CN113634101A - 一种炉窑烟气短流程超低排放处理工艺 - Google Patents
一种炉窑烟气短流程超低排放处理工艺 Download PDFInfo
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- CN113634101A CN113634101A CN202110850116.4A CN202110850116A CN113634101A CN 113634101 A CN113634101 A CN 113634101A CN 202110850116 A CN202110850116 A CN 202110850116A CN 113634101 A CN113634101 A CN 113634101A
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Abstract
本发明公开了一种炉窑烟气短流程超低排放处理工艺,该方法解决了现有系统工艺复杂,处理线路长,无法做到硫硝尘等多气态污染物的同步超低处理的难题;本发明通过喷淋冷却塔和电滤耦合液相催化净化装置,就能达到深度去除硫硝尘等多种气态污染物的目的,改造后的处理工艺不仅能大大缩短现有处理工艺流程,降低处理成本,实现硫硝尘等气态污染物的同步超低排放,具有很强的工业应用前景。
Description
技术领域
本发明属于烟气净化领域,具体涉及一种炉窑烟气短流程超低排放处理工艺。
背景技术
随着我国工业化和城市化的快速发展,环境问题日益突出,尤其是大气污染越来越严重,直接给人民健康、生态环境和经济发展造成了严重损失。而燃煤烟气、电炉尾气等产生的SO2、NOx、PM2.5和其他气态污染物,如氟化物,氯化物,重金属粉尘等,这些污染物对大气环境造成严重污染,因此,发展烟气同步脱硫脱硝除尘及其他气态污染物地净化技术是解决我国环境污染严重、保持经济绿色健康发展的关键任务。
目前国内炉窑烟气多采用正压袋式除尘方式,对烟气中颗粒物的净化效率较为有限,同时其中的SO2、NOx及氟化物、氯化物等有害气体无法得到有效治理的核心问题较为突出:1、目前普遍使用的袋式除尘器是通过纤维过滤除尘机理对烟气中的颗粒物进行捕集,从而实现对炉窑烟气的净化,但其净化程度较为有限,净化后的烟气中颗粒物浓度一般为50mg/m3;2、虽然已对工业冶炼企业逐步实施了烟气脱硫工程,但治理效果尚不明显,加之随着冶炼行业在冶炼过程中的木炭还原剂逐步被硅煤、油焦等替代,烟气中的SO2排放量还将进一步增加;3、现阶段部分有色冶炼企业尚未实施烟气脱硝工程,导致冶炼烟气中的NOx直接排入大气环境,根据对部分硅冶炼企业的调查发现,外排冶炼烟气中的NOx浓度均超过了100mg/m3,作为O3的前体物之一,其对环境产生的负面影响不容忽视;4、现行的烟气处理工艺流程普遍存在系统工艺复杂,处理线路长,无法做到硫硝尘氟等多气态污染物的同步超低处理等问题,在日趋严格的排放标准压力下应尽快进行升级改造。
CN202010838208.6公开的一种硅冶炼烟气的处理方法及装置,该方法利用等离子体发生器及吸收塔,实现硅冶炼烟气的多污染物同步去除,但是对于现有的处理工艺而言,该方法不仅没有缩短工艺流程,反而增加了处理成本,对于企业而言造成不小的改造负担。201210052982 .X公开了一种用于工业硅冶炼电炉的烟气净化及硅微粉回收系统,该技术方案由湿式除尘、脱硫、脱水一体化塔及湿式分选增密塔和离心喷雾干燥塔顺序排布连接组成,具有除尘脱硫脱水三大功能,可去除烟气中的粉尘和SO2排放,但未实现NOx的脱除,并且脱除的有害硫硝也没有实现资源化处置。
发明内容
针对现行的烟气处理工艺流程普遍存在系统工艺复杂,处理线路长,无法做到硫硝尘等多气态污染物的同步超低处理等问题,本发明提供了一种炉窑烟气短流程超低排放处理工艺,利用电化学协同液相催化以及电滤除尘技术相耦合,既解决了工业废气中硫硝尘等多污染物的一体化高效去除的目的,同时也缩短了现有工艺流程,减少企业运营成本。
本发明是将待处理废气由工业炉排出,经管道进入到喷淋冷却塔中,喷淋塔中喷头喷出喷淋液对烟气进行降温,并去除部分有害物质及烟尘;由喷淋冷却塔排出的气体经降温及初步预处理后进入到电滤耦合液相催化净化装置中,电滤耦合液相催化净化装置通过液相喷淋及电化学协同作用,产生强氧化物质,对烟气中的颗粒物进行荷电;烟气中的有害物质在液相吸收耦合电化学作用下氧化去除,荷电颗粒物在电场力、滤布微孔物理阻力及喷淋液作用下得到有效去除,净化后的气体由出气口排出。
所述待处理废气温度为100~1500 ℃,包括浓度为50~3000 mg/Nm3 SO2,浓度为50~3000 mg/Nm3 NOx,浓度为100~10000 mg/Nm3 颗粒物,根据处理烟气不同,烟气中还会附加有其他污染物,还包括浓度为10~1000 mg/Nm3 的H2S、氟化物、氯化氢或重金属粉尘等,气体流速为3 m/s~20 m/s。
所述喷淋冷却塔中的喷淋液为水、质量浓度10%~25%氨水溶液、质量浓度10%~30%亚硫酸氨水溶液、质量浓度10%~15% NaOH水溶液、质量浓度10%~30%Na3PO4水溶液、质量浓度5%~13%次氯酸钠水溶液中的一种或多种。
所述电滤耦合液相催化净化装置包括壳体、阳电极、阴电极、喷头,阳电极设置在壳体内,喷头设置在壳体内顶部并位于阳电极上方,阳电极是由纵筋和支撑环纵横叠交焊接而成的带有微孔的中空圆柱形笼体或者为带有微孔的中空圆柱体,纵筋、支撑环以及带有微孔的中空圆柱体由耐腐蚀的材料制得,阴电极为针状电极、双区柱状电极、中心骨刺状电极、线状电极,双区半骨刺电极、锥形栅状电极中的一种,一个以上的阴电极设置在阳电极周围,壳体内放置有吸收液,阳电极、阴电极分别与电源连接,喷淋冷却塔通过管道与壳体连通。
所述电滤耦合液相催化净化装置中的喷淋液为水、氨水、亚硫酸氨、二甲基亚砜、正己烷、正庚烷、N-甲基吡咯烷酮、N-甲基甲酰胺乙二醇苯醚、乙二醇苯醚、乙二醇、甘油、聚醚多元醇、环丁砜、四氯化碳、吡啶、DBE、液体石蜡、丙二醇苯醚、甲醇、丙醇、正丙醇、二卞基亚砜、司盘、吐温中的一种或多种。
所述阳极电极材料为碳化硅、碳纤维、铝合金、镁铝合金、氧化铜、镍铜合金、钼铬合金中的一种。
所述放电电源为高压直流电源或脉冲电源,电压为30kV~100kV,放电产生的强氧化物质主要为OH自由基、臭氧、高能等离子体等物质。
所述阳电极上带有滤布,滤布可为普通滤布,也可采用特殊滤布,如电滤布、金属滤布、表面附有催化材料具有催化功能的滤布等。
通过本发明方法处理后排出的烟气温度为10~100℃,SO2浓度为1~35 mg/Nm3,NOx浓度为1~50 mg/Nm3,颗粒物浓度为1~5 mg/Nm3。
本发明的创新点和技术效果:
1、与现有工艺流程相比,本发明能大大缩短原有的烟气处理工艺流程,且能实现硫硝尘等多污染物的一体化净化,有效的提高了传统工艺的净化效率,大大降低处理成本,具有很强的工业应用前景;
2、现行的烟气处理工艺流程普遍存在系统工艺复杂,处理线路长,无法做到硫硝尘等多污染物的同步超低处理等问题,在日趋严格的排放标准压力下应尽快进行升级改造,而本发明则能够很好的解决以上问题,响应国家环保政策的号召。
附图说明
图1为现有工艺流程示意图;
图2为本发明工艺流程示意图;
图中:1-工业炉,2-喷淋冷却塔,3-电滤耦合液相催化净化装置,4-冷却系统,5-旋风除尘器,6-布袋除尘器,7-脱硫装置。
具体实施方式
下面通过附图和实施例对本发明作进一步详细说明,但本发明保护范围不局限于所述内容。
实施例1:针对硅冶炼工厂排出的工业烟气,见图1,原处理工艺流程是烟气经工业电炉1排出后,进入冷却系统4先经过空气表冷,烟气温度由800℃降至300℃左右,此时烟气中SO2浓度为1200mg/Nm3,NOx浓度为300mg/Nm3,氟化物浓度为10mg/Nm3,颗粒物浓度为6000mg/Nm3,气体流速为15m/s;之后进入旋风除尘器5经一级旋风除尘,首先将较大颗粒物去除,此时烟气中各污染物浓度变化不大;再进入到布袋除尘器6中,布袋采用常规尼龙布袋,经处理后烟气颗粒物浓度降至200mg/Nm3,温度降至270℃左右,其他参数不变,进入到后续的脱硫装置7中;脱硫装置中喷淋液为氢氧化钙水溶液,经脱硫塔处理后的烟气排出的烟气温度为30℃,SO2浓度为35mg/Nm3,NOx浓度为200mg/Nm3,氟化物浓度为10mg/Nm3,颗粒物浓度为50mg/Nm3,气体流速为10m/s,此时的工艺流程无法达到硫硝尘超低排放的要求。
如图2所示,采用本发明方法,将硅冶炼工厂工业炉1排出的工业烟气直接通入喷淋冷却塔2,其中喷淋液为水,经喷淋冷却塔冷却后的烟气温度由800℃降为250℃,SO2浓度为1500mg/Nm3,NOx浓度为100mg/Nm3,氟化物浓度为10mg/Nm3,颗粒物浓度为3000mg/Nm3,气体流速为20m/s;排出的烟气从电滤耦合液相催化净化装置3下部的进气口进入其中,电滤耦合液相催化净化装置包括壳体、阳电极、阴电极、喷头,阳电极设置在壳体内,喷头设置在壳体内顶部并位于阳电极上方,4个阴电极设置在阳电极周围,本装置出气口与阳电极内腔连通,装置的阴电极(电晕电极)采用中心骨刺状电极,阳电极采用钼铬合金材料,由纵筋和支撑环纵横叠交焊接成的笼形件,在笼形件外部附有一层由玻璃纤维制成的滤布,电源为高压直流电源,电压为60kV;喷淋液是由以下质量百分比物质组成混合物:15%的二甲基亚砜、50%水、10%正庚烷、10%二卞基亚砜、15%的乙二醇,每吨上述混合物加入10kg司盘80和10kg吐温20,经过5h常温搅拌均匀后制得;烟气进入壳体后经过阳电极进入阳电极内并由排气口排出,通过电化学氧化以及滤布作用达到去除多种气态污染物的目的,由电滤耦合液相催化的净化装置中排出的烟气温度为50℃,SO2浓度为10mg/Nm3,NOx浓度为10mg/Nm3,氟化物浓度为1mg/Nm3颗粒物浓度为3 mg/Nm3,气体流速为10 m/s,达到超低排放的要求。
实施例2:本实施例处理对象和方法同实施例1,不同在于,喷淋冷却塔中的喷淋液为质量浓度10%的NaOH水溶液,经喷淋冷却塔处理后的气体温度由800℃降为300℃,SO2浓度为200mg/Nm3,NOx浓度为100mg/Nm3,氟化物浓度为10mg/Nm3,颗粒物浓度为2500mg/Nm3,气体流速为15m/s;排出的烟气从电滤耦合液相催化净化装置3下部的进气口进入其中,电滤耦合液相催化净化装置结构同实施例1,不同在于装置的阴极电晕电极采用针状电极,阳极采用镁铝合金,由纵筋和支撑环纵横叠交焊接成的笼形件,在笼形件外部附有一层由碳纤维制成的滤布,电源为高压直流电源,电压为30kV;喷淋液组成物及质量百分比为20%二甲基亚砜、20%正庚烷及20%正丙醇、60%水,常温搅拌2h均匀后制得喷淋液,烟气在电滤耦合液相催化净化装置中经电化学氧化以及滤布作用达到去除硫硝尘氟的目的,由电滤耦合液相催化的净化装置中排出的烟气温度为60℃,SO2浓度为5mg/Nm3,NOx浓度为5mg/Nm3,氟化物浓度为1mg/Nm3,颗粒物浓度为2mg/Nm3,气体流速为10m/s,达到超低排放的要求。
实施例3:本实施例针对电解铝烟气,目前电解铝生产以冰晶石-氧化铝熔体为电解质,以炭阳极、阴极为电极进行电解反应,在阴极上析出液态铝。在生产过程中,伴随着电化学反应,同时产生大量的烟气,其中在阳极气体中含有大量的氟化物,电解质挥发,阳极气体带走的氟化物固体颗粒,同时由于氧化铝含水0.3%-0.4%,原料中的水分以及空气中水蒸气,与固态氟化盐在高温(400-600℃)条件下发生电化学反应,生成HF气体。因此电解铝烟气的脱硫脱氟除尘显得尤为重要,也是行业难题。按照本发明方法,就能实现电解铝烟气的高效同步脱硫脱氟除尘。
烟气由电炉出发,先经过喷淋冷却塔进行喷淋冷却,其中喷淋液为质量25%的氨水溶液,经喷淋冷却塔处理后的气体温度为200℃,SO2浓度为1000mg/Nm3,NOx浓度为300mg/Nm3,氟化物浓度为100mg/Nm3,颗粒物浓度为1000mg/Nm3,气体流速为10m/s;排出的烟气从电滤耦合液相催化净化装置3下部的进气口进入其中,电滤耦合液相催化净化装置结构同实施例1,不同在于装置的阴极电晕电极采用中心针状电极,阳极采用镍铜合金,由纵筋和支撑环纵横叠交焊接成的笼形件,在笼形件外部附有一层由不锈钢金属丝编织制成的金属滤布,电源为脉冲电源,电压为50kV;喷淋液是由以下质量百分比物质组成混合物:10%的二甲基亚砜、10%的N-甲基吡咯烷酮、10%的环丁砜、70%的水,再在每吨上述混合物中加入20kg司盘80和20kg吐温20,经常温搅拌6h制得;烟气在电滤耦合液相催化的净化装置中经电化学产生的氢氧化物质氧化以及催化滤布作用下达到同步去除硫硝尘氟的目的,由电滤耦合液相催化的净化装置中排出的烟气温度为60℃,SO2浓度为1mg/Nm3,NOx浓度为1mg/Nm3,氟化物浓度为1mg/Nm3,颗粒物浓度为1mg/Nm3,达到超低排放的要求。
实施例4:本实施例针对锌冶炼烟气,该烟气主要污染物为:颗粒物浓度为200mg/cm3,其中主要为含铅等高危害重金属粉尘,SO2浓度为500mg/Nm3,NOx浓度为200mg/Nm3,氟化物浓度为100mg/Nm3,烟气中还含有一些有害的气态物质,如H2S、HCN、COS等,烟气流速为10m/s;按照本发明方法,对现有的锌冶炼烟气处理工艺进行升级,以达到短流程同步脱硫脱氟除尘的目的。
烟气由锌冶炼电炉出发,先经过喷淋冷却塔进行喷淋,其中喷淋液为水,经喷淋冷却塔处理后的气体温度为200℃,SO2浓度为400mg/Nm3,NOx浓度为150mg/Nm3,氟化物浓度为30mg/Nm3,颗粒物浓度为100mg/Nm3,气体流速为10m/s;排出的烟气从电滤耦合液相催化净化装置3下部的进气口进入其中,电滤耦合液相催化净化装置结构同实施例1,不同在于装置的阴极采用中心骨刺状电极,电极材料为不锈钢,阳极电极为带有微孔的中空碳化硅圆柱体。电源为高压直流电源,电压为80kV;喷淋液是由以下质量百分比物质组成混合物:10%N-甲基吡咯烷酮、10%乙二醇苯醚、20%环丁砜、20%二卞基亚砜、40%水,再在每吨上述混合物中加入15kg司盘80和15kg吐温20,经过6小时常温搅拌均匀后制得,烟气在电滤耦合液相催化的净化装置中经电化学产生的氢氧化物质氧化以及金属滤布作用达到同步去除硫硝尘氟的目的,由电滤耦合液相催化的净化装置中排出的烟气温度为60℃,SO2浓度为3mg/Nm3,NOx浓度为5mg/Nm3,氟化物浓度为2mg/Nm3,颗粒物浓度为5mg/Nm3,气体流速为10m/s,达到超低排放的要求。
实施例5:本实施例针对火力发电厂等燃煤锅炉烟气,以火力发电厂烟气为例,烟气主要污染物为:含颗粒物浓度为800mg/cm3,SO2浓度为2000mg/Nm3,NOx浓度为1500mg/Nm3,氟化物浓度为200mg/Nm3,氯化物浓度为100mg/Nm3,烟气流速为15m/s,气体温度为1200℃;按照本发明方法,对现有的火力发电厂烟气处理工艺进行升级,以达到短流程实现超低排放的目的。
烟气由燃煤锅炉出发,先经过喷淋冷却塔进行喷淋冷却,其中喷淋液为水溶液,经喷淋冷却塔处理后的气体温度为350℃,SO2浓度为1400mg/Nm3,NOx浓度为1300mg/Nm3,氟化物浓度为120mg/Nm3,氯化物浓度为60mg/Nm3,颗粒物浓度为600mg/Nm3,气体流速为20 m/s;排出的烟气从电滤耦合液相催化净化装置3下部的进气口进入其中,结构同实施例1,不同在于装置的阴极电及采双区半骨刺电极,电极材料为不锈钢,阳极电极为带有微孔的中空钼铬合金圆柱体,电源为高压直流电源,电压为100kV;喷淋液是由以下质量百分比物质组成混合物:10%二甲基亚砜、10%氨水、5%环丁砜、5%二卞基亚砜、10%正庚烷、10%乙二醇、50%水,再在每吨上述混合物中加入25kg司盘80和25kg吐温20,经过6小时常温搅拌均匀后制得,烟气在电滤耦合液相催化的净化装置中经电化学产生的强氧化物质氧化以及滤布作用达到同步去除硫硝尘及其他气态污染物的目的,由电滤耦合液相催化的净化装置中排出的烟气温度为40℃,SO2浓度为15 mg/Nm3,NOx浓度为8 mg/Nm3,氟化物浓度为2 mg/Nm3,氯化物浓度为1 mg/Nm3,颗粒物浓度为3 mg/Nm3,气体流速为10 m/s,达到超低排放的要求。
Claims (8)
1.一种炉窑烟气短流程超低排放处理工艺,其特征在于:待处理废气由工业炉(1)排出,经管道进入到喷淋冷却塔(2)中,喷淋塔中喷头喷出喷淋液对烟气进行降温,并去除部分有害物质及烟尘;由喷淋冷却塔排出的气体经降温及初步预处理后进入到电滤耦合液相催化净化装置(3)中,电滤耦合液相催化净化装置通过液相喷淋及电化学协同作用,产生强氧化物质,对烟气中的颗粒物进行荷电;烟气中的有害物质在液相吸收耦合电化学作用下氧化去除,荷电颗粒物在电场力、滤布微孔物理阻力及喷淋液作用下得到有效去除,净化后的气体由排气口排出。
2.根据权利要求1所述的炉窑烟气短流程超低排放处理工艺,其特征在于:待处理废气温度为100~1500℃,包括浓度为50~3000mg/Nm3 SO2,浓度为50~3000mg/Nm3 NOx,浓度为100~10000mg/Nm3 颗粒物,以及浓度为10~1000 mg/Nm3 的H2S、氟化物、氯化氢或重金属粉尘,气体流速为3m/s~20m/s。
3.根据权利要求1所述的炉窑烟气短流程超低排放处理工艺,其特征在于:喷淋冷却塔中的喷淋液为水、质量浓度10%~25%氨水溶液、质量浓度10%~30%亚硫酸氨水溶液、质量浓度10%~15% NaOH水溶液、质量浓度10%~30% Na3PO4水溶液、质量浓度5%~13%次氯酸钠水溶液中的一种或多种。
4.根据权利要求1所述的炉窑烟气短流程超低排放处理工艺,其特征在于:电滤耦合液相催化净化装置包括壳体、阳电极、阴电极、喷头,阳电极设置在壳体内,喷头设置在壳体内顶部并位于阳电极上方,阳电极是由纵筋和支撑环纵横叠交焊接而成的带有微孔的中空圆柱形笼体或者为带有微孔的中空圆柱体,纵筋、支撑环以及带有微孔的中空圆柱体由耐腐蚀的材料制得,阴电极为针状电极、双区柱状电极、中心骨刺状电极、线状电极,双区半骨刺电极、锥形栅状电极中的一种,一个以上的阴电极设置在阳电极周围,阳电极、阴电极分别与电源连接,喷淋冷却塔通过管道与壳体连通。
5.根据权利要求4所述的炉窑烟气短流程超低排放处理工艺,其特征在于:电滤耦合液相催化净化装置中的喷淋液为水、氨水、亚硫酸氨、二甲基亚砜、正己烷、正庚烷、N-甲基吡咯烷酮、N-甲基甲酰胺乙二醇苯醚、乙二醇苯醚、乙二醇、甘油、聚醚多元醇、环丁砜、四氯化碳、吡啶、DBE、液体石蜡、丙二醇苯醚、甲醇、丙醇、正丙醇、二卞基亚砜、司盘、吐温中的一种或多种。
6.根据权利要求4所述的炉窑烟气短流程超低排放处理工艺,其特征在于:阳极电极材料为碳化硅、碳纤维、铝合金、镁铝合金、氧化铜、镍铜合金、钼铬合金中的一种。
7.根据权利要求4所述的炉窑烟气短流程超低排放处理工艺,其特征在于:放电电源为高压直流电源或脉冲电源,电压为30kV~100kV。
8.根据权利要求4所述的炉窑烟气短流程超低排放处理工艺,其特征在于:阳电极上带有滤布,滤布为普通滤布、电滤布、金属滤布或涂覆有催化剂的滤布。
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