CN201380039Y - 双塔型烟气脱硫装置 - Google Patents
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Abstract
本实用新型涉及一种双塔型烟气脱硫净化装置，由脱硫塔和降温洗涤塔以烟气通道相连而成，降温洗涤塔设有原烟气进口和硫铵料浆排出口，脱硫塔设有脱硫吸收剂入口和净烟气出口；脱硫塔内自上至下包含有水洗除雾段、吸收段和氧化段，氧化段设有氧化空气和吸收剂入口；吸收段设有多个喷淋层，并通过料液循环管路与氧化段相连；降温洗涤塔内设有上层稀硫铵喷淋器和下层浓硫铵喷淋器，其中稀硫铵喷淋器与脱硫塔氧化段底部料液输出管路相连，浓硫铵喷淋器通过塔外循环管路与降温洗涤塔底部相连。本装置通过降温洗涤塔对原烟气预洗涤降温除尘，利用烟气热量对硫铵溶液进行浓缩结晶，降低了能耗，并能降低脱硫塔的运行阻力，具有节能高效的特点。
Description
技术领域
本发明涉及一种烟气净化装置，特别涉及用氨(氨水、碳铵、液氨)作为吸收剂的双塔型烟气脱硫净化装置。
背景技术
我国是能耗大国，每年所消耗的能量占世界消耗总量的8％～9％，而SO2排放总量却占世界排放量的15.1％，其他污染物如排放的NOx占10.1％，CO2占13.5％。而煤燃烟气则我国大气的最大污染源之一，燃煤烟气中除含有大量烟尘外，还含有SO2、NOx、CO2等有害成分。因此，全面推广烟气脱硫，对于改善我国的大气环境有着十分重要的意义。
目前我国脱硫装置基本上都是引进国外技术和设备并以钙法为主。一是因为钙法的脱硫剂石灰石来源丰富且价格便宜；二是钙法技术相对成熟。但是钙法脱硫工艺日益显现出其设备易结垢堵塞、副产物石膏处置困难、系统复杂、投资多、占地面积大、产生二次污染、运行费用高等问题。而氨法脱硫可充分利用我国广泛的氨源来副产化肥硫酸铵，弥补我国大量进口硫磺的缺口，既治理了SO2污染，又满足长期大量的化肥需求，并可产生一定的经济效益。氨法脱硫无二次污染，是一项适应国情和长远发展的绿色环保脱硫技术。
为实现烟气脱硫和硫铵生产的一体化，国内许多研究都着眼于吸收脱硫及浓缩结晶的多功能塔。但这就要提高塔的高度，制造成本相对较高。专利CN200998639则提供了一种浓缩结晶和氧化吸收的组合塔装置，有效降低了塔高，但该装置存在着结晶塔料浆易挂壁、吸收塔氨易逃逸的问题。
发明内容
本发明的目的是提供一种燃炉烟气净化的双塔型脱硫装置，通过该装置可实现烟气的洗涤降温和二氧化硫的脱除，同时利用烟气热量实现硫铵料浆的浓缩结晶，并还可有效消除浓硫铵壁流导致的挂壁现象。
本装置由脱硫塔和降温洗涤塔组成，二者之间以烟气通道相连，降温洗涤塔设有原烟气进口和硫铵料浆排出口，脱硫塔设有脱硫吸收剂入口和净烟气出口；脱硫塔内自上至下包含有水洗除雾段、吸收段和氧化段，氧化段设有氧化空气和吸收剂入口；吸收段设有多个喷淋层，并通过料液循环管路与氧化段相连；降温洗涤塔上部设有上层稀硫铵喷淋器和下层浓硫铵喷淋器，其中稀硫铵喷淋器与脱硫塔氧化段底部料液输出管路相连，浓硫铵喷淋器与降温洗涤塔下部引出的塔外循环管路相连。
降温洗涤塔和脱硫塔之间的烟气通道设有除雾器。
所说氧化段内设置有开孔率大于30％的多层填料，一般是格栅或筛板填料。
所说的脱硫吸收剂与氧化空气从氧化段底部的入口一并加入。
所说的除雾段设有比表面积大于300m2/m3的填料，如大空隙率波纹填料、丝网或折流板。
本装置设有双塔，原烟气先进入降温洗涤塔与两层喷淋器喷淋的吸收液洗涤接触，充分换热，降温除尘，从而可使脱硫塔内的运行阻力减小；另一方面，降温洗涤塔内设浓硫铵喷淋器，用以喷射吸收液，可使烟气降温增湿，吸收液浓缩结晶，便于硫铵料浆的进一步处理，节省了能耗；稀硫铵喷淋器置于浓硫铵喷淋器上方，并保持较高的喷淋覆盖率，可喷射吸收液与烟气进一步接触，并可有效消除浓硫铵壁流导致的挂壁现象；脱硫塔内应用多层喷淋层，流场分布合理，有效降低系统运行阻力，因此吸收段可不设置填料或设置空隙率高的格栅填料，简化了塔内结构，操作可靠稳定；吸收剂与氧化空气一同加入氧化段底部，可有效降低氨逃逸。
综上所述，本双塔装置通过降温洗涤塔对原烟气预洗涤降温除尘，有效降低了脱硫塔的运行阻力，利用烟气热量对硫铵溶液进行浓缩结晶，降低了能耗；可实现二氧化硫的充分吸收及亚硫铵的充分氧化，具有节能高效的特点。
附图说明
图1是本双塔型烟气脱硫净化装置的结构示意图。
图中，10-脱硫塔，111-烟气入口，12-出口，20——除雾段，21-填料，22-水喷淋器，23-为水洗填料，24-喷淋水进口，30-吸收段，31-三级脱硫喷淋层32-二级脱硫喷淋层、33-一级脱硫喷淋层，40-氧化段，41-多层填料，42-空气分布器，43-氧化段底部入口，50-降温洗涤塔，51-稀硫铵喷淋器，52-浓硫铵喷淋器，53-搅拌器，54-结晶除雾器，61-循环泵，62-料液泵，63-结晶泵，64-出料泵。
具体实施方式
如图1，经除尘的原烟气由烟气入口111进入降温洗涤塔50，与浓硫铵喷淋器52喷射出的高浓度硫酸铵溶液充分接触，进行热交换，烟温降到70-100℃，再与稀硫铵喷淋器51喷射的稀硫铵进一步接触后，经结晶除雾器54除去烟气夹带的结晶颗粒后，进入脱硫塔10吸收段30的中部，与吸收液进行接触降温到50-70℃左右，向上依次通过吸收段的一级脱硫喷淋层33、二级脱硫喷淋层32和三级脱硫喷淋层31，被喷淋后的烟气进入上部的水洗除雾段20；此段内，水从进口24通入水喷淋器22并向下喷淋，上升烟气经过水洗填料23与喷淋水充分接触，除去其夹带的氨，继续上升，通过填料21时，所夹带的雾状水合并成水滴而下降被除去，最后从出口12排出净烟气。除雾段填料21是比表面积大于300m2/m3的填料，如大空隙率波纹填料、丝网或折流板等，一般保证脱硫塔总压降在1500Pa以下。同时，经上述各级喷淋器喷出的吸收液吸收了烟气中的SO2下降至脱硫塔10的下部氧化段40，被氧化空气强制氧化。氧化段40内设置有开孔率大于30％的多层填料41，一般是格栅或筛板填料；氧化空气及脱硫剂氨从氧化段40底部入口43加入，经空气分布器42均匀分布并喷出。氧化段40内的料液由循环泵61经循环管路通入吸收段30的各脱硫喷淋层31、32、33。可由一台泵抽取吸收液输送至三段脱硫层，也可设置三台泵分别从氧化段不同部位抽取吸收液输送至对应脱硫层，具体则由烟气量及SO2含量来确定。至少一台料液泵62用于将氧化段40的吸收液送至稀硫铵喷淋器51。至少一台结晶泵63用于将降温结晶塔50的硫铵料浆循环返回塔50的喷淋器52进行循环浓缩结晶；为防止结晶沉淀，可设置侧向搅拌器53对塔50内的高浓度料浆进行搅拌；降温结晶塔50内达一定含固量的料浆由出料泵64送至后处理系统得副产品硫酸铵化肥。
Claims (6)
1.双塔型烟气脱硫装置，由脱硫塔和降温洗涤塔组成，二者之间以烟气通道相连，降温洗涤塔设有原烟气进口和硫铵料浆排出口，脱硫塔设有脱硫吸收剂入口和净烟气出口；脱硫塔内自上至下包含有水洗除雾段、吸收段和氧化段，氧化段设有氧化空气入口；吸收段设有多个喷淋层，并通过料液循环管路与氧化段相连；其特征是降温洗涤塔上部设有上层稀硫铵喷淋器和下层浓硫铵喷淋器，其中稀硫铵喷淋器与脱硫塔氧化段底部料液输出管路相连，浓硫铵喷淋器通过塔外循环管路与降温洗涤塔底部相连。
2.根据权利要求1所述的双塔型烟气脱硫装置，其特征是降温洗涤塔和脱硫塔之间的烟气通道设有除雾器。
3.根据权利要求1所述的双塔型烟气脱硫装置，其特征是氧化段内设置有开孔率大于30％的多层填料。
4.根据权利要求3所述的双塔型烟气脱硫装置，其特征是所说的填料是格栅或筛板填料。
5.根据权利要求1所述的双塔型烟气脱硫装置，其特征是所说的除雾段设有比表面积大于300m2/m3的填料。
6.根据权利要求1所述的双塔型烟气脱硫装置，其特征是所说填料是波纹填料、丝网或折流板。
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| CN102247741A (zh) * | 2011-07-15 | 2011-11-23 | 攀钢集团有限公司 | 一种烟气脱硫工艺 |
| CN104722193A (zh) * | 2015-03-06 | 2015-06-24 | 浙江蓝天求是环保股份有限公司 | 一种独立循环的湿法脱硫系统及方法 |
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