CN206604327U - 一种焚烧尾气除尘及硫回收系统 - Google Patents

一种焚烧尾气除尘及硫回收系统 Download PDF

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CN206604327U
CN206604327U CN201720099815.9U CN201720099815U CN206604327U CN 206604327 U CN206604327 U CN 206604327U CN 201720099815 U CN201720099815 U CN 201720099815U CN 206604327 U CN206604327 U CN 206604327U
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liquid
sulfur
outlet
gas
bearing
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马良
沈其松
刘安林
贾虹
何梦雅
王依谋
付鹏波
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Shanghai Zhejiang Chemical Technology Co Ltd
East China University of Science and Technology
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Shanghai Zhejiang Chemical Technology Co Ltd
East China University of Science and Technology
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Abstract

本实用新型公开了一种焚烧尾气除尘及硫回收系统,其包括吸附单元和脱附‑再生单元,所述吸附单元包括旋流喷射吸附器、气液分离器、碱液缓冲罐和吸附液泵;所述脱附‑再生单元包括过滤器、含硫液贮存罐、含硫液泵、脱附反应器和催化剂再生器。含尘含硫的焚烧尾气进入所述旋流喷射吸附器后可切向高速旋转形成超重力场,持续切割径向喷入的流线型吸附液,烟气和吸附液之间的传质得到强化,吸附液对粉尘和二氧化硫的吸附和反应效率大大提高。所述旋流喷射吸附器可同时进行除尘和脱硫,结构更加简单、占地面积大大减小、成本低且易于装配维修。

Description

一种焚烧尾气除尘及硫回收系统
[0001] 本实用新型申请要求名称为“一种高效硫化氢气体吸收装置”,申请日是2016年9 月21日,申请号是201610494578.6的实用新型,作为本实用新型中旋流喷射吸附器结构的 优先权。
技术领域
[0002]本实用新型属于石油化工与环保领域,涉及一种焚烧尾气除尘及硫回收系统。
背景技术
[0003] 我国大气污染物排放量巨大。据统计,我国so2年排放量超过2000万吨,烟尘排放 量超过1200万吨,居世界首位。S〇2是酸雨的前体物之一,人体吸入后对眼及呼吸道粘膜有 强烈的刺激作用,烟尘的直接排空使雾霾天气日益严重。
[0004] 研究发现,氨液对二氧化硫有较好的吸收效果,同时吸收产生的副产物为硫酸铵 可作为化肥用于农业生产,不但可以给电厂带来经济效益,弥补烟气污染控制费用支出,还 能实现二氧化硫的土壤和生物固定。
[0005]目前常用的除尘脱硫方法,是将脱硫与除尘两种工艺分开进行的。使得工艺流程 较为复杂,设备台数较多,操作难度较大,占地空间大,前期投资高,转化速度慢,副产物多, 不适用于小规模的气体处理装置。 实用新型内容
[0006] 因此,针对现有技术中的焚烧尾气的脱硫与除尘设备结构复杂、占地面积大、成本 高的技术问题,本实用新型的目的在于提供一种结构简单、占地面积小的脱硫与除尘同时 进行的焚烧尾气除尘及硫回收系统。
[0007] 本实用新型的焚烧尾气除尘及硫回收系统包括:
[0008]吸附单元,所述吸附单元包括旋流喷射吸附器、气液分离器、碱液缓冲罐和吸附液 栗,所述旋流喷射吸附器上部为旋流圆筒体,所述旋流圆筒体顶部设有切向接入的烟气入 口;所述旋流圆筒体内部沿着中心轴线设有一排气套管,所述排气套管顶端作为含液烟气 出口伸出所述旋流喷射吸附器,所述含液烟气出口与所述气液分离器的入口接通;所述旋 流圆筒体侧壁外设有圆柱形外夹套,所述圆柱形外夹套与所述旋流筒体外壁连接构成水力 喷射雾化室,所述旋流圆筒体侧壁上均匀开有小孔,所述圆柱形外夹套上端设有一个碱液 入口,所述碱液入口与所述碱液缓冲罐出口接通;所述旋流喷射吸附器底部设有含硫含尘 液出口;所述吸附液泵安装在所述碱液入口和所述碱液缓冲罐出口之间;所述气液分离器 的气体出口排空,所述气液分离器的液体出口与所述碱液缓冲罐入口接通;
[0009]脱附-再生单元,所述脱附-再生单元包括过滤器、含硫液贮存罐、含硫液栗、脱附 反应器和催化剂再生器,所述过滤器、所述含硫液贮存罐、所述含硫液栗和所述脱附反应器 依次连接在所述含硫含尘液出口的下游,所述脱附反应器侧壁设有含硫液入口和催化剂入 口,所述脱附反应器顶部设有硫磺出口,所述脱附反应器底部设有脱附反应物出口,所述催 化剂再生器侧壁设有脱附反应物入口、空气入口和催化剂出口,所述催化剂再生器底部设 有废液出口,所述脱附反应物出口与所述脱附反应物入口接通,所述催化剂出口与所述催 化剂入口接通。
[0010] 较佳的,所述吸附液泵下游、所述含硫液栗下游和所述含液烟气出口下游分别设 有调节阀,分别用于调节碱液进入所述旋流喷射吸附器的流量、含硫吸附液进入脱附反应 器的流量以及含液烟气进入所述气液分离器的流量,以此保证吸附液的用量适中能够对烟 气进行充分的除尘和脱硫同时避免用量过大而浪费,调整所述气压分离器和所述脱附反应 器的工作负荷。
[0011] 较佳的,所述排气套管侧壁外设有圆柱形内夹套,所述圆柱形内夹套与所述排气 套管侧壁连接也构成水力喷射雾化室,所述圆柱形内夹套外层均匀开有小孔;所述圆柱形 内夹套上端也设有一个碱液入口。
[0012] 较佳的,所述小孔孔径为〇. 5〜5mm。
[0013]较佳的,所述的旋流喷射吸附器为单级,或者为多级串连和/或并联。
[0014] 较佳的,所述气液分离器为气液聚结分离器。
[0015] 使用所述的焚烧尾气除尘及硫回收系统进行焚烧尾气的处理过程包括:
[0016] (a)焚烧尾气中粉尘、二氧化硫的吸附分离:含尘含硫的焚烧烟气降温后进入所述 旋流喷射吸附器,同时所述碱液贮存罐中的碱液作为吸附液经所述吸附液泵送入所述旋流 喷射吸附器,含尘含硫的烟气从所述旋流喷射吸附器入口高速切向进入,碱液从所述旋流 圆筒体上的小孔径向喷入,径向喷入的流线型吸附液被切向高速旋转的烟气持续切割,形 成无数吸附液雾滴;吸附液雾滴吸附聚并烟气中的粉尘颗粒,同时与烟气中的二氧化硫快 速反应将二氧化硫从烟气中分离出来,含尘含硫的吸附液在离心力的作用下沿着所述旋流 喷射吸附器的边壁流下自所述含硫液出口流出再进入所述过滤器;含少量吸附液的气体从 所述旋流喷射吸附器的顶部流出进入所述气液分离器,聚结回收的吸附液流回碱液贮存 罐,净化后的气体排入大气;
[0017] (b)产物脱附:含尘含硫的吸附液经所述过滤器过滤后粉尘被去除,含硫的吸附液 经所述含硫液泵送至所述脱附反应器中,所述脱附反应器中利用金属离子催化剂脱附出产 物硫,金属离子催化剂被还原,产物硫从所述脱附反应器顶部离开,送入后续设备,分离回 收单质硫,脱附反应流出物从所述脱附反应器底部流出;
[0018] (c)催化剂再生:脱附反应流出物同空气一起进入所述催化剂再生器,所述催化剂 再生器中的多酚物质与空气中的氧气结合生成醌,醌将金属离子催化剂氧化复活,恢复氧 化脱硫能力,由所述催化剂再生器顶部催化剂出口离开,进入所述脱附反应器,完成工艺的 脱硫一再生循环。
[0019]较佳的,所述的碱液为液氨、氢氧化钠溶液、氢氧化钾溶液或碳酸钠溶液。
[0020]较佳的,所述金属离子催化剂为离子型表面活性物质,可以采用市售产品。
[0021] 较佳的,通入的焚烧烟气的流量为50000〜200000Nm3/h,优选100000〜130000Nm3/ h;初始温度为6〇〜l6〇°C,优选7〇〜80°C;压力为3000〜7000Pa,优选5000Pa。
[0022]本实用新型的有益效果在于:
[0023] 1、本实用新型的焚烧尾气除尘及硫回收系统中,所述旋流喷射吸附器中利用了超 重力场强化传质的原理,即含尘含硫的焚烧尾气进入所述旋流喷射吸附器后切向高速旋转 形成超重力场,可持续切割径向喷入的流线型吸附液,烟气和吸附液之间的传质得到强化, 吸附液对粉尘和二氧化硫的吸附和反应效率大大提高。而且所述旋流喷射吸附器同时进行 除尘和脱硫,相比于传统的除尘和脱硫分开的组合设备,结构更加简单、占地面积大大减 小、成本低且易于装配维修。
[0024] 2、烟气中的粉尘和二氧化硫被吸附液洗涤、吸附、反应后,含少量吸附液的气体应 该所述气液分离器聚结后净化气体排入大气,聚结的碱液流回所述碱液1C存罐重新利用。 而含尘含硫吸附液经过所述过滤器后进入所述脱附反应器,在催化剂的作用下富集出单质 硫,与此同时,含有失活的催化剂的脱附反应流出物(溶液)进入所述催化剂再生器,在氧气 的作用下,催化剂复活后再次进入所述脱附反应器,如此循环,不仅可以高效的实现硫的回 收,而且金属离子催化剂可重复利用,有效降低生产成本。
附图说明
[0025]图1为本实用新型的焚烧尾气除尘及硫回收系统的示意图;
[0026] 图2为本实用新型的旋流喷射吸附器的示意图。
[0027] 附图标记
[0028]气液分离器1、风机2、焚烧炉3、碱液缓冲罐4、吸附液泵5、喷射吸附器6、过滤器7、 含硫液贮存罐8、含硫液泵9、脱附反应器10、催化剂再生器11。
具体实施方式
[0029]以下结合具体实施例,对本实用新型作进一步说明。应理解,以下实施例仅用于说 明本实用新型而非用于限定本实用新型的范围。
[0030] 实施例1
[0031]图1所示为本实用新型一较佳实施例的焚烧尾气除尘及硫回收系统,其包括连接 在焚烧炉3和风机2下游的吸附单元和脱附-再生单元。
[0032]吸附单元包括旋流喷射吸附器6、气液分离器1、碱液缓冲罐4和吸附液栗5,本实用 新型中旋流喷射吸附器结构,可参见名称为“一种高效硫化氢气体吸收装置”,申请日是 2016年9月21日,申请号是201610494578.6的实用新型。如图2所示,旋流喷射吸附器6上部 为旋流圆筒体,旋流圆筒体顶部设有切向接入的烟气入口,烟气入口与风机2的出口接通; 旋流圆筒体内部沿着中心轴线设有排气套管,排气套管顶端作为含液烟气出口伸出旋流喷 射吸附器,含液烟气出口与气液分离器1的入口接通;旋流圆筒体侧壁外设有圆柱形外夹 套,圆柱形外夹套与旋流筒体外壁连接构成水力喷射雾化室,旋流圆筒体侧壁上均匀开有 小孔,圆柱形外夹套上端设有一个碱液入口,碱液入口与碱液缓冲罐出口接通;旋流喷射吸 附器6底部设有含硫含尘液出口;吸附液泵5安装在旋流喷射吸附器6的碱液入口和碱液缓 冲罐4的出口之间;气液分离器的丨气体出口与排空管道接通,气液分离器丨的液体出口与碱 液缓冲罐4入口接通。
[0033] 脱附-再生单元包括过滤器7、含硫液贮存罐8、含硫液栗9、脱附反应器10和催化剂 再生器11,过滤器7、含硫液贮存罐8、含硫液泵9和脱附反应器10依次连接在旋流喷射吸附 器6的含硫含尘液出口下游,脱附反应器10侧壁设有含硫液入口和催化剂入口,脱附反应器 10顶部设有硫磺出口,脱附反应器10底部设有脱附反应物出口,催化剂再生器^侧壁设有 脱附反应物入口、空气入口和催化剂出口,催化剂再生器11底部设有废液出口,其中,脱附 反应物出口与脱附反应物入口接通,催化剂出口与催化剂入口接通。
[0034]较佳的,吸附液泵5下游、含硫液泵9下游以及旋流喷射吸附器6的含液烟气出口下 游分别设有调节阀。
[0035]较佳的,该系统中还可增设多个旋流喷射吸附器,可以是串联、并联,还可以是串 联和并联相结合,可根据烟气中含硫气体的含量选择。
[0036]实施例1技术效果
[0037]某在石化公司的2#催化装置焚烧C0焚烧锅炉烟气的处理中,通过本实用新型的焚 烧尾气除尘及硫回收系统,对烟气进行中的催化剂粉尘、S02进行去除回收,其具体运作过 程及效果描述如下:
[0038]在某石化公司的催化装置焚烧CO焚烧锅炉烟气的处理中,对烟气进行中的进行除 尘和硫回收处理,物料性质及相关参数为:
[0039] 1、物料性质及相关参数
[0040]催化裂化C0焚烧锅炉烟气的流量为l28761Nm3/h,初始温度为160°C,压力为 5000Pa,NOx为350mg/Nm3,S02为 1500mg/Nm3,粉尘颗粒物的浓度为200mg/Nm3,H2〇为 10.1 %。 [0041] 2、处理过程
[0042]吸附(除尘和脱硫):含尘含二氧化硫的焚烧尾气(烟气)降温后进入旋流喷射吸附 器6,同时碱液贮存罐4中的碱液(液氨)作为吸附液经吸附液泵5送入旋流喷射吸附器6。含 二氧化硫烟气从旋流喷射吸附器6顶部的烟气入口高速切向进入,碱液(液氨)从旋流圆筒 体上的小孔径向喷入;径向喷入的流线型吸附液被切向高速旋转的烟气持续切割,形成无 数吸附液雾滴;一方面,吸附液雾滴吸附聚并烟气中的粉尘颗粒,在离心力的作用下,含尘 液滴沿旋流喷射吸附器的边壁流下至底部碱液出口,经过滤器7后溶液中的粉尘被去除。另 一方面,碱液雾滴与烟气中的二氧化硫快速反应,经吸收后富含硫的吸附液从旋流喷射吸 附器的底部流出,经过滤器后流入含硫吸附液缓冲罐;含少量吸附液的气体从旋流喷射吸 附器6的顶部流出进入气液分离器1,聚结回收的吸附液流入碱液贮存罐4,净化后的气体排 入大气。
[0043]脱附:含硫液经含硫液栗9抽送至脱附反应器10中,脱附反应器10中利用金属离子 催化剂脱附出产物硫,金属离子催化剂被还原,产物硫从脱附反应器10顶部离开,送入后续 设备,分离回收单质硫;脱附反应流出物从脱附反应器10底部流出。
[0044]催化剂再生:脱附反应流出物同空气一起进入催化剂再生器11,催化剂再生器H 中的多酚物质与空气中的氧气结合生成醌,醌将金属离子催化剂氧化复活,恢复氧化脱硫 能力,由催化剂再生器11顶部溢流口离开,进入脱附反应器10,完成工艺的脱硫一再生循 环。
[0045] 3、处理结果分析
[0046]通过使用本法实用新型的焚烧尾气除尘及硫回收系统处理,烟气中的S02浓度由 1500mg/Nm3及以上降低至40mg/Nm3以下,脱硫总体效率在97 %以上,粉尘浓度由200mg/Nm3 及以上降低20mg/Nm3以下,粉尘的去除效率在以上,大大提高了除尘脱硫的效果与处 理量。采用可再生循环的金属离子催化剂,使硫磺单质回收率极大提高。和其他工艺及装置 相比,本实用新型的工艺及装置简化了系统,节省了成本,能产生极大的经济效益。
[0047]以上已对本实用新型创造的较佳实施例进行了具体说明,但本实用新型创造并不 限于实施例,熟悉本领域的技术人员在不违背本实用新型创新的前提下还可作出种种的等 同的变型或替换,这些等同的变型或替换均包含在本申请权利要求所限定的范围内。

Claims (5)

1.一种焚烧尾气除尘及硫回收系统,其特征在于,其包括: 吸附单元,所述吸附单元包括旋流喷射吸附器、气液分离器、碱液缓冲罐和吸附液泵, 所述旋流喷射吸附器上部为旋流圆筒体,所述旋流圆筒体顶部设有切向接入的烟气入口; 所述旋流圆筒体内部沿着中心轴线设有一排气套管,所述排气套管顶端作为含液烟气出口 伸出所述旋流喷射吸附器,所述含液烟气出口与所述气液分离器的入口接通;所述旋流圆 筒体侧壁外设有圆柱形外夹套,所述圆柱形外夹套与所述旋流筒体外壁连接构成水力喷射 雾化室,所述旋流圆筒体侧壁上均匀开有小孔,所述圆柱形外夹套上端设有一个碱液入口, 所述碱液入口与所述碱液缓冲罐出口接通;所述旋流喷射吸附器底部设有含硫含尘液出 口;所述吸附液栗安装在所述碱液入口和所述碱液缓冲罐出口之间;所述气液分离器的气 体出口排空,所述气液分离器的液体出口与所述碱液缓冲罐入口接通; 脱附-再生单元,所述脱附-再生单元包括过滤器、含硫液贮存罐、含硫液泵、脱附反应 器和催化剂再生器,所述过滤器、所述含硫液贮存罐、所述含硫液泵和所述脱附反应器依次 连接在所述含硫含尘液出口的下游,所述脱附反应器侧壁设有含硫液入口和催化剂入口, 所述脱附反应器顶部设有硫磺出口,所述脱附反应器底部设有脱附反应物出口,所述催化 剂再生器侧壁设有脱附反应物入口、空气入口和催化剂出口,所述催化剂再生器底部设有 废液出口,所述脱附反应物出口与所述脱附反应物入口接通,所述催化剂出口与所述催化 剂入口接通。
2. 如权利要求1所述的焚烧尾气除尘及硫回收系统,其特征在于,所述吸附液泵下游、 所述含硫液栗下游和所述含液烟气出口下游分别设有调节阀。
3. 如权利要求1所述的焚烧尾气除尘及硫回收系统,其特征在于,所述排气套管侧壁外 设有圆柱形内夹套,所述圆柱形内夹套与所述排气套管侧壁连接也构成水力喷射雾化室, 所述圆柱形内夹套外层均勾开有小孔;所述圆柱形内夹套上端也设有一个碱液入口。
4. 如权利要求3所述的焚烧尾气除尘及硫回收系统,其特征在于,所述小孔孔径为〇 •5 〜5mm〇
5. 如权利要求1〜4任一项所述的焚烧尾气除尘及硫回收系统,其特征在于,所述的旋 流喷射吸附器为单级,或者为多级串连和/或并联。
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