CN201529487U - 一种液相催化脱硝的烟气净化装置 - Google Patents
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Abstract
一种液相催化脱硝的烟气净化装置，该实用新型涉及环保设备，具体涉及的是一种燃煤烟气的脱硝装置。它包括吸收塔，吸收塔的顶部设有烟气出口，内部自上而下设置有水洗除雾段、吸收段和氧化段；所述的吸收段的下部设置有烟气入口，上部设置有脱硫喷淋层和脱硝喷淋层，在所述的先经过脱硫喷淋层，再经过脱硝喷淋层之间设有催化剂层设有催化剂层；所述的氧化段设置有脱硝循环层和脱硫循环层，通过管路分别与脱硝喷淋层、脱硫喷淋层相通。本实用新型公开一种液相催化脱除烟气中NOx的装置，采用该装置能有效提高脱硝效率、降低氨的耗量，同时系统结构简化、运行成本低廉。脱硝副产物硝酸铵还具有较高的经济价值。
Description
技术领域
本实用新型涉及环保设备，具体涉及的是一种燃煤烟气的脱硝装置。
背景技术
我国是以煤炭为主要燃料的发展中国家，随着经济的快速发展，燃煤造成的环境污染日趋严重，特别是燃煤烟气中的NOx，对大气的污染已成为一个不容忽视的问题。
目前，控制燃烧产生的NOx主要有燃烧前燃料脱氮、燃烧中改进燃烧方式和生产工艺脱氮、锅炉烟气脱硝3种方法。燃料脱氮技术相关的报道还很少，有待进一步开发。燃烧中改进燃烧方式和生产工艺脱氮技术，目前应用较多的是低NOx燃烧技术，但一般情况下低NOx燃烧技术只能降低NOx排放的50％左右，而国内外对NOx排放的限制愈来愈严，因此要进一步降低NOx的排放必须采用烟气脱硝技术。
烟气脱硝技术主要有选择性催化还原法(SCR)、选择性非催化还原法(SNCR)和选择性非催化还原与选择性催化还原联合法(SNCR-SCR)，皆是利用氨或尿素作还原剂，还原产物是氮气。其中SCR法脱硝效率高，但其工艺和设备系统较复杂，催化剂昂贵、耗量大，装置运行成本高；SNCR法工艺和设备系统较简单，装置运行成本不高，但脱硝效率不能保证。SNCR-SCR法则结合了两者工艺的特点，有效降低了催化剂的耗量，但其总体结构仍较复杂，还有着很大的改进空间。此外，上述三种工艺都需在高温(300℃)下反应，能耗过高。
因此开发一种脱硝效率高、反应条件温和、能耗较低且系统结构简捷的烟气脱硝装置就有着很强的现实意义和推广价值。
实用新型内容
1、实用新型目的
本实用新型的目的是公开一种液相催化脱除烟气中NOx的装置。采用该装置能有效提高脱硝效率、降低氨的耗量，同时系统结构简化、运行成本低廉。脱硝副产物硝酸铵还具有较高的经济价值。
2、技术方案
一种液相催化脱硝的烟气净化装置，它包括吸收塔，吸收塔的顶部设有烟气出口，内部自上而下设置有水洗除雾段、吸收段和氧化段；所述的吸收段的下部设置有烟气入口，上部设置有催化剂层，在催化剂层上部设置有脱硝喷淋层，下部设置有吸收脱硫喷淋层；所述的氧化段设置有脱硝循环层和脱硫循环层，通过管路分别与脱硝喷淋层、脱硫喷淋层相通。
本实用新型所述的喷淋层有四层，从下而上分为吸收脱硝喷淋层、一级脱硫喷淋层、二级脱硫喷淋层和催化脱硝喷淋层。
本实用新型所述的脱硝循环层设置有循环泵与吸收脱硝喷淋层相通，脱硫循环层设置有两个循环泵，分别和一级脱硫喷淋层、二级脱硫喷淋层相通，氧化层设置有循环泵，与催化脱硝层相通，
本实用新型所述的水洗除雾段包括除雾器、水喷淋层和水洗层。
本实用新型所述的氧化段底部为氧化层，设置有空气分布器、氧化空气和吸收剂氨的入口。
3、有益效果
(1)本实用新型与氨法烟气脱硫技术结合，仅在吸收塔上设置一段催化脱硝段便可达到55％以上的脱硝效率(大于SNCR的脱硝率)，使氨法脱硫与脱硝一体化，投资及运行成本大幅度降低；
(2)本实用新型先利用脱硫中间产物部分脱硝(脱硝率20％～30％)，再利用液相催化进一步脱硝，因此氨耗较低；
(3)本实用新型的NOx部分被还原为N2随净烟气排出，其余的则被氧化为HNO3并转化为硝酸铵，可实现脱硫脱硝产物的无害化和资源化利用。
(4)本实用新型投资小、能耗低、系统结构简单、运行成本低，同时在低氨耗的情况下，脱硝率也可达55％以上。
附图说明
图1为本实用新型的结构示意图
其中，10-吸收塔；11-烟气入口；12-净烟气出口；20-水洗除雾段；21-除雾层；22-水喷淋层；23-水洗层；30-吸收段；31-吸收脱硝喷淋层；32-一级脱硫喷淋层，33-二级脱硫喷淋层；34-催化脱硝喷淋层；35-催化剂层；40-氧化段；41-吸收脱硝循环层；42-脱硫循环层；43-空气分布器；44-氧化空气和吸收剂入口；51、52、53、54-循环泵；55-出料泵。
具体实施方式
如图1，一种液相催化脱硝的烟气净化装置，它包括吸收塔10，吸收塔的顶部设有烟气出口12，内部自上而下设置有水洗除雾段20、吸收段30和氧化段40；吸收段30的下部设置有烟气入口11，上部设置有四层喷淋层，从下而上为吸收脱硝喷淋层31、一级脱硫喷淋层32、二级脱硫喷淋层33和催化脱硝喷淋层34，在二级脱硫喷淋层33和催化脱硝喷淋层34之间设有催化剂层35；氧化段40的上部为吸收脱硝循环层41，中部为脱硫循环层42，底部为氧化层，各层通过各自循环管路与吸收段不同位置的喷淋层相通，吸收脱硝循环层41设置有循环泵51，与吸收脱硝喷淋层31相通，脱硫循环层42设置有两个循环泵52、53，分别和一级脱硫喷淋层32、二级脱硫喷淋层33相通，氧化层设置有循环泵54，与催化脱硝喷淋层34相通。氧化空气和吸收剂氨入口44在氧化段40底部；水洗除雾段20主要由除雾器21、水喷淋层22和水洗层23构成。
引风机输送的烟气从吸收塔10的烟气入口11进入吸收段30，与来自吸收脱硝喷淋层31及一级脱硫喷淋层32，二级脱硫喷淋层33的吸收液进行接触，脱硝并脱硫，同时烟气被降温到70℃以下。为保证脱硫脱硝效率，烟气与吸收液的接触吸收需保持较大的液气比，本装置一般控制在1∶2500以上，且应按流场分布要求分层布置。三个喷淋层，喷淋层间距应在1～3米，喷淋层喷头布置呈一定角度的交错，每层喷淋覆盖率大于110％。每层喷淋层对应一台循环泵，循环泵从吸收塔的氧化段不同部分抽取循环吸收液。
烟气继续上行与催化脱硝喷淋层34喷射的吸收液在催化剂层35表面进行充分接触，在催化剂的作用下利用吸收液中的溶解氧及烟气中剩余氧催化氧化NO并转化为HNO3。为保证氧的溶解度和催化剂的活性，需控制吸收液pH值在4.5～6.5之间，并保持较大的液气比，一般在1∶1500以上。液相催化所用催化剂由活性成分与惰性载体组成，气相和液相中的NO在催化剂表面进行氧化反应生成NO2。其中活性成分由几种金属化合物组成，惰性载体以二氧化硅为主。
脱硫脱硝后的烟气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。塔下部的氧化段40的上部为吸收脱硝循环层41，中部为脱硫循环层42，底部为氧化层，为防止溶液返混，各层之间可用开孔率大于35％的筛板、格栅等进行分离，氧化层还设有空气分布器43。
塔内吸收了二氧化硫和氮氧化物的吸收液含有大量亚硫酸(氢)铵及一定量的HNO3，吸收液因重力作用下降而集于吸收塔10的下部氧化段40，在该段内主要实现亚硫铵的氧化和HNO3的氨化，氧化段的上部为吸收脱硝循环层41，中部为脱硫循环层42，底部为氧化层，各层通过各自循环管路与吸收段喷淋层相通。为防止溶液返混，各层之间可用开孔率大于35％的筛板、格栅等进行分离。吸收脱硝循环层41应控制氧化率小于95％、pH值在3.5-5.5之间，高度为1m～6m，尤以1.5m～2.5m为佳；脱硫循环层42应控制氧化率大于95％、pH值在4.5～5.8之间，高度为2m～7m，尤以3m～5m为佳。氧化层42应控制氧化率大于98％、pH值在4.8～6.6之间，高度为1m～6m，尤以2.5m～4.5m为佳。
氧化空气及脱硫剂氨从44输入下部空气分布器43加入，充分利用烟气中剩余氧的自然氧化和辅助以空气对亚硫酸(氢)铵进行强制氧化生成硫酸铵。并在硫铵溶液中实现HNO3的氨化吸收，转化为NH4NO3。氧化层料液达到一定浓度后，由出料泵55输送至后系统经常规处理即可制得硫铵和硝铵商品化肥。
Claims (5)
1.一种液相催化脱硝的烟气净化装置，包括吸收塔，吸收塔的顶部设有烟气出口(12)，其特征在于：吸收塔的内部自上而下设置有水洗除雾段(20)、吸收段(30)和氧化段(40)；所述的吸收段(30)的下部设置有烟气入口(11)，上部设置有催化剂层(35)，在催化剂层(35)上部设置有脱硝喷淋层，下部设置有吸收脱硫喷淋层；所述的氧化段(40)设置有吸收脱硝循环层(41)和脱硫循环层(42)，通过管路分别与吸收脱硝喷淋层、脱硫喷淋层相通。
2.根据权利要求1所述的烟气净化装置，其特征在于：所述的喷淋层有四层，从下而上分为吸收脱硝喷淋层(31)、一级脱硫喷淋层(32)、二级脱硫喷淋层(33)和催化脱硝喷淋层(34)。
3.根据权利要求1或2所述的烟气净化装置，其特征在于：所述的吸收脱硝循环层(41)设置有循环泵(51)与吸收脱硝喷淋层(31)相通，脱硫循环层(42)设置有两个循环泵(52、53)，分别和一级脱硫喷淋层(32)、二级脱硫喷淋层(33)相通，氧化段(40)设置有循环泵(54)，与催化脱硝层(34)相通。
4.根据权利要求1所述的烟气净化装置，其特征在于：所述的水洗除雾段(20)包括除雾器(21)、水喷淋层(22)和水洗层(23)。
5.根据权利要求1所述的烟气净化装置，其特征在于：所述的氧化段(40)底部为氧化层，设置有空气分布器(43)、氧化空气和吸收剂氨的入口(44)。
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| CN2009202567336U Expired - Lifetime CN201529487U (zh) | 2009-10-30 | 2009-10-30 | 一种液相催化脱硝的烟气净化装置 |
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| 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 |
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