CN102961943B - 一种湿法烟气脱硫协同脱除微细颗粒的方法及装置 - Google Patents
一种湿法烟气脱硫协同脱除微细颗粒的方法及装置 Download PDFInfo
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- CN102961943B CN102961943B CN201210487767.2A CN201210487767A CN102961943B CN 102961943 B CN102961943 B CN 102961943B CN 201210487767 A CN201210487767 A CN 201210487767A CN 102961943 B CN102961943 B CN 102961943B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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Abstract
本发明提供了一种湿法烟气脱硫中微细颗粒物的脱除方法及装置，属于烟气中细颗粒物的控制技术领域，脱除方法特征在于：对湿法脱硫装置旳脱硫净烟道中进行简单改造,建立蒸汽相变区使微细颗粒凝结长大，和建立碰撞凝聚区使微细颗粒进一步凝聚长大，最后烟道除雾器对凝结长大的微细颗粒物进行有效捕捉，然后从烟道出口排出。实现所述方法的装置特征在于：吸收塔出口与脱硫净烟道进口端渐扩管连接，所述脱硫净烟道出口端与烟道出口渐缩管连接，其间沿烟气流向依次设置有烟气均布器、蒸汽喷嘴、隔板、清洗工艺水喷嘴、烟道集水口和烟道除雾器。本发明的有益效果是：通过对原设施简单改造,设备投资费用省，脱除微细颗粒效果好。
Description
技术领域
[0001] 本发明属于烟气中细颗粒物的控制技术领域，特别涉及一种湿法烟气脱硫协同脱除微细颗粒物的方法及装置。
背景技术
[0002] 在湿法烟气脱硫(WFGD)过程中，一方面，通过脱硫浆液的洗涤作用可协同脱除烟气中的颗粒物；同时，由于存在脱硫浆液雾化夹带、脱硫产物结晶析出，以及脱硫剂/微细颗粒物与烟气中的SO2等气态组分之间的复杂非均相反应过程，本身又可能会形成直径小于或等于2.5微米的PM 2 5微细颗粒物。而PM 2.5微细颗粒物，虽然粒径小，但对人体健康和大气环境质量的影响更大。2012年2月，国务院同意发布的《环境空气质量标准》中将PM2.5列为监测指标之一。但是，目前燃煤电厂常见的湿法烟气脱硫工程中对PM 2.5的处理效果往往不佳。
[0003] 依据蒸汽相变促使微细颗粒物凝结长大的机理，将蒸汽相变技术与现有燃煤锅炉湿法烟气脱硫技术相结合，可有效控制烟气中微细颗粒的排放。但是该项促进烟气脱硫微细颗粒物凝结长大技术，通常需要在现有设置烟气湿法脱硫装置中增加烟气湿度调节室和相变凝结室，然而相变室内蒸汽和含微细颗粒物烟气混合不均匀，不仅增加了设备费用，同时因不少水汽未能在微细颗粒物表面凝结，而导致微细颗粒物直接被烟气带走。
发明内容
[0004] 本发明的目的是:提供一种湿法烟气脱硫中微细颗粒物的脱除方法及装置，充分利用现有脱硫净烟道空间，应用蒸汽相变和撞击流技术促使微细颗粒物凝结长大，协同脱除湿法烟气脱硫中的微细颗粒。
[0005] 为达到上述目的，釆用的技术方案是:一种湿法烟气脱硫协同脱除微细颗粒的方法，其特征在于依次包括下述步骤:
[0006] ⑴原烟气经脱硫吸收塔湿法脱硫后，从脱硫吸收塔出口进入脱硫净烟道，经烟气均布器均布后，与注入烟道中的饱和蒸汽均匀混合，烟气达到过饱和状态，烟气中的微细颗粒凝结长大；
[0007] ⑵随后，过饱和烟气经过倾斜设置的隔板区域时，表面凝结有水膜的微细颗粒物在隔板间发生相互撞击，使微细颗粒物进一步凝结长大；
[0008] ⑶烟气经过烟道除雾器时流速控制在2〜7m/s，使烟道除雾器对凝结长大的微细颗粒物进行有效捕捉，然后从烟道出口排出。
[0009] 实现所述方法的脱除微细颗粒的装置，包括湿法烟气脱硫吸收塔，其特征在于:脱硫吸收塔出口与脱硫净烟道进口端渐扩管连接，所述脱硫净烟道出口端与烟道出口渐缩管连接，其间沿烟气流向依次设置有烟气均布器、蒸汽喷嘴、隔板、清洗工艺水喷嘴、烟道集水口和烟道除雾器；所述烟气均布器前后接口进行了等截面积拆分、接合，使烟气均匀扩充流至烟道扩大区域；所述隔板斜面与烟气流动方向夹角呈α角倾斜设置。
[0010] 所述α角在15°〜45°之间，或135°〜165°之间。
[0011] 所述倾斜设置的隔板至少3块，等斜度等距离设置。
[0012] 所述烟气均布器前后接口呈纵横交错格栅状拆分、拼合，与烟气流向垂直的每个截面拆分区域最少为4个。
[0013] 所述的湿法烟气脱硫工艺是指石灰石-石膏法、双碱法、海水法、钠碱法、氧化镁法、氨法中的任意一种。该类工艺其脱硫后烟气均具有很高的含湿度，通过布置在脱硫净烟道中的蒸汽喷嘴喷入少量的饱和蒸汽，建立起ΡΜ2.5等微细颗粒凝结长大所需的过饱和水汽环境，使烟气中微细颗粒物凝结长大。
[0014] 本发明的有益效果是:通过对湿法脱硫装置进行改进，在脱硫净烟道中建立起一个蒸汽相变区，从蒸汽喷嘴喷入少量的饱和蒸汽，建立起PM2.5等微细颗粒凝结长大所需的过饱和水汽环境，同时利用撞击流技术，在烟气与过饱和蒸汽均匀混合区域设置隔板，使过饱和烟气中的微细颗粒物在隔板间发生相互碰撞，使微细颗粒物进一步凝聚长大，最后由设置于烟道中的烟道除雾器脱除。本发明通过对湿法脱硫装置旳脱硫净烟道中进行简单改造，建立蒸汽相变区和碰撞凝并区，脱除微细颗粒效果好，不增加新的反应器，设备投资和建造费用省。
附图说明
[0015] 下面结合附图和实施案例，对本发明作进一步说明。
[0016] 图1是本发明一种湿法烟气脱硫中协同脱除微细颗粒的装置结构示意图；
[0017] 图2是图1中烟气均布器A-A向截面结构示意图；
[0018] 图3是图1中烟气均布器B-B向截面结构示意图；
[0019] 图4是图1中烟道隔板倾斜α角设置结构布置示意图；
[0020] 图5是图1中烟道隔板C-C向截面结构示意图。
[0021] 图中，1-脱硫吸收塔；2_吸收剂入口 ；3-吸收剂循环泵；4_原烟气入口 ；5_喷淋层；6_塔内除雾器清洗工艺水喷嘴；7_塔内除雾器；8_脱硫净烟道；9_烟气均布器；10_蒸汽喷嘴；11_隔板；12-烟道除雾器清洗工艺水喷嘴；13-烟道集水口 ；14_烟道除雾器；15-烟道出口。
具体实施方式
[0022] 图1为本发明一种湿法烟气脱硫协同脱除微细颗粒的装置结构示意图，如图所示，本装置包括湿法烟气脱硫吸收塔1，其特征在于:脱硫吸收塔I出口与脱硫净烟道8进口端渐扩管连接，所述脱硫净烟道8出口端与烟道出口 15渐缩管连接，其间沿烟气流向依次设置有烟气均布器9、蒸汽喷嘴10、隔板11、清洗工艺水喷嘴12、烟道集水口 13和烟道除雾器14 ;所述烟气均布器9前后接口进行了等截面积拆分、接合，使烟气均匀扩充流至烟道扩大区域；所述隔板斜面与烟气流动方向夹角呈α角倾斜设置。
[0023] 原烟气从脱硫吸收塔I的烟气入口 4进入脱硫塔I的SO2吸收区II，烟气中的SO2被脱硫吸收塔I喷淋层5喷淋出的脱硫吸收剂吸收，并在塔底反应区I内被氧化，脱硫吸收剂是从反应区I底部吸收剂入口 2加入的，经吸收剂循环泵3泵入喷淋层，脱硫后的烟气经脱硫塔内除雾器7除雾后，经烟气均布器9进入脱硫净烟道8，与从蒸汽喷嘴10注入的饱和蒸汽均匀混合，达到过饱和状态，烟气中的微细颗粒物发生凝结长大；同时，过饱和烟气经过设置于脱硫净烟道8内的3块隔板11时，表面凝结有水膜的微细颗粒物在3块隔板11间产生撞击，微细颗粒物进一步凝结长大，凝结长大的微细颗粒物由设置于脱硫净烟道8中的烟道除雾器14捕集脱除；烟道除雾器清洗工艺水喷嘴12喷出的清洗工艺水，清洗烟道后从烟道集水口 13流出。
[0024] 图1可见所述烟气均布器9设置于脱硫吸收塔I出口与脱硫净烟道进口端渐扩管的扩大区接口间，所述烟气均布器前后接口呈纵横交错格栅状拆分、拼合。图2、图3为所述烟气均布器9两端的截面结构示意图，为使烟气能较好的均匀扩散至烟道扩大区域，所述烟气均布器9前后接口进行了等截面积拆分，接合，图2和图3所示图示其拆分区域为16个。与烟气流向垂直的每个截面拆分区域最少为4个。
[0025] 所述烟道隔板11，设置于脱硫净烟道8中净烟气与过饱和蒸汽均匀混合区域(图1)，图4和图5所示可见烟道隔板11斜置，且与烟气流动方向夹角α在15°〜45°之间，或135°〜165°之间，为增强微细颗粒物撞击效果，隔板11数量至少设置3块，材质选用为聚丙烯塑料(PP)等防腐耐蚀材料。
[0026] 所述烟道除雾器14，布置于脱硫净烟道8出口端，将烟气通过该除雾器的流速控制在2-7m/s，烟道除雾器14可采用挡板除雾器、旋流板除雾器或丝网除雾器。
[0027] 为了进一步说明本发明的系统效果，我们进行了案例设计:
[0028] 实施例1:
[0029] 以某燃煤锅炉烟气为处理对象，该烟气烟气量为1.0X105Nm3/h，原烟气烟温为118°C，脱硫塔进口烟尘质量浓度为70mg/Nm3，SO2浓度1747 mg/Nm3,以石灰石浆液为吸收齐U，净烟道烟气均布器9截面被等面积分割为16块，并设置了 3块与烟气流动方向夹角为30 °烟道隔板11，蒸汽相变区内喷入蒸汽量为0.04kg/Nm3 ;烟气经处理后，烟囱出口烟温为49°C，烟尘质量浓度为28mg/Nm3，达到《火电厂大气污染排放标准》(GB13233-2011)规定的烟尘排放浓度小于30mg/Nm3的排放标准，SO2浓度68mg/Nm3，脱硫效率为96.1%，烟气中细颗粒物浓度为1.23 X 17个/cm3。
[0030] 对比例1:
[0031] 采用实施例1所用烟气，对烟道不进行任何改造，脱硫后，出口烟气烟尘质量浓度为60mg/Nm3，未达到《火电厂大气污染排放标准》(GB13233-2011)规定的烟尘排放浓度小于30mg/Nm3的排放标准，SO2浓度70mg/Nm3，脱硫效率为96%，烟气中细颗粒物浓度为4.53 X 17 个/cm3。
[0032] 对比例2:
[0033] 采用实施例1所用烟气，在烟道建立一蒸汽相变区域，但不设置烟气均布器和烟道隔板，烟气经处理后，出口烟气烟尘质量浓度为35mg/Nm3，未达到《火电厂大气污染排放标准》(GB13233-2011)规定的烟尘排放浓度小于30mg/Nm3的排放标准，SO2浓度68mg/Nm3，脱硫效率为96.1%，烟气中细颗粒物浓度为1.94X 107个/cm3。
[0034] 实施例1与对比例I比较可见，本发明通过对脱硫净烟道8中进行简单改造，充分利用现有脱硫净烟道空间，设置烟气均布器9，建立蒸汽相变区和碰撞凝并区，应用蒸汽相变和撞击流技术促使微细颗粒物凝结长大，协同脱除湿法烟气脱硫中的微细颗粒效果好，设备投资省。所述的湿法烟气脱硫工艺是指石灰石-石膏法、双碱法、海水法、钠碱法、氧化镁法、氨法中的任意一种。该类工艺其脱硫后烟气均具有很高的含湿度，加入少量的饱和蒸汽就可以使烟气发生蒸汽相变，烟气中微细颗粒物可凝结长大，过饱和烟气中的微细颗粒物在隔板间发生相互碰撞凝并，使微细颗粒物进一步凝聚长大，最后由设置于烟道中的烟道除雾器脱除。对比例2仅在烟道建立一蒸汽相变区域，但不设置烟气均布器和烟道隔板，与实施例1对比效果稍差。
Claims (2)
1.一种湿法烟气脱硫协同脱除微细颗粒的装置，包括湿法烟气脱硫吸收塔，其特征在于:脱硫吸收塔出口与脱硫净烟道进口端渐扩管连接，所述脱硫净烟道出口端与烟道出口渐缩管连接，其间沿烟气流向依次设置有烟气均布器、蒸汽喷嘴、隔板、清洗工艺水喷嘴、烟道集水口和烟道除雾器；所述烟气均布器前后接口进行了等截面积拆分、接合，使烟气均匀扩充流至烟道扩大区域；所述隔板斜面与烟气流动方向夹角呈α角倾斜设置； 所述α角在15°〜45°之间，或135°〜165°之间； 所述倾斜设置的隔板至少3块，等斜度等距离设置； 所述烟气均布器前后接口呈纵横交错格栅状拆分、拼合，与烟气流向垂直的每个截面拆分区域最少为4个。
2.用权利要求1所述装置湿法烟气脱硫协同脱除微细颗粒的方法，其特征在于依次包括下述步骤: ⑴原烟气经脱硫吸收塔湿法脱硫后，从脱硫吸收塔出口进入脱硫净烟道，经烟气均布器均布后，与注入烟道中的饱和蒸汽均匀混合，烟气达到过饱和状态，烟气中的微细颗粒凝结长大； ⑵随后，过饱和烟气经过倾斜设置的隔板区域时，表面凝结有水膜的微细颗粒物在隔板间发生相互撞击，利用撞击流技术使微细颗粒物进一步凝结长大； ⑶烟气经过烟道除雾器时流速控制在2〜7m/s，使烟道除雾器对凝结长大的微细颗粒物进行有效捕捉，然后从烟道出口排出。
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