CN105597477A - 脱除燃煤锅炉烟气中超细颗粒物的装置及方法 - Google Patents
脱除燃煤锅炉烟气中超细颗粒物的装置及方法 Download PDFInfo
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- CN105597477A CN105597477A CN201610169515.3A CN201610169515A CN105597477A CN 105597477 A CN105597477 A CN 105597477A CN 201610169515 A CN201610169515 A CN 201610169515A CN 105597477 A CN105597477 A CN 105597477A
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- flue gas
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 68
- 239000003546 flue gas Substances 0.000 title claims abstract description 68
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound data:image/svg+xml;base64,<?xml version='1.0' encoding='iso-8859-1'?>
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- OSGAYBCDTDRGGQ-UHFFFAOYSA-L Calcium sulfate Chemical compound 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[Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- 241000731961 Juncaceae Species 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Chemical compound 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- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000008105 calcium carbonate Substances 0.000 description 1
- 229910052944 calcium sulfate Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of devices for separating particles from gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
本发明涉及脱除燃煤锅炉烟气中超细颗粒物的装置及方法,其特征在于该装置沿烟气流动方向按照工艺流程在脱硫设备之后依次设置烟气蒸汽引射器、蒸汽相变团聚室、湍流团聚室和除雾器,除雾器的出口处与静电除尘器连接;所述烟气蒸汽引射器与脱硫设备连接的一端设有烟气入口,在烟气蒸汽引射器的上部设有水蒸汽入口;所述湍流团聚室内设有扰流圆柱和扰流涡片,扰流圆柱布置在湍流团聚室的前部,在扰流圆柱后等间距错列布置若干数量的扰流涡片;所述湍流团聚室一端与蒸汽相变团聚室的出口连接,另一端与除雾器的入口连接。
Description
技术领域
[0001]本发明涉及除尘装置技术领域,具体是一种脱除燃煤锅炉烟气中超细颗粒物的装置及方法。
背景技术
[0002]煤炭资源是我国最重要的化石燃料之一,储量丰富,短时期以火电为主的能源结构不会改变,燃煤产生的含尘烟气是大气中悬浮颗粒物的主要来源之一。这些颗粒物从传统设备(静电除尘器、湿式除尘器、机械除尘器等)中飘散到大气中,对人体和大气环境有很大的危害性。我国大部分燃煤电厂都装备了高效的除尘装置,对烟尘的质量脱除效率能达至Ij99%以上,对于大于ΙΟμπι的颗粒物基本都可以除去,但是对于PMiq尤其是PM2.5这样的细颗粒物脱除效率特别低,这部分细颗粒物以数量计可达到烟气中颗粒数量总数的90%以上。以PM2.5为主的超细颗粒具有粒径小、数量多、具有很强的吸附能力,能够使重金属(As、Se、Pb、Cr等)和有机污染物(二恶英类和多环芳香烃等)富集起来,除对人体健康有严重威胁夕卜,也是导致酸雨、雾霾天气等环境问题的主要原因。
[0003]申请号为2013106676615的中国专利公开了一种协同脱除燃煤锅炉烟气超细颗粒和微量污染物的装置和方法,该方法在脱硫设备前设置有吸附剂预喷射装置、超细颗粒团聚装置、吸附剂加入装置和布袋除尘装置,在脱硫设备后依次设置有喷淋清洗装置、反应剂加入装置和湿式电除尘装置,该方法增设的设备较多,没能充分利用脱硫设备来脱除部分大颗粒和增加烟气相对湿度的有利条件,使吸附剂用量较大,成本较高,实际操作复杂,推广不易。
[0004]申请号为2015104361111的中国专利公开了一种湿式脱硫塔脱硫除尘除雾节水工艺,该工艺主要采用撞击冷却室、凝并室等装置,采用两股含尘烟气撞击的方法,阻力较大,各个设备连接繁琐,成本较高,实际操作复杂,推广不易。
发明内容
[0005]针对现有技术的不足,本发明拟解决的技术问题是,提供一种脱除燃煤锅炉烟气中超细颗粒物的装置及方法。该装置主要用于脱除燃煤烟气中的超细颗粒物,在脱硫设备后沿烟气流动方向依次连接烟气蒸汽引射器、蒸汽相变团聚室、湍流团聚室、除雾器,之后连接静电除尘器,该装置可有效脱除PM2.5等超细颗粒物,且该装置具有结构简单,操作方便,运行成本低廉等优点。
[0006]该方法采用湍流团聚协同蒸汽相变团聚的机理,在蒸汽相变团聚过程中,通过增加烟气的湿度破坏颗粒物表面的气膜,为湍流团聚创造条件;湍流团聚采用扰流构件控制烟气的湍流度,增加细颗粒物的碰撞几率,阻力损失小,多组扰流构件组合优化烟气的流场分布,有效增加细颗粒物团聚效率。通过蒸汽相变团聚和湍流团聚技术使细颗粒物粒径达到除尘器可以脱除的范围;该方法不需要对电厂已有设备做较大的变动,适应性强,运行成本低,具有实际推广应用的价值。
[0007]本发明解决所述装置技术问题采用的技术方案是,设计一种脱除燃煤锅炉烟气中超细颗粒物的装置,其特征在于该装置沿烟气流动方向按照工艺流程在脱硫设备之后依次设置烟气蒸汽引射器、蒸汽相变团聚室、湍流团聚室和除雾器,除雾器的出口处与静电除尘器连接;所述烟气蒸汽引射器与脱硫设备连接的一端设有烟气入口,在烟气蒸汽引射器的上部设有水蒸汽入口;所述湍流团聚室内设有扰流圆柱和扰流涡片,扰流圆柱布置在湍流团聚室的前部,在扰流圆柱后等间距错列布置若干数量的扰流涡片;所述湍流团聚室一端与蒸汽相变团聚室的出口连接,另一端与除雾器的入口连接。
[0008]本发明解决所述方法技术问题采用的技术方案是,设计一种脱除燃煤锅炉烟气中超细颗粒物的方法,该方法使用本发明所述的脱除燃煤锅炉烟气中超细颗粒物的装置,该方法的工艺步骤如下:
[0009] I)蒸汽相变团聚
[0010]脱硫设备处理后的烟气经过烟气入口进入烟气蒸汽引射器,根据烟气流量引射器从水蒸汽入口自动引射相应的水蒸汽流量,控制蒸汽相变团聚室内过饱和度在1.05〜1.2之间;烟气和水蒸汽充分混合后流入到蒸汽相变团聚室中,烟气中的细颗粒物在蒸汽相变团聚室内发生蒸汽相变团聚;
[0011] 2)湍流团聚
[0012]经过蒸汽相变团聚室团聚后的烟气,进入湍流团聚室中,烟气经过湍流团聚室内扰流圆柱和扰流涡片后,实现烟气中的细颗粒物的湍流团聚;
[0013] 3)除雾
[0014]烟气流经除雾器,为静电除尘器除去多余的水分;
[0015] 4)静电除尘器脱除团聚后的细颗粒物
[0016] 经过上述蒸汽相变团聚、湍流团聚之后,粒径为2〜6μπι的细颗粒由静电除尘器脱除。
[0017]与现有技术相比,本发明所述装置和方法具有以下有益效果:
[0018] I)本发明增设烟气蒸汽引射器,在蒸汽相变团聚室中创造一个使超细颗粒物凝结长大的过饱和蒸汽环境。一般脱硫后烟气的相对湿度在70%〜95%之间,根据烟气流量引射水蒸汽流量的比值关系,调节水蒸汽流量,控制烟气中水蒸汽的过饱和度在1.05〜1.2之间。在建立的过饱和水汽场中,水蒸汽凝结在细颗粒物表面,发生相变,促使颗粒运动,使细颗粒粒径变大,为湍流碰撞团聚形成较好的条件;烟气蒸汽引射器所引射的蒸汽量与燃煤锅炉负荷的变化相适应,蒸汽用量较少,易于操作。
[0019] 2)本发明在增设的湍流团聚室内部布置自行设计的扰流构件,即扰流圆柱和扰流涡片,作为纵向涡流发生器,前端布置的并联扰流圆柱可起到很好的分流作用,与后端布置的扰流涡片可以产生不同尺度的涡街,对不同粒径的颗粒物在不同区域形成选择性卷吸,增加不同颗粒物的碰撞机会,促使烟气中的细颗粒物团聚成大颗粒,来增强细颗粒物团聚的效率。
[0020] 3)本发明在湍流团聚室布置的扰流圆柱并联排列,可以很好的起到分流作用;在湍流团聚室布置的“Τ”字扰流涡片,采用相互交错布置,可以产生大小不同的涡街,促使不同的细颗粒物发生碰撞,设计结构简单,易操作。
[0021]本发明采取的颗粒团聚技术因不需要对现有除尘设备做任何改变,且对电厂固有布局改动不大,适应性强,投资、运行成本较低,脱除效率高,具有很好的应用发展前景。
附图说明
[0022]图1是本发明脱除燃煤锅炉烟气中超细颗粒物的装置一种实施例的设备组成结构示意图;
[0023]图2是本发明脱除燃煤锅炉烟气中超细颗粒物的装置一种实施例的湍流团聚室4的模型图;
[0024]图3是本发明脱除燃煤锅炉烟气中超细颗粒物的装置一种实施例的湍流团聚室中扰流涡片42的立体结构示意图;
[0025]图4是本发明脱除燃煤锅炉烟气中超细颗粒物的方法一种实施例的湍流团聚室内含尘烟气的速度矢量图;
[0026]图5是经本发明装置及方法团聚前后的颗粒数密度百分比图。
[0027]图1中:I脱硫设备、2烟气蒸汽引射器(或引射器)、3蒸汽相变团聚室、4湍流团聚室、5除雾器、6静电除尘器,21烟气入口、22水蒸汽入口、41扰流圆柱、42扰流涡片。
具体实施方式
[0028]下面结合实施例及其附图对本发明作进一步的详细说明,但并不以此作为对本申请权利要求保护范围的限定。
[0029]本发明脱除燃煤锅炉烟气中超细颗粒物的装置(简称装置,参见图1和图2)位于燃煤锅炉尾部烟道脱硫设备I之后,且位于锅炉静电除尘器6之前,沿烟气流动方向按照工艺流程在脱硫设备I之后依次设置烟气蒸汽引射器2、蒸汽相变团聚室3、湍流团聚室4和除雾器5,除雾器5的出口处与静电除尘器6连接;所述烟气蒸汽引射器2与脱硫设备I连接的一端设有烟气入口 21,在烟气蒸汽引射器2的上部设有水蒸汽入口 22;所述湍流团聚室4内设有扰流圆柱41和扰流涡片42,扰流圆柱41布置在湍流团聚室的前部,在扰流圆柱41后等间距错列布置若干数量的扰流涡片42;所述湍流团聚室4 一端与蒸汽相变团聚室3的出口连接,另一端与除雾器5的入口连接。
[0030]本发明装置的进一步特征在于所述扰流涡片42的形状为“T”字柱形(参见图3),相邻扰流涡片42的中心行间距17与湍流团聚室的宽度w满足h/w= 1:2。
[0031]本发明装置的进一步特征在于所述扰流圆柱41的数量为偶数,且并联排列,相邻扰流圆柱41的中心间距11、扰流圆柱的直径d与瑞流团聚室的宽度w的比为11: d: w = 2:1:5;第一个扰流涡片前端到扰流圆柱的中心连线的距离I2和湍流团聚室4的总长I满足12/1 = 1:8。
[0032]本发明装置的进一步特征在于所述除雾器5为板波纹式除雾器,板波纹式除雾器对聚并长大后的含尘液滴具有很好的脱除效果,有利于脱除进入静电除尘器中多余的水分。
[0033]本发明脱除燃煤锅炉烟气中超细颗粒物的方法的步骤如下:
[0034] I)蒸汽相变团聚
[0035]脱硫设备I处理后的烟气经过烟气入口 21进入烟气蒸汽引射器2,根据烟气流量引射器从水蒸汽入口 22自动引射相应的水蒸汽流量,从而控制烟气和水蒸汽的流量比例,控制蒸汽相变团聚室内过饱和度在1.05〜1.2之间;烟气和水蒸汽充分混合后流入到蒸汽相变团聚室3中,并在蒸汽相变团聚室3内发生蒸汽相变团聚。
[0036] 2)湍流团聚
[0037]经过蒸汽相变团聚室3团聚后的烟气,进入湍流团聚室4中,烟气经过湍流团聚室内扰流圆柱41和扰流涡片42后,形成一定数量的涡街,使颗粒局部富集,能有效促进颗粒湍流团聚。其中经过扰流圆柱41时,起到分流作用,扰流圆柱41和扰流涡片42,二者相互结合,产生不同尺度的涡街,形成颗粒高浓度区,增加颗粒碰撞的几率,实现烟气中的细颗粒物的湍流团聚。
[0038] 3)除雾
[0039]烟气流经除雾器5,除雾器5用于分离烟气中夹带的液滴,为静电除尘器除去多余的水分。
[0040] 4)静电除尘器脱除团聚后的细颗粒物
[0041 ] 经过上述蒸汽相变团聚、瑞流团聚之后,绝大部分颗粒粒径能达到2〜6μηι,达到静电除尘器所能脱除的范围,由静电除尘器脱除团聚后的细颗粒物。
[0042]本发明的核心思想是在静电除尘器之前通过物理和化学的作用将亚微米级的颗粒团聚生成较大粒径的粒子,使进入静电除尘设备内的粒子处于有效捕集的范围内。
[0043]本发明装置及方法适用于燃煤烟气超细颗粒物、脱硫后形成的氯化铵、碳酸钙、硫酸钙及部分重金属等污染物粒子的脱除。
[0044] 实施例1
[0045]本实施例脱除燃煤锅炉烟气中超细颗粒物的装置位于燃煤锅炉尾部烟道脱硫设备I之后,且位于锅炉静电除尘器6之前,沿烟气流动方向按照工艺流程在脱硫设备I之后依次设置烟气蒸汽引射器2、蒸汽相变团聚室3、湍流团聚室4和除雾器5,除雾器5的出口处与静电除尘器6连接;所述烟气蒸汽引射器2与脱硫设备I连接的一端设有烟气入口 21,在烟气蒸汽引射器2的上部设有水蒸汽入口 22;所述湍流团聚室4内设有扰流圆柱41和扰流涡片42,扰流圆柱41布置在湍流团聚室的前部,在扰流圆柱41后等间距错列布置若干数量的扰流涡片42;所述湍流团聚室4一端与蒸汽相变团聚室3的出口连接,另一端与除雾器5的入口连接。
[0046]本实施例中烟气由全自动燃煤锅炉产生,烟气量为90Nm3/h,经脱硫后烟气温度由160°C降至45°C,相对湿度是95%。脱硫后烟气经导管进入到烟气蒸汽引射器2,烟气流速为10m/s ;依照所调节烟气和蒸汽的比值关系,在INm3烟气注入0.08kg常压饱和蒸汽,能使烟气的过饱和度达到1.12左右。蒸汽相变团聚室3设计成近似于长方体结构,长度500mm,宽I OOmm,高90mm,后面连接瑞流团聚室4。本实例中瑞流团聚室设计成矩形通道,如图2所示,总长l = 1200mm,高h = 300mm,宽w = 300mm。在矩形通道内布置扰流圆柱和扰流涡片,扰流圆柱41的数量是2个,扰流圆柱的直径d = 60mm,两个扰流圆柱并联排列,即两个扰流圆柱的中心连线与烟气流动方向垂直,两个扰流圆柱的中心间距I1 = 120mm;扰流涡片42的形状为“T”字柱形(参见图3),“T”字柱形扰流涡片的横截面为“T”字形,包括水平段和竖直段,横截面水平段的尺寸为20mm,横截面竖直段的尺寸为40mm,“T”字柱形扰流涡片的高度是300mm,扰流涡片42的数量为7个,布置方式如图2所示,即第一、三、五列扰流涡片数量为I个,第二、四列扰流涡片数量为2个,布置时,“T”字柱形扰流涡片的水平段朝向扰流圆柱所在方向,第一列扰流涡片的前端到扰流圆柱的中心连线的距离l2=150mm;扰流涡片的中心行间距17 =150mm,中心列间距(13〜16)均相等,即 13 = 14= 15 = 16 = 110mm。
[0047]图4为湍流团聚室内含尘烟气的速度矢量图,从图中可以看出扰流圆柱起到分流作用,将烟气分为三股流体分别冲向下游扰流涡片,烟气横向冲刷扰流涡片,在扰流涡片下游形成漩涡,不同粒径的颗粒分布在漩涡的不同区域,形成不同粒径颗粒的富集区;较小粒径的颗粒由于质量小跟随涡街旋转,较大粒径的颗粒被甩出漩涡,来流烟气的颗粒不断与漩涡中颗粒相互扰动,不同粒径的颗粒团聚在一起。将扰流圆柱和扰流涡片二者有机结合,可有效增加颗粒碰撞团聚的可能性,为细颗粒物的团聚创造有利条件。
[0048]图5是经本实施例装置团聚前后颗粒数密度百分比图,由图5可知,按数量计,团聚前约95%的颗粒处于0.021μηι〜Ιμπι范围内,约5%的颗粒粒径大于Ιμπι;而细颗粒物经过蒸汽相变团聚、瑞流团聚之后,约78%的颗粒处于2〜6μηι范围内,11 %的颗粒处于0.021〜Ιμπι范围内。由此可见,本装置可明显增强细颗粒团聚效果。
[0049]本发明未述及之处适用于现有技术。
[0050]上述仅为本发明的具体实施方式,本发明的技术特征并非局限于此,任何本领域的技术人员在本发明的领域内所作的变化或修饰均应纳入本发明权利要求的保护范围之中。
Claims (5)
1.一种脱除燃煤锅炉烟气中超细颗粒物的装置,其特征在于该装置沿烟气流动方向按照工艺流程在脱硫设备之后依次设置烟气蒸汽引射器、蒸汽相变团聚室、湍流团聚室和除雾器,除雾器的出口处与静电除尘器连接;所述烟气蒸汽引射器与脱硫设备连接的一端设有烟气入口,在烟气蒸汽引射器的上部设有水蒸汽入口 ;所述湍流团聚室内设有扰流圆柱和扰流涡片,扰流圆柱布置在湍流团聚室的前部,在扰流圆柱后等间距错列布置若干数量的扰流涡片;所述湍流团聚室一端与蒸汽相变团聚室的出口连接,另一端与除雾器的入口连接。
2.根据权利要求1所述的脱除燃煤锅炉烟气中超细颗粒物的装置,其特征在于所述扰流涡片的形状为“T”字柱形。
3.根据权利要求1所述的脱除燃煤锅炉烟气中超细颗粒物的装置,其特征在于所述扰流圆柱的数量为偶数,且并联排列,相邻扰流圆柱的中心间距、扰流圆柱的直径与湍流团聚室的宽度的比为2:1:5;第一个扰流涡片前端到扰流圆柱的中心连线的距离和湍流团聚室的总长之比为1:8。
4.根据权利要求1所述的脱除燃煤锅炉烟气中超细颗粒物的装置,其特征在于所述除雾器为板波纹式除雾器。
5.—种脱除燃煤锅炉烟气中超细颗粒物的方法,该方法使用权利要求1所述的脱除燃煤锅炉烟气中超细颗粒物的装置,该方法的工艺步骤如下: 1)蒸汽相变团聚 脱硫设备处理后的烟气经过烟气入口进入烟气蒸汽引射器,根据烟气流量引射器从水蒸汽入口自动引射相应的水蒸汽流量,控制蒸汽相变团聚室内过饱和度在1.05〜1.2之间;烟气和水蒸汽充分混合后流入到蒸汽相变团聚室中,烟气中的细颗粒物在蒸汽相变团聚室内发生蒸汽相变团聚; 2)湍流团聚 经过蒸汽相变团聚室团聚后的烟气,进入湍流团聚室中,烟气经过湍流团聚室内扰流圆柱和扰流涡片后,实现烟气中的细颗粒物的湍流团聚; 3)除雾 烟气流经除雾器,为静电除尘器除去多余的水分; 4)静电除尘器脱除团聚后的细颗粒物 经过上述蒸汽相变团聚、湍流团聚之后,粒径为2〜6μπι的细颗粒由静电除尘器脱除。
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