CN108246071B - 一种可调喉口文丘里管强电离放电脱硫脱硝装置 - Google Patents
一种可调喉口文丘里管强电离放电脱硫脱硝装置 Download PDFInfo
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Abstract
本发明公开了一种可调喉口文丘里管强电离放电脱硫脱硝装置,其包括气气换热器、吸收液储存罐、旋转喷雾器、烟气混合室、可调喉口文丘里管、喷淋塔,烟气混合室设置在可调喉口文丘里管入口处,可调喉口文丘里管出口与喷淋塔连通,旋转喷雾器设置在烟气混合室入口处,吸收液储存罐通过旋转喷雾器与烟气混合室连通,气气换热器通过管道与烟气混合室连通,氧气调节室设置在气气换热器与烟气混合室之间的管道上,喷淋塔顶端的烟气出口通过气气换热器与烟囱连通,喷淋塔底部设置有吸收液排放口;该装置同时脱硫脱硝,工艺流程短,设备简单,且文丘里喉管可调,提高烟气处理效率。
Description
技术领域
本发明专利涉及大气污染控制领域,具体涉及一种可调喉口文丘里管强电离放电脱硫脱硝装置。
背景技术
脱硫脱硝一体化技术因工艺设备结构紧凑,投资和运行费用低,已成为烟气净化的发展趋势。目前,脱硫脱硝一体化技术主要有:固相吸收/再生脱硫脱硝技术,如活性炭法、CuO法等,其中吸收剂再生后,物化性能下降,影响脱硫脱硝效率;气固催化脱硫脱硝技术,如SNRB法、CFB工艺等,其脱硫率、脱硝率较低,运行稳定性较差;吸收剂喷射脱硫脱硝技术,如尿素法、干式一体化NOx/SO2技术,该技术烟气停留时间较长,且脱硫脱硝率较低,只有70%~80%;湿法烟气脱硫脱硝技术,如氯酸法、湿式络合吸收工艺等,该工艺可产生废酸,对设备腐蚀性较强;高能电子活化氧化技术,如EBA法、PPCP法等,该技术产生的平均电子能量不高,活性粒子浓度满足不了实际脱硫脱硝的需求。
强电离放电过程中能产生平均电子能量高达10eV的高能电子(5~20eV),足够烟气中的大部分O2、N2、H2O等气体分子离解电离并行成高浓度的·OH、·O、HO2·、O3等活性粒子,可快速将烟气中的SO2、NOx直接氧化成H2SO4、HNO3。但目前该技术还不够成熟,对烟气净化方面研究较少,并且无工业化应用。
发明内容
针对现有技术不足,本发明提供了一种运行稳定、高效脱硫脱硝的可调喉口文丘里管强电离放电脱硫脱硝装置;
可调喉口文丘里管强电离放电脱硫脱硝装置包括气气换热器、吸收液储存罐、旋转喷雾器、烟气混合室、可调喉口文丘里管、喷淋塔,烟气混合室设置在可调喉口文丘里管入口处,可调喉口文丘里管出口与喷淋塔连通,旋转喷雾器设置在烟气混合室入口处,吸收液储存罐通过旋转喷雾器与烟气混合室连通,气气换热器通过管道与烟气混合室连通,氧气调节室设置在气气换热器与烟气混合室之间的管道上,喷淋塔顶端的烟气出口通过气气换热器与烟囱连通,喷淋塔底部设置有吸收液排放口。
所述可调喉口文丘里管是在文丘里管喉管处设置有由2个调节阀、2个挡板、支架、一个以上的放电电极、一个以上的介质阻挡层,放电电极、介质阻挡层通过支架交替固定在喉管中心处,放电电极与电源连接,2个挡板通过调节阀相对设置在喉管管壁上的挡板槽中,喉管管壁厚50~80 mm,挡板槽深度是40~60 mm,挡板为弧形板,挡板厚度等于挡板槽深度,文丘里管管体为碳钢材料,内侧刷涂玻璃鳞片涂料,管体接地。
所述喷淋塔内设置有喷头,喷头下方设置有除雾器。
所述可调喉口文丘里管喉管内径0.5~0.8 m,喉管长度1~2 m。
所述喉管中心处放电电极为棒状或管状电极,其余放电电极为管状电极,电极表面喷涂α-Al2O3,涂层厚度0.5~1 mm。
所述介质阻挡层为表面喷涂α-Al2O3的陶瓷管、石英管、聚四氟乙烯管或聚丙烯管,涂层厚度0.5~1 mm。
所述放电电极与介质阻挡层之间的间隙为20~30 mm。
所述氧气调节室调节烟气氧含量为6~10%。
所述吸收液为水、海水或质量浓度10~20%的氨水,由旋转喷雾器雾化吸收液,其中雾状吸收液在混合烟气中体积含量为10~30%。
所述进入可调喉口文丘里管的混合烟气流量为1~3×104 m3/h。
所述放电电极供电方式为交流电,电压5~10 kV,频率6~8 kHz。
所述喷淋塔中喷淋液可采用水、钠基吸收液、氨基吸收液或海水,喷淋量为20~40m3/h;钠基吸收液为碳酸钠、碳酸氢钠、硫酸钠或亚硫酸钠等;氨基吸收液为氨水、硫酸铵或尿素等。
除尘后的烟气通过风机进入脱硫脱硝***,烟气首先经过气气换热器降温,调节氧含量后,混合气体进入烟气混合室与雾状吸收液在烟气混合室混合后,混合烟气通过可调喉口文丘里管,在介质阻挡强电离放电作用下,混合烟气发生电离,产生高浓度活性粒子(·OH、·O、HO2·、O3等),快速氧化去除SO2、NOx;处理后的烟气进入喷淋塔,在除雾器上酸雾微粒或盐颗粒被捕集,由于重力及淋洗作用流入吸收液排放口,净化后的烟气则经气气换热器升温排入烟囱;淋洗液处理后可分离出酸、铵盐类等物质,剩余淋洗液回用进入喷淋***。
本发明的有益效果在于:
(1)介质阻挡强电离放电技术对烟气进行高效脱硫脱硝,设备简单,工艺流程短;
(2)吸收液可随烟气质量、地理条件变换,且副产品能得到有效处置;
(3)文丘里管管径可调,在烟气浓度低、流速较小时,缩小喉管管径,增大混合烟气流速,提高烟气处理效率,同时喉管管径缩小导致放电间隙减小,可降低放电电压,减小设备能耗。
附图说明
图1为本发明装置结构示意图;
图2为可调喉口文丘里管部分结构示意图;
图3为可调喉口文丘里管喉管剖面图。
图4为可调喉口文丘里管喉管管径缩小结构示意图;
图5为喷淋塔结构示意图;
图中:1-风机;2-气气换热器;3-氧气调节室;4-输送管;5-吸收液储存罐;6-旋转喷雾器;7-烟气混合室;8-可调喉口文丘里管;9-喷淋塔;10-烟气出口;11-吸收液排放口;12-烟囱;13-调节阀;14-挡板;15-支架;16-挡板槽;17-放电电极;18-介质阻挡层;19-喷头;20-除雾器。
具体实施方式
下面结合具体实施方式对本发明进行详细说明,但本发明保护范围不局限于所述内容。
实施例1:如图1-5所示,可调喉口文丘里管强电离放电脱硫脱硝装置包括气气换热器2、吸收液储存罐5、旋转喷雾器6、烟气混合室7、可调喉口文丘里管8、喷淋塔9,烟气混合室7设置在可调喉口文丘里管8入口处,可调喉口文丘里管8出口与喷淋塔9连通,旋转喷雾器6设置在烟气混合室7入口处,吸收液储存罐5通过输送管4、旋转喷雾器6与烟气混合室7连通,气气换热器2通过管道与烟气混合室7连通,氧气调节室3设置在气气换热器2与烟气混合室7之间的管道上,喷淋塔9顶端的烟气出口10通过气气换热器2与烟囱12连通,喷淋塔9底部设置有吸收液排放口11,喷淋塔9内设置有喷头19,喷头下方设置有除雾器20;可调喉口文丘里管8是在文丘里管喉管处设置有由2个调节阀13、2个挡板14、支架15、2个放电电极17、2个介质阻挡层18,放电电极17、介质阻挡层18通过支架15交替固定在喉管中心处,放电电极与介质阻挡层之间的间隙为25 mm;中心处放电电极为棒状电极,其余放电电极为管状电极,电极表面喷涂α-Al2O3,涂层厚度0.5 mm;介质阻挡层18为表面喷涂α-Al2O3的陶瓷管,涂层厚度0.5 mm;放电电极与电源连接,2个挡板14通过调节阀13相对设置在喉管管壁上的挡板槽16中,喉管管壁厚50 mm,挡板槽深度是40 mm,挡板为弧形板,圆心角为140°,挡板14厚度等于挡板槽深度,文丘里管管体为碳钢材料,内侧刷涂玻璃鳞片涂料,管体接地,可调喉口文丘里管喉管内径0.6 m,喉管长度1.5 m。
除尘后的烟气(SO2 1200 mg/m3、NO 300 mg/m3)通过风机1进入气气换热器2,经气气换热器2降温后通入氧气,调节烟气氧含量为8%;吸收液采用海水,海水由输送管4输送至旋转喷雾器6,烟气与雾状海水混合,混合烟气流量为1.5×104 m3/h,其中雾状海水在混合烟气中体积含量为20%;混合烟气通过可调喉口文丘里管时,放电电压为5 kV,频率为6.5kHz(交流电),在强电离放电作用下混合烟气发生电离,喉管内产生高浓度活性粒子,快速氧化去除SO2、NOx。处理后的烟气经过喷淋塔9,液滴被除雾器20捕集,在重力及海水淋洗作用下流入吸收液排放口11,喷头19喷淋量为40 m3/h;净化后的烟气(SO2去除率大于90%、NO去除率大于90%)经气气换热器2升温排入烟囱12;淋洗液经海水稀释后,可直接排放。
实施例2:本实施例装置结构同实施例1,不同在于:可调喉口文丘里管8喉管内径0.8 m,喉管长度2 m;喉管管壁厚80 mm,挡板槽深度是60 mm,挡板为弧形板,圆心角为120°,喉管中的放电电极均为管状电极,电极表面喷涂α-Al2O3,涂层厚度1 mm;介质阻挡层18为表面喷涂α-Al2O3的聚四氟乙烯管;介质阻挡层表面喷涂α-Al2O3,涂层厚度1 mm;放电电极与所述介质阻挡层之间放电间隙为30 mm。
除尘后的烟气(SO2 2000 mg/m3、NO 300 mg/m3)通过风机1进入气气换热器2,经气气换热器2降温后通入氧气,调节烟气氧含量为9%;吸收液采用质量浓度20%的氨水,氨水由输送管4输送至旋转喷雾器6,烟气与雾状氨水混合,混合烟气流量为2×104 m3/h,其中雾状氨水在混合烟气中体积含量为10%;旋转调节阀13,使挡板14下移40 mm,文丘里管喉管直径缩小;混合烟气通过可调喉口文丘里管时,放电电压为8 kV,频率为8 kHz(交流电),在强电离放电作用下混合烟气发生电离,喉管内产生高浓度活性粒子,快速氧化去除SO2、NOx。处理后的烟气经过喷淋塔9,液滴被除雾器20捕集,在重力及硫酸铵淋洗液淋洗作用下流入吸收液排放口11,喷头19喷淋量为30 m3/h;净化后的烟气(SO2去除率大于95%、NO去除率大于90%)经气气换热器2升温排入烟囱12;淋洗液中含有硝酸铵、硫酸铵等副产品,经分离后可用作肥料,分离液即稀淋洗液可回用至喷淋塔。
实施例3:本实施例装置结构同实施例1,不同在于:可调喉口文丘里管8喉管内径0.6 m,喉管长度1 m;喉管管壁厚60 mm,挡板槽深度是50 mm,挡板为弧形板,圆心角为130°,喉管中的放电电极均为管状电极,电极表面喷涂α-Al2O3,涂层厚度0.5 mm;介质阻挡层18为表面喷涂α-Al2O3的石英管;介质阻挡层表面喷涂α-Al2O3,涂层厚度0.8 mm;放电电极与所述介质阻挡层之间放电间隙为25 mm。
除尘后的烟气(SO2 1000 mg/m3、NO 200 mg/m3)通过风机1进入气气换热器2,经气气换热器2降温后通入氧气,调节烟气氧含量为6%;吸收液采用质量浓度10%的氨水,氨水由输送管4输送至旋转喷雾器6,烟气与雾状氨水混合,混合烟气流量为3×104 m3/h,其中雾状氨水在混合烟气中体积含量为30%;旋转调节阀13,使挡板14下移30 mm,文丘里管喉管直径缩小;混合烟气通过可调喉口文丘里管时,放电电压为6 kV,频率为7 kHz(交流电),在强电离放电作用下混合烟气发生电离,喉管内产生高浓度活性粒子,快速氧化去除SO2、NOx。处理后的烟气经过喷淋塔9,液滴被除雾器20捕集,在重力及水的淋洗作用下流入吸收液排放口11,喷头19喷淋量为20 m3/h;净化后的烟气(SO2去除率大于90%、NO去除率大于90%)经气气换热器2升温排入烟囱12;淋洗液中含有硝酸铵、硫酸铵等副产品,经分离后可用作肥料,分离液即稀淋洗液可回用至喷淋塔。
以上描述了本发明的基本原理。凡依本发明权利要求范围所做的均等变化与修饰,应属本发明权利要求的涵盖范围。
Claims (8)
1.一种可调喉口文丘里管强电离放电脱硫脱硝装置,其特征在于:包括气气换热器(2)、吸收液储存罐(5)、旋转喷雾器(6)、烟气混合室(7)、可调喉口文丘里管(8)、喷淋塔(9),烟气混合室(7)设置在可调喉口文丘里管(8)入口处,可调喉口文丘里管(8)出口与喷淋塔(9)连通,旋转喷雾器(6)设置在烟气混合室(7)入口处,吸收液储存罐(5)通过旋转喷雾器(6)与烟气混合室(7)连通,气气换热器(2)通过管道与烟气混合室(7)连通,氧气调节室(3)设置在气气换热器(2)与烟气混合室(7)之间的管道上,喷淋塔(9)顶端的烟气出口(10)通过气气换热器(2)与烟囱(12)连通,喷淋塔(9)底部设置有吸收液排放口(11);
可调喉口文丘里管(8)是在文丘里管喉管处设置有2个调节阀(13)、2个挡板(14)、支架(15)、一个以上的放电电极(17)、一个以上的介质阻挡层(18),放电电极(17)、介质阻挡层(18)通过支架(15)交替固定在喉管中心,放电电极与电源连接,2个挡板(14)通过调节阀(13)相对设置在喉管管壁上的挡板槽中,喉管管壁厚50~80mm,挡板槽深度是40~60 mm,挡板为弧形板,挡板(14)厚度等于挡板槽深度,文丘里管管体为碳钢材料,内侧刷涂玻璃鳞片涂料,管体接地;
喉管中心处的放电电极为棒状或管状电极,其余放电电极为管状电极,电极表面喷涂α-Al2O3,涂层厚度0.5~1 mm;
吸收液为水、海水或质量浓度10~20%的氨水,由旋转喷雾器(6)雾化吸收液,其中雾状吸收液在混合烟气中体积含量为10~30%。
2.根据利要求1所述的可调喉口文丘里管强电离放电脱硫脱硝装置,其特征在于:喷淋塔(9)内设置喷头(19),喷头下方设置有除雾器(20)。
3.根据利要求1所述的可调喉口文丘里管强电离放电脱硫脱硝装置,其特征在于:可调喉口文丘里管(8)喉管内径0.5~0.8 m,喉管长度1~2 m。
4.根据利要求1所述的可调喉口文丘里管强电离放电脱硫脱硝装置,其特征在于:介质阻挡层(18)为表面喷涂α-Al2O3的陶瓷管、石英管、聚四氟乙烯管或聚丙烯管,涂层厚度0.5~1 mm。
5.根据利要求1所述的可调喉口文丘里管强电离放电脱硫脱硝装置,其特征在于:放电电极(17)与介质阻挡层(18)之间的间隙为20~30 mm。
6.根据利要求1所述的可调喉口文丘里管强电离放电脱硫脱硝装置,其特征在于:氧气调节室(3)调节烟气氧含量为6~10%。
7.根据利要求1所述的可调喉口文丘里管强电离放电脱硫脱硝装置,其特征在于:进入可调喉口文丘里管的混合烟气流量为1×104~3×104 m3/h。
8.根据利要求1所述的可调喉口文丘里管强电离放电脱硫脱硝装置,其特征在于:放电电极(17)供电方式为交流电,电压5~10 kV,频率6~8 kHz。
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