CN103316553B - 湿式变流喷雾喷淋高效除尘净化装置 - Google Patents
湿式变流喷雾喷淋高效除尘净化装置 Download PDFInfo
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- CN103316553B CN103316553B CN201310281391.4A CN201310281391A CN103316553B CN 103316553 B CN103316553 B CN 103316553B CN 201310281391 A CN201310281391 A CN 201310281391A CN 103316553 B CN103316553 B CN 103316553B
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- layer
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- 238000005507 spraying Methods 0.000 title claims abstract description 63
- 238000000746 purification Methods 0.000 title abstract description 22
- 239000010410 layers Substances 0.000 claims abstract description 130
- 239000000779 smoke Substances 0.000 claims abstract description 29
- 238000005406 washing Methods 0.000 claims abstract description 29
- 239000007921 sprays Substances 0.000 claims description 118
- 239000007788 liquids Substances 0.000 claims description 79
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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- 239000000292 calcium oxide Substances 0.000 description 1
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Abstract
Description
技术领域
[0001] 本发明涉及一种除尘净化装置,尤其涉及一种用于大气污染防治的湿式变流喷雾喷淋高效除尘净化装置,属于烟气除尘脱硫净化装置技术领域。
背景技术
[0002] 我国正处在工业化和城市化快速发展进程之中,改善环境质量的难度持续增加和人民群众不断提高的环境需求之间的矛盾更加突出。在大气污染防治领域,细颗粒物、二氧化硫、氮氧化物、二恶英等多因子污染物协同诒理提到议事日程。2013年初,全国大范围的雾霾天气引起了政府高层、公众舆论的广泛关注。2013年2月27日,国家决定钢铁、水泥等行业均将在不同时段开始执行大气污染物特别排放限值。强化可吸入性粉尘,特别是大气细颗粒物(PM2.5)的治理。为确保大气污染物排放全面、高水平达到特别排放限值标准要求,对大部分在用烟气净化装置进行技术改造,实现净化装置的能效升级;为新建项目提供更高性能的烟气净化技术装备已成为污染减排的紧迫性任务。
[0003] 湿法烟气除尘净化技术是应用最为广泛的技术。用于除尘,能够处理高温、高湿、黏度大及含高比电阻粉尘的气体,处理可燃性、爆炸性气体或粉尘时,可将着火、爆炸的可能减至最低。可以有效去除直径为0.1〜20 μπι的液态或固态粒子,亦能脱除气态污染物。
[0004] 而逆流接触喷淋净化塔是湿法烟气除尘净化装置的主流塔型,属低能湿式除尘器。具有内部构件少、塔内不易结垢和堵塞、压力损失小、运行费用低、性能稳定、操作方便等优点。通常压力损失为0.2〜2.5kPa,广泛应用烟气除尘及脱硫等有害气体净化过程。
[0005] 逆流接触喷淋净化塔用于除尘,是惯性碰撞、拦截作用、扩散效应、热泳和静电作用等多种效应共同实现的过程,其中惯性碰撞和拦截作用是湿式除尘器的主要除尘机制。在捕集很小的尘粒时,会受到布朗运动引起的扩散作用的影响。塔内惯性碰撞作用主要取决于尘粒质量及其与水滴之间的相对运动速度;同时与水滴大小有重要关系。一般来说水滴小时,惯性碰撞作用增强,有利于从含尘气体中分离尘粒。所以,对于给定的含尘系统,要提高斯托克斯准数St值,必须提高气液之间的相对运动速度并减少水滴直径。在喷水量一定时,水滴愈细,下降水滴布满塔截面的比例愈大,产生拦截捕集尘粒的概率愈大。
[0006] 但逆流接触喷淋净化塔用于除尘过程,水滴直径不是愈小愈好,细水滴的沉降速度较慢,甚至出现直径太小的水滴随气流一起运动的现象,细水滴与气体之间的相对运动速度比粗水滴小,因而靠惯性碰撞捕集尘粒的概率随水滴直径减小而减小,不利于从含尘气体中把尘粒分离出来,同时增加净化后烟气的气液分离难度。因此水滴直径要受到水滴在塔中的降落时间及被气流带走的限制。
[0007] 传统逆流接触喷淋净化塔用于烟气脱硫等有害气体净化过程,同样存在吸收剂雾化粒径太大,吸收剂利用率低,太小容易被烟气携带出洗涤区,造成未完全反应的脱硫剂损失,给工艺后段除雾器等设备增加负荷。通常湿法脱硫的雾化粒径在13003000 μ mo而依据薄膜理论,强化传质措施主要是通过良好的雾化,产生细小的液滴,同时增大相对运动速度。
[0008] 可见传统逆流接触喷淋除尘净化塔,较高的空塔速度,对应的喷淋(雾)水滴粒径相对要大,反之较细的喷淋(雾)水滴粒径,对应的喷淋洗涤塔空塔速度要较低,在同一塔内提高空塔速度与减小喷淋(雾)水滴粒径不能同时并举,这巳成为提高湿式除尘脱硫装置除尘净化效率的技术瓶颈。
[0009] 通常做法是综合这两种对立机制,权衡效率与投资、场地条件、运行费用等因素,求证得对粉尘的各种粒径捕集效率之最佳水滴直径和与之相应的空塔临界速度。
[0010] 问题是:通常即便优化设计的低能湿式喷淋净化塔用于烟气净化除尘,其对粒径为O — 5um细颗粒的分级效率仅为50-72%,对5 — 1um可吸入性粉尘的分级效率仅为80%-90%,对10 μ m以上粉尘的净化效率可达90%〜98%,在通常粉尘粒径频率分布下除尘总效率为86.5%—94.5%。对粒径在1um以下粉尘分布占较大比重时除尘总效率会低于90%。
[0011] 显然,通常现有湿法烟气喷淋净化技术己难以满足大气污染物特别排放限值要求。
[0012] 对于多分散气溶胶体系,控制装置的总除尘效率将取决于颗粒的粒径分布和对这种粉尘的分级效率。
[0013] 通常湿式净化洗涤器对40um以上颗粒物的分级效率能够达到98%以上。可见要实现湿法烟气喷淋吸收净化装置的能效升级,提高其对粒径为< 40um颗粒物的分级效率成为技术关键。
发明内容
[0014] 针对上述缺陷,本发明的目的在于提供一种能够满足大气污染物特别排放限值要求,提高对粒径< 40um颗粒物的分级净化效率,提高在低耗能条件下对烟气的除尘净化效率的湿式变流喷雾喷淋高效除尘净化装置。
[0015] 为此本发明所采用的技术方案是:包括洗涤塔,所述洗涤塔下端设有与其相切的烟气入口,洗涤塔下端中间设有中心稳流柱与洗涤塔组成环形通道,稳流柱上方自下而上依次设有雾凝捕集区、喷淋洗涤区和脱水除雾区,雾凝捕集区与喷淋洗涤区之间设有变流喷射拦截层,所述洗涤塔上端设有烟气出口。
[0016] 所述变流喷射拦截层是由一组外向型旋流板和一组单层或多层棒栅层串联复合组成或由一组单层或多层棒栅层组成,所述外向型旋流板的旋向与烟气切向入洗涤塔的旋向一致。
[0017] 所述外向型旋流板的中心盲板上方设有一喷雾布液器,所述喷雾布液器的喷射角呈45-120 °,所述喷雾布液器的喷嘴朝向外向型旋流板的中心盲板,所述喷嘴出口与中心盲板的距离为100-700mm。
[0018] 所述单层或多层棒栅层的相邻棒栅层的棒栅截面布列方向相同且呈相间交错排列,每层棒栅层的棒栅截面形状相同,布列方向相同,棒栅间距相等,所述棒栅是由实心圆棒或空心圆管排列组成。
[0019] 所述变流喷射拦截层还可以棒栅层、托盘层、填料层、丝网层、浮动筛板、穿流式塔板、筛孔板单独组成或相互串联组成。
[0020] 所述变流喷射拦截层与雾凝捕集区之间设有一组双流体喷枪和一组细液雾喷枪,所述双流体喷枪位于细液雾喷枪下方且呈顺气流方向布置,所述细液雾喷枪呈逆气流布置并与双流体喷枪呈相间交错排列,所述细液雾喷枪的出口液雾流速为25-37m/s。
[0021] 所述喷淋洗涤区内自下而上设有三层或三层以上的喷淋层,所述喷淋层由带连接支管的洗涤液母管和喷嘴组成,最顶层的喷淋层的喷嘴为单向喷嘴,方向向下,其他喷淋层的喷嘴为双向喷嘴,相邻喷淋层的喷嘴呈相间交错排列。
[0022] 所述脱水除雾区内设有两层脱水除雾层,所述脱水除雾层上下两端设有若干冲洗喷嘴朝向脱水除雾层。
[0023] 本发明的优点是:本专利烟气入口采用切向入塔,与现有旋风(或水膜)洗涤器不同,烟气入口采用低流速llm/s)切向入塔,在中心稳流柱与塔体围成的环形通道断面上采用低速旋流速度,使该断面雾场密度分布沿径向梯度大大降低,增强了细雾夹带的洗涤液与含尘气流的均匀旋切接触,充分利用了洗涤液的位能对细微粉尘的拦截作用。
[0024] 同时含尘烟气流在环形通道内旋转上升,延长了含尘烟气流与洗涤液在相变区域的停留接触时间和接触面积。
[0025] 通常采用的旋风(或水膜)洗涤器采用较高的入口气流速度,一般为15 — 22m/s,阻损一般为550Pa—800Pa,采用低速旋流速度与通常的旋风水膜洗涤器相比该段的阻损降低 32%。
[0026] 烟气在入口区域快速降温并趋于饱和,加速了烟气在入口处的调湿效果,提高了洗涤液对细微粉尘的润湿、凝聚效率。也为降低后续液雾颗粒的蒸发速率创造适宜的湿环境。同时过饱和水气在细颗粒表面凝结长大,有效提高超细颗粒脱除率。
[0027] 洗涤塔内自下而上设有雾凝捕集区、喷淋洗涤区和脱水除雾区,在雾凝捕集区与喷淋洗涤区之间设有变流喷射拦截层,使烟气流向依次完成旋流向喷射流、平推流转变。
[0028] 在变流喷射拦截层下方呈逆气流设置一组一组细液雾喷枪,同时在该断面向上与细雾喷枪喷射角呈相间、交错排列,顺气流设置一组双流体(气、水)喷枪或细液雾喷枪。在该区域注入水雾或吸收剂的雾滴群,大量增加该区域内的雾场(雾化态的吸收剂)密度。烟气与雾滴群发生强烈旋切和扰动、掺混,雾滴群与湿态烟气流之间的相对运动速度显著快加,高速的水雾颗粒通过弹性碰撞使粉尘颗粒湿润,拦截、凝聚、传质作用增强,克服气膜与液膜的阻力,增强了捕集、吸收的推动力。重要的是该区域获得了大量和较细粉尘颗粒大小接近的雾滴群或吸收剂的雾滴群,并形成较高的雾场密度。由此,形成动态有效凝聚、拦截以悬浮颗粒包括细颗粒物及可吸入性粉尘为核的雾滴群的功能。从而提高净化系统对烟气中< 40um粉尘粒径的分级效率,进而提高净化系统在低能耗条件下的总除尘净化效率。突破了在同一塔内提高空塔速度与减小喷淋(雾)水滴粒径不能同时并举的技术瓶颈。
[0029] 携带不同细粒径的以悬浮颗粒为核的快速雾滴群流一水雾或吸收剂的气雾混和烟气向上通过外向型旋流板,产生旋转和离心运动,其作用增补了雾凝捕集区入口预处理段烟气旋流上升的能量,强化了下泄洗涤液与烟气旋切、混和、传质的过程。
[0030] 同时中心盲板上方设置的一套中心布液器,成一定喷射角喷入的水雾或吸收液被旋流分配至各叶片,在叶片上形成流动的液膜层,下泄洗涤液与旋转向上的气雾挟带的含尘烟气流产生撞击、搅动、掺混,凝聚、拦截,部分喷淋液趋壁下泄,部分喷淋液沿叶面钭向甩出下泄。
[0031] 混合烟气通过单层或多层棒栅层,由于棒栅层烟气流通面积缩小,烟气在棒栅层的每相邻两截面空隙之间加速通过,塔内喷淋而下的洗涤液与逆流而上的携带气雾的含尘混合烟气形成悬浮错动,气、固、液三相之间湍流接触,发生激烈的惯性碰撞、凝聚和拦截,极大地增加了气、液两相之间的传质、传热表面,另一方面混合烟气通过棒栅层时,形成强烈的”以液体包围气体”的鼓泡喷射态,提高了净化系统对微细尘粒的捕集率和气体净化的传质效率。
[0032]由于在雾凝捕集区提高了其对粒径为<40um颗粒物的分级净化效率,从而在喷淋洗涤段可改变通常在该区段为捕集细颗粒物而采用大液气比”过度洗涤”的做法,在更低的液气比下达到较高的除尘净化效率,降低了循环液的循环量。从而降低了湿式净化系统的总电耗。
[0033] 相比通常湿式喷淋洗涤塔净化系统用于除尘,同等条件下液气比可减少33%,便可达到理想除尘效率。由于循环量的减少,(烟气量不变,液气比减少),喷淋洗涤塔湿阻相应降低,也就降低了风机能耗。与通常湿式喷淋洗涤塔相比,总喷淋液量不变的情况下,又由于降低喷淋洗涤层的液气比,用于增加雾凝捕集区低位扬程喷雾量,则洗涤液循环泵的总电耗可减小,按喷淋洗涤层喷淋液量占总洗涤液量的80%计,则电耗下降5%。这样由于洗涤液循环量的减少、供液泵总扬程降低,与通常湿式喷淋洗涤塔相比,总电耗约降低38%。
[0034] 湿式变流喷雾喷淋高效除尘净化装置,由于在雾凝捕集区提高了其对粒径为< 40um颗粒物的分级效率,除尘总效率达到98%,相比通常湿式喷淋洗涤塔除尘总效率提高2-8%,全塔阻损彡1500Pa。
[0035] 通常逆流接触喷淋洗涤塔用于烟气脱硫等有害气体净化过程,适当提高吸收塔内空塔烟气流速,可提高气、液二相的湍动,降低烟气与液滴之间的膜厚度,从而提高总传质系数。在相同的吸收段高度条件下,提高塔内烟气流速,将降低传质单元高度,从而便于增大传质单元数,利于强化传质过程,显著提高脱硫率。再则,提高塔内烟气流速,喷淋液滴的下降速度将减小,塔断面持液量将增大,相当于增大了塔内的洗涤液喷淋密度,增大了吸收段的总传质面积,从而相当于增大了可用于吸收S02等有害气体的总碱度等。
[0036] 吸收剂的浆粒粒径愈小,比表面积愈大,吸收段的总传质面积愈大,愈有利于提高脱硫效率。但吸收塔内空塔烟气流速、浆粒粒径等参数同样受到气、液、固三相分离临界速度、临界粒径的限制。
[0037] 在烟气入口断面与变流喷射拦截层之间,与烟气入口洗涤增湿断面一定距离断面上呈逆气流设置一组细液雾喷枪,同时在该断面向上与细雾喷枪喷射角呈相间、交错排列,,顺气流设置一组双流体喷枪或细液雾喷枪,向该区段注入大量不同细粒径的快速流(喷枪出口液雾流速达到25m/s-37m/s)吸收剂的雾滴群。实现塔内分区段注入不同粒径的吸收剂,有利于增加总传质面积,降低钙硫比,降低供浆能耗,提高脱硫效率。
[0038] 另一方面在钙法烟气脱硫喷淋洗涤塔中,飞灰在一定程度上阻碍了 S02与脱硫剂的接触,降低了石灰石中Ca2+的溶解速率。因此设置变流喷射拦截层,减少进入喷淋吸收区的总悬浮颗粒物,有利于提尚脱硫效率。
[0039] 通常逆流接触喷淋脱硫塔内,逆烟气流动方向,塔内总碱度呈逐渐减弱之态势,通过在塔的中下部设置变流喷射拦截层,向该区段低位补入适当量的雾态碱性吸收液,促使塔内碱度均化,保持较高的气液传质效率,从而提高总脱硫效率,同时降低吸收剂浆泵能耗。
[0040] 通过设置变流喷射拦截层,适当增加烟气在相变区域的停留时间,强化了烟气湍流,从而强化了气液固三相的传质,使吸收剂与烟气中的有害气体反应更充分。
[0041] 同样用于脱硫等气体净化过程,由于吸收液循环量的减少、供液泵总扬程降低,总电耗约降低25.8%。
附图说明
[0042] 图1是本发明的结构示意图。
[0043] 图2是图1中A-A的剖视图。
[0044] 图中I是洗涤塔、2是烟气入口、3是中心稳流柱、4是烟气出口、5是外向型旋流板、6是棒栅层、7是细液雾喷枪、8是双流体(气水)喷枪、9是中心布液器、10是第一喷淋层、11是第二喷淋层、12是第三喷淋层、13是供液接口、14是喷淋层供液管接口、15是二级脱水除雾器、16是二级脱水除雾器冲洗工艺水接口、17是细液雾喷枪组供液接口、18是双流体(气水)喷枪组供液接口、19是双流体(气水)喷枪组供压气接口,20是排污斜槽、21是排污管道、22是循环沉淀池。
具体实施方式
[0045] 实施例1
[0046] 湿式变流喷雾喷淋高效除尘净化装置,包括洗涤塔I,所述洗涤塔I下端设有与其相切的烟气入口 2,洗涤塔I下端中间设有中心稳流柱3与洗涤塔I组成环形通道,中心稳流柱3上方自下而上依次设有雾凝捕集区1、喷淋洗涤区II和脱水除雾区III,雾凝捕集区I与喷淋洗涤区11之间设有变流喷射拦截层,所述洗涤塔I上端设有烟气出口 4。所述变流喷射拦截层是由一组外向型旋流板5和一组单层或多层棒栅层6串联复合组成或由一组单层或多层棒栅层6组成,所述外向型旋流板5的旋向与烟气切向入洗涤塔I的旋向一致。
[0047] 烟气由烟气入口 2低速llm/s)切向进入洗涤塔1,入洗涤塔I后沿中心稳流柱3与洗涤塔I围成的环形通道旋流向上,首先与喷淋下泄的吸收液接触洗涤、降温、增湿,烟气旋流而上一定距离,在烟气入口 2横断面至变流喷射拦截层之间适当断面上呈逆气流设置一组细液雾喷枪7,同时在该断面向上与细液雾喷枪7喷射角呈相间、交错排列的顺气流设置一组双流体(气水)喷枪8,对应烟气中< 10um粉尘粒径分布向该区段均匀喷射不同细粒径的雾滴群或吸收剂的雾滴群,烟气与之旋切混合。
[0048] 采用上述组合喷雾系统或单独使用细液雾喷枪7喷雾系统,向该区段注入不同细粒径的雾滴群或吸收剂的雾滴群雾滴邵特平均粒径SMD32覆盖:50um - 150um。
[0049] 双流体(气水)喷枪8正常工作时,需要控制操作条件,同时供给一定压力的压缩气(空气或氮气、蒸汽)和一定压力的水(或吸收液)。双流体(气水)喷枪8喷嘴的内部,压缩气与水或吸收剂的溶液经过若干次的打击,产生非常细小的颗粒。喷枪出口液雾流流速达到25m/s-37m/s,喷嘴正常工作时,通常情况下喷嘴入口处的气体工作压力为0.3-0.5Mpa,水或吸收剂的工作压力为0.3-0.65 Mpa。
[0050] 携带不同雾滴粒径的液雾颗粒群的混合烟气向上通过外向型旋流板5,与外向型旋流板5之上中心布液器9喷射出的洗涤液形成的强力液膜混合、传质,被捕集烟尘或生成物呈气、液挟裹、离心趋壁,汇聚成水膜在设定的环形通道下泄;在外向型旋流板5向上小于800m距离截面上设置单层或多层棒栅层6,流通面占断面积38-55%。
[0051] 棒栅层6向上为喷淋洗涤区II,喷淋洗涤区II分别设置第一喷淋层10、第二喷淋层11、第三喷淋层12。喷淋层均由带连接支管的母管洗涤液分布管道和喷嘴组成,该区段自下而上设置三层或多层喷淋层,第一喷淋层10和第二喷淋层11喷嘴为双向喷嘴,第三喷淋层12喷嘴为单向喷嘴且方向为向下,相邻喷淋层的喷嘴呈相间交错排列,喷嘴均匀布置于上流区的横截面上,其喷淋覆盖率大于200%。喷淋液采用单元制供液设计,外向型旋流板5之上中心布液器9与第一喷淋层10由供液接口 13接入,第二喷淋层11和第三喷淋层12由喷淋层供液管接口 14接入,二级脱水除雾器15由二级脱水除雾器冲洗工艺水接口 16接入,细液雾喷枪7由细液雾喷枪组供液接口 17接入,双流体(气水)喷枪8由双流体(气水)喷枪组供液接口 18接入,双流体(气水)喷枪8由双流体(气水)喷枪组供压气接口19接入,每组喷淋层及二级脱水除雾器15分别独立设置供液循环泵,以便选择经济运行模式。最顶端喷淋层向上为脱水除雾区III,设置二级折板式除雾器及支撑组件或在吸收塔后的烟道上设置除雾器组。二级脱水除雾器15均引入工艺冲洗水,冲洗过程通过程序控制自动完成,两经高效除雾后其出口水滴携带量< 75mg/Nm3 (干基),确保进入风机的气流洁净,净烟气经烟气出口引入排气筒排放。
[0052] 被捕集的泥水进入除尘塔底部排污斜槽20,汇集后经排污管道21水封冲灰结构排至循环沉淀池22 ;在循环沉淀池22内完成冷却、澄清,上清液进入循环池22清水区、由循环泵供给设备循环使用,除尘灰泥在循环沉淀池22中得到浓缩,由渣浆液下泵定时提取,送至干化场处理。
[0053] 本专利由于处理装置为一体化设备,布局紧凑,包括风机动力站、排气筒等占地面积仅105m2,污水排入沉淀统一沉淀处理,操作方便,所有喷枪均为可拆卸方式安装于塔体上,细液雾喷枪7和双流体(气水)喷枪8均设为中央控制和现场手动控制模式。在相同的处理风量条件下,基建投资费用、设备投资费用及运行费用都低于己有技术,同等条件下液气比可减少33%,除尘效率多98%,完全满足国家新的大气污染物特别排放限值要求的新一代湿式净化技术及装置,广泛应用于钢铁、有色金属、水泥建材、电力、化工等行业的高温、高湿、黏度大及含高比电阻粉尘的烟气净化。
[0054] 实施例2
[0055] 大型钢铁公司渣处理综合改造项目,采用滚筒法渣处理工艺,从渣处理装置引出的含尘蒸汽流烟气含湿量高:13%—15%,所挟带的粉尘为钢渣的超细粉,具有水硬性和黏(结)性。从含尘粒径分布看:所占体积百分数/%:粒径> 1um占56%,粒径2 — 1um占32%其余< 2um占12%。该粉尘在布袋和塑烧板上易板结,清灰困难,故选用湿式喷淋除尘设备,设于引风机之前,净化后气体经风机、排气筒排放至大气。
[0056] 本实施例有关运行参数如下:
[0057]处理烟气量 15 X 104m3/h
[0058] 进口烟气温度 80~100°C
[0059] 粉尘入口初始浓度 1300mg/Nm3
[0060] 空塔烟气速度 3.6 (m/s)
[0061] 脱水除雾区烟气速度 3.4(m/s)
[0062] 洗涤液采用工业浊环水(水压0.3MPa),与通常喷淋洗涤塔相比,同等条件下液气比减少33%。
[0063] 双流体(气水)喷枪8 —组
[0064] 细液雾喷枪7 —组
[0065] 经除尘净化装置处理后,除尘效率彡98%,喷淋除尘塔总阻力Pa ( 1380Pa,出口烟气温度66 °C
[0066] 具体工作过程如下:
[0067] 烟气由烟气入口 2低速(10.4m/s)切向进入洗涤塔I内,入洗涤塔I后沿中心稳流柱3与洗涤塔I围成的环形通道旋流向上,上流速度取4.3m/s,首先与喷淋下泄的吸收液接触洗涤、降温、增湿。
[0068] 烟气入口 2上流一定距离设置变流喷射拦截层。该层由一块外向型旋流板5和单层圆柱型棒栅层6串联复合组成,使冼涤塔I内烟气入口 2至烟气出口 4,自下而上动态形成一区段雾凝捕集区1、二区段喷淋洗涤区I1、三区段脱水除雾区III。
[0069] 在变流喷射拦截层下方雾凝捕集区I内,距烟气入口 2上沿边向上彡1.7m断面上呈间隔、交错排列,顺气流设置一组双流体(气水)喷枪8,逆气流设置一组细液雾喷枪7。向该区段注入不同细粒径的雾滴群或吸收剂的雾滴群,形成高密度的雾群雾场,
[0070] 双流体(气水)喷枪8正常工作时,同时供给满足条件的工业净环水,水量7.5T/h,水压0.46MPa,压缩空气量366Nm3/h,压力0.42MPa。
[0071] 细液雾喷枪7正常工作时,供给工业净环水量15T/h,(水压0.3—0.5MPa。
[0072] 携带不同粒径净化液雾粒的混和烟气向上通过外向型旋流板5,外向型旋流板5中心盲板上方设置的一套中心布液器9,喷射角呈90°,喷嘴(向下)朝向中心盲板,喷嘴出口距中心盲板400_。
[0073] 烟气与喷入的水雾布液形成的强力液膜混合、传质,生成物与被捕集烟尘由气、液挟裹、离心趋壁,汇聚成为水膜在设定的环形通道下泄;在外向型旋流板5向上小于800m距离截面上设置单层圆柱棒栅层6。流通面占断面积44%。
[0074] 变流喷射拦截层向上二区段二区段喷淋洗涤区II,该区段自下而上分别设置三层或多层喷淋层,顶层喷淋层喷嘴为单向喷嘴,方向为向下,其他喷淋层喷嘴为双向喷嘴,相邻喷淋层的喷嘴呈相间交错排列。
[0075] 顶层喷淋层向上采用变径塔,设置平板式脱水除雾层,净化后的烟气经高效除雾后其出口液滴含量< 65mg/Nm3 (干基),确保进入风机的气流洁净。净烟气经下降管道接入一台引风机送入排气筒排放。
[0076] 被捕集的泥水进入除尘塔底部排污斜槽20,汇集后经排污管道21,水封冲灰结构排至循环沉淀池22 ;在循环沉淀池22内完成冷却、澄清,上清液进入循环沉淀池22清水区、由循环泵供给设备循环使用,除尘灰泥在循环沉淀池22中得到浓缩,由渣浆液下泵定时提取,送至干化场处理。
[0077] 双流体(气水)喷枪8和细液雾喷枪7、双流体(气水)喷枪8、脱水除雾层冲洗喷嘴均为独立的整体设备,配备有独立的控制系统和必要的水源、气源过滤器、压力、流量检测控制元件。
[0078] 工作操作可设为中央控制和现场手动控制模式,主要调节控制喷枪入口水压和气压(一般调节水压),从而获得满意的流量、液滴粒径及完成设定的冲洗程序。
[0079] 实施例3
[0080] 某大型钢铁公司采用热泼法钢渣处理工艺,其基本工艺原理为:在炉渣高于可淬温度时以有限的水向炉渣喷洒,使渣产生的温度应力大于渣本身的极限应力产生碎裂,游离氧化钙的水化作用使渣粒进一步裂解。处理过程中粉尘含量高,含湿量高:12%-16%,蒸气量大。从渣处理装置一组2个热拨渣箱,引出的含尘蒸汽流烟气所挟带的粉尘为钢渣的超细粉,具有水硬性和黏(结)性。
[0081 ] 从含尘粒径分布看:所占体积百分数/%:粒径> 1um占46%,粒径< 1um占54%。该粉尘在布袋和塑烧板上易板结,清灰困难,故选用湿式喷淋除尘设备,设于引风机之前,净化后气体经风机、排气筒排放至大气。
[0082] 本实施例有关运行参数如下:
[0083]处理烟气量 24 X 104m3/h
[0084] 进口烟气温度 80~110°C
[0085] 粉尘入口初始浓度 1000mg/Nm3
[0086] 空塔烟气速度 4 (m/s)
[0087] 脱水除雾区烟气速度 3.6 (m/s)
[0088] 洗涤液采用工业浊环水(水压0.3MPa),与通常喷淋洗涤塔相比,同等条件下液气比减少30%ο
[0089] 工业浊环水流量(水压0.3MPa) 180T/h
[0090] 间隙冲洗水(工业净环水) 40T/h
[0091] 双流体(气水)喷枪8 —组
[0092] 细液雾喷枪7 —组
[0093] 经除尘净化装置处理后,除尘效率彡98%,喷淋除尘塔总阻力Pa ( 1500Pa。
[0094] 具体工作过程如下:
[0095] 烟气由烟气入口 2低速(llm/s)切向进入洗涤塔1,入洗涤塔I后沿中心稳流柱3与洗涤塔I围成的环形通道旋流向上,上流速度取4m/s。首先与喷淋下泄的吸收液接触洗涤、降温、增湿。
[0096] 烟气入口 2上流一定距离设置变流喷射拦截层。该层由一块外向型旋流板5和单层圆柱型棒栅层6串联复合组成,使冼涤塔I内烟气入口 2至烟气出口 4,自下而上动态形成一区段雾凝捕集区1、二区段喷淋洗涤区I1、三区段脱水除雾区II。
[0097] 在变流喷射拦截层下方雾凝捕集区I内,距烟气入口 2上沿边向上彡2m断面上呈间隔、交错排列,顺气流设置一组双流体(气水)喷枪8,逆气流设置一组细液雾喷枪7,向该区段注入不同细粒径的雾滴群或吸收剂的雾滴群,形成高密度的雾群雾场,双流体(气水)喷枪8正常工作时,同时供给满足条件的工业净环水和压气,细液雾喷枪7正常工作时,供给工业净环水。
[0098] 携带不同粒径净化液雾粒的混和烟气向上通过外向型旋流板5,外向型旋流板5中心盲板上方设置的一套中心布液器9,喷射角呈120°,喷嘴(向下)朝向中心盲板,喷嘴出口距中心盲板550mm。
[0099] 烟气与喷入的水雾布液形成的强力液膜混合、传质,生成物与被捕集烟尘由气、液挟裹、离心趋壁,汇聚成为水膜在设定的环形通道下泄;在外向型旋流板5向上小于800m距离截面上设置单层圆柱棒栅层6,流通面占断面积39%。
[0100] 变流喷射拦截层向上二区段喷淋洗涤区II,该区段自下而上分别设置三层或多层喷淋层,顶层喷淋层喷嘴为单向喷嘴,方向为向下,其他喷淋层喷嘴为双向喷嘴,相邻喷淋层的喷嘴呈相间交错排列。
[0101] 顶层喷淋层向上采用变径塔,设置平板式脱水除雾层,净化后的烟气经高效除雾后其出口液滴含量< 65mg/Nm3 (干基),确保进入风机的气流洁净。净烟气经下降管道接入一台引风机送入排气筒排放。
[0102] 被捕集的泥水进入除尘塔底部排污斜槽20,汇集后经排污管道21,水封冲灰结构排至循环沉淀池22 ;在循环沉淀池22内完成冷却、澄清,上清液进入循环沉淀池22清水区、由循环泵供给设备循环使用,除尘灰泥在循环沉淀池21中得到浓缩,由渣浆液下泵定时提取,送至干化场处理。
[0103] 双流体(气水)喷枪8和细液雾喷枪7、双流体(气水)喷枪8、脱水除雾层冲洗喷嘴均为独立的整体设备,配备有独立的控制系统和必要的水源、气源过滤器、压力、流量检测控制元件。
[0104] 工作操作可设为中央控制和现场手动控制模式,主要调节控制喷枪入口水压和气压(一般调节水压),从而获得满意的流量、液滴粒径及完成设定的冲洗程序。
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CN106244767B (zh) * | 2015-09-04 | 2018-08-07 | 江苏博际喷雾系统股份有限公司 | 一种转炉一次烟气可调环缝洗涤脱水除雾一体塔 |
CN105771515B (zh) * | 2016-04-29 | 2019-02-05 | 武汉天空蓝环保科技有限公司 | 旋汇团聚塔及其团聚除尘方法 |
CN105797526B (zh) * | 2016-05-13 | 2018-05-04 | 上海龙净环保科技工程有限公司 | 适用于脱硫除尘吸收塔的高效耦合除尘器及除尘方法 |
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CN106621659A (zh) * | 2016-11-30 | 2017-05-10 | 韦永秀 | 一种适用于锅炉的湿法喷淋除尘器 |
WO2019071705A1 (zh) * | 2017-10-13 | 2019-04-18 | 山东佩森环保科技股份有限公司 | 船舶尾气洗涤塔 |
CN107754529A (zh) * | 2017-11-07 | 2018-03-06 | 成都恒力达科技有限公司 | 一种基于水旋装置的循环式空气净化设备 |
CN108499318B (zh) * | 2018-04-04 | 2020-10-13 | 丛伟 | 分径式洗涤塔 |
CN108837639B (zh) * | 2018-07-03 | 2020-11-17 | 昆明理工大学 | 一种用于甲醇裂解反应的多级涡流电磁超细粉尘烟气处理器 |
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CN201543367U (zh) * | 2009-11-21 | 2010-08-11 | 罗忠凯 | 湿式烟气脱硫除尘装置 |
CN202191835U (zh) * | 2011-07-21 | 2012-04-18 | 杨培灿 | 麻石喷淋脱硫设备 |
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