CN105964405A - 一种促进湿式电除尘器脱除pm2.5的装置及方法 - Google Patents
一种促进湿式电除尘器脱除pm2.5的装置及方法 Download PDFInfo
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- CN105964405A CN105964405A CN201610375177.9A CN201610375177A CN105964405A CN 105964405 A CN105964405 A CN 105964405A CN 201610375177 A CN201610375177 A CN 201610375177A CN 105964405 A CN105964405 A CN 105964405A
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- 238000003915 air pollution Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Classifications
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- 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
- B03C3/02—Plant or installations having external electricity supply
- B03C3/16—Plant or installations having external electricity supply wet type
-
- 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
- B03C3/01—Pretreatment of the gases prior to electrostatic precipitation
- B03C3/014—Addition of water; Heat exchange, e.g. by condensation
-
- 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
- B03C3/34—Constructional details or accessories or operation thereof
-
- 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
- B03C3/34—Constructional details or accessories or operation thereof
- B03C3/74—Cleaning the electrodes
- B03C3/78—Cleaning the electrodes by washing
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water, or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Abstract
本发明公开了一种促进湿式电除尘器脱除PM2.5的装置及方法，具体是通过给湿式电除尘器的喷淋水在进入喷嘴前设置换热器来降低水温，使得收尘极内壁附近温度降低，提高了PM2.5的热泳力脱除性能，同时使得烟气温度降低，过饱和度增大，促进了过饱和水汽在PM2.5表面凝结与PM2.5长大，进一步提高了湿式电除尘器的脱除性能；其装置由涡流热膜换热器、湿式电除尘器主体、冷却夹层、废液处理装置、循环泵等组成。本发明通过设置换热器对湿式电除尘器的喷淋水进行了有效冷却，提高了烟气与收尘极内壁面的温差，增强了PM2.5的热泳力脱除效果，同时增大了烟气过饱和度，有利于水汽在颗粒物与壁面实现相变凝结易于脱除。
Description
技术领域
[0001] 本发明设计一种湿法脱硫后烟气高效除尘的装置及方法，属于大气污染控制技术领域。二.背景技术
[0002] 目前，PM2.5污染已成为我国突出的大气环境问题，是导致大气能见度降低、酸雨、 阴霾天气和全球气候变化等重大环境问题的重要因素。燃煤是引起我国大气环境中PM2.5含量增加的主要原因。为应对日益严重的大气污染现状，2011年出台的《火电厂大气污染物排放标准》设定了火电厂烟尘30mg/m3的排放限值；2014年9月，国内火电企业提出了“超低排放”；2015年12月，环保部、发改委、国家能源局联合印发了《全面实施燃煤电厂超低排放和节能改造工作方案》，规定了我国东、中、西部超低排放完成的期限。
[0003] 对于烟尘颗粒物的脱除设备，主要以常规电除尘器、袋式除尘器、电袋复合式除尘器为主。其中电除尘器具有除尘效率高、应用范围广、使用寿命长、维修成本低的优点，是最常见的燃煤电厂除尘设备。但其对低温高湿烟气条件适应性不好，对空气动力学直径小于 2.5wii的PM2.5细颗粒物脱除效率较低，也不能有效脱除烟气中S03。多数电厂会在其下游布置湿法脱硫装置与湿式电除尘装置。湿法脱硫装置能去除大多数烟气中的硫，同时去除部分烟气细颗粒物，下游的湿式电除尘装置能去除大部分细颗粒物、S03酸雾、脱硫浆液滴及部分重金属污染物，实现了多种污染物协同脱除。然而，常规湿式电除尘装置对于0.lMi〜1 Mi的亚微米级细颗粒物脱除效率并不高，分析其原因，主要是因为此粒径区域细颗粒既不能有效场荷电，也不能有效扩散荷电，综合荷电能力较差，故而脱除效率不高。三.发明内容
[0004] 发明目的:本发明的目的在于克服目前湿电技术对PM2.5的脱除存在穿透窗口的不足，提供一种促进湿式电除尘器脱除PM2.5的装置及方法，能有效提高0.lMi〜lwii的亚微米级细颗粒物的脱除效率，同时能有效促进湿法脱硫后多种污染物协同脱除。
[0005] 技术方案:一种促进湿式电除尘器脱除PM2.5的方法，烟气在湿法脱硫塔后进入湿式电除尘器主体，烟气自下向上流动，在从顶上自上而下喷淋的收尘极板清洗水和冷却夹层中冷却水的共同作用下，湿式电除尘器主体中的收尘极板内壁温度降低，同时烟气温度降低，过饱和度增大，过饱和水汽在PM2.5表面凝结与PM2.5长大，烟气中的PM2.5被吸附去除， 处理后的烟气由上部排出；收尘极板清洗水清洗收尘极板内壁后由下方的灰斗收集，进入废液处理装置，处理后的清液再流入涡流热膜换热器换热降温作为循环水;冷却水也由收尘极板下方的集液槽收集后流入涡流热膜换热器换热降温作为循环水;涡流热膜换热器换热降温后的循环水进入湿式电除尘装置一路作为收尘极板清洗水使用，另一路作为冷却夹层的冷却水使用。
[0006] 涡流热膜换热器的冷却水进水为自来水或冷却塔冷却水，冷却水进水水温在15°C 〜25。。。
[0007] 涡流热膜换热器的循环水的进水温度和经涡流热膜换热器换热后的出水温度之间的温差彡10 °C。
[0008] 烟气入口温度45〜55°C，相对湿度95 %左右，体积流量为350〜400m3/h，出口温度相比进口下降3〜5°C。
[0009] 涡流热膜换热器的冷却水出水进入冷却塔降温。
[0010] 用于所述的促进湿式电除尘器脱除PM2.5的方法的装置，主要由湿式电除尘器和涡流热膜换热器组成；湿式电除尘器包括湿式电除尘器主体，湿式电除尘器主体包括外层的冷却夹层和内层的除尘极板和阴极线;在湿式电除尘器主体顶部设有二级喷淋管路和冷却夹层进水管路，与涡流热膜换热器的循环水出口管路连接;在湿式电除尘器主体的底部设有废液处理装置进液管路和冷却夹层出水管路，废液处理装置进液管路与废液处理装置连接，废液处理装置和冷却夹层出水管路经循环栗与涡流热膜换热器的循环水进口连接;涡流热膜换热器的顶部冷却水进水口与自来水进水管路和冷却塔冷却水进水管路连接，涡流热膜换热器的上部与循环水出口管路连接，涡流热膜换热器的底部冷却水出口与冷却塔回水管路连接，涡流热膜换热器下部的循环水入口与循环栗连接。
[0011] 所述的湿式电除尘器的收尘极板包括正多边形管、圆型管、卧式极板中的任一种。
[0012] 所述的收尘极板材质包括金属、导电玻璃钢、柔性纤维中的任一种。
[0013] 有益效果:
[0014] (1)本发明将湿式电除尘器主体与涡流热膜换热器结合，由于这种换热器与普通换热器相比具有很高的传热系数，能使喷淋循环水在流经换热器后温度下降l〇°C以上，有效降低了收尘极内壁附近的温度，提高了 PM2.5的热泳力脱除性能，同时使得烟气温度降低， 过饱和度增大，促进了过饱和水汽在PM2.5表面凝结与PM2.5长大，进一步提高了湿式电除尘器的脱除性能。
[0015] (2)涡流热膜换热器的冷却介质选用冷却塔冷却水和自来水相结合的方式，一方面，水是工业生产过程最常用的换热介质，同时具有换热能力强与廉价易得的优点；另一方面，在不同环境温度下冷却塔冷却水水温有较大差别，通过控制阀门流量与自来水相结合可以得到相对稳定的温度，有利于换热器稳定运行，同时冷却水在流经换热器后循环进入冷却塔，使得整套系统尽可能节约能耗。
[0016] (3)整套装置的结构简单，只需要另设置一套换热装置并连接相关管路，改造简单，投资运行费用低，并且效果显著。通过对相关阀门进一步改造还可以实现计算机控制系统的运行，更加方便直观，有效提高了工作效率。四、 附图说明
[0017] 图1是本发明的装置结构示意图[〇〇18]图中:1-自来水进水管路;2-冷却塔冷却水进水管路;3-涡流热膜换热器;4-冷却塔回水管路;5-循环栗;6-循环水出口管路;7-二级喷淋管路;8-冷却夹层进水管路;9-冷却夹层；10-湿式电除尘器主体；11-废液处理装置进液管路；12-冷却夹层出水管路；13-废液处理装置;14-冷却塔五、 具体实施方式
[0019]下面结合附图1与具体实施方式，对本发明作详细说明:
[0020] 一种促进湿式电除尘器脱除PM2.5的方法，烟气在湿法脱硫塔后进入湿式电除尘器主体10，烟气自下向上流动，在从顶上自上而下喷淋的收尘极板清洗水和冷却夹层中冷却水的共同作用下，湿式电除尘器主体中的收尘极板内壁温度降低，同时烟气温度降低，过饱和度增大，过饱和水汽在PM2.5表面凝结，PM2.5长大，烟气中的PM2.5荷电更充分并被收尘极板吸附去除，处理后的烟气由上部排出；收尘极板清洗水清洗收尘极板内壁后由下方的灰斗收集，进入废液处理装置13，处理后的清液再流入涡流热膜换热器3换热降温作为循环水；冷却水也由收尘极板下方的集液槽收集后流入涡流热膜换热器3换热降温作为循环水;涡流热膜换热器3换热降温后的循环水进入湿式电除尘装置一路作为收尘极板清洗水使用，另一路作为冷却夹层9的冷却水使用。
[0021 ]涡流热膜换热器3的冷却水进水为自来水或冷却塔冷却水，冷却水进水水温在15Γ〜25Γ。
[0022]涡流热膜换热器3的循环水的进水温度和经涡流热膜换热器3换热后的出水温度之间的温差彡10 °C。
[0023]用于所述的促进湿式电除尘器脱除PM2.5的方法的装置，主要由湿式电除尘器和涡流热膜换热器3组成;湿式电除尘器包括湿式电除尘器主体10，湿式电除尘器主体10包括外层的冷却夹层9和内层的除尘极板和阴极线;在湿式电除尘器主体10顶部设有二级喷淋管路7和冷却夹层进水管路8，与涡流热膜换热器3的循环水出口管路6连接;在湿式电除尘器主体10的底部设有废液处理装置进液管路11和冷却夹层出水管路12，废液处理装置进液管路11与废液处理装置13连接，废液处理装置13和冷却夹层出水管路12经循环栗5与涡流热膜换热器3的循环水进口连接;涡流热膜换热器3的顶部冷却水进水口与自来水进水管路I和冷却塔冷却水进水管路2连接，涡流热膜换热器3的上部与循环水出口管路连接，涡流热膜换热器3的底部冷却水出口与冷却塔回水管路4连接，涡流热膜换热器3下部的循环水入口与循环栗5连接。
[0024]优选地，所述涡流热膜换热器冷却介质为冷却塔冷却水或自来水，进水管路上有阀门控制流量大小。
[0025]优选地，所述涡流热膜换热器内的冷却介质经过换热升温后重新流入冷却塔冷却，冷却介质为自来水时也可作为冷却塔补充水使用。
[0026]优选地，所述湿式电除尘装置上方设置喷淋管路，管路供水来自经涡流热膜换热器降温后的循环水，喷淋管路分为两支，一支作为收尘极板清洗水由下方的喷嘴向四周喷出，另一支作为收尘极板冷却夹层冷却水进水管路。根据湿式电除尘装置具体布置，这两支管路均可以设置若干支，管路上有阀门控制流量大小。
[0027]优选地，所述湿式电除尘装置收尘极形式不固定，可以为正多边形管、圆型管、臣卜式极板等;材质不固定，可以为金属、导电玻璃钢、柔性纤维等。
[0028]优选地，所述湿式电除尘装置下方设置废液回收管路，清洗水清洗收尘极板内壁后由下方的灰斗收集，再进入废液处理装置，处理后的清液再经循环栗流入涡流热膜换热器;冷却夹层中的冷却水在收尘极板下方由集液槽收集后也经循环栗流入涡流热膜换热器。喷淋水与夹层冷却水实现了循环利用，在提高湿电性能的同时有效控制了水耗与能耗。
[0029] —种促进湿式电除尘器脱除PM2.5的方法，包含如下步骤:湿式电除尘器主体旁设置涡流热膜换热器，使用自来水或冷却塔冷却水作为冷却介质对湿式电除尘器循环喷淋水换热降温，冷却介质经换热后再流回冷却塔冷却降温，循环喷淋水经过换热降温后由湿式电除尘装置上方的喷淋管路分为两支，一支作为收尘极板清洗水由下方的喷嘴向四周喷出，另一支作为收尘极板冷却夹层冷却水进水管路，在二者的共同作用下，使得收尘极内壁附近温度降低，有效提高了 PM2.5的热泳力脱除性能，同时使得烟气温度降低，过饱和度增大，促进了过饱和水汽在PM2.5表面凝结与PM2.5长大，进一步提高了湿式电除尘器的脱除性能。湿式电除尘装置下方设置废液回收管路，清洗水清洗收尘极板内壁后由下方的灰斗收集，再进入废液处理装置，处理后的清液再经循环栗流入涡流热膜换热器;冷却夹层中的冷却水在收尘极板下方由集液槽收集后也经循环栗流入涡流热膜换热器。
[0030] 实施例
[0031] 本发明促进湿式电除尘器脱除PM2.5的装置包括:涡流热膜换热器3、冷却塔回水管路4、进水管路1和2、多支喷淋管路、冷却夹层9、湿式电除尘器主体10、废液回收管路11和 12、废液处理装置13、循环栗5。
[0032] 涡流热膜换热器3采用普利龙公司生产的WMH型涡流热膜换热器，竖直布置在湿式电除尘器主体10的旁边，自来水进水管路1和冷却塔冷却水进水管路2都打开，温度计测得自来水水温19°C，冷却水水温25°C，通过流量计与阀门保持二者流量都控制在500kg/h。循环栗出口测得循环水温38°C，经涡流热膜换热器3换热后测得循环水温降为26°C。湿式电除尘器主体10采用实验室单管式装置，阳极管截面为正六边形，采用导电玻璃钢，阴极线采用铅锑合金。烟气由实验室全自动燃煤锅炉产生，在湿法脱硫塔后进入湿式电除尘器主体10， 烟气自下向上流动，测得入口温度45°C，相对湿度95 %，体积流量为380m3/h。在装置上方， 设置单个二级喷淋管路7与单个冷却夹层进水管路8,冷却夹层9连续进水，流量控制在 200kg/h，喷淋喷嘴间歇喷淋，间隔时间为4小时。废液处理装置13包括碱液池、沉淀池、混合池等部分。[〇〇33] 一种利用如上所述的促进湿式电除尘器脱除PM2.5的装置进行促进PM2.5的脱除的方法，所述方法包括以下步骤:
[0034]湿式电除尘器主体10旁设置涡流热膜换热器3,使用自来水或冷却塔冷却水1和2 作为冷却介质对湿式电除尘器循环喷淋水换热降温，冷却介质经换热后再由冷却塔回水管路4流回冷却塔14冷却降温，循环喷淋水经过换热降温后由湿式电除尘装置上方的喷淋管路6分为两支，一支作为收尘极板清洗水由下方的喷嘴向四周喷出，由二级喷淋管路7实现； 另一支作为收尘极板冷却夹层9冷却水进水管路8,在二者的共同作用下，使得收尘极内壁附近温度降低，有效提高了PM2.5的热泳力脱除性能，同时使得烟气温度降低，过饱和度增大，促进了过饱和水汽在PM2.5表面凝结与PM2.5长大，进一步提高了湿式电除尘器的脱除性能。湿式电除尘装置下方设置废液回收管路，清洗水清洗收尘极板内壁后由下方的灰斗收集，通过废液处理装置进水管路11进入废液处理装置13,处理后的清液再经循环栗5流入涡流热膜换热器3;冷却夹层中的冷却水在收尘极板下方由集液槽收集后由冷却夹层出水管路12经循环栗5流入涡流热膜换热器3。[〇〇35]所述促进湿式电除尘器脱除PM2.5的装置的总尘脱除效率可达95%，PM2.5脱除效率可达82%，出口烟尘浓度低于5mg/m3。
[0036] 对比例
[0037]其余同实施例，仅去掉涡流热膜换热器3，不设置冷却夹层9。
[0038]所述湿式电除尘装置的总尘脱除效率为91 %，PM2.5脱除效率为76%，出口烟尘浓度低于10mg/m3。
[0039]最后说明的是，以上所述仅是本发明的优选实施方式。本领域技术人员对本发明可以做适当变形，这些变形均包含在本申请权利要求所限定的范围内。
Claims (8)
1.一种促进湿式电除尘器脱除PM2.5的方法，其特征在于，烟气在湿法脱硫塔后进入湿式电除尘器主体(10)，烟气自下向上流动，在从顶上自上而下喷淋的收尘极板清洗水和冷却夹层中冷却水的共同作用下，湿式电除尘器主体中的收尘极板内壁温度降低，同时烟气温度降低，过饱和度增大，过饱和水汽在PM2.5表面凝结，PM2.5长大，烟气中的PM2.5荷电更充分并被收尘极板吸附去除，处理后的烟气由上部排出；收尘极板清洗水清洗收尘极板内壁后由下方的灰斗收集，进入废液处理装置(13)，处理后的清液再流入涡流热膜换热器(3)换热降温作为循环水;冷却水也由收尘极板下方的集液槽收集后流入涡流热膜换热器(3)换热降温作为循环水；涡流热膜换热器(3)换热降温后的循环水进入湿式电除尘装置一路作为收尘极板清洗水使用，另一路作为冷却夹层(9)的冷却水使用。
2.如权利要求1所述的促进湿式电除尘器脱除PM2.5的方法，其特征在于，涡流热膜换热器(3)的冷却水进水为自来水或冷却塔(14)冷却水，冷却水进水水温在15 °C〜25 °C。
3.如权利要求1所述的促进湿式电除尘器脱除PM2.5的方法，其特征在于，涡流热膜换热器(3)的循环水的进水温度和经涡流热膜换热器(3)换热后的出水温度之间的温差多10°C。
4.如权利要求1所述的促进湿式电除尘器脱除PM2.5的方法，其特征在于，烟气入口温度45〜55°C，相对湿度95%左右，体积流量为350〜400m3/h，出口温度相比进口下降3〜5°C。
5.如权利要求1所述的促进湿式电除尘器脱除PM2.5的方法，其特征在于，涡流热膜换热器(3)的冷却水出水进入冷却塔(14)降温。
6.用于权利要求1〜5任一所述的促进湿式电除尘器脱除PM2.5的方法的装置，包括湿式电除尘器，其特征在于，主要由湿式电除尘器和涡流热膜换热器(3)组成;湿式电除尘器包括湿式电除尘器主体(10)，湿式电除尘器主体(10)包括外层的冷却夹层(9)和内层的除尘极板和阴极线;在湿式电除尘器主体(10)顶部设有二级喷淋管路(7)和冷却夹层进水管路(8)，与涡流热膜换热器(3)的循环水出口管路(6)连接;在湿式电除尘器主体(10)的底部设有废液处理装置进液管路(11)和冷却夹层出水管路(12)，废液处理装置进液管路(11)与废液处理装置(13)连接，废液处理装置(13)和冷却夹层出水管路(12)经循环栗(5)与涡流热膜换热器(3)的循环水进口连接;涡流热膜换热器(3)的顶部冷却水进水口与自来水进水管路(I)和冷却塔冷却水进水管路(2)连接，涡流热膜换热器(3)的上部与循环水出口管路连接，涡流热膜换热器(3)的底部冷却水出口与冷却塔回水管路(4)连接，涡流热膜换热器(3)下部的循环水入口与循环栗(5)连接。
7.如权利要求6所述的用于促进湿式电除尘器脱除PM2.5的方法的装置，其特征在于，所述的湿式电除尘器的收尘极板包括正多边形管、圆型管、卧式极板中的任一种。
8.如权利要求6所述的用于促进湿式电除尘器脱除PM2.5的方法的装置，其特征在于，所述的收尘极板材质包括金属、导电玻璃钢、柔性纤维中的任一种。
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