CN111871141A - A fan-shaped pipeline type ultra-fine particle condenser - Google Patents
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- 239000011882 ultra-fine particle Substances 0.000 title claims abstract description 15
- 238000009833 condensation Methods 0.000 claims abstract description 34
- 230000005494 condensation Effects 0.000 claims abstract description 34
- 239000000428 dust Substances 0.000 claims abstract description 31
- 239000002245 particle Substances 0.000 claims abstract description 24
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000003546 flue gas Substances 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 4
- 238000005345 coagulation Methods 0.000 claims description 22
- 230000015271 coagulation Effects 0.000 claims description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 14
- 239000003463 adsorbent Substances 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000004581 coalescence Methods 0.000 claims 2
- 239000003595 mist Substances 0.000 claims 1
- 238000007596 consolidation process Methods 0.000 abstract 1
- 239000010419 fine particle Substances 0.000 description 6
- 239000004071 soot Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000012717 electrostatic precipitator Substances 0.000 description 3
- 230000007246 mechanism Effects 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000005054 agglomeration Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 2
- 229910052753 mercury Inorganic materials 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 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
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- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000005192 partition Methods 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
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- 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
- B01D53/02—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 by adsorption, e.g. preparative gas chromatography
- B01D53/06—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 by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
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- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/017—Combinations of electrostatic separation with other processes, not otherwise provided for
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- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/017—Combinations of electrostatic separation with other processes, not otherwise provided for
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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
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Abstract
一种扇形管道式超细颗粒凝并器，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，横条的断面形状为扇形；经凝并之后的烟气进入主体除尘器进行处理。本发明针对性强、适应面广、构造简单、可靠性好。
A fan-shaped pipeline type ultra-fine particle condenser, which is pipeline type, is suitable for being installed in the intake pipeline before the main dust collector. The condenser is composed of a charging area and a condensing area. The parallel channels between the negative phases are equipped with negative plates, positive plates and insulating plates for separation. The dust particles in the flue gas enter the condensing area after being charged; there are 2~4 sets of horizontal bars in the condensing area. The strips are placed horizontally in the condensation area, and the cross-sectional shape of the horizontal strips is fan-shaped; the flue gas after condensation and consolidation enters the main dust collector for treatment. The invention has strong pertinence, wide adaptability, simple structure and good reliability.
Description
技术领域technical field
本发明属于烟气除尘处理领域，涉及一种扇形管道式超细颗粒凝并器。The invention belongs to the field of flue gas dedusting treatment, and relates to a fan-shaped pipeline type ultrafine particle 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 seriously affects 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 generation 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 fume 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, and the turbulent vortex mechanism includes a turbulent vortex chamber, Soot inlet pipe and soot outlet pipe. The turbulent vortex chamber is in the shape of a bucket with an inverted isosceles trapezoid in cross section, and the bottom of which is connected with the ash bucket. After the second-stage treatment, the soot containing finer particles enters the soot inlet pipe, passes through the wind deflector, deflects the airflow downward, and enters the turbulent vortex chamber. The finer particles diffuse and collide with the inner wall of the turbulent vortex to promote fine Particle precipitation separates fine particulate matter from the soot. However, in this treatment process, the turbulent vortex chamber is used alone for the physical, coagulation and 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 a condenser, which includes 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 ash cleaning device is arranged on the frame beside the vortex generating sheet. However, too many vortices affect the flow rate of flue gas 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 an ultra-fine particle coagulator with enhanced coagulation on the basis of the existing technology. On the basis of the traditional dust collector, a coagulation and treatment device is added to make the ultrafine particles condense into larger particles by physical methods or physicochemical methods, so that they can be removed smoothly in the main dust collector, which is the current development trend of dust removal technology.
发明内容SUMMARY 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扇形管道式超细颗粒凝并器。Purpose of the invention: The purpose of the present invention is to solve the deficiencies of the prior art, and propose a fan-shaped pipeline type ultrafine particle condenser with strong pertinence, wide adaptability, simple structure, and good reliability to strengthen condensation.
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 scheme: In order to achieve the purpose of the present invention, the present invention adopts the following technical scheme.
一种扇形管道式超细颗粒凝并器，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，横条的断面形状为扇形；经凝并之后的烟气进入主体除尘器进行处理。A fan-shaped pipeline type ultra-fine particle condenser, the whole condenser is pipeline type, suitable for installation in the intake pipeline before the main dust collector; the condenser is composed of a charging area and a condensation area; the charging area There is a group of parallel channels between positive and negative phases, with negative plates, positive plates and insulating plates for separation. The dust particles in the flue gas enter the condensation area after being charged; there are 2 to 4 groups in the condensation area. The horizontal strip is placed horizontally in the condensation area, and the cross-sectional shape of the horizontal strip is fan-shaped; the flue gas after condensation and 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，横条的扇形开口角度为30~90度；横条的高度为10~25cm；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 arranged in the condensation area is arranged up and down, and the fan-shaped opening angle of the horizontal bars is 30 to 90 degrees; the height of the horizontal bars is 10 to 25 cm; the spacing between two adjacent horizontal bars is taken as the horizontal bars. 1.0 to 2.0 times the height; the spacing between adjacent two groups of horizontal bars is 1.0 to 2.0 times the length of the cross-section of the horizontal bars, and the adjacent two groups of horizontal bars are arranged in dislocation.
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 area, a group of nozzles are arranged vertically, and the nozzles are connected with the air pump through pipes, and adsorbents such as activated carbon can be sprayed into the condensation area 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 coagulation zone, a group of nozzles are arranged vertically, and the coagulation accelerator and water are fully mixed by the liquid dosing pump. After the mixed coagulation accelerator solution is atomized, it is connected through the guide pipe. Nozzle, spray into the condensation area to form a fog cloud.
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 airflow first passes through the bipolar charging area, and the bipolar charging area has a set of parallel channels with positive and negative phases. When the dust passes through, it will obtain positive or negative charges according to the positive or negative of its channels. In this way, the dust particles are half positively charged and half negatively charged. Then enter the condensation zone, the positively charged particles and the negatively charged particles collide and agglomerate under the combined action of "electrostatic force condensation", "turbulent condensation" and "chemical condensation", and the ultrafine particles become large particles. It is referred to as particle coarsening; then it enters the subsequent main dust collector (electrostatic precipitator or bag filter), and the coarsened particles are convenient for the dust collector to collect dust, 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。"Turbulent condensation" refers to the change of flue gas flow through special structures, forming a state close to turbulent flow. The main influencing factors of agglomeration are particle size, particle agglomeration properties and collision probability. In the smoke and dust to be treated, there is no shortage of large particles, and the large particles can be used as the core to collide with ultra-fine particles. In terms of cohesion 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 area, the positively charged particles and the negatively charged particles have good condensation performance under the action of "electrostatic force". Turbulence greatly increases the chance of collision of particles in the flue gas. Due to the special structure of the condenser, the intersection of the 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 strengthened through turbulent coagulation.
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 crushed under the action of the atomizer to form a fog cloud with a certain diffusion angle and high adhesion activity on the surface. A liquid bridge is generated between them, and in the flue before the bag filter, it is converted into a solid bridge, which promotes the coagulation of the particles, makes the fine particles form larger agglomerates, and the fine particles are adsorbed by the 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 is to inject powdered activated carbon before the particles are condensed, and the mercury in the flue gas is removed by the adsorption of the activated carbon adsorbent. Injecting activated carbon sorbent into flue gas is one of the most effective ways to remove mercury. The adsorbent is a porous particle with rich specific surface area formed by modified and activated fly ash with a certain carbon content, and 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 device, the device provided by the present invention has the following advantages.
（1）通过本发明所提供的扇形特殊构造，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 fan-shaped structure provided by the present invention, a variety of coagulation and synergistic effects are used to improve the coagulation efficiency. The number concentration of PM 2.5 in the particles in the dust is reduced by 30% to 50% compared with that before the coagulation, and the mass concentration is higher than that of the coagulation. And the former decreased by 10~20%.
（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. In addition to efficiency, reduce the emission of ultra-fine soot. Under the same working state and collection method of the main dust collector, the removal rate of PM 2.5 in the smoke 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 partitions and compatible functions.
附图说明Description of drawings
图1为本发明提供的一种扇形管道式超细颗粒凝并器构造示意图。FIG. 1 is a schematic structural diagram of a fan-shaped pipeline ultrafine particle condenser provided by the present invention.
在图1中：1:荷电区, 2:凝并区,3:负极板,4:绝缘板,5:正极板，6：横条，7：引导管，8: 喷嘴。In Fig. 1: 1: charging area, 2: condensation area, 3: negative plate, 4: insulating plate, 5: positive plate, 6: horizontal bar, 7: guide tube, 8: nozzle.
具体实施方式Detailed ways
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 illustrated 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采用扇形管道式超细颗粒凝并器。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，横条的断面形状为扇形；经凝并之后的烟气进入主体除尘器进行处理。An industrial flue gas waste gas with a treatment capacity of 80000m 3 /h adopts a fan-shaped pipeline type ultra-fine particle condenser. The whole condenser is pipeline type and is installed in the main precipitator - electrostatic precipitator, in the previous intake pipe; the condenser is composed of a bipolar charging area and a condensing area; the bipolar charging area has a set of positive and negative The parallel channels between the phases are equipped 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, and the cross-sectional shape of the horizontal bars It is fan-shaped; the condensed flue gas enters the main dust collector for treatment.
凝并区中设置的横条每组上下排列，横条的扇形开口角度为30度；横条的高度为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，相邻两组横条错位设置。The horizontal bars set in the condensation area are arranged up and down in each group, and the fan-shaped opening angle of the horizontal bars is 30 degrees; the height of the horizontal bars is 15cm; the distance between two adjacent horizontal bars is 1.5 times the height of the horizontal bars; The distance between the two groups of horizontal bars is 1.5 times the length of the cross-section of the horizontal bars, and the adjacent two groups of horizontal bars are arranged in dislocation.
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 area, a group of nozzles are set up, and the liquid dispensing pump will fully mix the condensation accelerator with water. After the mixed condensation accelerator solution is atomized, it is connected to the nozzle through the guide pipe, and sprayed into the condensation accelerator. merged, forming fog clouds. 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%. The flue gas treated by electrostatic precipitator will be discharged from the exhaust pipe through the induced draft fan.
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99.97%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％。The ultra-fine particle condenser provided by the invention is used to strengthen the condensation and then connect to the main dust collector. The total dust removal efficiency of the whole process is over 99.97%, the emission concentration of dust in the flue gas is less than 30 mg/Nm 3 , and PM 2.5 in the exhaust gas is The removal rate is increased by 50%.
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Citations (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0995495A1 (en) * | 1998-10-20 | 2000-04-26 | The Boc Group, Inc. | Electrostatic control for contact between gases and solid particles |
| CN103495322A (en) * | 2013-09-17 | 2014-01-08 | 西安理工大学 | Dust removal and mercury removal integrated device and method |
| CN104525372A (en) * | 2014-12-02 | 2015-04-22 | 中国重型机械研究院股份公司 | Fine particle electric coagulation apparatus |
| CN204841306U (en) * | 2015-06-19 | 2015-12-09 | 航天环境工程有限公司 | High -efficient pneumatic tube bank phase transition dust removal defogging device |
| CN106621665A (en) * | 2016-12-27 | 2017-05-10 | 盐城工学院 | Combined ultrafine particle coagulation box |
| CN106693579A (en) * | 2016-12-27 | 2017-05-24 | 盐城工学院 | Transversely arranged anchored pipeline type ultrafine particle coagulation device |
| CN106693592A (en) * | 2016-12-27 | 2017-05-24 | 盐城工学院 | Double-jet type streamlined ultra-fine particle coagulation box |
| CN106693593A (en) * | 2016-12-27 | 2017-05-24 | 盐城工学院 | Double-ejection type angle type ultrafine particle coagulation tank |
| CN106731436A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | A kind of streamline ductwork formula ultra-fine grain coalescer |
| CN106731391A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | The horizontal Y types ultra-fine grain coalescence case of double jet type |
| CN106731392A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | A kind of Novel super-thin particle coalescer |
| CN106731388A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | A kind of angle-style duct type ultra-fine grain coalescer |
| CN106731432A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | Combined tubular type coalescer |
| CN106731437A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | The horizontal anchor type ultra-fine grain coalescence case of double jet type |
| CN207024989U (en) * | 2016-12-27 | 2018-02-23 | 盐城工学院 | A kind of streamline ductwork formula ultra-fine grain coalescer |
| CN108479285A (en) * | 2018-06-05 | 2018-09-04 | 盐城工学院 | A kind of modified ultra-fine grain duct type coalescer |
-
2020
- 2020-08-09 CN CN202010792414.8A patent/CN111871141A/en active Pending
Patent Citations (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0995495A1 (en) * | 1998-10-20 | 2000-04-26 | The Boc Group, Inc. | Electrostatic control for contact between gases and solid particles |
| CN103495322A (en) * | 2013-09-17 | 2014-01-08 | 西安理工大学 | Dust removal and mercury removal integrated device and method |
| CN104525372A (en) * | 2014-12-02 | 2015-04-22 | 中国重型机械研究院股份公司 | Fine particle electric coagulation apparatus |
| CN204841306U (en) * | 2015-06-19 | 2015-12-09 | 航天环境工程有限公司 | High -efficient pneumatic tube bank phase transition dust removal defogging device |
| CN106621665A (en) * | 2016-12-27 | 2017-05-10 | 盐城工学院 | Combined ultrafine particle coagulation box |
| CN106693579A (en) * | 2016-12-27 | 2017-05-24 | 盐城工学院 | Transversely arranged anchored pipeline type ultrafine particle coagulation device |
| CN106693592A (en) * | 2016-12-27 | 2017-05-24 | 盐城工学院 | Double-jet type streamlined ultra-fine particle coagulation box |
| CN106693593A (en) * | 2016-12-27 | 2017-05-24 | 盐城工学院 | Double-ejection type angle type ultrafine particle coagulation tank |
| CN106731436A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | A kind of streamline ductwork formula ultra-fine grain coalescer |
| CN106731391A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | The horizontal Y types ultra-fine grain coalescence case of double jet type |
| CN106731392A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | A kind of Novel super-thin particle coalescer |
| CN106731388A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | A kind of angle-style duct type ultra-fine grain coalescer |
| CN106731432A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | Combined tubular type coalescer |
| CN106731437A (en) * | 2016-12-27 | 2017-05-31 | 盐城工学院 | The horizontal anchor type ultra-fine grain coalescence case of double jet type |
| CN207024989U (en) * | 2016-12-27 | 2018-02-23 | 盐城工学院 | A kind of streamline ductwork formula ultra-fine grain coalescer |
| CN108479285A (en) * | 2018-06-05 | 2018-09-04 | 盐城工学院 | A kind of modified ultra-fine grain duct type coalescer |
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