CN203437036U - 一种烧结烟气脱硫脱硝装置 - Google Patents
一种烧结烟气脱硫脱硝装置 Download PDFInfo
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- CN203437036U CN203437036U CN201320565147.6U CN201320565147U CN203437036U CN 203437036 U CN203437036 U CN 203437036U CN 201320565147 U CN201320565147 U CN 201320565147U CN 203437036 U CN203437036 U CN 203437036U
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- China
- Prior art keywords
- fluidized bed
- absorption tower
- flue gas
- bed absorption
- sintering flue
- Prior art date
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- 238000005245 sintering Methods 0.000 title claims abstract description 40
- 238000006477 desulfuration reactions Methods 0.000 title claims abstract description 30
- 230000003009 desulfurizing Effects 0.000 title claims abstract description 30
- 239000003546 flue gases Substances 0.000 claims abstract description 39
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 38
- 238000010521 absorption reactions Methods 0.000 claims abstract description 26
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 15
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- 281000120149 Gas Gas companies 0.000 abstract description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound 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[Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract 2
- 229910052791 calcium Inorganic materials 0.000 abstract 2
- 239000011575 calcium Substances 0.000 abstract 2
- 239000002594 sorbents Substances 0.000 abstract 2
- 238000005516 engineering processes Methods 0.000 description 9
- 238000000034 methods Methods 0.000 description 9
- 239000003344 environmental pollutants Substances 0.000 description 8
- 231100000719 pollutant Toxicity 0.000 description 7
- 229910000831 Steel Inorganic materials 0.000 description 6
- 239000003054 catalysts Substances 0.000 description 6
- 239000010959 steel Substances 0.000 description 6
- 239000011901 water Substances 0.000 description 6
- 229910001890 sulfur dioxide Inorganic materials 0.000 description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reactions Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitric oxide Chemical compound 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O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 2
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous Oxide Chemical compound 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[O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 2
- 229910052761 rare earth metals Inorganic materials 0.000 description 2
- 150000002910 rare earth metals Chemical class 0.000 description 2
- 239000007921 sprays Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 241001466460 Alveolata Species 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 229910002089 NOx Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound 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Abstract
Description
一种烧结烟气脱硫脱硝装置
【技术领域】
[0001] 本实用新型涉及一种废气处理装置,具体涉及一种烧结烟气脱硫脱硝装置,其用于钢铁行业烧结机尾端脱除二氧化硫和氮氧化物,属于环保设备技术领域。
【背景技术】
[0002] 钢铁行业的烟气污染物主要来自烧结烟气,其中排放的70%的二氧化硫(SO2),50%的氮氧化物(NOx)来自烧结机。国家对钢铁烧结机污染控制日益重视,即将出台的《钢铁工业大气污染物排放标准-烧结》中对SO2和NOx排放标准要求更加严格,对烧结烟气净化技术提出了更高的要求,特别对多组份复合污染物脱除技术开发更加迫切。目前我国烧结烟气污染治理技术处于起步阶段,主要技术只是针对烧结烟气中单一污染物SO2脱除,而对烧结烟气另一主要污染物NOx没有考虑。烧结机烟气NOx排放具有如下特点:N0X浓度低(100~400mg/m3),流量大(可达106m3/h、N0x排放总量高),烟气温度低(100~200。。)等特点。在燃煤锅炉中大量使用的选择催化还原脱硝技术(SCR)由于在烧结工段中无法直接获得320~400°C烟气,从而不能在烧结烟气净化中使用。另外我国大部分钢铁烧结工序场地狭小,决定了可用于燃煤锅炉烟气污染治理的长流程工艺并不适合大多数烧结机治污项目改造的。因此针对烧结烟气特点及烧结工序现状,迫切需要短流程、经济型脱硝工艺技术,以满足烧结烟气污染物综合控制的需要。
[0003]目前烧结烟气脱硫脱硝技术已经达到工业应用水平的主要是日本及韩国开发的烧结烟气脱硫脱硝技术工艺,采用活性炭固定床同时捕集粉尘、二氧化硫及二恶英,采用喷氨减排氮氧化物,然后粉尘、二氧化硫及二恶英在再生塔中400°C条件下实现分离,分离后的高二氧化硫气体被回收制硫酸,同时产生工业废水需进行处理。该工艺路线长、技术复杂、占地大,产生废水,投资大、运行成本高,不适合中国国情。
[0004] 中国发明专利200610102077.5报道了一种锅炉烟气污染物同时脱除的方法及装置,将锅炉烟气引入循环流化床反应器,在反应器中喷入富氧高活性吸收剂,将NO氧化成NO2,同时在增湿水的作用下,吸收剂吸收S02、NO2,实现同时脱硫脱硝。中国发明专利200910153849.1公开了一种用于燃煤锅炉的石灰石_石膏湿法多种污染物同时脱除装置及方法,主要通过向吸收液中添加氧化剂将烟气中难溶于水的NO氧化成较易溶于水的NO2,实现利用石灰石-石膏法同时脱除烟气中S02、NOx等污染物。目前专利技术主要针对燃煤锅炉多种污染物的脱除,尚没有用于钢铁烧结烟气S02、N0x综合脱除的技术及装置。
[0005] 因此,为解决上述技术问题,确有必要提供一种具有改良结构的烧结烟气脱硫脱硝装置,以克服现有技术中的所述缺陷。
【实用新型内容】
[0006] 为解决上述问题,本实用新型的目的在于提供一种结构简单、成本低、占地面积小且处理效果好的烧结烟气脱硫脱硝装置。
[0007] 为实现上述目的,本实用新型采取的技术方案为:一种烧结烟气脱硫脱硝装置,其包括预除尘器、GGH换热器、燃烧器、氨注入器、SCR反应器、循环流化床吸收塔、雾化喷嘴、旋风分离器、钙基吸收剂储仓、布袋除尘器以及烟® ;其中,所述预除尘器、GGH换热器、燃烧器、SCR反应器、循环流化床吸收塔、旋风分离器、布袋除尘器和烟囱依次连接;所述氨注入器连接至SCR反应器的顶部;所述钙基吸收剂储仓连接至循环流化床吸收塔的下方;所述雾化喷嘴收容于循环流化床吸收塔内。
[0008] 本实用新型的烧结烟气脱硫脱硝装置进一步设置为:所述循环流化床吸收塔的底部设有一烟气进口,烟气进口的上方从下往上依次为收缩段、喉管和扩散段;所述收缩段上设置有吸收剂入口以及循环灰入口。
[0009] 本实用新型的烧结烟气脱硫脱硝装置进一步设置为:所述循环流化床吸收塔的上部设有烟气出口,该烟气出口与旋风分离器的进口连通。
[0010] 本实用新型的烧结烟气脱硫脱硝装置进一步设置为:所述旋风分离器下端设置有两个出口,其中一出口通过输送装置与一灰仓连接,另一出口通过螺旋反料机与所述循环灰入口连接。
[0011] 本实用新型的烧结烟气脱硫脱硝装置进一步设置为:所述布袋除尘器的底部亦连接至灰仓上。
[0012] 本实用新型的烧结烟气脱硫脱硝装置还设置为:所述钙基吸收剂储仓通过一输送装置连接至吸收剂入口上。
[0013] 与现有技术相比,本实用新型具有如下有益效果:
[0014] I)本实用新型的烧结烟气脱硫脱硝装置结构简单,占地面积小,操作调节方便,投资和运行费用低;
[0015] 2)本实用新型的烧结烟气脱硫脱硝装置采用了稀土非贵金属NOx阱催化剂,脱硝反应在较低的温度下就可完成催化还原反应,仅利用烟气预热进入脱硝反应器的烟气既可达到脱硝催化还原反应温度要求`。
[0016] 3)本实用新型的烧结烟气脱硫脱硝装置的脱硫与脱硝功能独立,其在原有半干法脱硫技术的基础上,通过增加SCR反应器,实现系统的脱硝功能。两个系统独立运行,调控灵活,可根据需要实现系统脱硫与脱硝的功能。
[0017] 4)本实用新型的烧结烟气脱硫脱硝装置采用干态进料方式,避免了湿态进料方式可能带来的腐蚀、堵塞等问题,同时与浆态进料方式相比省去了制浆系统,占地面积小,投资和运行费用降低。
【附图说明】
[0018] 图1是本实用新型的烧结烟气脱硫脱硝装置的示意图。
【具体实施方式】
[0019] 请参阅说明书附图1所示,本实用新型为一种烧结烟气脱硫脱硝装置,其由预除尘器1、GGH (Gas Gas Heater)换热器2、燃烧器3、氨注入器4、SCR反应器5、循环流化床吸收塔6、雾化喷嘴7、旋风分离器15、钙基吸收剂储仓12、布袋除尘器19以及烟囱21等几部分组成。
[0020] 其中,所述预除尘器1、GGH换热器2、燃烧器3、SCR反应器5、循环流化床吸收塔6、旋风分离器15、布袋除尘器19和烟囱21依次连接;所述氨注入器4连接至SCR反应器5的顶部;所述钙基吸收剂储仓12连接至循环流化床吸收塔6的下方;所述雾化喷嘴7收容于循环流化床吸收塔6内,用于喷射雾化水。
[0021] 所述GGH换热器2用于对烧结烟气进行预热;预热后的烧结烟气在由燃烧器3进行加热,达到SCR反应的温度;氨注入器4注入氨气后,与烟气一同从上往下进入SCR反应器5进行反应,烟气中的NOx被还原成N2,达到去除NOx的目的。其中,氨气注入量与NOx摩尔比为1:1。
[0022] 所述SCR反应器5内安装有3-4层脱硝催化剂,催化剂选择稀土非贵金属NOx阱催化剂,采用蜂窝状结构,该催化剂特点可在300〜400°C左右温度下,进行氮氧化物与氨气的催化还原反应。
[0023] 所述循环流化床吸收塔6的底部设有一烟气进口 8,烧结烟气在经过SCR反应器5脱硝并进行余热回收后,由烟气进口 8进入循环流化床吸收塔6。烟气进口 8的上方采用文丘里结构11,该结构从下往上依次为收缩段、喉管和扩散段;所述收缩段上设置有吸收剂入口 9以及循环灰入口 10,所述钙基吸收剂储仓12通过一输送装置13连接至该吸收剂入口 10上,钙基吸收剂添加量与SO2的摩尔比为1.1〜2.0。于所述循环流化床吸收塔6的上部设有烟气出口 14,该烟气出口 14与旋风分离器15的进口 16连通。
[0024] 所述旋风分离器15下端设置有两个出口,其中一出口通过另一输送装置13与一灰仓20连接,另一出口通过螺旋反料机18与所述循环灰入口 10连接。所述布袋除尘器19的底部亦连接至灰仓20上。
[0025] 本实用新型的烧结烟气脱硫脱硝装置的处理工艺如下:
[0026] 步骤1,烧结烟气首先预除尘后,经燃烧器3加热达到可与氨气进行SCR反应的温度(约300〜400°C )。烟气携带由氨注入器4注入的NH3 —起从上往下进入SCR反应器5进行催化反应,使得烟气中的NOx被还原成N2,达到去除NOx的目的。
[0027] 步骤2,烟气经GGH换热器2进行换热处理回收余热,再从循环流化床吸收塔6底部进入进行下一步的脱硫反应。
[0028] 步骤3,含有SO2的烧结烟气在循环流化床吸收塔6内与分别喷入的钙基吸收剂(生石灰或熟石灰)和雾化水混合,钙基吸收剂在雾化水的作用下吸收so2。最后经布袋除尘器19除尘,实现对烧结烟气中NOx和SO2的联合脱除。
[0029] 以上的具体实施方式仅为本创作的较佳实施例,并不用以限制本创作,凡在本创作的精神及原则之内所做的任何修改、等同替换、改进等,均应包含在本创作的保护范围之内。
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