CN102059029B - 高湿烟气中细颗粒物的脱除方法及其装置 - Google Patents
高湿烟气中细颗粒物的脱除方法及其装置 Download PDFInfo
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- CN102059029B CN102059029B CN 201010557868 CN201010557868A CN102059029B CN 102059029 B CN102059029 B CN 102059029B CN 201010557868 CN201010557868 CN 201010557868 CN 201010557868 A CN201010557868 A CN 201010557868A CN 102059029 B CN102059029 B CN 102059029B
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- fine particle
- humidity
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- 239000010419 fine particle Substances 0.000 title claims abstract description 73
- 239000007789 gas Substances 0.000 title claims abstract description 27
- 239000003517 fume Substances 0.000 title abstract 11
- 238000005406 washing Methods 0.000 claims abstract description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound 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- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound 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- 230000035683 MEAN RESIDENCE TIME Effects 0.000 description 1
- BFKJFAAPBSQJPD-UHFFFAOYSA-N Tetrafluoroethylene Chemical compound 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Abstract
本发明涉及一种高湿烟气中细颗粒物的脱除方法及其装置，高湿烟气进入烟气导管，在烟气导管中注入常压饱和蒸汽与高湿烟气进行预混合后，相向进入撞击流相变室主体中，高湿烟气与常压饱和蒸汽的混合物相互撞击，在撞击流相变室主体中心形成一个高度湍动、细颗粒物浓度最高的撞击区，促进过饱和蒸汽凝结于细颗粒物表面；同时，表面凝结有水膜的细颗粒物之间发生相互碰撞凝并，使细颗粒物粒度进一步增大，凝并长大的细颗粒物由置于撞击流相变室主体上端烟气出口处的高效除雾器脱除。其装置由烟气导管、撞击流相变室主体、高效除雾器、除雾器冲洗水系统、冲洗废液贮槽组成，蒸汽喷嘴设在烟气导管内；高效除雾器设在撞击流相变室主体上端烟气出口处。
Description
高湿烟气中细颗粒物的脱除方法及其装置
技术领域
[0001] 本发明属于脱除烟气中细颗粒物的技术领域，特别涉及一种经吸收处理、半干法脱硫或湿式洗涤除尘的高湿烟气中细颗粒物的脱除方法及其装置。
背景技术
[0002] 空气动力学直径小于2.5mm的细颗粒物(PM2.5)污染已成为我国突出的大气环境问题，主要原因在于细颗粒物比表面积大，易富集各种重金属及化学致癌物质，而常规除尘技术对其难以有效捕集，造成大量细颗粒物排入大气环境。如静电除尘装置的总除尘效率虽可达99%以上，但对细颗粒物的脱除效率并不高，且随粒径减小脱除效率显著下降；湿法脱硫装置、湿式洗涤除尘装置也难以有效捕集细颗粒物，在部分湿法脱硫工艺(如氨法脱硫)中，由于无机盐气溶胶和硫酸雾滴的形成，脱硫后细颗粒物浓度反而增加。目前，细颗粒物控制技术发展的主要途径是通过物理或化学作用使细颗粒物长大成较大颗粒后加以清除，以及运用新颖合理的技术措施提高现有烟气污染物控制装置对细颗粒物的脱除性能；其中，将蒸汽相变预处理技术与现有烟气污染物治理技术结合是最有可能实现工程应用的重要途径之一。依据蒸汽相变促使细颗粒物长大的机理，利用该预调节技术，首先应建立过饱和水汽环境；因此，该技术只有与烟气水汽含量较高、烟温较低的过程结合才有实用价值。在吸收法净化气态污染物(如湿法脱硫)及湿式洗涤除尘中，高温烟气与中低温洗涤吸收液相接触，发生强烈的传热传质过程，高温烟气使部分洗涤吸收液汽化，烟气相对湿度增大并可接近或达到饱和状态，烟温可降至5(T60°C以下。在喷雾干燥、炉内喷钙尾部增湿活化等半干法烟气脱硫技术中，由于脱硫过程中需在高温烟气喷入Ca(OH)2浆液或雾化水，烟气将热量传递给浆液或雾化水滴，使之不断蒸发干燥，同时烟气温度由14(T16(TC降至5(T65°C，含湿量显著增加，脱硫后烟气相对湿度可达50-60%以上。
[0003]目前，应用蒸汽相变促进细颗粒物长大通常在一空的腔体(相变室)中进行，相变室内水汽和含细颗粒物烟气混合不均匀，导致不少水汽未能在细颗粒物表面凝结而直接由烟气带走。同时，鉴于细颗粒物凝结长大后成为外表面覆盖一层液膜的含尘雾滴，需与可脱除雾滴的除尘设备配套，如湿式除尘器、高效除雾器、旋风分离器等，其中高效除雾器是最适宜的设备之一，上述除尘设备对于粒径:T5mm以上的雾滴才有较佳的脱除效果。虽理论上，提高蒸汽添加量，可使细颗粒物凝结长大至更大的尺寸，但由于蒸汽相变潜热的释放、加入蒸汽后烟温的上升及其过高水汽过饱和度下的均相成核作用，对于PM2.5中的亚微米级微粒，单靠过饱和水汽在颗粒物表面的凝结作用，长大至3~5mm以上有一定难度，且过高的蒸汽添加量会导致能耗过大。撞击流是强化相间传递和促进混合(尤其是微观混合)最有效的方法之一，但撞击流技术在蒸汽相变促进细颗粒物长大中未见应用。
发明内容
[0004] 发明目的:本发明针对烟气经吸收处理、半干法脱硫或湿式洗涤除尘后相对湿度较高的特点，提供一种高湿烟气中细颗粒物的脱除方法及其装置，耦合应用蒸汽相变与撞击流技术促使细颗粒物凝并长大并高效脱除。
[0005] 技术方案:一种高湿烟气中细颗粒物的脱除方法，相对湿度> 50%、烟温< 70°C的含有细颗粒物的高湿烟气进入烟气导管，在烟气导管中，注入常压饱和蒸汽与高湿烟气进行预混合后，以25~40m/s的速率相向进入撞击流相变室主体中，含有细颗粒物的高湿烟气与常压饱和蒸汽的混合物相互撞击，在撞击流相变室主体中心形成一个高度湍动、细颗粒物浓度最高的撞击区，促进过饱和蒸汽凝结于细颗粒物表面；同时，表面凝结有水膜的细颗粒物之间发生相互碰撞凝并，使细颗粒物粒度进一步增大，凝并长大的细颗粒物由置于撞击流相变室主体上端烟气出口处的高效除雾器脱除。
[0006] 所述的高湿烟气是指经吸收处理、半干法脱硫或湿式洗涤除尘后的烟气。
[0007] 所述的细颗粒物是指空气动力学直径小于2.5mm的PM2 5,除原始烟气中的细颗粒物外，还包括烟气吸收洗涤中形成的液态和固态细颗粒物。
[0008] 注入常压饱和蒸汽的量以使高湿烟气的过饱和度S由S £1增至S=L 05^1.25确定。
[0009] 一种实现所述的高湿烟气中细颗粒物的脱除方法的装置，该装置由上到下依次设有净烟气出口、除雾器冲洗水系统、高效除雾器、撞击流相变室主体、冲洗水废液贮槽和冲洗水废液出口组成；烟气导管沿撞击流相变室主体的周壁呈中心对称布置，烟气导管内设有蒸汽喷嘴。
[0010] 烟气导管根据待处理高湿烟气量的大小设置为一对或二对。
[0011] 当烟气导管为二对时，烟气导管沿撞击流相变室主体的周壁的在同一横截面或者两个不同横截面水平或倾斜呈中心对称的布置。
[0012] 当在同一横截面倾斜布置时，烟气导管均向下倾斜，倾斜角度< 45°
[0013] 当在两个不同横截面倾斜布置时，上层烟气导管向下倾斜，下层烟气导管向上倾斜，倾斜角度均<45°。
[0014] 所述的高效除雾器为丝网除雾器、板波纹除雾器。
[0015] 所述的撞击流相变室主体为圆柱形或方形结构，内衬具有增进相变效果和防腐双重功效的耐蚀低表面能材料；冲洗水废液贮槽为锥形结构。
[0016] 有益效果:
[0017] (1)本发明工艺简单，只需在气态污染物吸收塔(如脱硫塔)、湿式洗涤塔出口或半干法脱硫系统的静电除尘器烟气出口增设撞击流相变室，添加少量蒸汽即可建立细颗粒物凝结长大所需的过饱和水汽条件。
[0018] (2)由于采用撞击流技术，可有效解决传统相变室中因水汽和含细颗粒物烟气混合不均匀，不少水汽未能在细颗粒物表面凝结而直接由烟气带走及其亚微米级微粒单靠蒸汽相变作用不易凝结长大至常规除尘(除雾)技术可高效脱除的粒度的缺陷。鉴于撞击流操作动力主要消耗在加速颗粒，而本发明处理的是PM2.5，动力消耗小，系统阻力不超过20(T300Pa ;除可脱除原始烟气中的细颗粒物外，还可脱除吸收洗涤中形成的细颗粒物，如硫酸雾滴、无机盐气溶胶微粒。可广泛应用于吸收法净化气态污染物(如烟气湿法)、湿式洗涤除尘、半干法脱硫等烟气污染物治理设施。
[0019] (3)利用过饱和水汽在细颗粒物表面核化凝结是促使细颗粒粒度增大的重要措施，特别适合于烟气水汽含量较高、烟温较低的过程。烟气经吸收处理、湿式洗涤除尘后，烟气相对湿度增大并可接近或达到饱和状态，烟温可降至60°C以下；在喷雾干燥、炉内喷钙尾部增湿活化等半干法烟气脱硫技术中，由于脱硫过程中需在高温烟气喷入Ca(OH)2浆液或雾化水，使脱硫后烟气相对湿度也可达50-60%以上。在上述烟气环境中只要添加少量蒸汽即可建立细颗粒物凝结长大所需的过饱和水汽条件。采用撞击流相变室，一方面，撞击区高度湍动的状态为水汽与细颗粒物的结合创造了极佳的传递与混合条件，进而增进过饱和水汽在细颗粒物表面的凝结，并可减少蒸汽在相变室内壁面上的核化凝结；同时，表面凝结有水膜的细颗粒物受反向气流的作用在撞击区内来回振荡和相互渗透，增加了其在撞击区的停留时间，并形成高浓度区，从而提高细颗粒物间相互碰撞的概率，强化团聚效应，促使其进一步碰撞凝并长大，易于被后续设备(如高效除雾器)脱除。烟气导管采用倾斜式向下布置时，可使气流撞击后偏向相变室底部方向运动，延长了水汽与细颗粒物在撞击区的平均停留时间，从而强化水汽在细颗粒物表面凝结及凝结有水膜的细颗粒物间的碰撞团聚效应。
附图说明
[0020] 图1是本发明的装置结构示意图；
[0021] 图2是在同一横截面采用一对烟气导管向下倾斜布置的示意图；
[0022] 图3是在同一横截面采用二对烟气导管水平或向下倾斜布置的示意图；
[0023] 图4为在不同横截面烟气导管水平布置的示意图；
[0024] 图5为两对 烟气导管一对向下倾斜布置，一对向上倾斜布置的示意图。
[0025] 图中:1 一烟气导管；2 —撞击流相变室主体；3—冲洗水废液贮槽；4 一蒸汽喷嘴；5 —高效除雾器；6 —除雾器冲洗水系统，α为倾斜角。
具体实施方式
[0026] 下面结合附图广5，对本发明作详细说明:
[0027] 本发明的高湿烟气中细颗粒物的脱除过程如下:经吸收处理、半干法脱硫或湿式洗涤除尘后的高湿烟气，相对湿度50%以上，烟温低于70°C，进入烟气导管1，在烟气导管I中，由蒸汽喷嘴4注入I大气压左右的常压饱和蒸汽与高湿烟气进行预混合，使烟气过饱和度S可由S £1增至S=L 05^1.25。然后，蒸汽与烟气混合物以25~40m/s的速率进入撞击流相变室主体2中，相向的含细颗粒物烟气与常压饱和蒸汽的混合物相互撞击，在中心形成一个高度湍动、细颗粒物浓度最高的撞击区，促进过饱和蒸汽凝结于细颗粒物表面；同时，表面凝结有水膜的细颗粒物受反向气流的作用在撞击区内来回振荡和相互渗透，增加其在撞击区的停留时间，并形成高浓度区，发生相互碰撞凝并，使细颗粒物粒度进一步增大、质量增加；凝并长大的细颗粒物由置于撞击流相变室主体2上部的烟气出口处的高效除雾器5脱除。并由除雾器上端的除雾器冲洗水系统6，定期对高效除雾器5冲洗，被捕集的细颗粒物随冲洗水落入冲洗水废液贮槽3，定期排出。脱除的细颗粒物是指空气动力学直径小于2.5mm的PM2.5，除原始烟气中的细颗粒物外，还包括吸收洗涤中形成的细颗粒物，如硫酸雾滴、无机盐气溶胶微粒。
[0028] 一种实现所述的高湿烟气中细颗粒物脱除方法的装置，该装置由上到下依次设有净烟气出口、除雾器冲洗水系统6、高效除雾器5、撞击流相变室主体2、冲洗水废液贮槽3和冲洗水废液出口组成；烟气导管I沿撞击流相变室主体2的周壁呈中心对称布置，烟气导管I内设有蒸汽喷嘴4。烟气导管I沿撞击流相变室主体2的周壁水平或倾斜对称布置，烟气导管数量根据处理烟气量的大小可设置一对或二对。当烟气导管为二对时，烟气导管沿撞击流相变室主体的周壁的在同一横截面或者两个不同横截面水平或倾斜呈中心对称的布置。当在同一横截面倾斜布置时，烟气导管均向下倾斜，倾斜角度<≤45°。当在两个不同横截面倾斜布置时，上层烟气导管向下倾斜，下层烟气导管向上倾斜，倾斜角度均≤45°。图1和图2中采用一对烟气导管，图3飞中采用二对烟气导管，其中，图3为沿相变室主体周壁同一横截面水平或倾斜向下对称布置，图4、图5分别为沿相变室主体的高度方向分二层水平、倾斜对称布置。蒸汽喷嘴4设在烟气导管I内。所述高效除雾器5为丝网除雾器、板波纹除雾器，优选丝网除雾器；高效除雾器上端设置除雾器冲洗水系统6，以对除雾器定期冲水洗涤。所述撞击流相变室主体2可为圆柱形或方形结构，内衬具有增进相变效果和防腐双重功效的耐蚀低表面能材料，如聚四氟乙烯、四氟乙烯乙烯基醚共聚物、氟乙烯乙烯基醚共聚物涂料等。冲洗水废液贮槽3为锥形结构，连接于撞击流相变室主体2的下端。
[0029] 以下结合具体实施例对本发明作进一步说明，但本发明不只限于此实施例。
[0030] 实施例1:[0031] 烟气由全自动燃煤锅炉产生，烟气量为150Nm3/h，采用石灰石/石膏湿法脱硫工艺，经脱硫后烟气温度由110°C降至51°C，相对湿度97%。脱硫净化湿烟气由一对烟气导管分两股进入撞击流相变室主体，相变室烟气出口处安装丝网除雾器，每Nm3烟气注入0.06kg常压饱和蒸汽，所能达到的过饱和度S约为1.22。经电称低压冲击器实时在线测量，添加蒸汽后，丝网除雾器出口细颗粒物数浓度由4.2’ IO7个/cm3降至1.37' IO7个/cm3，数浓度脱除率提高67.4%。
[0032] 实施例2:
[0033] 烟气由全自动燃煤锅炉产生，烟气量为150Nm3/h，烟气脱硫技术为喷雾干燥法，经脱硫后烟气温度由157°C降至59°C，相对湿度63%。脱硫净化湿烟气经旋风除尘器脱除粗颗粒后，分两股进入撞击流相变室主体，相变室烟气出口处安装丝网除雾器，每Nm3烟气注入
0.12kg蒸汽，所能达到的过饱和度约为1.15。经电称低压冲击器实时在线测量，添加蒸汽后，丝网除雾器出口细颗粒物数浓度由5.62r IO7个/cm3降至3.08' IO7个/cm3，数浓度脱除率提闻45.2%。
[0034] 对比例1:
[0035] 采用实施例1试验系统，但蒸汽相变室未采用撞击流技术。经电称低压冲击器实时在线测量，添加蒸汽后，丝网除雾器出口细颗粒物数浓度由4.15' IO7个/cm3降至
2.24' IO7个/cm3，数浓度脱除率仅提高46.0%。
[0036] 对比例2:
[0037] 采用实施例2试验系统，但蒸汽相变室未采用撞击流技术。经电称低压冲击器实时在线测量，添加蒸汽后，丝网除雾器出口细颗粒物数浓度由5.54' IO7个/cm3降至
3.81‘ IO7个/cm3，数浓度脱除率仅提高31.2%。
Claims (3)
1.一种高湿烟气中细颗粒物的脱除方法，其特征在于，相对湿度> 50%、烟温< 70°C的含有细颗粒物的高湿烟气进入烟气导管(I )，在烟气导管(I)中，注入常压饱和蒸汽与高湿烟气进行预混合后，以25〜40m/s的速率相向进入撞击流相变室主体(2)中，含有细颗粒物的高湿烟气与常压饱和蒸汽的混合物相互撞击，在撞击流相变室主体中心形成一个高度湍动、细颗粒物浓度最高的撞击区，促进过饱和蒸汽凝结于细颗粒物表面；同时，表面凝结有水膜的细颗粒物之间发生相互碰撞凝并，使细颗粒物粒度进一步增大，凝并长大的细颗粒物由置于撞击流相变室主体(2)上端烟气出口处的高效除雾器(5)脱除；所述的细颗粒物是指空气动力学直径小于2.5 μ m的PM2.5，除原始烟气中的细颗粒物外，还包括烟气吸收洗涤中形成的液态和固态细颗粒物。
2.根据权利要求1所述的高湿烟气中细颗粒物的脱除方法，其特征在于，所述的高湿烟气是指经吸收处理、半干法脱硫或湿式洗涤除尘后的烟气。
3.根据权利要求1所述的高湿烟气中细颗粒物的脱除方法，其特征在于，注入常压饱和蒸汽的量以使高湿烟气的过饱和度S由S < I增至S=L 05〜1.25确定。
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| CN105536423B (zh) * | 2016-01-31 | 2017-09-12 | 河北工业大学 | 燃煤锅炉烟气细颗粒物的脱除装置及工艺 |
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| JP2742562B2 (ja) * | 1988-10-11 | 1998-04-22 | 千代田化工建設株式会社 | 有毒性排ガスの燃焼処理方法 |
| JP3000109B2 (ja) * | 1990-09-20 | 2000-01-17 | 株式会社住友シチックス尼崎 | 高純度シリコン鋳塊の製造方法 |
| CN201105202Y (zh) * | 2007-09-14 | 2008-08-27 | 东南大学 | 烟气湿法脱硫中协同脱除细颗粒的装置 |
| CN101732977A (zh) * | 2010-01-20 | 2010-06-16 | 东南大学 | 燃煤烟气脱硫工艺中提高细颗粒物脱除的装置及方法 |
| CN201880450U (zh) * | 2010-11-25 | 2011-06-29 | 东南大学 | 脱除高湿烟气中细颗粒物的装置 |
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