CN106731432A - Combined tubular type coalescer - Google Patents
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- 239000000428 dust Substances 0.000 claims abstract description 41
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000003546 flue gas Substances 0.000 claims abstract description 19
- 238000004581 coalescence Methods 0.000 claims abstract description 7
- 238000009833 condensation Methods 0.000 claims description 35
- 230000005494 condensation Effects 0.000 claims description 35
- 238000005345 coagulation Methods 0.000 claims description 33
- 230000015271 coagulation Effects 0.000 claims description 33
- 239000002245 particle Substances 0.000 claims description 30
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 16
- 239000003463 adsorbent Substances 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000009826 distribution Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 238000009434 installation Methods 0.000 claims description 2
- 238000000889 atomisation Methods 0.000 claims 1
- 239000008187 granular material Substances 0.000 abstract 1
- 238000009413 insulation Methods 0.000 abstract 1
- 239000011882 ultra-fine particle Substances 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 239000010419 fine particle Substances 0.000 description 6
- 239000012717 electrostatic precipitator Substances 0.000 description 5
- 239000000779 smoke Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 4
- 229910052753 mercury Inorganic materials 0.000 description 4
- 239000010881 fly ash Substances 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 230000007246 mechanism Effects 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- 230000003213 activating effect Effects 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000011362 coarse particle Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 230000009916 joint effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000000053 physical method Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D51/00—Auxiliary pretreatment of gases or vapours to be cleaned
- B01D51/02—Amassing the particles, e.g. by flocculation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/64—Heavy metals or compounds thereof, e.g. mercury
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/60—Heavy metals or heavy metal compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/60—Heavy metals or heavy metal compounds
- B01D2257/602—Mercury or mercury compounds
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Abstract
Description
技术领域technical field
本发明属于烟气除尘处理领域，涉及一种组合型管式凝并器。The invention belongs to the field of flue gas dust removal treatment, and relates to a combined tubular condenser.
背景技术Background technique
近年来，我国大中城市雾霾天气越来越多，严重影响了城市居民的健康工作和生活，其中城市环境中PM2.5(主要为PM0.4-1.0)含量过高是导致雾霾天气的主要原因。因此，如何控制PM2.5产生，并减少其存在，成为亟待解决的问题。In recent years, there have been more and more smog weather in large and medium-sized cities in China, which has seriously affected the healthy work and life of urban residents. Among them, the high content of PM 2.5 (mainly PM 0.4-1.0 ) in the urban environment is the main cause of smog weather. reason. Therefore, how to control the production of PM 2.5 and reduce its existence has become an urgent problem to be solved.
中国专利CN101664623A公开了涉及用于工业烟尘治理的微细粒子除尘器。具体是通过对现有二级过滤方式的电袋复合除尘器改进，在滤袋除尘机构的出口与引风机的进口之间设有湍流涡旋机构，该湍流涡旋机构包括湍流涡旋室、烟尘入口管和烟尘出口管。湍流涡旋室为横截面为倒等腰梯形的斗状，其底部连接着灰斗室。经过第二级处理的含有较细颗粒物的烟尘进入烟尘入口管，经过导风板，使气流发生向下偏转，进入湍流涡旋室，较细颗粒物与湍流涡旋室内壁产生扩散和碰撞促使微细粒子沉淀，使微细颗粒物从烟尘中分离出来。但该处理工艺中单独用湍流涡旋室进行细颗粒物的物化凝并，凝并效率并不高。Chinese patent CN101664623A discloses a fine particle dust collector for industrial smoke control. Specifically, a turbulent vortex mechanism is provided between the outlet of the filter bag dust removal mechanism and the inlet of the induced draft fan through the improvement of the electric bag composite dust collector of the existing two-stage filtration method. The turbulent vortex mechanism includes a turbulent vortex chamber, Fume inlet pipe and fume outlet pipe. The turbulent vortex chamber is in the shape of a bucket with an inverted isosceles trapezoidal cross section, and the bottom of the vortex chamber is connected with the ash chamber. After the second-stage treatment, the dust containing finer particles enters the dust inlet pipe, passes through the wind deflector, deflects the airflow downward, and enters the turbulent vortex chamber, where the finer particles diffuse and collide with the inner wall of the turbulent vortex to promote the fine particles Particle precipitation separates fine particulate matter from the soot. However, in this treatment process, the turbulent vortex chamber is used alone for the physical-chemical coagulation of fine particles, and the coagulation efficiency is not high.
中国专利CN103071591A公开了一种凝聚器产涡装置，包括机架、电机、由电机驱动的主动轴、从动轴，主动轴和从动轴之间设有至少一条传动链条，所述传动链条上设有产涡片，所述产涡片旁的机架上设有清灰装置。但涡片过多影响烟气过流速度，增加了凝聚器的压力降。Chinese patent CN103071591A discloses a vortex generating device for agglomerators, including a frame, a motor, a driving shaft driven by the motor, and a driven shaft. At least one transmission chain is arranged between the driving shaft and the driven shaft. A vortex generating sheet is provided, and a dust cleaning device is arranged on the frame next to the vortex generating sheet. However, too many swirls affect the flue gas flow velocity and increase the pressure drop of the condenser.
因而，针对凝并效率不高、工艺设备复杂等问题，很有必要在现有技术的基础上，研究开发强化凝并的超细颗粒凝并器。在传统的除尘器的基础上，增设凝并处理装置，使超细颗粒物通过物理方法或物化方法凝并成较大颗粒，从而在主体除尘器内顺利脱除，是现在除尘技术发展的趋势。Therefore, in view of the problems of low coagulation efficiency and complex process equipment, it is necessary to research and develop ultra-fine particle coagulators that strengthen coagulation on the basis of existing technologies. On the basis of the traditional dust collector, it is the current development trend of dust removal technology to add a coagulation treatment device to make the ultrafine particles condense into larger particles through physical methods or physical and chemical methods, so that they can be successfully removed in the main dust collector.
发明内容Contents of the invention
发明目的：本发明的目的是为了解决现有技术的不足，提出一种针对性强、适应面广、构造简单、可靠性好的强化凝并的凝并器。Purpose of the invention: The purpose of the invention is to solve the deficiencies of the prior art, and to propose a kind of intensive coalescer with strong pertinence, wide adaptability, simple structure and good reliability.
技术方案：为了实现本发明的目的，本发明采用如下的技术方案。Technical solution: In order to realize the object of the present invention, the present invention adopts the following technical solutions.
组合型管式凝并器，整个凝并器呈管道式，适于安装在主体除尘器之前的进气管道中；凝并器由荷电区和凝并区组成；荷电区有一组正、负相间的平行通道，内设负极板、正极板以及用来分隔的绝缘板，烟气中的粉尘颗粒经荷电后进入凝并区；凝并区中设置有2~4组横条，横条横置于凝并区中，横条的断面形状为角形和圆形，并依次交替组合；经凝并之后的烟气进入主体除尘器进行处理。Combined tube type condenser, the whole condenser is pipe type, suitable for installation in the intake pipe before the main dust collector; the condenser is composed of a charging area and a condensation area; the charging area has a set of positive, The parallel channels between the negative and negative phases are equipped with negative plates, positive plates and insulating plates for separation. The dust particles in the flue gas enter the condensation area after being charged; The strips are placed horizontally in the condensation area, and the cross-sectional shapes of the horizontal strips are angular and circular, and they are combined alternately in sequence; the flue gas after condensation enters the main dust collector for treatment.
进一步地，凝并区中设置的每组横条上下排列，横条的角形开口角度为70~120度；横条的高度为10~25cm；交替间隔设置的断面形状为圆形的横条，圆形的直径为10~25cm；角形和圆形的高度要一致；相邻两只横条之间的间距取横条高度的1.0~2.0倍；相邻两组横条之间的间距取横条断面长度的1.0~2.0倍，相邻两组横条之间错位设置。Further, each group of horizontal bars set in the condensation zone is arranged up and down, the angular opening angle of the horizontal bars is 70-120 degrees; the height of the horizontal bars is 10-25 cm; The diameter of the circle is 10~25cm; the height of the corner shape and the circle should be the same; the distance between two adjacent horizontal bars shall be 1.0~2.0 times the height of the horizontal bar; the distance between two adjacent horizontal bars shall be the horizontal 1.0~2.0 times the length of the bar section, and the offset between two adjacent groups of bars is set.
进一步地，在凝并区的入口处，竖向设置一组喷嘴，喷嘴通过管道与气泵相连，可将活性炭等吸附剂通过引导管经喷嘴喷入凝并区。Further, at the entrance of the condensation zone, a group of nozzles are vertically arranged, and the nozzles are connected to the air pump through pipelines, and adsorbents such as activated carbon can be sprayed into the condensation zone through the nozzles through the guide pipe.
进一步地，在凝并区的入口处，竖向设置一组喷嘴，由配液泵将凝并促进剂和水充分混合，混合后的凝并促进剂溶液经雾化后,通过引导管接入喷嘴，喷入凝并区，形成雾云。Further, at the entrance of the condensation zone, a group of nozzles are vertically arranged, and the coagulation accelerator and water are fully mixed by the liquid distribution pump. After the mixed coagulation accelerator solution is atomized, it is connected to the Nozzles are sprayed into the condensation zone to form fog clouds.
凝并器工作原理：气流首先经过双极荷电区，双极荷电区有一组正、负相间的平行通道，粉尘通过时，按其通道的正或负，分别获得正电荷或负电荷。这样，粉尘粒子一半荷正电，一半荷负电。然后进入凝并区，带正电的粒子和带负电的粒子在“静电力凝并”、“湍流凝并”和“化学凝并”的共同作用下碰撞凝聚，超细颗粒变成大颗粒，简称粒子粗大化；接着进入到后续主体除尘器（电除尘器或布袋除尘器）内部，粗大化的粒子便于除尘器收尘，这样便减少了细微颗粒的排放。The working principle of the condenser: the air flow first passes through the bipolar charging area. The bipolar charging area has a set of positive and negative parallel channels. In this way, the dust particles are half positively charged and half negatively charged. Then enter the coagulation zone, where positively charged particles and negatively charged particles collide and condense under the joint action of "electrostatic coagulation", "turbulent coagulation" and "chemical coagulation", and ultrafine particles become large particles, Referred to as particle coarsening; then it enters the interior of the subsequent main body dust collector (electric precipitator or bag filter), and the coarsened particles are convenient for dust collection by the dust collector, thus reducing the emission of fine particles.
“湍流凝并”是指通过特殊的构造，造成烟气气流的变化，形成接近湍流的状态。凝并的主要影响因素是颗粒大小、颗粒的凝聚性能与碰撞几率。待处理烟尘中，不缺乏大的粒子，大的粒子可作为核心，与超细粒子碰撞结大。凝聚性能方面：气流首先经过双极荷电区，分别获得正电荷或负电荷。这样，粉尘粒子一半荷正电，一半荷负电，在凝并区，带正电的粒子和带负电的粒子在“静电力”作用下有良好的凝并性能。湍流大大增加了烟气中颗粒的碰撞几率。由于凝并器的特殊构造，使得凝并器内分部气流交汇处成为湍流凝并主要发生区域。在静电力和化学凝并的基础上，进一步通过湍流凝并，强化了整体的凝并效果。气流通过圆形横条时，呈流线型，在形成湍流凝并的同时减小了压力降。"Turbulent condensation" refers to the change of the flue gas flow through a special structure, forming a state close to turbulence. The main influencing factors of coagulation are particle size, coagulation performance and collision probability of particles. There is no lack of large particles in the dust to be treated, and large particles can be used as nuclei to collide with ultrafine particles to form larger particles. In terms of condensation performance: the airflow first passes through the bipolar charging area to obtain positive or negative charges respectively. In this way, half of the dust particles are positively charged and half are negatively charged. In the condensation zone, the positively charged particles and negatively charged particles have good coagulation performance under the action of "electrostatic force". Turbulence greatly increases the chances of particle collisions in the flue gas. Due to the special structure of the condenser, the intersection of sub-airflows in the condenser becomes the main area where turbulent condensation occurs. On the basis of electrostatic force and chemical coagulation, the overall coagulation effect is enhanced through turbulent coagulation. When the airflow passes through the circular bar, it is streamlined, which reduces the pressure drop while forming turbulent condensation.
化学凝并原理：喷入的凝并促进剂在雾化器作用下经破碎后形成有一定扩散角度、且表面具有较高粘附活性的雾云，雾云吸附于飞灰颗粒表面，在颗粒之间产生液桥，在布袋除尘器前的烟道里，进而转化为固桥，促进颗粒凝并，使细小颗粒形成较大的聚团，以及细小颗粒被粗颗粒吸附。The principle of chemical coagulation: the sprayed coagulation accelerator is broken under the action of the atomizer to form a mist cloud with a certain diffusion angle and a high adhesion activity on the surface. The mist cloud is adsorbed on the surface of the fly ash particles, A liquid bridge is formed between them, and in the flue in front of the bag filter, it is transformed into a solid bridge, which promotes the coagulation of particles, makes fine particles form larger agglomerates, and fine particles are adsorbed by coarse particles.
本发明采用的活性炭吸附剂喷射装置，是在颗粒凝并前喷入粉末状活性炭，通过活性炭吸附剂的吸附作用来除去烟气中的汞。在烟气中喷入活性炭吸附剂是最有效除汞的方法之一。吸附剂为具有一定含碳量的粉煤灰经改性活化后形成的多孔状、比表面积丰富的颗粒物，同时具有物理和化学吸附功能，其平均粒径在20μm左右，比表面积>55m2/g，飞灰含碳量在6％~7％左右。The activated carbon adsorbent injection device used in the present invention sprays powdered activated carbon before the particles are coagulated, and removes mercury in the flue gas through the adsorption of the activated carbon adsorbent. Spraying activated carbon adsorbent in flue gas is one of the most effective methods for mercury removal. The adsorbent is a porous particle with a rich specific surface area formed by modifying and activating fly ash with a certain carbon content. It has both physical and chemical adsorption functions. g, the carbon content of fly ash is about 6%~7%.
有益效果：本发明提供的装置和现有装置相比具有以下优点。Beneficial effects: compared with the existing devices, the device provided by the invention has the following advantages.
（1）通过本发明所提供的特殊构造，多种凝并协同作用，提高了凝并效率，PM2.5占烟尘中颗粒的数量浓度较凝并前下降30%~50%，质量浓度较凝并前下降10~20%。(1) Through the special structure provided by the present invention, a variety of coagulation synergies have improved the coagulation efficiency, and the number concentration of PM 2.5 in the dust particles is reduced by 30% to 50% compared with that before coagulation, and the mass concentration is higher than that of coagulation 10~20% before.
（2）本发明主要通过在主体除尘装置前对超细颗粒物进行凝并，使之能够在主体除尘器的作用下加以脱除，本发明提供的装置可以提高主体除尘器对超细颗粒物的脱除效率，减少超细烟尘的排放。可以在同等的主体除尘器的工作状态和收集方式的条件下，烟尘中PM2.5去除率提高30％~50%。(2) The present invention mainly condenses the ultrafine particles before the main dust removal device, so that they can be removed under the action of the main dust collector. The device provided by the present invention can improve the removal of ultrafine particles by the main dust collector. Removal efficiency, reduce the emission of ultra-fine smoke. Under the same working condition and collection method of the main dust collector, the removal rate of PM 2.5 in the dust can be increased by 30% to 50%.
（3）本发明所提供的凝并器的各部分，分区合理，功能兼容匹配。(3) Each part of the condenser provided by the present invention has reasonable divisions and compatible functions.
（4）本发明所提供的凝并器为主体除尘器（电除尘器或袋式除尘器）的减容创造了条件。(4) The condenser provided by the present invention creates conditions for volume reduction of the main dust collector (electric dust collector or bag filter).
（5）本发明所提供的凝并器显著减少PM2.5及汞等有毒重金属的排放。(5) The condenser provided by the present invention significantly reduces the emission of toxic heavy metals such as PM 2.5 and mercury.
（6）本发明所提供的凝并器功能多样，调节灵活，喷入活性炭等吸附剂加强除汞、砷等有毒重金属，喷入化学高分子吸附剂即可强化凝并效果；与多种污染物控制的体系相比，在实现多功能的前提下，减少了投资，简化了运行，阻力损失小，压力降低，减少了能耗，运行成本低。(6) The condenser provided by the present invention has various functions and flexible adjustment. It can enhance the removal of toxic heavy metals such as mercury and arsenic by spraying activated carbon and other adsorbents. It can strengthen the condensation effect by spraying chemical polymer adsorbents; Compared with the physical control system, on the premise of realizing multi-function, it reduces investment, simplifies operation, has small resistance loss, reduces pressure, reduces energy consumption, and low operating cost.
（7）安装方便，适应面广，适于各种主体除尘器之前预处理，也提高了电除尘器或袋式除尘器对各种不同工业烟尘的适应性。(7) It is easy to install and has a wide range of applications. It is suitable for pretreatment before various main dust collectors, and also improves the adaptability of electrostatic precipitators or bag filter to various industrial fumes.
附图说明Description of drawings
图1为本发明提供的组合型管式凝并器构造示意图。Fig. 1 is a schematic diagram of the structure of a combined tubular condenser provided by the present invention.
图2为本发明中超细颗粒凝并原理示意图。Fig. 2 is a schematic diagram of the coagulation principle of ultrafine particles in the present invention.
在图1，2中：1:荷电区, 2:凝并区,3:负极板,4:绝缘板,5:正极板，6：角形横条，7：引导管，8: 喷嘴，9: 凝并前颗粒，10: 凝并后结大的颗粒，11:圆形横条，A:湍流凝并主要发生区域。In Figure 1, 2: 1: charging area, 2: condensation area, 3: negative plate, 4: insulating plate, 5: positive plate, 6: angular bar, 7: guide tube, 8: nozzle, 9 : particles before condensation, 10: large particles after condensation, 11: circular bars, A: the main area where turbulent condensation occurs.
具体实施方式detailed description
下面结合附图和具体实施例，进一步阐明本发明。The present invention will be further explained below in conjunction with the accompanying drawings and specific embodiments.
实施例1Example 1
某工业烟尘废气，处理量为80000m3/h采用组合型管式凝并器。整个凝并器呈管道式，安装在主体除尘器—电除尘器，之前的进气管道中；凝并器由双极荷电区和凝并区组成；双极荷电区有一组正、负相间的平行通道，内设负极板、正极板以及用来分隔的绝缘板，烟气中的粉尘经荷电后进入凝并区；凝并区中设置有4组横条，横条的断面形状为角形和圆形，并依次交替组合；经凝并之后的烟气进入主体除尘器进行处理。An industrial smoke and dust waste gas with a treatment capacity of 80,000m 3 /h uses a combined tubular condenser. The entire condenser is in the pipeline type, installed in the main dust collector - electrostatic precipitator, in the intake pipe before; the condenser is composed of a bipolar charging area and a condensation area; the bipolar charging area has a set of positive and negative Alternate parallel channels, with negative plates, positive plates and insulating plates for separation, the dust in the flue gas enters the condensation area after being charged; there are 4 sets of horizontal bars in the condensation area, the cross-sectional shape of the bars is It is angular and circular, and they are combined alternately in sequence; the condensed flue gas enters the main dust collector for processing.
凝并区中设置的每组横条上下排列，横条的角形开口角度为90度；横条的高度为15cm；交替间隔设置的断面形状为圆形的横条，圆形的直径为15cm；相邻两只横条之间的间距取横条高度的1.5倍；相邻两组横条之间的间距取横条断面长度的1.5倍，相邻两组横条之间错位设置。在图2中，A为湍流凝并主要发生的区域。Each group of horizontal strips set in the condensation zone is arranged up and down, the angular opening angle of the horizontal strips is 90 degrees; the height of the horizontal strips is 15cm; the cross-sectional shape arranged alternately is circular horizontal strips, and the diameter of the circle is 15cm; The distance between two adjacent horizontal bars shall be 1.5 times the height of the horizontal bars; the distance between two adjacent groups of horizontal bars shall be 1.5 times the section length of the horizontal bars. In Fig. 2, A is the region where turbulent condensation mainly occurs.
在凝并区的入口处，设置一组喷嘴，由配液泵将凝并促进剂和水充分混合，混合后的凝并促进剂溶液经雾化后，通过引导管接入喷嘴，喷入凝并区，形成雾云。凝并促进剂占水的质量百分比为1.5%；凝并促进剂溶液流量占烟气流量体积百分比为0.1%。经电除尘处理后的烟气，通过引风机将净化后达到排放标准的烟气从排气筒排出。At the entrance of the condensation zone, a set of nozzles is set up, and the coagulation accelerator and water are fully mixed by the liquid distribution pump. After the mixed coagulation accelerator solution is atomized, it is connected to the nozzle through the guide pipe and sprayed into the condensation Combined area, forming fog cloud. The mass percentage of the coagulation accelerator in water is 1.5%; the volume percentage of the coagulation accelerator solution in the flue gas flow is 0.1%. After the flue gas has been treated by electrostatic precipitator, the flue gas that has been purified and meets the emission standard is discharged from the exhaust pipe through the induced draft fan.
采用该装置处理使超细烟尘凝并成较大粒径的颗粒，并通过静电除尘器加以脱除，可以在不影响静电除尘器的工作状态和收集方式的条件下，烟尘中PM2.5去除率提高50%。所喷入的凝并促进剂在雾化器作用下，经破碎后形成具有较高粘附活性的雾云，促进颗粒凝并，烟尘中PM2.5去除率提高。采用本发明提供的超细颗粒凝并器，进行强化凝并，后接主体除尘器，整个工艺总除尘效率99.98%以上，烟气含尘排放浓度小于30mg/Nm3，排放烟气中PM2.5去除率提高50％。Using this device to condense ultra-fine smoke and dust into larger particles and remove them through the electrostatic precipitator can increase the removal rate of PM 2.5 in the dust without affecting the working status and collection mode of the electrostatic precipitator. Increase by 50%. The sprayed coagulation accelerator is broken under the action of the atomizer to form a mist cloud with high adhesion activity, which promotes the coagulation of particles and improves the removal rate of PM 2.5 in the smoke. The ultra-fine particle coalescer provided by the present invention is used to strengthen the coalescence, followed by the main dust collector, the total dust removal efficiency of the whole process is over 99.98%, the dust emission concentration of the flue gas is less than 30mg/Nm 3 , and PM 2.5 in the exhaust flue gas Removal rate increased by 50%.
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| CN108479285A (en) * | 2018-06-05 | 2018-09-04 | 盐城工学院 | A kind of modified ultra-fine grain duct type coalescer |
| CN111871141A (en) * | 2020-08-09 | 2020-11-03 | 盐城工学院 | A fan-shaped pipeline type ultra-fine particle condenser |
| CN111871135A (en) * | 2020-08-07 | 2020-11-03 | 盐城工学院 | Oval horizontal bar pipeline type ultrafine particle condenser |
| CN111871137A (en) * | 2020-08-09 | 2020-11-03 | 盐城工学院 | A diamond-shaped pipeline ultrafine particle condenser |
| CN116116578A (en) * | 2023-02-14 | 2023-05-16 | 宁波大学 | An electric bag dust collector with periodic bipolar charging of dust |
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| CN116116578B (en) * | 2023-02-14 | 2024-05-14 | 宁波大学 | Electric bag dust collector with dust periodically charged in bipolar mode |
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