CN105056671B - 一种湿式脱硫塔脱硫除尘除雾节水工艺及其装置 - Google Patents
一种湿式脱硫塔脱硫除尘除雾节水工艺及其装置 Download PDFInfo
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- CN105056671B CN105056671B CN201510436126.8A CN201510436126A CN105056671B CN 105056671 B CN105056671 B CN 105056671B CN 201510436126 A CN201510436126 A CN 201510436126A CN 105056671 B CN105056671 B CN 105056671B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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- 241000196324 Embryophyta Species 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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- 230000015572 biosynthetic process Effects 0.000 description 3
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- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances 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O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N Sulfur trioxide Chemical compound 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Abstract
一种湿式脱硫塔脱硫除尘除雾节水工艺及其装置，涉及废气净化领域，解决湿式脱硫出现“石膏雨”的问题以及采用湿式静电除尘成本太高的问题，包括撞击冷却室、凝并室和细颗粒滤清单元，所述撞击冷却室的上开口处通过喉道与凝并室的下开口处连接，细颗粒滤清单元固定在凝并室的顶部；所述撞击冷却室内靠近下开口处的中心位置处还设有雾化喷嘴，所述雾化喷嘴的开口朝上雾化喷嘴通过管路与外部的供水设备相连。本发明造价低，安装简单，使用寿命长，无结垢堵塞风险，解决了“石膏雨”问题，分离的烟气中的水可通过管路回收至脱硫系统中，分离出来的水可用于脱硫系统，基本实现脱硫系统零补水。
Description
一种湿式脱硫塔脱硫除尘除雾节水工艺及其装置
技术领域
[0001] 本发明涉及废气净化领域，具体设计一种湿式脱硫塔除尘除雾节水装置，适用于 湿法脱硫系统中，脱硫塔后饱和烟气的进一步除尘除雾，并回收饱和烟气中所携带的的游 离水和部分水蒸气。
背景技术
[0002]我国是一个燃煤大国，燃煤产生的二氧化硫、氮氧化物和粉尘给我国的大气环境 造成了严重的污染，烟气脱硫脱硝除尘装置为改善我国的大气环境发挥了重要的作用。 [0003]目前我国的脱硝装置主要以SCR工艺为主、以SNCR为辅的技术路线;除尘装置以电 除尘器、布袋除尘器、电袋复合为主、以湿式电除尘器及其他除尘器为辅的技术路线;脱硫 装置主要以湿法为主、一半干法、千法为辅的技术路线。
[0004]随着我国环保排放要求的日益严格，许多地方要求烟气排放中的二氧化硫浓度小 于35mg/Nm3，粉尘浓度小于20mg/Nm3，有些地方甚至提出了 5mg/Nm3的要求。许多电厂采用了 “湿式脱硫塔+湿式电除尘器”的配置方式，以满足超低排放的要求。但湿式电除尘器投资 高、占地面积大、运行费用也非常高，性价比很差，特别是对于我国这样一个处于发展中、并 且以燃煤为主的国家来说，更难于承受。实际上，西方发达国家电厂也极少采用湿式电除尘 器，仅在燃烧高硫煤、三氧化硫排放浓度高、烟气带色严重的场合使用。
[0005] 湿法脱硫容易带来的另一个问题是“烟囱雨”问题，烟囱雨呈酸性，含有粉尘、石 膏、石灰石及溶解盐等物质，给电厂周边带来新的环境问题。
[0006]此外，我国是一个严重缺水的国家，特别是西北、华北以及内蒙古地区。而西北、内 蒙古等地煤炭资源丰富，新老电厂众多，进一步加剧了当地的水荒问题。
发明内容
[0007]针对现有技术存在的不足，本发明的目的之一是提供一种低成本高效率湿式脱硫 塔除尘除雾节水的工艺;本发明的目的之二是提供该工艺所需的装置。
[0008] 为实现上述目的，本发明采用如下技术方案实现：
[0009] —种湿式脱硫塔脱硫除尘除雾节水工艺，其特征是，在脱硫后的脱硫塔内或烟道 内安装有除尘除雾节水装置，脱硫后的烟气进入除尘除雾节水装置进行净化，包括以下步 骤：
[0010] 1)喷淋，脱硫后的烟气首先进入除尘除雾节水装置的撞击冷却室，撞击冷却室内 的雾化喷嘴对脱硫后的烟气进行持续性喷淋，烟气中的细微颗粒与从除尘除雾节水装置内 喷出的雾滴发生强烈碰撞，水汽开始在细微颗粒表面凝聚，并使细微颗粒直径变大，形成含 有小颗粒的烟气；
[0011] 2)压缩，含有中等颗粒的烟气经过除尘除雾节水装置的喉道时，烟气中中等颗粒 之间的空间进一步压缩，增大了微细颗粒(粉尘与粉尘之间、粉尘与雾滴之间、液滴与液滴 之间）的碰撞几率，微细颗粒直径继续增大，形成含有中等颗粒的烟气；
[0012] 3)凝并，含有中等颗粒的烟气进一步进入除尘除雾节水装置的凝并室，在凝并室， 烟气速度降低，温度也开始下降，压力开始回升，烟气中微细颗粒直径进一步增大，形成含 有大颗粒的烟气；
[0013] 4)分离，最后含有大颗粒的烟气进入除尘除雾节水装置的细颗粒滤清单元，通过 离心力将大颗粒与气体分离，从而排出合格烟气，分离后的液体通过管路回收至脱硫塔内。 [00M] —种湿式脱硫塔脱硫除尘除雾节水装置，其特征是，包括撞击冷却室、凝并室和细 颗粒滤清单元，所述撞击冷却室的上开口处通过喉道与凝并室的下开口处连接，细颗粒滤 清单元固定在凝并室的顶部;所述撞击冷却室内靠近下开口处的中心位置处还设有雾化喷 嘴，所述雾化喷嘴的开口朝上雾化喷嘴通过管路与外部的供水设备相连。
[0015] 所述撞击冷却室呈球形，球形直径为150mm〜1200mm。
[0016] 所述撞击冷却室呈椭圆形，长短径比为丨.8:丨〜4.5:!。
[0017]所述雾化喷嘴为超广角单流体或双流体喷嘴，雾化角度为130 °〜170 °。
[0018]所述凝并室为拉法尔喷管型面，扩散角为4 °〜10 °。
[0019] 所述喉道为喇叭状，下口小上口大，长为5〇〜15〇〇mm，扩散角为〇°〜8°。
[0020]所述细颗粒滤清单元由带一定型面的涡扇叶片构成，叶片数量为3〜36片，叶片和 叶片之间带疏水槽。
[0021]与现有技术相比，本发明的效果为:造价低，安装简单，可通过螺栓或焊接方式安 装于脱硫后的脱硫塔内或烟道内，装置整体无运动部件，使用寿命长，维护费用低(8年之内 免维护），具有自洁性能，可利用收集的气液进行清洗，无结垢堵塞风险，解决了 “石膏雨”问 题，分离的烟气中的水可通过管路回收至脱硫系统中，分离出来的水可用于脱硫系统，基本 实现脱硫系统零补水。
附图说明
[0022]图1为除尘除雾节水装置总体结构示意图。
[0023]图2为细颗粒分离单元结构示意图。
[0024]图中，1撞击冷却室，2雾化喷嘴，3喉道，4凝并室，5细颗粒滤清单元，51涡扇叶片， 52疏水槽。
具体实施方式
[0025] 下面结合附图，对本发明所解决的技术问题、技术方案和实施效果作进一步详细 说明。此说明仅用于解释本发明，并非用于限定本发明。
[0026] 如图1、2所示，经湿式脱硫塔脱硫后的烟气进入除尘除雾节水装置，首先通过撞击 冷却室，撞击冷却室下方设有雾化喷嘴，雾化喷嘴为超广角单流体或双流体喷嘴，雾化角度 为130°〜170°，有利于液滴和细颗粒物之间的碰撞脱除，雾化喷嘴通过管路与供水设备相 连。烟气中的微细粉尘和液滴与从雾化喷嘴喷出的雾滴发生强烈碰撞，水汽开始在粉尘颗 粒表面凝聚并长大。撞击冷却室呈球形或椭圆形，球形直径为150mm〜1200mm，椭圆形时长 短径比为1.8:1〜4.5:1，这样可以增加细颗粒物之间碰撞的概率，同时也有利于细颗粒物 之间的凝聚长大。雾化喷嘴持续性喷出雾滴，以便可以与持续经过的烟气进行碰撞，使粉尘 颗粒凝聚，细微颗粒形成小颗粒。当喷雾后的烟气流经喉道时，微细粉尘和液滴之间的空间 进一步压缩，增大了微细颗粒(粉尘与粉尘之间、粉尘与雾滴之间、液滴与液滴之间）的碰撞 几率，微细颗粒直径继续增大，形成中等颗粒，所述喉道为喇叭状，下口小上口大，长为50〜 1500mm，扩散角为0°〜8°，既方便压缩烟气，又便于与凝并室连接。含有中等颗粒的烟气进 一步进入凝并室，所述凝并室为拉法尔喷管型面，扩散角为4°〜1〇°，烟气速度降低，温度也 开始下降，压力开始回升，烟气中微细颗粒直径进一步增大，形成大颗粒。最后烟气进入细 颗粒滤清单元，所述细颗粒滤清单元由带一定型面的涡扇叶片构成，叶片数量为3〜36片， 叶片和叶片之间带疏水槽，涡扇叶片自身不运动，依靠辐射角，当烟气气流冲击到叶片时涡 扇叶片自动产生运动，在离心力的作用，烟气中的微细颗粒(包括粉尘、液滴)被分离出来， 分离出来的水可以回收至脱硫系统中，深度净化后的烟气最终排至烟囱。在深度净化过程 中，由于温度的降低，烟气饱和含湿量降低，烟气中的饱和蒸汽部分析出。
[0027]以某台6〇万KW机组脱硫为例，采用除尘除雾节水装置后，烟气中的粉尘排放浓度 由12〇mg/Nm3降至3〇mg/Nm3，液滴浓度由5〇tng/Nm3降低至8mg/Nm3，从烟气中回收水约50 t/h， 彻底解决了石膏雨问题，脱硫系统基本实现了零补水。
[0028]又以某台3〇万KW机组脱硫为例，采用除尘除雾节水装置后，烟气中的粉尘排放浓 度由3〇mg/Nm3降至8mg/Nm3，液滴浓度由3〇mg/Nm3降低至7mg/Nm3，从烟气中回收水约3〇t/h， 彻底解决了石膏雨问题，脱硫系统实现了零补水。 _9]賴明并不限于上述实施方式，在不背离本发麵实质内容_况下，本领域技 术人员可以想到的任何变形、改进、替换均落入本发明的范围。
Claims (2)
1.一种湿式脱硫塔脱硫除尘除雾节水工艺，其特征是，在脱硫后的脱硫塔内或烟道内 安装有除尘除雾节水装置，脱硫后的烟气进入除尘除雾节水装置进行净化，包括以下步骤： 1) 喷淋，脱硫后的烟气首先进入除尘除雾节水装置的撞击冷却室，撞击冷却室内的雾 化喷嘴对脱硫后的烟气进行持续性喷淋，烟气中的细微颗粒与从除尘除雾节水装置内喷出 的雾滴发生强烈碰撞，水汽开始在细微颗粒表面凝聚，并使细微颗粒直径变大，形成含有小 颗粒的烟气； 2) 压缩，含有中等颗粒的烟气经过除尘除雾节水装置的喉道时，烟气中中等颗粒之间 的空间进一步压缩，增大了微细颗粒，即粉尘与粉尘之间、粉尘与雾滴之间或液滴与液滴之 间的碰撞几率，微细颗粒直径继续增大，形成含有中等颗粒的烟气； 3) 凝并，含有中等颗粒的烟气进一步进入除尘除雾节水装置的凝并室，在凝并室，烟气 速度降低，温度也开始下降，压力开始回升，烟气中微细颗粒直径进一步增大，形成含有大 颗粒的烟气； 4) 分离，最后含有大颗粒的烟气进入除尘除雾节水装置的细颗粒滤清单元，通过离心 力将大颗粒与气体分离，从而排出合格烟气，分离后的液体通过管路回收至脱硫塔内； 所述的除尘除雾节水装置包括撞击冷却室、凝并室和细颗粒滤清单元，所述撞击冷却 室的上开口处通过喉道与凝并室的下开口处连接，细颗粒滤清单元固定在凝并室的顶部； 所述撞击冷却室内靠近下开口处的中心位置处还设有雾化喷嘴，所述雾化喷嘴的开口朝上 雾化喷嘴通过管路与外部的供水设备相连，所述撞击冷却室呈球形，球形直径为150mm〜 1200mm； 所述雾化喷嘴为超广角单流体或双流体喷嘴，雾化角度为130°〜170°，所述凝并室为 拉法尔喷管型面，扩散角为4°〜10°，所述喉道为喇叭状，下口小上口大，长为50〜1500mtn， 扩散角为0°〜8°，所述细颗粒滤清单元由带一定型面的涡扇叶片构成，叶片数量为3〜36 片，叶片和叶片之间带疏水槽。
2.如权利要求1所述的一种湿式脱硫塔脱硫除尘除雾节水工艺，其特征是，所述撞击冷 却室呈椭圆形，长短径比为1.8:1〜4.5:1。
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