湿膜技术做进一步的改进和提高。The condensed wet film centrifugal dust removal and defogging technology is a huge technical innovation in the field of soot treatment, but for extremely fine dust and liquid droplets, such as particle size less than 1 Micron even less than 0.5 Micron dust and droplets are difficult to be removed and separated by subsequent ultrafine separation even after amplification. Therefore, in order to further deepen the removal of extremely fine dust and droplets, it is necessary to further improve and improve the condensed wet film technology. .

因此，现有技术中具有如下技术问题需要解决：Therefore, the following technical problems in the prior art need to be solved:

1. 采用'协同治理方案 ' 治理烟尘出口浓度小于 5mg/Nm³ 的不现实性，或者更准确地说 ' 协同治理方案'不具有确保烟尘出口浓度小于 5mg/Nm³ 的科学必然性。1. The use of a 'co-governance scheme' to control the unrealisticity of soot exit concentrations below 5 mg/Nm ³ or, more precisely, the 'cooperative treatment scheme' does not have the scientific necessity to ensure that the soot exit concentration is less than 5 mg/Nm ³ .

2. 某些特定工况项目（比如粉尘入口浓度小于 10 ～ 15mg/Nm³ ），即使采用协同治理方案达到小于 5mg/Nm³ 的排放标准，也难以判断究竟是哪个环节对粉尘的治理起到核心关键作用，为避免给烟尘治理技术路线一个错误的指引：即只要配进口三级屋顶高效除雾器就能保证吸收塔出口粉尘浓度小于 5mg/Nm³ 。2. For certain specific working conditions (such as dust inlet concentration less than 10 ~ 15mg/Nm ³ ), even if the synergistic treatment scheme is used to achieve emission standards of less than 5mg/Nm ³ , it is difficult to determine which part of the dust treatment The core key role is to avoid a wrong guideline for the dust control technology route: that is, as long as the imported three-stage roof high-efficiency mist eliminator can ensure that the dust concentration at the outlet of the absorption tower is less than 5mg/Nm ³ .

3. 采用'协同治理方案'，一旦烟尘出口浓度大于 5mg/Nm³ ，则无法判断究竟是哪个技术环节达不到协同治理的效果，因此也无从诊断对***如何消除缺陷。3. Using the 'collaborative management plan', once the concentration of smoke and dust is greater than 5mg/Nm ³ , it is impossible to judge which technical link does not achieve the effect of coordinated management, so there is no way to diagnose the system to eliminate defects.

4. 为进一步深度去除极细粉尘和液滴，对冷凝湿膜技术进行技术改进。4. Technical improvements to the condensed wet film technology for further deep removal of very fine dust and droplets.

5. 去除旋流板除雾器气液分离功能，进行特殊设计后转为粉尘和液滴聚合功能。5. Remove the gas-liquid separation function of the cyclone defogger, and then transfer it to dust and droplet polymerization function after special design.

发明内容Summary of the invention

有鉴于现有技术的上述缺陷，本发明所要解决的技术问题是提供一种更有效地增大细微粉尘和 / 或液滴，使得增大后的粉尘和 / 或液滴可以被后续的超精细分离器有效分离的聚合器，并提供一种性能可靠、功能清晰的高效除尘除雾一体化***。In view of the above drawbacks of the prior art, the technical problem to be solved by the present invention is to provide a more effective increase in fine dust and / Or a droplet, such that the enlarged dust and / or droplets can be effectively separated by a subsequent ultra-fine separator, and provide a reliable and functionally efficient high-efficiency dust removal and defogging integrated system.

为实现上述目的，本发明提供了一种用于聚合细微颗粒的聚合器，即细微颗粒聚合器，该聚合器能够使烟气中的细微粉尘和 / 或微小液滴聚合长大，具体来说是将预分离器去除后的残余微小液滴（粒径 0 ～ 20 微米）以及细微粉尘 ( 粒径 0~10 微米 ) 通过碰撞方式进行聚合。经过大量试验表明，通过本发明的细微颗粒聚合器，微小液滴和细微粉尘的总数量至少可以减少 50% ，由此数量减少导致颗粒物增大。In order to achieve the above object, the present invention provides a polymerizer for polymerizing fine particles, that is, a fine particle aggregator capable of making fine dust in a flue gas and/or Or the growth of tiny droplets, specifically the residual tiny droplets (particle size 0 to 20 microns) and fine dust (particle size 0 to 10 microns) after removal of the pre-separator Aggregation is performed by collision. A large number of tests have shown that the total number of fine droplets and fine dust can be reduced by at least 50% by the fine particle aggregator of the present invention, whereby the reduction in the amount leads to an increase in particulate matter.

本发明的用于聚合细微颗粒的聚合器包括一个或多个旋风装置，旋风装置包括至少两个旋流叶片，旋流叶片被设置为使得包含细微颗粒的气流通过所述旋风装置时形成旋转气流。The polymerizer for polymerizing fine particles of the present invention comprises one or more cyclone devices, the cyclone device comprising at least two swirling vanes arranged to cause a swirling gas flow when the gas stream comprising fine particles passes through the cyclone device .

进一步地，当聚合器包括多个旋风装置时，任意两个相邻的旋风装置中的旋流叶片的设置方向相同。Further, when the aggregator includes a plurality of cyclones, the swirling vanes in any two adjacent cyclones are arranged in the same direction.

进一步地，旋风装置还包括中心柱体和外筒，旋流叶片的一端固接于中心柱体，另一端固接于外筒。Further, the cyclone device further includes a central cylinder and an outer cylinder, one end of the swirling vane is fixed to the central cylinder, and the other end is fixed to the outer cylinder.

更进一步地，外筒具有圆形截面，圆形截面与外筒的轴线垂直；旋流叶片固接于外筒的另一端的高度与外筒的高度基本相同，或者小于外筒的高度，且两者的高度差不超过圆形截面的直径的三分之一。Further, the outer cylinder has a circular cross section, and the circular cross section is perpendicular to the axis of the outer cylinder; the height of the swirl vane fixed to the other end of the outer cylinder is substantially the same as the height of the outer cylinder, or is smaller than the height of the outer cylinder, and The height difference between the two does not exceed one third of the diameter of the circular section.

更进一步地，外筒具有正多边形截面，正多边形截面与外筒的轴线垂直；旋流叶片固接于外筒的另一端的高度与外筒的高度基本相同，或者小于外筒的高度，且两者的高度差不超过正多边形截面的最长对角线长度的三分之一。Further, the outer cylinder has a regular polygonal cross section, and the regular polygonal cross section is perpendicular to the axis of the outer cylinder; the height of the swirl vane fixed to the other end of the outer cylinder is substantially the same as the height of the outer cylinder, or is smaller than the height of the outer cylinder, and The height difference between the two does not exceed one third of the longest diagonal length of the regular polygonal section.

进一步地，多个旋风装置的轴线相互平行。Further, the axes of the plurality of cyclones are parallel to each other.

进一步地，多个旋风装置分别位于两个形成 V 字形或人字形的平面内，位于同一平面内的旋风装置的轴线相互平行。Further, a plurality of cyclones are respectively located in two forming V In the plane of the glyph or herringbone, the axes of the cyclones in the same plane are parallel to each other.

更进一步地，旋流叶片的仰角，即旋流叶片从一端到另一端延伸的长度方向与外筒的水平横截面之间形成的夹角 α ，为 12.5 ～ 60° ，优选为 22~27° 。Further, the elevation angle of the swirling vane, that is, the angle formed between the length direction of the swirl vane extending from one end to the other end and the horizontal cross section of the outer cylinder α It is 12.5 to 60°, preferably 22 to 27°.

更进一步地，旋流叶片的数量为 3~18 片。Further, the number of swirling vanes is 3 to 18 pieces.

优选地，旋流叶片的数量为 6~8 片。Preferably, the number of swirling vanes is 6-8 pieces.

进一步地，各个旋风装置的规格被设置为相同，以降低装置的投资成本。对于不同的区域可以采用差异化的旋风装置，以适应不同区域的气体流场，比如旋风装置中的旋流叶片数量不同，外筒的直径不同或者旋风装置的高度不相同。科学地实施差异化布置对细微粉尘和微小液滴的聚合将产生更有益的效果。Further, the specifications of the respective cyclones are set to be the same to reduce the investment cost of the device. Different regions can be used to differentiate the cyclone device to adapt to the gas flow field in different regions. For example, the number of swirling vanes in the cyclone device is different, the diameter of the outer cylinder is different, or the height of the cyclone device is different. The scientific implementation of the differential arrangement will result in a more beneficial effect on the polymerization of fine dust and fine droplets.

进一步地，为了提高旋风装置的使用寿命和结构强度，优选地将旋流叶片、中心柱体和外筒制造成一整体，即一体成型。Further, in order to improve the service life and structural strength of the cyclone device, it is preferable to manufacture the swirl vane, the center cylinder and the outer cylinder as a whole, that is, integrally formed.

进一步地，聚合器还包括用于安装旋风装置的固定件，固定件上设置有用于安装旋风装置的安装孔，多个旋风装置通过安装孔安装在固定件上；固定件上还设置有通气孔。通气孔的作用为降低聚合器的压力损失，并避免聚合器产生积液池，从而维持聚合器的聚合作用。Further, the aggregator further includes a fixing member for installing the cyclone device, the fixing member is provided with a mounting hole for installing the cyclone device, and the plurality of cyclone devices are mounted on the fixing member through the mounting hole; the fixing member is further provided with the vent hole . The function of the vent is to reduce the pressure loss of the polymerizer and to prevent the polymerizer from creating a pool to maintain the polymerization of the polymerizer.

更进一步地，固定件整体上为平面结构，安装在固定件上的多个旋风装置处于同一平面内，且多个旋风装置的轴线相互平行。Further, the fixing member has a planar structure as a whole, and the plurality of cyclone devices mounted on the fixing member are in the same plane, and the axes of the plurality of cyclone devices are parallel to each other.

更进一步地，固定件包括两个形成人字形或 V 字形的平面，安装在同一平面内的旋风装置的轴线相互平行。Further, the fixing member includes two planes forming a chevron or a V shape, and the axes of the cyclones mounted in the same plane are parallel to each other.

本发明的上述用于聚合细微颗粒的聚合器的工作原理如下：The above-described working principle of the aggregator for polymerizing fine particles of the present invention is as follows:

聚合器中的旋风装置能够实现粉尘与粉尘聚合、液滴与液滴聚合、粉尘与液滴聚合、大颗粒与大颗粒聚合、小颗粒与小颗粒聚合、大颗粒与小颗粒聚合，并且同时发生一次聚合、二次聚合甚至多次聚合。The cyclone in the polymerizer can realize dust and dust polymerization, droplet and droplet polymerization, dust and droplet polymerization, large particle and large particle polymerization, small particle and small particle polymerization, large particle and small particle polymerization, and simultaneously Primary polymerization, secondary polymerization or even multiple polymerizations.

旋风装置中的旋流叶片存在如下三大效应促使上述聚合过程：The swirling vanes in the cyclone have the following three major effects that contribute to the above polymerization process:

首先，大液滴和（或）大粉尘追击小液滴和（或）小粉尘的追捕效应导致液滴和（或）粉尘发生长大。携带大量微小液滴和（或）细微粉尘的气流经过旋风装置后，气流方向发生改变，产生旋转气流。由于相邻两旋风装置的旋流叶片均为顺时针方向或者逆时针方向，所以相邻两旋风装置的交汇耦合区产生气流逆流效应，逆流效应发生，导致烟气流速下降，但由于液滴（密度为 1000 ～ 1200Kg ／ m³ ）和（或）粉尘 ( 堆积密度大约为 1600 ～ 2200kg/m³) 的密度远远高于气流 ( 密度为 1.1-1.3Kg/m³) 的密度，因此液滴和（或）粉尘在较高的惯性力作用下和同向前进的气流发生相对滑移，而且由于气流存在一定的黏度（ 在 1 个大气压 50 ℃ 工况下动力黏度约 1.96×10^-5Pa.s ）对发生相对滑移的液滴和（或）粉尘产生粘性力（即粘性内摩擦力，与粉尘和（或）液滴的表面积成正比关系）来阻止这种相对滑移，由于更微小的液滴和（或）粉尘的比表面积大，所以较大液滴和（或）较大粉尘的相对滑移速度要高于较小液滴和（或）较小粉尘，因此较大液滴和（或）较大粉尘将发生追击更小液滴和（或）更小粉尘效应并很大概率将更小液滴和（或）更小粉尘捕获从而导致液滴和（或）粉尘长大。First, the trapping effect of large droplets and/or large dust chasing small droplets and/or small dust causes droplets and/or dust to grow. After the airflow carrying a large amount of minute droplets and/or fine dust passes through the cyclone, the direction of the airflow changes, producing a swirling airflow. Since the swirling vanes of the adjacent two cyclones are clockwise or counterclockwise, the cross-coupling effect of the adjacent two cyclones produces a reverse flow effect, and the countercurrent effect occurs, causing the flue gas flow rate to decrease, but due to the droplets ( Densities of 1000 to 1200 Kg / m ³ ) and/or dust (bulk density of approximately 1600 to 2200 kg/m ³ ) are much higher than those of gas streams (density of 1.1-1.3 Kg/m ³ ), so droplets And/or the dust is relatively slipped by the high inertial force and the forward-moving airflow, and there is a certain viscosity due to the airflow (the dynamic viscosity is about 1.96×10 ^-5 Pa under the condition of 1 atm and 50 °C). .s) to create a viscous force (ie, viscous internal friction, proportional to the surface area of the dust and/or droplets) of droplets and/or dust that occurs relative to slip, to prevent this relative slip, due to The droplets and/or dust have a large specific surface area, so the relative slip speed of larger droplets and/or larger dust is higher than that of smaller droplets and/or smaller dust, so larger liquid Drop and (or) larger powder It will take place in pursuit of smaller droplets and (or) less dust effects and a great probability will be smaller droplets and (or) resulting in less dust captured droplets and (or) grew up dust.

其次，相邻两旋风装置交汇耦合区域的逆流效应将直接导致烟气流中的细微粉尘和（或）微小液滴与迎面而来气流中的微小液滴和（或）细微粉尘直接相向碰撞从而实现粉尘和（或）液滴长大。由于相邻两旋风装置的旋流叶片均为顺时针方向或者逆时针方向，所以相邻两旋风装置的交汇耦合区域产生气流逆流效应，气流中的大量的细微粉尘和（或）微小液滴与迎面而来的气流中的细微粉尘和（或）微小液滴发生碰撞导致粉尘和粉尘之间、粉尘和液滴之间、液滴和液滴之间发生一次聚合、二次聚合甚至多次聚合从而形成大粉尘和（或）大液滴颗粒。Secondly, the countercurrent effect of the intersection of the two adjacent cyclone devices will directly cause the fine dust and/or tiny droplets in the flue gas stream to directly collide with the tiny droplets and/or fine dust in the oncoming airflow. Achieve dust and/or droplet growth. Since the swirling blades of the adjacent two cyclones are clockwise or counterclockwise, the intersection coupling region of the adjacent two cyclones generates a reverse flow effect of the airflow, and a large amount of fine dust and/or minute droplets in the airflow The collision of fine dust and/or tiny droplets in the oncoming airflow causes a single polymerization, secondary polymerization or even multiple polymerization between the dust and dust, between the dust and the droplets, between the droplets and the droplets. Thereby large dust and/or large droplet particles are formed.

再次，高速气流致使停留在旋流叶片上的液膜被重新卷起现象（下称携带现象）形成新增超大液滴，超大液滴捕获细微粉尘和（或）液滴效应。下游位置的波纹薄板分离器或冷凝湿膜离心分离器分离下的液滴形成水膜在重力作用下会汇聚在旋风装置的旋流叶片上，其表面上会形成一层薄薄的液膜，经过特殊设计的旋风装置，烟气流过相邻两旋流叶片之间构成的狭小流道时，发生的携带现象将形成大量的超大液滴，这些新增的超大液滴，在上述两种液滴和（或）粉尘增大效应中将发挥更为巨大的聚合作用。Again, the high velocity gas stream causes the liquid film remaining on the swirling vanes to be re-rolled (hereinafter referred to as carrying phenomenon) to form new super large droplets, which capture fine dust and/or droplet effects. The droplet forming water film separated by the corrugated thin plate separator or the condensed wet film centrifugal separator at the downstream position will accumulate on the swirling vane of the cyclone device under the action of gravity, and a thin liquid film will be formed on the surface. After a specially designed cyclone device, when the smoke flows through the narrow flow path formed between the adjacent two swirling blades, the carrying phenomenon will form a large number of super large droplets, and these newly added super large droplets are in the above two kinds. A greater polymerization will occur in the droplet and/or dust augmentation effect.

本发明还提供了一种烟气流道，包括一级或多级上述任意一种用于聚合细微颗粒的聚合器，聚合器被布置于含有细微颗粒的烟气气流的断面上。The present invention also provides a flue gas flow path comprising one or more of the above-described polymerizers for polymerizing fine particles, the polymerizer being disposed on a section of the flue gas stream containing fine particles.

进一步地，聚合器所在的平面与烟气气流的方向基本垂直。Further, the plane in which the aggregator is located is substantially perpendicular to the direction of the flue gas stream.

进一步地，聚合器所在的平面与烟气气流的方向具有夹角 β ，夹角 β 为 22.5 ～ 65° 。Further, the plane in which the aggregator is located has an angle β with the direction of the flue gas flow, and the angle β is 22.5 to 65°.

进一步地，烟气流道采用钢基础结构分区布置，每个区所在的平面内相应地设置有聚合器。Further, the flue gas passages are arranged in a partitioned manner of a steel infrastructure, and a polymerizer is disposed correspondingly in a plane in which each zone is located.

进一步地，设置在每个区内的聚合器的多个旋风装置分别位于两个形成 V 字形或人字形的平面内。Further, a plurality of cyclones arranged in the aggregator in each zone are respectively located in two planes forming a V-shape or a chevron.

进一步地，所述烟气流道的直径为 1.5~30m 。Further, the diameter of the air flow passage is 1.5 to 30 m.

由于本发明提供的上述用于聚合细微颗粒的聚合器主要实现细微颗粒物聚合，在实际应用中，通常不适宜单独作为分离器使用，因此本发明还提供了一种除尘除雾一体化***，该***包括一级或多级上述任意一种用于聚合细微颗粒聚合器，该聚合器的上游和 / 或下游位置设置有弯曲流道式分离器，弯曲流道式分离器中的分离元件构成多个弯曲的气流通道，使得气流经过多个弯曲的气流通道时，气流不断改变流动方向，气流中的液滴在离心力作用下撞击分离元件，大量撞击在分离元件的液滴形成水膜，水膜在重力作用下回落。Since the above-mentioned polymerizer for polymerizing fine particles mainly realizes the polymerization of fine particles, in practical applications, it is generally not suitable to be used as a separator alone, and therefore the present invention also provides an integrated dust removal and defogging system. The system includes one or more of the above-described ones for polymerizing a fine particle aggregator, upstream of the aggregator and / Or a downstream position is provided with a curved flow path type separator, and the separation elements in the curved flow path type separator form a plurality of curved air flow passages, so that when the air flow passes through the plurality of curved air flow passages, the air flow continuously changes the flow direction, and the air flow The droplets collide with the separating element under the action of centrifugal force, and a large amount of droplets impinging on the separating element form a water film, and the water film falls back under the action of gravity.

进一步地，聚合器与弯曲流道式分离器的距离小于 1500mm 。Further, the distance between the polymerizer and the curved channel separator is less than 1500 mm.

优选地，聚合器与弯曲流道式分离器的距离小于 50mm 。Preferably, the distance between the polymerizer and the curved channel separator is less than 50 mm.

进一步地，弯曲流道式分离器中的分离元件为波纹板组件，因而该弯曲流道式分离器为波纹板式气液分离器，波纹板组件包括多个间隔的、均匀布置的波纹板，多个波纹板形成弯曲的气流通道，使得气流不断改变流动方向；相邻两波纹板之间的距离为 10~60mm ；波纹板优选为正弦曲线形波纹薄板，波纹板具有钩和 / 或孔等附属结构，钩和孔均具有一个或多个；波纹板的厚度为 1.0~3.5mm ；波纹板为实心或中空结构。Further, the separating element in the curved flow path separator is a corrugated plate assembly, and thus the curved flow path type separator is a corrugated plate type gas-liquid separator, and the corrugated plate assembly comprises a plurality of spaced, uniformly arranged corrugated plates, The corrugated plates form a curved air flow passage, so that the air flow continuously changes the flow direction; the distance between the adjacent two corrugated plates is 10~60mm; the corrugated plate is preferably a sinusoidal corrugated sheet, the corrugated plate has an auxiliary structure such as a hook and/or a hole, and the hook and the hole have one or more; the thickness of the corrugated plate is 1.0~3.5mm The corrugated board is a solid or hollow structure.

更进一步地，波纹板为中空结构，内流有冷却介质，冷却介质的温度小于气流的温度，冷却介质由冷却介质供应***供应。此时该波纹板式气液分离器具体为冷凝湿膜离心分离器。Further, the corrugated plate is a hollow structure having a cooling medium flowing therein, the temperature of the cooling medium being lower than the temperature of the air flow, and the cooling medium being supplied by the cooling medium supply system. At this time, the corrugated plate type gas-liquid separator is specifically a condensed wet film centrifugal separator.

进一步地，旋风装置中的外筒的内直径优选地与弯曲流道式分离器中相邻两波纹板的距离相同，且旋风装置的出口气流完全被该两波纹板所接纳。Further, the inner diameter of the outer cylinder in the cyclone device is preferably the same as the distance between adjacent corrugated plates in the curved flow channel separator, and the outlet air flow of the cyclone device is completely received by the two corrugated plates.

进一步地，弯曲流道式分离器中的分离元件为 2~5 层相互交错的管束，因而弯曲流道式分离器为管式气液分离器，每一层管束包括多个间隔的、均匀布置的管，相邻两层管束中的管呈交错布置，形成弯曲的气流流道，使得气流不断改变流动方向；处于同一层管束中的管的中心间距为该层管束的管径的 1.2~4 倍；管的横截形状为圆形、水滴形或子弹头形等适合空气动力学的截面。Further, the separation element in the curved flow path separator is 2~5 The tube bundles are interlaced with each other, and thus the curved channel separator is a tubular gas-liquid separator, each tube bundle includes a plurality of spaced, uniformly arranged tubes, and the tubes in the adjacent two tube bundles are staggered to form a bend Air flow path, so that the air flow constantly changes the flow direction; the center distance of the tubes in the same layer of tube bundle is the diameter of the tube bundle 1.2~4 times; the cross-sectional shape of the tube is aerodynamically shaped cross section such as round, drop-shaped or bullet-shaped.

本发明还提供了另一种除尘除雾一体化***，包括一级或多级上述任意一种用于聚合细微颗粒的聚合器，聚合器的上游位置设置有一级或多级预分离器，和 / 或聚合器的下游位置设置有一级或多级精细分离器和 / 或一级或多级超精细分离器；The present invention also provides another integrated dust removal and defogging system, comprising one or more of the above-mentioned polymerizers for polymerizing fine particles, the first position of the polymerization device being provided with one or more stages of pre-separators, and / Or a downstream position of the polymerizer is provided with one or more stages of fine separators and / or one or more stages of superfine separators;

精细分离器具有比预分离器更高的液滴分离性能，超精细分离器具有比精细分离器更高的液滴分离性能。The fine separator has higher droplet separation performance than the pre-separator, and the ultra-fine separator has higher droplet separation performance than the fine separator.

进一步地，预分离器包括弯曲流道式分离器，或者精细分离器包括弯曲流道式分离器。Further, the pre-separator includes a curved flow channel separator, or the fine separator includes a curved flow channel separator.

进一步地，预分离器为管式设计预分离器、平板设计预分离器、屋顶设计预分离器、水平气流预分离器中的一种或者多种的组合；超精细分离器为平板设计超精细分离器、屋顶设计超精细分离器、水平气流超精细分离器中的一种或者多种的组合。Further, the pre-separator is a combination of one or more of a tubular design pre-separator, a flat design pre-separator, a roof design pre-separator, a horizontal air pre-separator; the ultra-fine separator is a super-fine design for the flat plate A combination of one or more of a separator, a roof design superfine separator, a horizontal gas flow ultrafine separator.

进一步地，一级或多级预分离器、一级或多级聚合器以及一级或多级精细分离器和 / 或超精细分离器全部布置在烟气吸收塔内，气流的流动方向为竖直方向。Further, one or more stages of pre-separators, one or more stages of aggregators, and one or more stages of fine separators and / Or the ultra-fine separators are all arranged in the flue gas absorption tower, and the flow direction of the airflow is a vertical direction.

进一步地，一级或多级预分离器、一级或多级聚合器以及一级或多级精细分离器和 / 或超精细分离器全部布置在吸收塔出口水平烟道内，气流的流动方向为水平方向。Further, one or more stages of pre-separators, one or more stages of aggregators, and one or more stages of fine separators and / Or the ultra-fine separators are all arranged in the horizontal flue of the absorption tower outlet, and the flow direction of the airflow is horizontal.

进一步地，一级或多级预分离器、一级或多级聚合器以及一级或多级精细分离器和 / 或超精细分离器中的一部分布置在吸收塔内，另一部分布置在吸收塔出口水平烟道内，在吸收塔内气流呈竖直方向，在吸收塔水平出口烟道内气流呈水平方向。Further, one or more stages of pre-separators, one or more stages of aggregators, and one or more stages of fine separators and / Or a portion of the ultrafine separator is disposed in the absorption tower, and another portion is disposed in the horizontal flue of the absorption tower outlet. The airflow in the absorption tower is in a vertical direction, and the airflow in the horizontal outlet flue of the absorption tower is horizontal.

进一步地，任何一级预分离器、任何一级聚合器和任何一级精细分离器和 / 或超精细分离器均根据实际运行工况需要在各自对应的气流入口侧和 / 或气流出口测设置有自动和 / 或手动清洗装置，清洗装置包括管道和冲洗喷嘴。Further, any primary pre-separator, any primary aggregator and any primary fine separator and / Or the ultra-fine separators are provided with automatic and/or manual cleaning devices on their respective gas inlet side and/or air outlet outlets according to actual operating conditions, and the cleaning devices include pipes and flushing nozzles.

本发明还提供了一种使烟气中细微颗粒聚合的方法，该方法为，使烟气通过旋风装置，从而产生多股旋转方向相同的旋转气流，旋转气流与相邻的旋转气流之间发生交汇与对冲。The present invention also provides a method for polymerizing fine particles in a flue gas by passing the flue gas through a cyclone device to generate a plurality of swirling gas streams of the same direction of rotation, which occurs between the swirling gas stream and the adjacent swirling gas stream. Convergence and hedging.

本发明还提供了一种一体化除尘除雾方法，该方法为，使烟气通过旋风装置，从而产生多股旋转方向相同的旋转气流，旋转气流与相邻的旋转气流之间发生交汇与对冲；还使烟气通过设置在旋风装置上游和 / 下游位置的弯曲流道式分离器，弯曲流道式分离器中的分离元件构成多个弯曲的气流通道，使得气流经过多个弯曲的气流通道时，气流不断改变流动方向，气流中的雾滴或携有固体颗粒物的液滴在离心力作用下撞击分离元件，并形成水膜，水膜在重力作用下回落。The invention also provides an integrated dust removal and defogging method, which is to make the flue gas pass through the cyclone device, thereby generating a plurality of rotating airflows having the same rotation direction, and the intersection and the heel between the rotary airflow and the adjacent rotary airflow. Also allowing the flue gas to pass upstream of the cyclone and / A curved flow path separator at a downstream position, the separation element in the curved flow path separator constitutes a plurality of curved air flow passages, so that when the air flow passes through the plurality of curved air flow passages, the air flow continuously changes the flow direction, and the air flow in the air flow Or the droplets carrying the solid particles collide with the separating element under the action of centrifugal force, and form a water film, and the water film falls back under the action of gravity.

进一步地，弯曲流道式分离器设置在旋风装置的下游位置，使得水膜在重力作用下回落到旋风装置的旋流叶片上。Further, the curved flow path separator is disposed at a position downstream of the cyclone device such that the water film falls back to the swirling blades of the cyclone device by gravity.

进一步地，还使烟气通过设置在旋风装置的上游位置的一级或多级预分离器和 / 或设置在旋风装置的下游位置的一级或多级超精细分离器。Further, the flue gas is also passed through a primary or multi-stage pre-separator disposed at an upstream position of the cyclone device and/or Or a one-stage or multi-stage superfine separator disposed downstream of the cyclone.

在本 发明 的较佳实施方式中 ，除尘除雾一体化***布置在烟气吸收塔的下游位置，气流依次经过除尘除雾一体化***中的预分离器、细微颗粒聚合器、冷凝湿膜离心分离器（或波纹板式气液分离器）以及超精细分离器等，预分离器、细微颗粒聚合器、冷凝湿膜离心分离器（或波纹板式气液分离器）以及超精细分离器可以全部布置在烟气吸收塔内顶部位置，也可以全部布置在烟气吸收塔出口水平烟道内，也可以一部分布置在吸收塔内顶部位置一部分布置在烟气吸收塔出口水平烟道内，具体的实施方案将由各个项目现场的空间所决定。In a preferred embodiment of the invention The dust removal and defogging integrated system is arranged downstream of the flue gas absorption tower, and the air flow passes through the pre-separator, the fine particle aggregator, the condensed wet film centrifugal separator (or the corrugated plate type gas-liquid separation) in the dust removal and defogging integrated system. And superfine separators, etc., pre-separators, fine particle aggregators, condensed wet film centrifugal separators (or corrugated plate gas-liquid separators) and ultra-fine separators can all be placed at the top of the flue gas absorption tower. It may also be arranged in the horizontal flue of the flue gas absorption tower outlet, or a part of the top position in the absorption tower may be arranged in the horizontal flue of the flue gas absorption tower outlet. The specific embodiment will be determined by the space of each project site.

预分离器，其主要功能是去除烟气吸收塔喷淋层产生的大液滴，对于粒径 18 微米以上的大液滴，其去除效率可以达到 100% ；对于粒径 5 ～ 18 微米的液滴，具有不同程度的分离效率，液滴越小，分离效率越低，液滴越大，分离效率越高；对于粒径 5 微米以下的液滴，理论上没有分离效果，只存在极少数量的液滴撞击在分离元件上被拦截去除。典型的燃煤电厂烟气脱硫吸收塔，原烟气经过 3-6 层喷淋层洗涤后，约有 10000mg/Nm³ 的液滴可能进入预分离器，因此首先需要将大量的液滴浓度降低到 ≤75mg/Nm³ ，甚至小于 ≤35mg/Nm³ 。Pre-separator, its main function is to remove large droplets generated by the spray layer of the flue gas absorption tower. For large droplets with a particle size of more than 18 microns, the removal efficiency can reach 100%; for liquids with a particle size of 5-18 microns Drops have different degrees of separation efficiency. The smaller the droplets, the lower the separation efficiency. The larger the droplets, the higher the separation efficiency. For droplets with a particle size below 5 microns, there is theoretically no separation effect, only a small amount. The droplets impinge on the separation element are intercepted and removed. A typical coal-fired power plant flue gas desulfurization absorber tower, after the original flue gas is washed by the 3-6 layer spray layer, about 10000mg/Nm ³ droplets may enter the pre-separator, so it is first necessary to reduce the concentration of a large number of droplets. To ≤75mg/Nm ³ , even less than ≤35mg/Nm ³ .

预分离器优选地采用一级管式分离器、一级粗屋顶分离器和一级细屋顶分离器。The pre-separator preferably employs a primary tubular separator, a primary coarse roof separator and a primary fine roof separator.

管式分离器，优选地采用 2 ～ 3 层交错布置的圆管作为分离元件，同一层圆管之间距离优选地采用 90 ～ 110mm ，圆管直径优选地选用 D50 ～ D90 ；圆管呈水平布置（在吸收塔内安装）或者垂直布置（在吸收塔出口水平烟道内安装）；The tubular separator preferably uses two to three layers of staggered circular tubes as the separating elements, and the distance between the tubes of the same layer is preferably 90 ～. 110mm, the diameter of the round pipe is preferably D50 ~ D90; the round pipe is arranged horizontally (installed in the absorption tower) or vertically (installed in the horizontal flue of the absorption tower outlet);

粗屋顶分离器，优选地采用似正弦波纹薄板作为分离元件，相邻两波纹薄板之间的间距 S 优选地选用 25 ～ 30mm ，分离元件倾斜角度（分离元件与水平面的夹角）优选地选用 25 ～ 37.5° ；屋顶分离器可以呈' V '字形布置或者'人'字形布置，优选地选用'人'字形布置。The coarse roof separator preferably uses a sinusoidal corrugated sheet as the separating element, and the spacing S between adjacent corrugated sheets is preferably 25 ～ 30mm, the angle of inclination of the separating element (the angle between the separating element and the horizontal plane) is preferably 25 to 37.5°; the roof separator can be 'V A 'glyph arrangement' or a 'human' glyph arrangement, preferably a 'human' glyph arrangement.

细屋顶除雾器，优选地采用似正弦波纹薄板作为分离元件，分离元件带钩设计，相邻两波纹薄板之间间距述 S 优选地选用 22.0 ～ 27.5mm, 分离元件倾斜角度优选地选用 25 ～ 37.5° ；细屋顶分离器可以呈' V '字形布置或者'人'字形布置。The fine roof defogger preferably uses a sinusoidal corrugated thin plate as a separating element, and the separating element has a hook design, and the spacing between adjacent corrugated sheets is S Preferably, 22.0 to 27.5 mm is selected, and the inclination angle of the separating member is preferably 25 to 37.5 degrees; the thin roof separator may be arranged in a 'V' shape or a 'human' shape.

预分离器的选型只要满足预分离器后方的液滴浓度小于 75 mg/Nm³ 即可，优选考虑小于 35 mg/Nm³ ，因此预分离器采用其他的现有技术方案，比如一级管式分离器、一级平板式分离器和一级细屋顶除雾器，也可以只采用一级管式分离器和一级细屋顶分离器或者一级粗屋顶分离器和一级细屋顶分离器，这种设置对净烟气的污染物排放略有影响。The pre-separator can be selected as long as the droplet concentration behind the pre-separator is less than 75 mg/Nm ³ , preferably less than 35 mg/Nm ³ , so the pre-separator adopts other prior art solutions, such as the first-stage tube. Separator, primary flat separator and primary fine roof demister, or only primary pipe separator and primary fine roof separator or primary coarse roof separator and primary fine roof separator This setting has a slight impact on the emissions of net flue gas pollutants.

更进一步地，当细微颗粒聚合器、冷凝湿膜离心分离器（或波纹板式气液分离器）设计为两级或者两级以上时候，预分离器优选为一级管式分离器和一级屋顶分离器，预分离器后方的液滴浓度小于 150 mg/Nm³ 通常也是可行的。Further, when the fine particle aggregator, the condensed wet film centrifugal separator (or the corrugated plate type gas-liquid separator) is designed to be two or more stages, the pre-separator is preferably a first-stage tubular separator and a primary roof. It is also generally feasible to have a separator with a droplet concentration behind the pre-separator of less than 150 mg/Nm ³ .

冷凝湿膜离心分离器，其主要功能是进一步深度将被细微颗粒聚合器聚合过的微小液滴以及细微粉尘通过冷凝方式再次进行二级增大，同时由于自身结构形式为多弯波纹形状，兼有卓越液滴分离性能。通过冷凝方式二级增大，经过试验表明，在控制好合适的冷凝水汽析出量时，可以将所有微小液滴和细微粉尘的粒径都将增大到 6 微米以上，大部分的液滴的粒径超过 10 微米，甚至超过 13 微米，这些增大后的微小液滴和细微粉尘足以使得自身作为分离器作用和后续的超精细分离器表现出非常出色的分离性能。Condensed wet film centrifugal separator, whose main function is to further deepen the secondary droplets and fine dusts which have been polymerized by the fine particle aggregator by the condensation method, and at the same time, due to the self-structure form, the shape of the multi-bend corrugated shape Excellent droplet separation performance. Through the second increase of the condensation mode, it has been experimentally shown that when the proper amount of condensed water vapor is controlled, the particle size of all the fine droplets and fine dust can be increased to Above 6 microns, most droplets have a particle size of more than 10 microns, or even more than 13 Micron, these enlarged microdroplets and fine dust are sufficient to provide excellent separation performance as a separator and subsequent ultrafine separators.

冷凝湿膜离心分离器，其分离元件优选为中空的波纹板，内流有冷却水，饱和的湿烟气经过冷凝湿膜离心分离器时，烟气温度下降而析出大量的水汽，产生的水汽自动寻找残余微小液滴和（或）微小粉尘作为凝结核，微小液滴和（或）微小粉尘吸附大量水汽后长大，在相同气体流速下将受到更大的离心力；更为重要的是不规则表面的粉尘通过吸附水汽后变成球体，将粉尘和烟气接触转化为水滴和烟气接触从而大幅降低粉尘和烟气之间的粘性力，因此在弯曲的流道内流动时形成较大的离心力从而撞击在分离元件上。而且由于中空波纹板具有冷壁效应，在中空波纹板的外表面会形成一层均匀稳定的水膜，撞击在中空波纹板的液滴和（或）粉尘被水膜瞬间湮灭，使得微小液滴和（或）微小粉尘被捕获拦截并去除。The condensing wet film centrifugal separator has a separation element which is preferably a hollow corrugated plate, and has cooling water flowing therein. When the saturated wet flue gas passes through the condensing wet film centrifugal separator, the temperature of the flue gas drops to precipitate a large amount of water vapor, and the generated water vapor Automatically find residual tiny droplets and/or tiny dust as condensation nuclei. Small droplets and/or tiny dusts will grow up after adsorbing a large amount of water vapor, and will receive greater centrifugal force at the same gas flow rate; more importantly, no The dust on the regular surface becomes a sphere by adsorbing water vapor, and the contact between the dust and the flue gas is converted into contact between the water droplets and the flue gas, thereby greatly reducing the viscous force between the dust and the flue gas, and thus forming a large flow when flowing in the curved flow passage. The centrifugal force thus impinges on the separating element. Moreover, since the hollow corrugated plate has a cold wall effect, a uniform and stable water film is formed on the outer surface of the hollow corrugated plate, and the droplets and/or dust impinging on the hollow corrugated plate are instantaneously quenched by the water film, so that the minute droplets are caused. And/or tiny dust is captured and intercepted and removed.

当烟尘排放要求可以略低时（比如允许烟尘浓度小于 10mg/Nm³ ），退而求其次的可选择的技术方案是采用传统的平板式分离器或者屋顶式分离器来代替冷凝湿膜离心分离器，即分离元件不具有中空结构，不具有冷凝对细微粉尘和（或）微小液滴增大功能。When the soot emission requirement can be slightly lower (such as allowing the soot concentration to be less than 10 mg/Nm ³ ), the alternative technical solution is to use a conventional flat separator or roof separator instead of the condensation wet film centrifugal separation. The separation element does not have a hollow structure and does not have the function of condensing against fine dust and/or minute droplets.

需要特别说明的是，试验结果表明，细微颗粒聚合器和冷凝湿膜离心分离器（或波纹板式气液分离器）组合使用时，将产生令人非常惊喜的聚合效果和分离效果，其组合后的性能要远远高于细微颗粒聚合器和冷凝湿膜离心分离器（或波纹板式气液分离器）各自单个聚合效果和分离效果之和。In particular, the test results show that when the fine particle aggregator and the condensed wet film centrifugal separator (or corrugated plate gas-liquid separator) are used in combination, it will produce a very pleasant polymerization effect and separation effect. The performance is much higher than the sum of the individual polymerization effects and separation effects of the fine particle aggregator and the condensed wet film centrifugal separator (or the corrugated plate gas-liquid separator).

超精细分离器，拥有非常卓越的分离性能，根据相应的工况优化设计后，其极限液滴粒径可以低至 12 ～ 13 微米 , 对 10 微米的液滴具有 80% 以上的分离效率；对 8 微米的液滴具有 60% 以上的分离效率；对 6 微米的液滴具有 40% 以上的分离效率。Ultra-fine separator with excellent separation performance. After optimization according to the corresponding working conditions, the limit droplet size can be as low as 12 ~ 13 Micron, with more than 80% separation efficiency for 10 micron droplets; 60% separation efficiency for 8 micron droplets; 40% for 6 micron droplets The above separation efficiency.

极限液滴粒径是指当液滴的粒径达到或者超过该尺寸时，该液滴将 100% 被分离去除。因此极限液滴粒径是分离器的最重要性能技术指标。The limit droplet size means that when the droplet size reaches or exceeds the size, the droplet will be 100% It is separated and removed. Therefore, the ultimate droplet size is the most important performance specification for the separator.

可以对比的是，现有的细屋顶分离器，通常采用两弯一钩的正弦波纹薄板、旋流叶片间距为 22 ～ 25mm 、倾斜角度为 35 ～ 37.5° 、在设计空塔烟气流速 3.85m/ 间距下，极限液滴粒径约为 18 微米。In contrast, the existing fine roof separators usually use two-bend and one-hook sinusoidal corrugated sheets with a swirling blade spacing of 22 to 25 mm. The angle of inclination is 35 ~ 37.5 °, and the limit droplet size is about 18 microns at the design of the empty tower flue gas flow rate of 3.85 m / spacing.

超精细分离器，极限液滴粒径低至 12 ～ 13 微米，仅为 18 微米液滴质量的约 1/3 。Ultra-fine separators with a minimum droplet size as low as 12 to 13 microns, which is only about 1/3 of the mass of a 18 micron droplet.

超精细分离器，优选地采用三弯似正弦波纹薄板作为分离元件，分离元件带一钩和一孔设计，相邻两波纹薄板之间间距 S 优选地选用 22.0 ～ 33.0mm ，倾斜角度优选地选用 30 ～ 37.5° 。Ultrafine separator, preferably using a three-bend sinusoidal corrugated sheet as the separating element, the separating element with a hook and a hole design, the spacing between two adjacent corrugated sheets S is preferably selected from 22.0 to 33.0 mm, and the inclination angle is preferably from 30 to 37.5.

超精细分离器，优选地设计净面积率 ≥85% ，在小吸收塔内（比如小于 10m ），设计净面积率通常不低于 80% 。Ultra-fine separator, preferably designed with a net area ratio of ≥ 85%. In a small absorption tower (such as less than 10m), the design net area ratio is usually not lower than 80%.

本发明的高效除尘除雾一体化***，气流依次经过预分离器、细微颗粒聚合器、冷凝湿膜离心分离器（或波纹板式气液分离器）以及超精细分离器后，液滴含量将小于 10.0mg/Nm³ ( 采用 Mg²⁺ 示踪法 ) 或者小于 1.0mg/Nm³( 采用 TüV >15 微米撞击法检测 ) ；当采用两级或多级细微颗粒聚合器、冷凝湿膜离心分离器（或波纹板式气液分离器）设计时，液滴含量将小于 5.0mg/Nm³ ( 采用 Mg²⁺ 示踪法 ) 或者小于 0.5mg/Nm³( 采用 TüV >15 微米撞击法检测 ) 。雾滴分离效果远远高于高效除雾器（比如三级屋顶除雾器）所表现的除雾效果。The high-efficiency dust removal and defogging integrated system of the invention has the droplet content less than that of the pre-separator, the fine particle aggregator, the condensed wet film centrifugal separator (or the corrugated plate gas-liquid separator) and the ultrafine separator. 10.0mg/Nm ³ (using Mg ²⁺ tracer method) or less than 1.0mg/Nm ³ (tested by TüV >15 μm impact method); when using two or more stages of fine particle aggregator, condensing wet film centrifugal separator (or corrugated plate gas-liquid separator) design, the droplet content will be less than 5.0mg / Nm ³ (using Mg ²⁺ tracer method) or less than 0.5mg / Nm ³ (tested by TüV > 15 micron impact method). The droplet separation effect is much higher than that of a high-efficiency mist eliminator (such as a three-stage roof defogger).

本发明的高效除尘除雾一体化***，气流依次经过预分离器、细微颗粒聚合器、冷凝湿膜离心分离器（或波纹板式气液分离器）以及超精细分离器后，当吸收塔入口粉尘小于 20mg/Nm³ 下，可确保气流中残余的烟尘浓度小于 3.5mg/Nm³ ；当脱硫吸收塔入口粉尘小于 30mg/Nm³ 下，可确保气流中残余的烟尘浓度小于 5.0mg/Nm³ ；当脱硫吸收塔入口粉尘小于 50mg/Nm³ 下，可确保气流中残余的烟尘浓度小于 10.0 mg/Nm³ 。若采用两级或者多级细微颗粒聚合器、冷凝湿膜离心分离器（或波纹板式气液分离器），无论入***量多少，都可以实现小于 5.0mg/Nm³ 。The high-efficiency dust removal and defogging integrated system of the invention passes through the pre-separator, the fine particle aggregator, the condensed wet film centrifugal separator (or the corrugated plate gas-liquid separator) and the ultra-fine separator, and then the dust at the inlet of the absorption tower Less than 20mg/Nm ³ can ensure that the residual soot concentration in the gas stream is less than 3.5mg/Nm ³ ; when the desulfurization absorber inlet dust is less than 30mg/Nm ³ , the residual soot concentration in the gas stream can be ensured to be less than 5.0mg/Nm ³ ; When the dust at the inlet of the desulfurization absorber is less than 50 mg/Nm ³ , the residual soot concentration in the gas stream is ensured to be less than 10.0 mg/Nm ³ . If a two-stage or multi-stage fine particle aggregator, a condensing wet film centrifugal separator (or a corrugated plate gas-liquid separator) is used, less than 5.0 mg/Nm ³ can be achieved regardless of the inlet content.

本发明的一种高效除尘除雾一体化***，如果气流中的液滴浓度本身不高，可以取消预处理器，只采用细微颗粒聚合器、冷凝湿膜离心分离器以及超精细分离器。In the high-efficiency dust removal and defogging integrated system of the invention, if the concentration of the droplets in the gas stream itself is not high, the pre-processor can be eliminated, and only the fine particle aggregator, the condensed wet film centrifugal separator and the ultra-fine separator are used.

本发明的一种高效除尘除雾一体化***，如果气流中的液滴浓度本身不高，出口烟尘浓度也要求不高，比如入口烟尘浓度为 50mg/Nm³, 出口烟尘浓度允许小于 20mg/Nm³, 可以取消预处理器和超精细分离器，只采用细微颗粒聚合器、冷凝湿膜离心分离器。The high-efficiency dust removal and defogging integrated system of the invention has low requirements on the concentration of the outlet soot if the concentration of the droplets in the airflow is not high, such as the inlet soot concentration is 50 mg/Nm ³ and the outlet soot concentration is allowed to be less than 20 mg/Nm. ³ , Can remove the pre-processor and ultra-fine separator, using only fine particle aggregator, condensing wet film centrifugal separator.

本发明的一种高效除尘除雾一体化***，是否采用预处理器或者超精细分离器或者采用 1 级或者多级细微颗粒聚合器均取决于设计参数。根据提供的设计参数后，利用计算机模拟计算并结合科学实验、工程实践做设计修正即可满足。The invention relates to an integrated dust removal and defogging integrated system, whether a preprocessor or a superfine separator is used or adopts 1 Grade or multistage fine particle aggregators depend on design parameters. According to the design parameters provided, the computer simulation can be used to make design corrections in combination with scientific experiments and engineering practices.

本发明的一种高效除尘除雾一体化***，由于应用环境中不是水滴，而是浆液滴，所以对于任何一级预分离器、细微颗粒聚合器、冷凝湿膜离心分离器（或波纹板式气液分离器）和超精细分离器均根据实际运行工况需要而在其气流入口侧和（或）气流出口侧设有自动（或手动）清洗装置，清洗装置由管道和冲洗喷嘴组成。The high-efficiency dust removal and defogging integrated system of the invention has no pre-separator, fine particle aggregator, condensed wet film centrifugal separator (or corrugated plate gas) because it is not water droplets but slurry droplets in the application environment. Both the liquid separator and the ultrafine separator are provided with automatic (or manual) cleaning devices on their gas inlet side and/or gas outlet side according to actual operating conditions. The cleaning device consists of a pipe and a flushing nozzle.

与现有技术相比，本发明的除尘除雾一体化***具有以下有益效果：Compared with the prior art, the dust removal and defogging integrated system of the invention has the following beneficial effects:

（ 1 ）本发明的高效除尘除雾一体化***既是卓越的液滴分离器也是卓越的粉尘分离器；(1) The high-efficiency dust removal and defogging integrated system of the present invention is both an excellent droplet separator and an excellent dust separator;

（ 2 ）使得整个烟气脱硫吸收塔的设计更为简化，喷淋层、托盘、旋风耦合、 FGD 普拉斯等设施只是吸收 SO₂ 功能，而并不额外需要考虑去尘功能；(2) The design of the entire flue gas desulfurization absorption tower is simplified, and the facilities such as the spray layer, the tray, the cyclone coupling, and the FGD Plass only absorb the SO ₂ function, and there is no need to consider the dust removal function;

（ 3 ）降低整个脱硫装置的投资成本；(3) reducing the investment cost of the entire desulfurization unit;

（ 4 ）降低整个脱硫装置的运行成本，符合国家节能减排发展战略；(4) Reducing the operating cost of the entire desulfurization unit, in line with the national energy conservation and emission reduction development strategy;

（ 5 ）通过碰撞聚合和冷凝吸附双重增大功效，将细微粉尘和微小液滴更有效放大，提高了整套除尘除雾一体化***的综合效率；(5 By double-increasing the effect of collision polymerization and condensation adsorption, the fine dust and minute droplets are more effectively amplified, and the overall efficiency of the integrated dust removal and defogging integrated system is improved;

（ 6 ）设备全部采用耐腐蚀的非金属材料，使用寿命长；(6) The equipment is made of corrosion-resistant non-metallic materials and has a long service life;

（ 7 ）装置日常维护成本低，无需经常更换零部件；(7) The daily maintenance cost of the device is low, and it is not necessary to replace parts frequently;

（ 8 ）设备可靠性高，可长期运行超过 25000 hr 。(8) The equipment has high reliability and can operate for more than 25000 hr for a long time.

以下将结合附图对本发明的构思、具体结构及产生的技术效果作进一步说明，以充分地了解本发明的目的、特征和效果。The concept, the specific structure and the technical effects of the present invention will be further described in conjunction with the accompanying drawings in order to fully understand the objects, features and effects of the invention.

附图说明DRAWINGS

图 1 是本发明的实施例 1 的高效除尘除雾一体化***的结构剖视图；Figure 1 is a cross-sectional view showing the structure of an integrated dust removal and defogging integrated system according to Embodiment 1 of the present invention;

图 2 为图 1 的 A － A 剖面图；Figure 2 is a cross-sectional view taken along line A - A of Figure 1;

图 3 为单个旋风装置三维图；Figure 3 is a three-dimensional view of a single cyclone;

图 4 为单个旋风装置的俯视图；Figure 4 is a plan view of a single cyclone device;

图 5 为细微颗粒聚合器工作原理图；Figure 5 is a schematic diagram of the operation of the fine particle aggregator;

图 6 为本发明实施例 1 的高效除尘除雾一体化***的第二方案结构示意图；6 is a schematic structural diagram of a second scheme of an integrated dust removal and defogging integrated system according to Embodiment 1 of the present invention;

图 7 为本发明实施例 1 的高效除尘除雾一体化***的第三方案结构示意图；7 is a schematic structural diagram of a third scheme of an integrated dust removal and defogging integrated system according to Embodiment 1 of the present invention;

图 8 为本发明实施例 1 的高效除尘除雾一体化***的第四方案结构示意图；8 is a schematic structural diagram of a fourth scheme of an integrated dust removal and defogging integrated system according to Embodiment 1 of the present invention;

图 9 为本发明的实施例 2 的高效除尘除雾一体化***的第一方案结构示意图；9 is a schematic structural diagram of a first scheme of an integrated dust removal and defogging integrated system according to Embodiment 2 of the present invention;

图 10 为典型的管式预分离器 11 的示意图；Figure 10 is a schematic view of a typical tubular pre-separator 11;

图 11 为典型的人字形屋顶式分离器的结构示意图；Figure 11 is a schematic view showing the structure of a typical herringbone roof type separator;

图 12 为一孔一钩形波纹板式气液分离器结构示意图；Figure 12 is a schematic view showing the structure of a hole-and-hook corrugated plate type gas-liquid separator;

图 13 为本发明的实施例 2 的高效除尘除雾一体化***的第二方案结构示意图；13 is a schematic structural view of a second embodiment of an integrated dust removal and defogging integrated system according to Embodiment 2 of the present invention;

图 14 为本发明的实施例 2 的高效除尘除雾一体化***的第三方案结构示意图。Figure 14 is a schematic view showing the structure of a third embodiment of the high-efficiency dust removal and defogging integrated system of Embodiment 2 of the present invention.

具体实施方式detailed description

实施例 1Example 1

如附图 1 所示，本实施例的高效除尘除雾一体化***的第一方案是除尘除雾一体化***安装在吸收塔内，该***包含细微颗粒聚合器 20 和冷凝湿膜离心分离器 30 两部分，其中细微颗粒聚合器 20 和冷凝湿膜离心分离器 30 被布置于含有细微颗粒的烟气气流的断面上。细微颗粒聚合器 20 所在的平面和冷凝湿膜离心分离器 30 所在的平面与烟气气流的方向基本垂直。As shown in Figure 1 As shown, the first aspect of the high efficiency dust removal and defogging integrated system of the present embodiment is that the dust removal and defogging integrated system is installed in an absorption tower, and the system comprises a fine particle aggregator 20 and a condensed wet film centrifugal separator. The two parts, wherein the fine particle aggregator 20 and the condensed wet film centrifugal separator 30 are arranged on a section of the flue gas stream containing fine particles. Planar and condensing wet film centrifugal separator in which the fine particle aggregator 20 is located 30 The plane in which it is located is substantially perpendicular to the direction of the flue gas flow.

所述细微颗粒聚合器 20 和冷凝湿膜离心分离器 30 安装在一层支撑梁上。The fine particle aggregator 20 and the condensed wet film centrifugal separator 30 are mounted on a support beam.

在细微颗粒聚合器 20 的下部和冷凝湿膜离心分离器 30 的上部设有自动冲洗***。An automatic flushing system is provided at the lower portion of the fine particle aggregator 20 and at the upper portion of the condensed wet film centrifugal separator 30.

所述细微颗粒聚合器 20 和冷凝湿膜离心分离器 30 紧挨着（距离小于 10mm ）构成一个整体。The fine particle aggregator 20 and the condensed wet film centrifugal separator 30 are next to each other (distance less than 10 mm) ) constitutes a whole.

如图 2~4 所示，本实施例的细微颗粒聚合器 20 包括多个旋风装置 21 ，每个旋风装置 21 包括中心柱体 212 、外筒 213 和 s 个（ s≥2 ）旋流叶片 211 ，旋流叶片 211 能够使得包含细微颗粒的气流通过旋风装置 21 时形成旋转气流。As shown in Figures 2 to 4, the fine particle aggregator 20 of the present embodiment includes a plurality of cyclones 21, each of which is 21 The central cylinder 212, the outer cylinder 213 and the s (s≥2) swirling vanes 211 are provided, and the swirling vanes 211 can pass the airflow containing the fine particles through the cyclone device 21 A swirling airflow is formed.

本实施例中旋风装置 21 被设置为具有 6 片旋流叶片 211 。任意相邻两个旋风装置 21 的旋流叶片 211 均为逆时针方向（俯视）。多个旋流叶片 211 的一端固接于中心柱体 212 ，另一端固接于外筒 213 。本实施例的外筒 213 具有圆形截面，该圆形截面与外筒 213 的轴线垂直。旋流叶片 211 固接于外筒 213 的另一端的高度与外筒 213 的高度基本相同，或者小于外筒 213 的高度，且两者的高度差不超过外筒 213 的上述圆形截面的直径的三分之一。In the present embodiment, the cyclone device 21 is provided to have six swirling vanes 211. Swirl vane of any two adjacent cyclones 21 211 are all counterclockwise (top view). One end of the plurality of swirl vanes 211 is fixed to the center cylinder 212, and the other end is fixed to the outer cylinder 213. The outer cylinder 213 of this embodiment There is a circular cross section perpendicular to the axis of the outer cylinder 213. The height of the other end of the swirling vane 211 fixed to the outer cylinder 213 is substantially the same as the height of the outer cylinder 213, or smaller than the outer cylinder 213. The height, and the height difference between the two does not exceed one third of the diameter of the circular cross section of the outer cylinder 213.

在其它实施例中外筒 213 也可以具有正多边形截面，且该正多边形与外筒 213 的轴线垂直，此时旋流叶片 211 固接于外筒 213 的另一端的高度与外筒 213 的高度基本相同，或者小于外筒 213 的高度，且两者的高度差不超过外筒 213 的上述正多边形截面的最长对角线长度的三分之一。In other embodiments, the outer cylinder 213 may also have a regular polygonal cross section, and the regular polygon is perpendicular to the axis of the outer cylinder 213, at which time the swirling vane The height of the other end fixed to the outer cylinder 213 is substantially the same as the height of the outer cylinder 213, or is smaller than the height of the outer cylinder 213, and the height difference between the two does not exceed the outer cylinder 213. One-third of the longest diagonal length of the above regular polygonal section.

本实施例中，多个旋风装置 21 位于同一平面内，多个旋风装置 21 的轴线相互平行。在其它实施例中，多个旋风装置 21 分别位于两个形成 V 字形或人字形的平面内，位于同一平面内的旋风装置 21 的轴线相互平行。In this embodiment, the plurality of cyclones 21 are located in the same plane, and the plurality of cyclones 21 The axes are parallel to each other. In other embodiments, the plurality of cyclones 21 are respectively located in two planes forming a V-shape or a chevron, and the axes of the cyclones 21 in the same plane are parallel to each other.

旋风装置 21 的旋流叶片 211 的仰角为 12.5 ～ 60° ，本实施例优选为 22.5° 。The elevation angle of the swirling vane 211 of the cyclone 21 is 12.5 to 60°, preferably 22.5 in this embodiment. .

旋风装置 21 采用相同规格，外筒 213 的内直径为 32.5mm 。The cyclone device 21 has the same specifications, and the inner diameter of the outer cylinder 213 is 32.5 mm.

本实施例中，旋风装置 21 为将旋流叶片 211 、中心柱体 212 和外筒 213 注塑成一整体形成的。In this embodiment, the cyclone device 21 is a swirling vane 211, a central cylinder 212, and an outer cylinder 213. Injection molded into a whole.

本实施例的细微颗粒聚合器 20 还包括用于安装旋风装置 21 的固定件 22 ，固定件 22 上设置有用于安装固定旋风装置 21 的安装孔 221 ，多个旋风装置 21 通过安装孔 211 安装在固定件 22 上。固定件 22 还设置有通气孔 222 ，以降低聚合器 20 的压力损失，并避免聚合器产生积液而引起的聚合器 20 的聚合作用降低。The fine particle aggregator 20 of the present embodiment further includes a fixing member 22 for mounting the cyclone device 21, and the fixing member 22 Mounting holes 221 for mounting the fixed cyclone 21 are provided, and a plurality of cyclones 21 are mounted on the fixing member 22 through the mounting holes 211. The fixing member 22 is also provided with a vent 222 In order to reduce the pressure loss of the polymerizer 20 and to prevent the polymerization of the polymerizer 20 from being lowered by the polymerization of the polymerizer.

图 5 为本实施例的细微颗粒聚合器 20 的工作原理图，通过特殊设计（即旋流叶片 211 与外筒 213 的高度被设计为差不多）的旋风装置 21 ，可以实现粉尘与粉尘聚合、液滴与液滴聚合、粉尘与液滴聚合、大颗粒与大颗粒聚合、小颗粒与小颗粒聚合、大颗粒与小颗粒聚合，并且同时发生一次聚合、二次聚合甚至多次聚合。Fig. 5 is a schematic view showing the operation of the fine particle aggregator 20 of the present embodiment, which is specially designed (i.e., the swirling vane 211 and the outer cylinder 213). Cyclone device with a height designed to be similar) 21 It can realize the polymerization of dust and dust, the polymerization of droplets and droplets, the polymerization of dust and droplets, the polymerization of large particles and large particles, the polymerization of small particles and small particles, the polymerization of large particles and small particles, and the simultaneous polymerization and secondary polymerization. Polymerization or even multiple polymerizations.

如图 5 所示，旋风装置 21 中的旋流叶片 211 存在如下三大效应促使上述聚合过程：As shown in Fig. 5, the swirling vane 211 in the cyclone device 21 has the following three major effects to promote the above polymerization process:

首先，大液滴和（或）大粉尘追击小液滴和（或）小粉尘的追捕效应导致液滴和（或）粉尘发生长大。携带大量微小液滴和（或）细微粉尘的气流经过旋风装置 21 后，气流方向发生改变，产生旋转气流。由于相邻两旋风装置 21 的旋流叶片 211 均为顺时针方向或者逆时针方向，所以相邻两旋风装置 21 的交汇耦合区产生气流逆流效应，逆流效应发生，导致烟气流速下降，但由于液滴（密度为 1000 ～ 1200Kg ／ m³ ）和（或）粉尘 ( 堆积密度大约为 1600 ～ 2200kg/m³) 的密度远远高于气流 ( 密度为 1.1-1.3Kg/m³) 的密度，因此液滴和（或）粉尘在较高的惯性力作用下和同向前进的气流发生相对滑移，而且由于气流存在一定的黏度（ 在 1 个大气压 50 ℃ 工况下动力黏度约 1.96×10^-5Pa.s ）对发生相对滑移的液滴和（或）粉尘产生粘性力（即粘性内摩擦力，与粉尘和（或）液滴的表面积成正比关系）来阻止这种相对滑移，由于更微小的液滴和（或）粉尘的比表面积大，所以较大液滴和（或）较大粉尘的相对滑移速度要高于较小液滴和（或）较小粉尘，因此较大液滴和（或）较大粉尘将发生追击更小液滴和（或）更小粉尘效应并很大概率将更小液滴和（或）更小粉尘捕获从而导致液滴和（或）粉尘长大。First, the trapping effect of large droplets and/or large dust chasing small droplets and/or small dust causes droplets and/or dust to grow. After the airflow carrying a large amount of minute droplets and/or fine dust passes through the cyclone device 21, the direction of the airflow changes to generate a swirling airflow. Since the swirling vanes 211 of the adjacent two cyclones 21 are both clockwise or counterclockwise, the cross-coupling effect of the adjacent two cyclones 21 produces a counterflow effect of the airflow, and the countercurrent effect occurs, causing the flue gas flow rate to decrease, but due to The density of droplets (density of 1000 to 1200 Kg / m ³ ) and/or dust (bulk density of approximately 1600 to 2200 kg / m ³ ) is much higher than that of airflow (density of 1.1-1.3 Kg / m ³ ). Therefore, the droplets and/or dusts are relatively slipped by the high inertial force and the airflow in the same direction, and the viscosity of the airflow is certain (the dynamic viscosity is about 1.96×10 under the condition of 1 atm 50 °C). ^-5 Pa.s ) to prevent viscous forces (ie viscous internal friction, proportional to the surface area of dust and/or droplets) of relatively slipped droplets and/or dust to prevent this relative slip Because of the large specific surface area of smaller droplets and/or dust, the relative slip speed of larger droplets and/or larger dust is higher than that of smaller droplets and/or smaller dust, so Large droplets and/or Large dust will occur chase smaller droplets and (or) less dust effects and a great probability will be smaller droplets and (or) resulting in less dust captured droplets and (or) grew up dust.

其次，相邻两旋风装置 21 交汇耦合区域的逆流效应将直接导致烟气流中的细微粉尘和（或）微小液滴与迎面而来气流中的微小液滴和（或）细微粉尘直接相向碰撞从而实现粉尘和（或）液滴长大。由于相邻两旋风装置 21 的旋流叶片均为顺时针方向或者逆时针方向，所以相邻两旋风装置 21 的交汇耦合区域产生气流逆流效应，气流中的大量的细微粉尘和（或）微小液滴与迎面而来的气流中的细微粉尘和（或）微小液滴发生碰撞导致粉尘和粉尘之间、粉尘和液滴之间、液滴和液滴之间发生一次聚合、二次聚合甚至多次聚合从而形成大粉尘和（或）大液滴颗粒。Secondly, adjacent two cyclones 21 The countercurrent effect of the junction coupling region will directly cause the fine dust and/or tiny droplets in the flue gas stream to directly collide with the tiny droplets and/or fine dust in the oncoming airflow to achieve dust and/or liquid. The drop grows big. Due to the adjacent two cyclones The swirling vanes of 21 are clockwise or counterclockwise, so the adjacent two cyclones 21 The intersection region of the intersection creates a countercurrent effect of the airflow. A large amount of fine dust and/or tiny droplets in the airflow collide with fine dust and/or tiny droplets in the oncoming airflow, resulting in dust and dust between the dust and dust. A single polymerization, a secondary polymerization, or even multiple polymerizations occur between the droplets and between the droplets and the droplets to form large dust and/or large droplet particles.

再次，高速气流致使停留在旋流叶片上的液膜被重新卷起现象（下称携带现象）形成新增超大液滴，超大液滴捕获细微粉尘和（或）液滴效应。下游位置的冷凝湿膜离心分离器 30 分离下的液滴形成水膜在重力作用下会汇聚在旋风装置的旋流叶片 211 上，其表面上会形成一层薄薄的液膜，经过旋风装置 21 后，烟气流过相邻两旋流叶片 211 之间构成的狭小流道时，发生的携带现象将形成大量的超大液滴，这些新增的超大液滴，在上述两种液滴和（或）粉尘增大效应中将发挥更为巨大的聚合作用。Again, the high velocity gas stream causes the liquid film remaining on the swirling vanes to be re-rolled (hereinafter referred to as carrying phenomenon) to form new super large droplets, which capture fine dust and/or droplet effects. Condensed wet film centrifugal separator in the downstream position 30 The droplet forming water film under separation will converge on the swirling vane 211 of the cyclone device under the action of gravity, and a thin liquid film will be formed on the surface. After passing through the cyclone device 21, the flue gas flow passes adjacent Two swirling blades When a narrow flow path is formed between 211, the carrying phenomenon will form a large number of super large droplets, and these newly added super large droplets will play a greater role in the above two droplet and/or dust augmentation effects. The polymerization.

冷凝湿膜离心分离器 30 的分离元件采用三弯波纹中空板 31 ，内流有循环冷却水 32 。相邻两波纹中空板间距 S 为 32.5mm 。The separating element of the condensing wet film centrifugal separator 30 is a three-bend corrugated hollow plate 31 with circulating cooling water therein. . The spacing S between two adjacent corrugated hollow plates is 32.5 mm.

携带着液滴和粉尘的气流经过本实施例的上述高效除尘除雾一体化***后，气流的残余雾滴含量将小于 40mg/Nm³ ；当高效除尘除雾一体化***入口粉尘浓度小于 50mg/Nm³ 时，出口粉尘浓度将小于 20mg/Nm³ ，即除尘效率超过 60% 。After the airflow carrying the droplets and dust passes through the above-mentioned high-efficiency dust removal and defogging integrated system of the embodiment, the residual droplet content of the airflow will be less than 40 mg/Nm ³ ; when the inlet dust concentration of the high-efficiency dust removal and defogging integrated system is less than 50 mg/ At Nm ³ , the outlet dust concentration will be less than 20 mg/Nm ³ , ie the dust removal efficiency will exceed 60%.

如图 6 所示，本实施例的可选择的第二方案是将冷凝湿膜离心分离器 30 采用以实心的波纹板为分离元件的波纹板式气液分离器 302 代替，即高效除尘除雾一体化***包括细微颗粒聚合器 20 和波纹板式气液分离器 302 两部分，且与气流呈垂直布置。波纹板式气液分离器 302 的分离元件可以为两弯似正弦波曲线无钩形，如图 1 所示的三弯波纹中空板 31 ；或者两弯似正弦波曲线带钩形，如图 10 所示的带钩的分离元件 132 ；三弯似正弦波曲线无钩形、三弯似正弦波曲线带钩形、带有一个或多个孔和（或）钩形等等。As shown in Fig. 6, an alternative second embodiment of the present embodiment is to condense the wet film centrifugal separator 30. The corrugated plate type gas-liquid separator 302 with a solid corrugated plate as a separating element is replaced by a high-efficiency dust removing and defogging integrated system including a fine particle aggregator 20 and a corrugated plate type gas-liquid separator 302. Two parts, and arranged perpendicular to the airflow. The separating element of the corrugated plate type gas-liquid separator 302 may have two hook-like sinusoidal curves without a hook shape, as shown in Fig. 1 for the three-bend corrugated hollow plate 31 Or two sinusoidal curves with a hook shape, as shown in Figure 10, with the hooked separating element 132 The three-bend sinusoidal curve has no hook shape, the three-bend sinusoidal curve has a hook shape, one or more holes and/or a hook shape, and the like.

如图 7 所示，在本实施例的可选择的第三方案中，高效除尘除雾一体化***包括包括细微颗粒聚合器 20 和冷凝湿膜离心分离器 30 （或波纹板式气液分离器）两部分，本方案中，将细微颗粒聚合器 20 、冷凝湿膜离心分离器 30 （或波纹板式气液分离器）采用倾斜布置，即和烟气流方向构成一夹角 β （ β 大于 0° ），其中细微颗粒聚合器 20 所在的平面与烟气气流的方向构成的夹角 β 为 22.5 ～ 65° ，其主要作用在于提高分离器的有效面积并改善冲洗效果。As shown in FIG. 7, in an alternative third aspect of the present embodiment, the high efficiency dust removal and defogging integrated system includes a fine particle aggregator 20 And a condensed wet film centrifugal separator 30 (or a corrugated plate gas-liquid separator), in this embodiment, a fine particle aggregator 20, a condensing wet film centrifugal separator 30 (or corrugated plate gas-liquid separator) adopts a slanting arrangement, that is, an angle β (β greater than 0°) with the direction of the flue gas flow, wherein the plane of the fine particle aggregator 20 and the direction of the flue gas flow form an angle β It is 22.5 ~ 65 °, its main function is to improve the effective area of the separator and improve the flushing effect.

如图 8 所示，在本实施例的可选择的第四方案中，高效除尘除雾一体化***包括细微颗粒聚合器 20 和冷凝湿膜离心分离器 30 （或波纹板式气液分离器）两部分，并将细微颗粒聚合器 20 、冷凝湿膜离心分离器 30 （或波纹板式气液分离器）采用人字形或 V 字形布置，其主要作用在于提高分离器的有效面积并改善冲洗效果。对于大烟气流道（比如直径为 1.5~3m ），烟气流道采用钢基础结构分区布置，每个区所在的平面内相应地设置有细微颗粒聚合器 20 ，其中设置在每个区内的细微颗粒聚合器 20 的多个旋风装置 21 分别位于两个形成人字形或 V 字形的平面内。As shown in Fig. 8, in an alternative fourth aspect of the embodiment, the high efficiency dust removal and defogging integrated system comprises a fine particle aggregator 20 And the condensed wet film centrifugal separator 30 (or corrugated plate gas-liquid separator), and the fine particle aggregator 20, the condensing wet film centrifugal separator 30 (or the corrugated plate gas-liquid separator) adopts a herringbone or V The glyph arrangement, its main function is to increase the effective area of the separator and improve the flushing effect. For large smoke air passages (such as 1.5~3m in diameter) The flue gas passages are arranged in a steel infrastructure partition, and a fine particle aggregator 20 is disposed correspondingly in the plane in which each zone is located, wherein a plurality of cyclone devices of the fine particle aggregator 20 disposed in each zone 21 They are located in two planes that form a chevron or a V shape.

实施例 2Example 2

如图 9 所示，本实施例的除尘除雾一体化***包括一级预处理器 10 ，细微颗粒聚合器 20 、冷凝湿膜离心分离器 30 （或波纹板式气液分离器）以及超精细分离器 40 ，且全部安装在吸收塔内。As shown in FIG. 9, the dust removal and defogging integrated system of the present embodiment includes a primary preprocessor 10 and a fine particle aggregator 20 The condensed wet film centrifugal separator 30 (or corrugated plate gas-liquid separator) and the ultrafine separator 40 are all installed in the absorption tower.

锅炉尾烟气经电除尘器后烟尘浓度以 ≤20mg/Nm³ 进入脱硫吸收塔 60 。在吸收塔 60 内设有 3 ～ 6 层喷淋层 70 以及可能的 1 ～ 2 层托盘或 FGD 普拉斯 80 ，烟气经过托盘或 FGD 普拉斯 80 和喷淋层 70 后依次经过预处理器 10 ，细微颗粒聚合器 20 、冷凝湿膜离心分离器 30 以及超精细分离器 40 。图 9 中的箭头指示了烟气的流动方向。After the boiler tail flue gas passes through the electrostatic precipitator, the soot concentration enters the desulfurization absorption tower 60 at ≤ 20 mg/Nm ³ . There are 3 to 6 spray layers 70 and possibly 1 to 2 trays or FGD Plass 80 in the absorption tower 60. The flue gas is pretreated through the tray or FGD Plas 80 and spray layer 70. The device 10, the fine particle aggregator 20, the condensed wet film centrifugal separator 30, and the ultrafine separator 40. The arrows in Figure 9 indicate the direction of flow of the flue gas.

所述预分离器 10 包括一级管式分离器 11 、一级粗屋顶分离器 12 和一级细屋顶分离器 13 。The pre-separator 10 includes a primary tubular separator 11 , a primary coarse roof separator 12 and a primary fine roof separator 13 .

管式除雾器 11 在吸收塔内水平布置，包括两排或三排相互错开布置的圆管 111 ，如图 10 所示，其中每排圆管 111 处于水平状态，圆管 111 可自由转动。位于同一排内的相邻圆管 111 之间中心间距为 90 ～ 120mm ，圆管 111 管径为 Ø63mm 。圆管 111 的两端具有管道堵头 112 ，并套有端板 113 ，圆管 111 上套有多个中间隔板 114 。多个圆管 111 通过中间隔板 114 和端板 113 组装在一起。携带大量液滴的烟气经过管式分离器 11 后，体积比例的 85 ～ 90% 的液滴被管式分离器 11 所去除，并且烟气得到有效的整流。The tubular mist eliminator 11 is horizontally arranged in the absorption tower, and includes two or three rows of circular tubes 111 which are arranged in a staggered manner, as shown in FIG. As shown, each row of tubes 111 is horizontal and the tube 111 is free to rotate. The distance between the adjacent tubes 111 in the same row is 90 to 120 mm, and the tube 111 The pipe diameter is Ø63mm. The pipe 111 has a pipe plug 112 at both ends, and is provided with an end plate 113, and the pipe 111 is provided with a plurality of intermediate partitions 114. Multiple round tubes 111 It is assembled by intermediate partition 114 and end plate 113. After the flue gas carrying a large amount of droplets passes through the tubular separator 11, a volume ratio of 85 to 90% of the droplets is passed through the tubular separator 11 It is removed and the flue gas is effectively rectified.

图 11 示出了粗屋顶分离器 12 和细屋顶分离器 13 ，两者的区别在于分离元件不同，粗屋顶分离器的左模块和右模块的分离元件 121 不带钩，细屋顶分离器的左模块和右模块分离元件 131 带钩。具体来说，粗屋顶式除雾器和细屋顶除雾器分别包括第一波纹板组件 121 和第二波纹板组件 131 ，第一波纹板组件 121 和第二波纹板组件 131 均由多片波纹薄板组成，波纹板的截面具有半正弦波形状，相邻波纹板之间的距离为 20.0 ～ 40mm 。第二波纹板组件 131 中的波纹板上设置有钩部 132 ，该钩部 132 的开口方向与烟气的流动方向相反，该钩部 132 位于半正弦波形状的波峰处或波谷处。第一波纹板组件 121 和第二波纹板组件 131 组合形成'人'字形布置，波纹板的厚度优选为 2.0 ～ 3.5mm 。烟气经过细屋顶式除雾器 13 后，净烟气中只残留了微小的液滴，液滴浓度可以 ≤ 35mg/Nm³ 。Figure 11 shows the coarse roof separator 12 and the thin roof separator 13, the difference being that the separation elements are different, the separation elements 121 of the left and right modules of the coarse roof separator are not hooked, and the left side of the fine roof separator The module and right module separating element 131 are hooked. Specifically, the rough roof defogger and the fine roof defogger respectively include a first corrugated plate assembly 121 and a second corrugated plate assembly 131, and the first corrugated plate assembly 121 and the second corrugated plate assembly 131 are each composed of a plurality of corrugations The thin plate is composed of a cross section having a half sine wave shape, and the distance between adjacent corrugated plates is 20.0 to 40 mm. The corrugated plate in the second corrugated plate assembly 131 is provided with a hook portion 132 having an opening direction opposite to the flow direction of the flue gas, and the hook portion 132 is located at a peak or a trough of a half sine wave shape. The first corrugated plate assembly 121 and the second corrugated plate assembly 131 are combined to form a 'human' shaped arrangement, and the thickness of the corrugated plate is preferably 2.0 to 3.5 mm. After the flue gas passes through the fine roof type mist eliminator 13, only tiny droplets remain in the net flue gas, and the droplet concentration can be ≤ 35 mg/Nm ³ .

本高效除尘除雾一体化***的细微颗粒聚合器 20 和冷凝湿膜离心分离器 30 同实施例一的第一方案相同。The fine particle aggregator 20 and the condensed wet film centrifugal separator of the high efficiency dust removal and defogging integrated system 30 The same as the first embodiment of the first embodiment.

超精细分离器 40 由多片波纹板 41 组成，如图 12 所示，波纹板的截面为至少包含一个波长的正弦波形状；在正弦波形状的波峰处设置有孔 411 ，在正弦波形状的波谷处设置有钩部 412 ；或者在正弦波形状的波谷处设置有孔 411 ，在正弦波形状的波峰处设置有钩部 412 。其中，钩部 412 的开口方向与烟气的流动方向相反。相邻波纹板之间的距离优选为 20.0 ～ 38mm 。优选地在烟气流速高的区域将波纹板之间的距离设计为小，在烟气流速低的区域将波纹板之间的距离设计为大。波纹板间距也可以采用固定间距。波纹板呈倾斜布置，具体为呈人字形或 V 字形布置，波纹板的倾斜角度（波纹板与水平面的夹角）优选为 28 ～ 39.0° ，波纹板的厚度优选为 2.0 ～ 3.5mm 。烟气经过超精细除雾器后，净烟气中对于粒径大于 13 微米的液滴 100% 被去除分离；对粒径 10 微米的液滴具有 80% 以上的分离效率；对粒径 8 微米的液滴具有 60% 以上的分离效率；对粒径 6 微米的液滴具有 40% 以上的分离效率。The ultrafine separator 40 is composed of a plurality of corrugated plates 41, as shown in Fig. 12. As shown, the cross section of the corrugated plate is a sine wave shape containing at least one wavelength; a hole 411 is provided at the crest of the sine wave shape, and a hook portion 412 is provided at the trough of the sine wave shape. Or a hole 411 is provided in the valley of the sine wave shape, and a hook portion 412 is provided at the peak of the sine wave shape. Wherein the hook portion 412 The direction of the opening is opposite to the direction of flow of the flue gas. The distance between adjacent corrugated plates is preferably 20.0 to 38 mm . Preferably, the distance between the corrugated plates is designed to be small in a region where the flue gas flow rate is high, and the distance between the corrugated plates is designed to be large in a region where the flue gas flow rate is low. The corrugated board spacing can also be fixed. The corrugated board is arranged obliquely, specifically in herringbone shape or V-shaped arrangement, the inclination angle of the corrugated plate (the angle between the corrugated plate and the horizontal plane) is preferably 28 to 39.0°, and the thickness of the corrugated plate is preferably 2.0 to 3.5 mm. . After the flue gas passes through the ultra-fine mist eliminator, 100% of the droplets with a particle size larger than 13 microns are removed and separated in the net flue gas; the separation efficiency is more than 80% for the droplets with a particle size of 10 microns; Micron droplets have a separation efficiency of more than 60%; droplets with a particle size of 6 microns have a separation efficiency of more than 40%.

本实施例中，管式分离器 11 和粗屋顶式分离器 12 安装在下层支撑梁上；细屋顶式分离器 13 安装在中间层支撑梁上；细微颗粒聚合器 20 、冷凝湿膜离心分离器 30 和屋顶型超精细分离器 40 安装在上层支撑梁上。In this embodiment, the tubular separator 11 and the thick roof separator 12 are mounted on the lower support beam; the thin roof separator 13 Mounted on the intermediate support beam; the fine particle aggregator 20, the condensing wet film centrifugal separator 30, and the roof type ultrafine separator 40 are mounted on the upper support beam.

为避免本实施例的高效除尘除雾一体化***发生堵塞，设有六层冲洗*** 50 ，第一层冲洗*** 51 用来冲洗管式分离器 11 下游侧和粗屋顶分离器 12 的上游侧，第二层冲洗*** 52 用来冲粗屋顶分离器 11 的下游侧，第三层冲洗*** 53 用来细粗屋顶分离器 13 的上游侧，第四层冲洗*** 54 用来冲洗细微颗粒聚合器 20 ，且兼顾冲洗细粗屋顶分离器 13 的下游侧，第五层冲洗*** 55 用来冲洗超精细分离器 40 上游侧，且兼顾冲洗细冷凝湿膜离心分离器 30 的下游侧，第六层冲洗*** 56 用来冲洗超精细分离器 40 下游侧。第一到第五层冲洗 51 ～ 56 采用自动冲洗***，第六层冲洗*** 56 采用手动冲洗***，也可以采用自动冲洗***。In order to avoid the blockage of the high-efficiency dust removal and defogging integrated system of the present embodiment, a six-layer flushing system 50 is provided, and the first layer flushing system 51 Used to flush the downstream side of the tubular separator 11 and the upstream side of the coarse roof separator 12, the second layer flushing system 52 is used to flush the downstream side of the coarse roof separator 11, the third layer flushing system 53 For the upstream side of the fine roof separator 13, a fourth layer flushing system 54 is used to flush the fine particle aggregator 20, taking into account the downstream side of the rinsing fine roof separator 13, the fifth layer rinsing system 55 It is used to flush the upstream side of the ultrafine separator 40, and to balance the downstream side of the rinsing fine condensing wet film centrifugal separator 30, which is used to flush the downstream side of the ultrafine separator 40. First to fifth layer rinse 51 to 56 With automatic flushing system, the sixth flushing system 56 uses a manual flushing system or an automatic flushing system.

采用本实施例高效除尘除雾一体化***，当入口烟尘浓度 ≤20mg/Nm³ 时，可以使得烟气中的烟尘含量 ≤3.5mg/Nm³ ；当脱硫吸收塔入口粉尘小于 30mg/Nm³ 下，可确保气流中残余的烟尘浓度小于 5.0mg/Nm³ ；当脱硫吸收塔入口粉尘小于 50mg/Nm³ 下，可确保气流中残余的烟尘浓度小于 10.0 mg/Nm³ ；液滴含量将小于 10.0mg/Nm³ ( 采用 Mg²⁺ 示踪法 ) 或者小于 1.0mg/Nm³( 采用 TüV >15 微米撞击法检测 ) 。The high-efficiency dust removal and defogging integrated system of the present embodiment can make the soot content in the flue gas ≤3.5 mg/Nm ³ when the inlet soot concentration is ≤20 mg/Nm ³ ; and the dust at the inlet of the desulfurization absorption tower is less than 30 mg/Nm ³ It can ensure that the residual soot concentration in the gas stream is less than 5.0mg/Nm ³ ; when the desulfurization absorber inlet dust is less than 50mg/Nm ³ , the residual soot concentration in the gas stream can be ensured to be less than 10.0 mg/Nm ³ ; the droplet content will be less than 10.0 Mg/Nm ³ (using Mg ²⁺ tracer method) or less than 1.0 mg/Nm ³ (tested by TüV >15 μm impact method).

受到现场吸收塔 60 空间的限制，可以将图 9 中的高效除尘除雾一体化***的超精细分离器 40 安装在水平烟道 601 内（如图 13 所示）。烟气经过一级预分离器（包括管式预分离器 11 ，粗屋顶分离器 12 ，细屋顶分离器 13 ）、细微颗粒聚合器 20 、冷凝湿膜离心分离器 30 （或波纹板式气液分离器）和超精细水平气流分离器 40 ；预分离器和细微颗粒聚合器 20 、冷凝湿膜离心分离器 30 （或波纹板式气液分离器）安装在吸收塔内；超精细水平气流分离器 40 安装在吸收塔出口水平烟道内。Subject to the space of the absorption tower 60 on site, the ultra-fine separator of the high-efficiency dust removal and defogging integrated system in Figure 9 can be used. Installed in horizontal flue 601 (shown in Figure 13). The flue gas passes through a primary pre-separator (including tubular pre-separator 11 , coarse roof separator 12 , fine roof separator 13 ), fine particle aggregator 20, condensing wet film centrifugal separator 30 (or corrugated plate gas-liquid separator) and ultra-fine horizontal gas flow separator 40; pre-separator and fine particle aggregator 20, condensing wet film centrifugal separator 30 (or corrugated plate gas-liquid separator) is installed in the absorption tower; ultra-fine horizontal gas flow separator 40 is installed in the horizontal flue of the absorption tower outlet.

针对特殊项目，在吸收塔 60 内不设有分离器的安装空间，可以将本实施例高效除尘除雾一体化***安装在吸收塔 60 的出口水平烟道 601 内。其中烟气经过一级预分离器（包括管式预分离器 11 ，水平气流粗分离器 12 ，水平气流粗细分离器 13 ）、细微颗粒聚合器 20 、冷凝湿膜离心分离器 30 （或波纹板式气液分离器）和超精细水平气流分离器 40 。（如图 14 所示）。For the special project, the installation space of the separator is not provided in the absorption tower 60, and the integrated dust removal and defogging integrated system of the embodiment can be installed in the absorption tower. 60 exit level flue inside 601. The flue gas passes through the primary pre-separator (including the tubular pre-separator 11 , the horizontal gas flow coarse separator 12 , the horizontal gas flow separator 13 ), and the fine particle aggregator 20. Condensate wet film centrifugal separator 30 (or corrugated plate gas-liquid separator) and ultra-fine horizontal gas flow separator 40. (As shown in Figure 14).

无论将超精细水平气流分离器 40 或者整个高效除尘除雾一体化***被布置在出口水平烟道内，在超精细水平气流分离器 40 或者整个高效除尘除雾一体化***的上游位置的烟道外壳体可以不采取保温措施用以降低脱硫***的总体成本，同时冷凝水可以捕获一小部分细微粉尘和微小雾滴，这些冷凝水可以被安装在水平烟道内的超精细水平气流分离器 40 或者整个高效除尘除雾一体化***所拦截去除，因此反而提高了除尘和除雾效果。Regardless of the ultra-fine horizontal airflow separator 40 Or the entire high-efficiency dust removal and defogging integrated system is arranged in the outlet horizontal flue, in the ultra-fine horizontal air flow separator 40 Or the flue outer casing of the upstream position of the integrated high-efficiency dust removal and defogging integrated system may not adopt insulation measures to reduce the overall cost of the desulfurization system, and the condensed water may capture a small amount of fine dust and tiny droplets, and the condensed water may Superfine horizontal airflow separator installed in horizontal flue 40 or the entire high-efficiency dust removal and defogging integrated system intercepts and removes, thus improving the dust removal and defogging effect.

以上详细描述了本 发明 的较佳具体实施例。应当理解，本领域的普通技术人员无需创造性劳动就可以根据本 发明 的构思作出诸多修改和变化。因此，凡本技术领域中技术人员依本 发明 的构思在现有技术的基础上通过逻辑分析、推理或者有限的实验可以得到的技术方案，皆应在由权利要求书所确定的保护范围内。The above has described in detail the preferred embodiments of the invention. It should be understood that one of ordinary skill in the art can use the present invention without creative labor. The idea has been changed and changed. Therefore, those skilled in the art according to the present invention The technical solution that can be obtained by logic analysis, reasoning or limited experiment on the basis of the prior art is within the scope of protection determined by the claims.

Claims (37)

1. 一种用于聚合细微颗粒的聚合器，其特征在于，所述聚合器包括一个或多个旋风装置，所述旋风装置包括至少两个旋流叶片，所述旋流叶片被设置为使得包含细微颗粒的气流通过所述旋风装置时形成旋转气流。 A polymerizer for polymerizing fine particles, characterized in that the polymerizer comprises one or more cyclones, the cyclone device comprising at least two swirling vanes, the swirling vanes being arranged such that they contain subtle A swirling gas stream is formed as the gas stream of particles passes through the cyclone.
2. 如权利要求1所述的用于聚合细微颗粒的聚合器，其特征在于，当所述聚合器包括多个所述旋风装置时，任意两个相邻的所述旋风装置中的所述旋流叶片的设置方向相同。A polymerizer for polymerizing fine particles according to claim 1, wherein said swirling flow in any two adjacent said cyclone devices when said aggregator comprises a plurality of said cyclones The blades are set in the same direction.
3. 如权利要求1所述的用于聚合细微颗粒的聚合器，其特征在于，所述旋风装置还包括中心柱体和外筒，所述旋流叶片的一端固接于所述中心柱体，另一端固接于所述外筒。A polymerizer for polymerizing fine particles according to claim 1, wherein said cyclone device further comprises a central cylinder and an outer cylinder, one end of said swirling vane being fixed to said central cylinder, and the other One end is fixed to the outer cylinder.
4. 如权利要求3所述的用于聚合细微颗粒的聚合器，其特征在于，所述外筒具有圆形截面，所述圆形截面与所述外筒的轴线垂直。A polymerizer for polymerizing fine particles according to claim 3, wherein said outer cylinder has a circular cross section perpendicular to an axis of said outer cylinder.
5. 如权利要求4所述的用于聚合细微颗粒的聚合器，其特征在于，所述旋流叶片固接于所述外筒的所述另一端的高度与所述外筒的高度基本相同，或者小于所述外筒的高度，且两者的高度差不超过所述圆形截面的直径的三分之一。A polymerizer for polymerizing fine particles according to claim 4, wherein a height of said swirling vane fixed to said other end of said outer cylinder is substantially the same as a height of said outer cylinder, or It is smaller than the height of the outer cylinder, and the height difference between the two does not exceed one third of the diameter of the circular cross section.
6. 如权利要求3所述的用于聚合细微颗粒的聚合器，其特征在于，所述外筒具有正多边形截面，所述正多边形截面与所述外筒的轴线垂直。A polymerizer for polymerizing fine particles according to claim 3, wherein said outer cylinder has a regular polygonal cross section perpendicular to an axis of said outer cylinder.
7. 如权利要求6所述的用于聚合细微颗粒的聚合器，其特征在于，所述旋流叶片固接于所述外筒的所述另一端的高度与所述外筒的高度基本相同，或者小于所述外筒的高度，且两者的高度差不超过所述正多边形截面的最长对角线长度的三分之一。A polymerizer for polymerizing fine particles according to claim 6, wherein a height of said swirling vane fixed to said other end of said outer cylinder is substantially the same as a height of said outer cylinder, or It is smaller than the height of the outer cylinder, and the height difference between the two does not exceed one third of the longest diagonal length of the regular polygonal section.
8. 如权利要求1所述的用于聚合细微颗粒的聚合器，其特征在于，所述多个旋风装置的轴线相互平行。A polymerizer for polymerizing fine particles according to claim 1, wherein axes of said plurality of cyclones are parallel to each other.
9. 如权利要求1所述的用于聚合细微颗粒的聚合器，其特征在于，所述多个旋风装置分别位于两个形成V字形或人字形的平面内，位于同一平面内的旋风装置的轴线相互平行。A polymerizer for polymerizing fine particles according to claim 1, wherein said plurality of cyclones are respectively located in two planes forming a V-shape or a chevron shape, and axes of the cyclone devices located in the same plane are mutually parallel.
10. 如权利要求3所述的用于聚合细微颗粒的聚合器，其特征在于，所述旋流叶片的仰角为12.5～60°。A polymerizer for polymerizing fine particles according to claim 3, wherein said swirling vanes have an elevation angle of from 12.5 to 60°.
11. 如权利要求3所述的用于聚合细微颗粒的聚合器，其特征在于，所述旋流叶片的数量为3~18片。The polymerizer for polymerizing fine particles according to claim 3, wherein the number of the swirling vanes is from 3 to 18 sheets.
12. 如权利要求11所述的用于聚合细微颗粒的聚合器，其特征在于，所述旋流叶片的数量为6~8片。The polymerizer for polymerizing fine particles according to claim 11, wherein the number of the swirling vanes is 6 to 8.
13. 如权利要求1所述的用于聚合细微颗粒的聚合器，其特征在于，所述聚合器还包括用于安装所述旋风装置的固定件，所述固定件上设置有用于安装所述旋风装置的安装孔，所述多个旋风装置通过所述安装孔安装在所述固定件上；所述固定件上还设置有通气孔。A polymerizer for polymerizing fine particles according to claim 1, wherein said polymerizer further comprises a fixing member for mounting said cyclone device, said fixing member being provided with said cyclone device for mounting The mounting hole is mounted on the fixing member through the mounting hole; the fixing member is further provided with a vent hole.
14. 如权利要求13所述的用于聚合细微颗粒的聚合器，其特征在于，所述固定件整体上为平面结构，安装在所述固定件上的所述多个旋风装置处于同一平面内，且所述多个旋风装置的轴线相互平行。A polymerizer for polymerizing fine particles according to claim 13, wherein said fixing member is a planar structure as a whole, and said plurality of cyclones mounted on said fixing member are in the same plane, and The axes of the plurality of cyclones are parallel to each other.
15. 如权利要求13所述的用于聚合细微颗粒的聚合器，其特征在于，所述固定件包括两个形成人字形或V字形的平面，安装在同一平面内的旋风装置的轴线相互平行。A polymerizer for polymerizing fine particles according to claim 13, wherein said fixing member comprises two planes forming a chevron or a V shape, and axes of the cyclone devices mounted in the same plane are parallel to each other.
16. 一种烟气流道，其特征在于，包括一级或多级如权利要求1~15中任意一项所述的用于聚合细微颗粒的聚合器，所述聚合器被布置于含有细微颗粒的烟气气流的断面上。A flue gas passage characterized by comprising one or more stages of a polymerizer for polymerizing fine particles according to any one of claims 1 to 15, the polymerizer being disposed on a fine particle containing On the section of the flue gas stream.
17. 如权利要求16所述的烟气流道，其特征在于，所述聚合器所在的平面与所述烟气气流的方向基本垂直。The flue gas duct of claim 16 wherein the plane of the aggregator is substantially perpendicular to the direction of the flue gas stream.
18. 如权利要求16所述的烟气流道，其特征在于，所述聚合器所在的平面与所述烟气气流的方向具有夹角β，所述夹角β为22.5～65°。The flue gas duct according to claim 16, wherein the plane in which the polymerizer is located has an angle β with the direction of the flue gas stream, and the angle β is 22.5 to 65°.
19. 如权利要求16所述的烟气流道，其特征在于，所述烟气流道采用钢基础结构分区布置，每个区所在的平面内相应地设置有所述聚合器。A flue gas duct according to claim 16, wherein said flue gas passages are arranged in a steel infrastructure partition, and said polymerizer is disposed in a plane in which each zone is located.
20. 如权利要求19所述的烟气流道，其特征在于，设置在每个区内的所述聚合器的所述多个旋风装置分别位于两个形成V字形或人字形的平面内。A smoke flow path according to claim 19, wherein said plurality of cyclones of said aggregator disposed in each zone are respectively located in two planes forming a V-shape or a chevron shape.
21. 一种除尘除雾一体化***，其特征在于，包括一级或多级如权利要求1~15中任意一项所述的用于聚合细微颗粒的聚合器，所述聚合器的上游和/或下游位置设置有弯曲流道式分离器，所述弯曲流道式分离器中的分离元件构成多个弯曲的气流通道。An integrated dust removal and defogging system, comprising: one or more stages of a polymerizer for polymerizing fine particles according to any one of claims 1 to 15, upstream and/or A downstream flow path is provided with a curved flow path type separator, the separation elements in the curved flow path type separator forming a plurality of curved gas flow channels.
22. 如权利要求21所述的除尘除雾一体化***，其特征在于，所述聚合器与所述弯曲流道式分离器的距离小于1500mm。The integrated dust removal and defogging system according to claim 21, wherein the distance between the aggregator and the curved flow path separator is less than 1500 mm.
23. 如权利要求22所述的除尘除雾一体化***，其特征在于，所述聚合器与所述弯曲流道式分离器的距离小于50mm。The integrated dust removal and defogging system according to claim 22, wherein the distance between the polymerizer and the curved flow path separator is less than 50 mm.
24. 如权利要求21所述的除尘除雾一体化***，其特征在于，所述弯曲流道式分离器中的分离元件为波纹板组件，所述波纹板组件包括多个间隔的、均匀布置的波纹板，多个所述波纹板形成弯曲的气流通道；相邻两所述波纹板之间的距离为10~60mm；所述波纹板为正弦曲线形波纹板，所述波纹板具有钩和/或孔，所述钩和所述孔均具有一个或多个；所述波纹板的厚度为1.0~3.5mm。A dust removal and defogging integrated system according to claim 21, wherein the separating element in the curved flow path separator is a corrugated plate assembly, the corrugated plate assembly comprising a plurality of spaced, uniformly arranged corrugations a plurality of the corrugated plates form a curved air flow passage; a distance between two adjacent corrugated plates is 10 to 60 mm; the corrugated plate is a sinusoidal corrugated plate, the corrugated plate having a hook and/or The hole, the hook and the hole each have one or more; the corrugated plate has a thickness of 1.0 to 3.5 mm.
25. 如权利要求24所述的除尘除雾一体化***，其特征在于，所述波纹板为中空结构，内流有冷却介质，所述冷却介质的温度小于所述气流的温度，所述冷却介质由冷却介质供应***供应。The integrated dust removal and defogging system according to claim 24, wherein the corrugated plate is a hollow structure, and a cooling medium is flowed therein, and a temperature of the cooling medium is smaller than a temperature of the air flow, and the cooling medium is Cooling media supply system supply.
26. 如权利要求21所述的除尘除雾一体化***，其特征在于，所述弯曲流道式分离器中的分离元件为2~5层相互交错的管束，每一层所述管束包括多个间隔的、均匀布置的管，相邻两层所述管束中的管呈交错布置，形成弯曲的气流流道；处于同一层所述管束中的管的中心间距为该层管束的管径的1.2~4倍；所述管的横截形状为圆形、水滴形或子弹头形。The integrated dust removal and defogging system according to claim 21, wherein the separation element in the curved flow path separator is 2 to 5 layers of mutually interleaved tube bundles, and each layer of the tube bundle includes a plurality of intervals. a uniformly arranged tube, the tubes in the adjacent two layers of the tube bundle are staggered to form a curved air flow channel; the center spacing of the tubes in the same layer of the tube bundle is 1.2~ of the tube diameter of the tube bundle 4 times; the tube has a circular shape, a teardrop shape or a bullet shape.
27. 一种除尘除雾一体化***，包括一级或多级如权利要求1~15中任意一项所述的用于聚合细微颗粒的聚合器，所述聚合器的上游位置设置有一级或多级预分离器，和/或所述聚合器的下游位置设置有一级或多级精细分离器和/或一级或多级超精细分离器； 所述精细分离器具有比所述预分离器更高的液滴分离性能，所述超精细分离器具有比所述精细分离器更高的液滴分离性能。A dust removal and defogging integrated system comprising one or more stages of a polymerizer for polymerizing fine particles according to any one of claims 1 to 15, wherein the upstream position of the polymerizer is set to one or more stages a pre-separator, and/or a downstream location of the aggregator is provided with one or more stages of fine separators and/or one or more stages of superfine separators; The fine separator has a higher droplet separation performance than the pre-separator, and the ultrafine separator has a higher droplet separation performance than the fine separator.
28. 如权利要求27所述的除尘除雾一体化***，其特征在于，所述预分离器包括弯曲流道式分离器，或者所述精细分离器包括弯曲流道式分离器。A dust removal and defogging integrated system according to claim 27, wherein said pre-separator comprises a curved flow path type separator, or said fine separator comprises a curved flow path type separator.
29. 如权利要求27所述的除尘除雾一体化***，其特征在于，所述预分离器为管式设计预分离器、平板设计预分离器、屋顶设计预分离器、水平气流预分离器中的一种或者多种的组合；所述超精细分离器为平板设计超精细分离器、屋顶设计超精细分离器、水平气流超精细分离器中的一种或者多种的组合。The integrated dust removal and defogging system according to claim 27, wherein the pre-separator is a tubular design pre-separator, a flat design pre-separator, a roof design pre-separator, and a horizontal air pre-separator. One or more combinations; the ultrafine separator is a combination of one or more of a flat design ultrafine separator, a roof design hyperfine separator, and a horizontal airflow hyperfine separator.
30. 如权利要求27所述的除尘除雾一体化***，其特征在于，一级或多级所述预分离器、一级或多级所述聚合器以及一级或多级所述精细分离器和/或所述超精细分离器全部布置在烟气吸收塔内，气流的流动方向为竖直方向。A dust removal and defogging integrated system according to claim 27, wherein one or more of said pre-separators, one or more stages of said aggregators, and one or more stages of said fine separators and / or the ultra-fine separators are all arranged in the flue gas absorption tower, the flow direction of the gas flow is a vertical direction.
31. 如权利要求27所述的除尘除雾一体化***，其特征在于，一级或多级所述预分离器、一级或多级所述聚合器以及一级或多级所述精细分离器和/或所述超精细分离器全部布置在吸收塔出口水平烟道内，气流的流动方向为水平方向。A dust removal and defogging integrated system according to claim 27, wherein one or more of said pre-separators, one or more stages of said aggregators, and one or more stages of said fine separators and / or the superfine separators are all arranged in the horizontal flue of the absorption tower outlet, and the flow direction of the airflow is horizontal.
32. 如权利要求27所述的除尘除雾一体化***，其特征在于，一级或多级所述预分离器、一级或多级所述聚合器以及一级或多级所述精细分离器和/或所述超精细分离器中的一部分布置在吸收塔内，另一部分布置在吸收塔出口水平烟道内，在吸收塔内气流呈竖直方向，在吸收塔水平出口烟道内气流呈水平方向。A dust removal and defogging integrated system according to claim 27, wherein one or more of said pre-separators, one or more stages of said aggregators, and one or more stages of said fine separators and / or a part of the ultrafine separator is arranged in the absorption tower, and another part is arranged in the horizontal flue of the absorption tower outlet, the airflow in the absorption tower is in a vertical direction, and the airflow in the horizontal exit flue of the absorption tower is horizontal.
33. 如权利要求27所述的除尘除雾一体化***，其特征在于，任何一级所述预分离器、任何一级所述聚合器和任何一级所述精细分离器和/或所述超精细分离器均根据实际运行工况需要在各自对应的气流入口侧和/或气流出口测设置有自动和/或手动清洗装置，所述清洗装置包括管道和冲洗喷嘴。A dust removal and defogging integrated system according to claim 27, wherein any one of said pre-separators, any one of said first stage aggregators and any one of said first stage fine separators and/or said superfine The separators are each provided with automatic and/or manual cleaning devices on their respective gas inlet side and/or gas outlet outlets according to actual operating conditions, including cleaning pipes and flushing nozzles.
34. 一种使烟气中细微颗粒聚合的方法，其特征在于，使所述烟气通过旋风装置，从而产生多股旋转方向相同的旋转气流，所述旋转气流与相邻的旋转气流之间发生交汇与对冲。A method for polymerizing fine particles in a flue gas, wherein the flue gas is passed through a cyclone device to generate a plurality of swirling airflows having the same direction of rotation, and the swirling airflow intersects with adjacent swirling airflows With hedging.
35. 一种一体化除尘除雾方法，其特征在于，使烟气通过旋风装置，从而产生多股旋转方向相同的旋转气流，所述旋转气流与相邻的旋转气流之间发生交汇与对冲；还使烟气通过设置在所述旋风装置上游和/下游位置的弯曲流道式分离器，所述弯曲流道式分离器中的分离元件构成多个弯曲的气流通道，使得气流经过所述多个弯曲的气流通道时，气流不断改变流动方向，气流中的雾滴或携有固体颗粒物的液滴在离心力作用下撞击所述分离元件，并形成水膜，所述水膜在重力作用下回落。An integrated dust removal and defogging method, characterized in that the flue gas is passed through a cyclone device, thereby generating a plurality of rotating airflows having the same direction of rotation, and the swirling airflow intersects and hedges with the adjacent swirling airflow; The flue gas passes through a curved flow path separator disposed at an upstream and/or downstream position of the cyclone device, the separation element in the curved flow path separator forming a plurality of curved air flow passages, such that the air flow passes through the plurality of bends In the air flow passage, the air flow continuously changes the flow direction, and the droplets in the air flow or the droplets carrying the solid particles impinge on the separating element under the centrifugal force and form a water film, which falls back under the action of gravity.
36. 如权利要求35所述的一体化除尘除雾方法，其特征在于，所述弯曲流道式分离器设置在所述旋风装置的下游位置，使得所述水膜在重力作用下回落到所述旋风装置的旋流叶片上。The integrated dust removal and defogging method according to claim 35, wherein said curved flow path type separator is disposed at a downstream position of said cyclone device such that said water film falls back to said cyclone under the action of gravity On the swirling vanes of the device.
37. 如权利要求35所述的一体化除尘除雾方法，其特征在于，还使烟气通过设置在所述旋风装置的上游位置的一级或多级预分离器和/或设置在所述旋风装置的下游位置的一级或多级超精细分离器。The integrated dust removal and defogging method according to claim 35, wherein the flue gas is further passed through a first or multistage pre-separator disposed at an upstream position of the cyclone device and/or disposed in the cyclone device One or more stages of superfine separators at downstream locations.