CN201320447Y - 脱硫脱硝一体化烟气净化装置 - Google Patents
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Abstract
本实用新型涉及一种烟气脱硫脱硝一体化净化装置，塔体设有烟气进口和净烟出口，塔内包含水洗除雾段、吸收段和氧化段；水洗除雾段包含装有除雾装置的除雾层、设有喷淋器的水喷淋层和水洗层；吸收段位于烟气进口的上方，包含上层脱硫喷淋器、下层脱硝喷淋器，所说的氧化段位于塔的下部，氧化段的底部设有与氨和空气输入口相通的喷嘴；氧化段上部抽出口通过塔外循环管路与吸收段的下层脱硝喷淋器相通，下部抽出口通过塔外循环管路与吸收段的上层脱硫喷淋器相通。本装置利用利用氨脱硫过程的中间物质亚硫氢酸铵及亚硫酸铵的还原性能，对烟气中的氮氧化物进行还原后脱除，不增加氨的消耗。
Description
技术领域
本实用新型涉及烟气中SO2和NOx脱除的装置，特别涉及用氨(氨水、碳铵、液氨)作为吸收剂的脱硫脱硝一体化烟气净化装置。
背景技术
工业烟气，尤其是燃煤锅炉烟气是大气污染的酸雨形成的最主要的因素，其中SO2和NOx排放是关键的因素，所以治理SO2和NOx是烟气治理的重点。
目前国内众多的钙法烟气脱硫装置存在投资高、运行成本高、消耗优质的石灰石资源、副产脱硫石膏市场容量有限、废水需进行处理排放等问题，给脱硫企业带来沉重的负担。
随着氨法脱硫技术的广泛应用，氨法脱硫的优势日益显现。氨法脱硫在脱硫的同时可副产硫酸铵化肥等有价产品，实现了硫资源的回收利用，不产生任何的二次污染，是一种于绿色清洁完全资源化的脱硫技术。
目前烟气脱硝技术主要有SCR(选择性催化还原)和SNCR(选择性非催化还原)，皆是利用氨作还原剂，还原的产物是氮气，既要投资建设相应的装置还要消耗大量的氨，催化剂昂贵消耗大，运行成本很高。
发明内容
本实用新型的目的是提供一种用氨作吸收剂的脱硫脱硝一体化净化装置，可在同一装置中同时实现脱硫脱硝，避免重复投资，降低运行费用。
本实用新型脱硫脱硝一体化净化装置，有一个塔体，设有烟气进口和净烟气出口，塔内包含水洗除雾段、吸收段和氧化段；所说的水洗除雾段包含装有除雾装置的除雾层、设有喷淋器的水喷淋层和水洗层；所说的吸收段位于烟气进口的上方，包含上层脱硫喷淋器、下层脱硝喷淋器，所说的氧化段位于塔的下部，氧化段的底部设有与氨和空气输入口相通的喷嘴；氧化段上部抽出口通过塔外循环管路与吸收段的下层脱硝喷淋器相通，下部抽出口通过塔外循环管路与吸收段的上层脱硫喷淋器相通。
所说的吸收段脱硝喷淋器根据喷淋量大小可设置一层或多层。
所说的吸收段脱硫喷淋器根据喷淋量大小可设置一层或多层。
所说的氧化段的中部设有抽出口，该抽出口与氧化段的下部抽出口合并或通过独立的塔外循环管路与吸收段的一层或多层脱硫喷淋器相通。
所说的氧化段内设置有开孔率＞30％的填料，一般是格栅或筛板，并可设置侧向搅拌器等搅拌混合设备。
所说的除雾填料层填有比表面积大于200m2/m3的大空隙率填料，如大空隙率波纹填料、丝网或折流板等高效低压降的除雾装置。
本装置能通过氨吸收烟气中的二氧化硫，并将吸收产物亚硫酸铵或亚硫酸氢铵氧化产生高浓度的结晶硫酸铵浆液，然后通过常规的生产配置就可低成本地制成商品农用硫酸铵。同时利用氨及脱硫中间物质亚硫氢酸铵及亚硫酸铵的还原性能，通过循环泵将氧化段上层和中层的主要含亚硫氢酸铵及亚硫酸铵的稀浆液循环返回吸收段再喷淋，对烟气中的氮氧化物进行还原后脱除，即利用氨脱硫过程物质进行脱硝，不增加氨的消耗。利用烟气的蒸发能力使脱硫液硫酸铵在塔内进行浓缩甚至结晶，从而节省能耗。本塔可在同一装置中同时实现脱硫脱硝，避免重复投资，降低运行费用，且操作简单，可靠稳定。
附图说明
图1是脱硫脱硝一体化烟气净化装置的结构示意图。
图中：10-塔体，11-烟气进口，12-净烟出口，20-水洗除雾段，21-除雾填料层，22-水喷淋层，23-水洗层、24-喷淋用水进口，30-吸收段，31、32-脱硫喷淋器，33-脱硝喷淋器，40-氧化段，41-脱硝循环池、42-脱硫循环池、43-氧化层，44-氨和氧化空气进口，45-母液或回流液进口、53-脱硝循环泵，52-一级脱硫循环泵，51-二级脱硫循环泵，54-塔底浆液泵。
具体实施方式
如图所示，塔体10设有原煤烟气进口11、净烟出口12，塔内上部为水洗除雾段20，包括除雾层21、水喷淋层22和水洗层23；塔10的中部、烟气进口11的上方是吸收段30，它自上至下包含喷淋层31、32和33，塔10的下部是氧化段40，它包含上部二级脱硫喷淋层31、中部一级脱硫喷淋层32、下部脱硝喷淋层33；塔10的下部是氧化段40，它的上部是脱硝循环池41、中部是脱硫循环池42，下部是氧化层，氧化层43设有氧化空气和氨吸收剂的输入口44和与之相连的空气分布器。吸收段30设有回流母液和回收液的进口45。
烟气从中部入口11进入塔10的吸收段30，在中部与来自脱硝喷淋层31、脱硫喷淋层32、33的吸收液进行接触，脱硝并脱硫，同时烟气被降温到65℃以下，向上进入上部的水洗除雾段20，经水洗层23、水喷淋层22，吸收除去烟气中未被反应的氨，然后通过除雾层21，除雾后从出口12排出净烟气。喷淋用水24可使用锅炉排水或低碱度的吸收液，也可直接利用上段除雾器来的冲洗水进行洗涤，这样使净化后的烟气中的气溶胶大大减少，氨耗大大降低。塔下部的氧化段40的上部为脱硝循环池41，中部为脱硫循环池42，底部为氧化层43，氧化层设有空气分布器；脱硝循环层41通过塔外循环管路与吸收段的下层脱硝喷淋器33相通，脱硫循环层42通过塔外循环管路与吸收段的中层一级脱硫喷淋器32相通，氧化层通过塔外循环管路与吸收段的上层的二级脱硫喷淋器31相通，各循环管路分别设有循环泵53、52、51。
塔10内吸收了二氧化硫的吸收液含有大量硫酸铵和硫酸氢铵，吸收液因重力作用下降而集于塔10的下部氧化段40，氧化空气及脱硫剂氨从进口44输入下部空气分布层43加入在氧化段40，充分利用烟气中剩余氧的自然氧化和辅助以空气对硫酸铵和硫酸氢铵进行强制氧化生成硫酸铵，由泵54输出。氧化率可达95％以上。
Claims (9)
1.脱硫脱硝一体化烟气净化装置，有一个塔体，设有烟气进口和净烟出口，塔内包含水洗除雾段、吸收段和氧化段；所说的水洗除雾段包含装有除雾装置的除雾层、设有喷淋器的水喷淋层和水洗层；其特征是所说的吸收段位于烟气进口的上方，包含上层脱硫喷淋器、下层脱硝喷淋器，所说的氧化段位于塔的下部，氧化段的底部设有与氨和空气输入口相通的分布器；氧化段上部抽出口通过塔外循环管路与吸收段的下层脱硝喷淋器相通，下部抽出口通过塔外循环管路与吸收段的上层脱硫喷淋器相通。
2.根据权利要求1所述的脱硫脱硝一体化烟气净化装置，其特征是所说的吸收段脱硝喷淋器设置一层或多层。
3.根据权利要求1所述的脱硫脱硝一体化烟气净化装置，其特征是所说的吸收段脱硫喷淋器根据喷淋量大小可设置一层或多层。
4.根据权利要求3所述的脱硫脱硝一体化烟气净化装置，其特征是所说的氧化段的中部设有抽出口，该抽出口与氧化段的下部抽出口合并或通过独立的塔外循环管路与吸收段的一层或多层脱硫喷淋器相通。
5.根据权利要求1所述的脱硫脱硝一体化烟气净化装置，其特征是所说的氧化段内设置有开孔率＞30％的填料。
6.根据权利要求5所述的脱硫脱硝一体化烟气净化装置，其特征是所说的填料是格栅或筛板。
7.根据权利要求1或2或3或4或5或6所述的脱硫脱硝一体化烟气净化装置，其特征是氧化段设有侧向搅拌器。
8.根据权利要求1所述的脱硫脱硝一体化烟气净化装置，其特征是除雾装置是比表面积大于200m2/m3的大空隙率填料。
9.根据权利要求1所述的脱硫脱硝一体化烟气净化装置，其特征是所说的填料是大空隙率波纹、丝网或折流板。
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101934191A (zh) * | 2010-09-06 | 2011-01-05 | 江苏新世纪江南环保有限公司 | 氨法烟气同时脱硫脱硝的方法 |
| CN102225310A (zh) * | 2011-05-01 | 2011-10-26 | 镇江金锐环保设备有限公司 | 脱硫脱硝一体化脱硫塔 |
| CN102974205A (zh) * | 2012-12-14 | 2013-03-20 | 国电龙源电力技术工程有限责任公司 | 塔内结晶氨法脱硫塔 |
| CN103203175A (zh) * | 2013-04-11 | 2013-07-17 | 浙江天蓝环保技术股份有限公司 | 一种回收硫酸铵的烟气脱硫脱硝工艺及装置 |
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