CN103263828A - 燃煤锅炉sncr与scr联合法烟气脱硝系统 - Google Patents
燃煤锅炉sncr与scr联合法烟气脱硝系统 Download PDFInfo
- Publication number
- CN103263828A CN103263828A CN2013101886119A CN201310188611A CN103263828A CN 103263828 A CN103263828 A CN 103263828A CN 2013101886119 A CN2013101886119 A CN 2013101886119A CN 201310188611 A CN201310188611 A CN 201310188611A CN 103263828 A CN103263828 A CN 103263828A
- Authority
- CN
- China
- Prior art keywords
- scr
- sncr
- flue gas
- denitrification
- reducing agent
- Prior art date
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- 239000007789 gases Substances 0.000 title claims abstract description 19
- 238000010531 catalytic reduction reactions Methods 0.000 title abstract description 6
- 239000003638 reducing agent Substances 0.000 claims abstract description 54
- 239000000203 mixture Substances 0.000 claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims abstract description 18
- 238000002347 injection Methods 0.000 claims description 60
- 239000007924 injection Substances 0.000 claims description 60
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 48
- 239000003546 flue gas Substances 0.000 claims description 48
- 229910002089 NOx Inorganic materials 0.000 claims description 24
- 238000006722 reduction reaction Methods 0.000 claims description 13
- 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 description 9
- 230000001603 reducing Effects 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 9
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Natural products 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NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 8
- 239000004202 carbamide Substances 0.000 claims description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 3
- 239000000839 emulsion Substances 0.000 claims description 3
- 239000003517 fume Substances 0.000 abstract description 5
- 239000000779 smoke Substances 0.000 abstract description 5
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O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
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Abstract
一种燃煤锅炉SNCR+SCR联合法烟气脱硝系统,包括锅炉和SCR脱硝装置;所述的锅炉包括炉膛,炉膛的烟气出口,旋风分离器、返料装置、尾部烟道;炉膛的烟气出口与旋风分离器的入口相连,旋风分离器的下部出口通过返料装置与炉膛的密相区相连;所述尾部烟道与旋风分离器上部出口相连,尾部烟道内布置有一级省煤器,二级省煤器;所述的旋风分离器入口处、和/或炉膛出口、和/或旋风分离器上部设有SNCR还原剂喷射装置;所述的SCR脱硝装置设置于一、二级省煤器之间,和/或一级省煤器前,和/或二级省煤器之后,所述的SCR脱硝装置包括SCR脱硝催化剂层。
Description
燃煤锅炉SNCR与SCR联合法烟气脱硝系统
技术领域
[0001] 本发明属于燃煤锅炉排放污染物控制领域,具体涉及一种燃煤锅炉SNCR+SCR联合脱硝系统。
背景技术
[0002] 氮氧化物是造成大气污染的主要污染源之一,通常所说的氮氧化物(NOx)主要包括NO、NO2, N203、N2O5等几种,其中污染大气的主要是NO和NO2。NOX在阳光的作用下会引起光化学反应,形成光化学烟雾,从而造成严重的大气污染。七十年代以来NOx的大气污染问题已被日益重视,人们发现:人体健康的伤害、高含量硝酸雨、光化学烟雾、臭氧减少以及其他一些问题均与低浓度NOx有关系,而且其危害性比人们原先设想的要大得多。
[0003] 我国氮氧化物的排放量中近70%来自于煤炭的直接燃烧,电力工业又是我国的燃煤大户,因此火力发电厂是NOx排放的主要来源之一,随着我国现代工业生产的发展和生活水平的提高,大气污染成了人们十分关注的问题。
[0004] 烟气脱硝,是指把已生成的NOx还原为N2,从而脱除烟气中的N0X,按治理工艺可分为湿法脱硝和干法脱硝。主要包括:酸吸收法、碱吸收法、SCR (选择性催化还原法)、SNCR(非选择性催化还原法)、吸附法、离子体活化法等。国内外一些科研人员还开发了用微生物来处理NOx废气的方法。
[0005] 由于从燃烧系统排放的烟气中的N0x,90%以上是NO,而NO难溶于水,因此对NOx的湿法处理不能用简单的洗涤法,湿法脱硝的原理是用氧化剂O3将NO氧化成NO2,生成的NO2再用水或碱性溶液吸收,从而实现脱硝。该法的生成物HNO3液体需经浓缩处理,而且O3需要高电压制取 ,初投资及运行费用高。ClO2氧化还原法是用ClOJfNO氧化成NO2,然后用Na2SO3水溶液将NO2还原成N2。该法可以和采用NaOH作为脱硫剂的湿法脱硫技术结合使用,脱硫的反应产物Na2SO3又可作为NO2的还原剂,ClO2法的脱硝率可达95%,且可同时脱硫,但ClO2和NaOH的价格较高,运行成本增加。
[0006]目前,火电厂燃煤锅炉烟气脱硝装置的主流技术为SCR (选择性催化还原)技术,以及SNCR (选择性非催化还原)技术,其中SCR技术利用布置在锅炉省煤器和空气预热器之间的反应器将烟气中NOx去除,反应器中布置有脱硝催化剂,脱硝还原剂通过入口烟道布置得氨注射系统喷入烟道与烟气中的NOx充分混合。
[0007] 对于常规电站锅炉,省煤器出口烟气温度为SCR脱硝反应需要的温度窗口,且为高尘布置,脱硝效率适中、技术应用成熟。但是,对于循环流化床燃煤锅炉,其主要特点为高尘、省煤器出口温度低,对于部分氮含量高且挥发分高的燃料,锅炉出口 NOx含量达到甚至超过500mg/Nm3(6%02,干基),根据《火电厂大气污染物排放标准GB13223-2011》,到2014年7月,火电厂燃煤锅炉NOx的排放控制标准为100,仅依靠SCR技术对烟气进行脱硝,投资大、运行成本高、难以满足烟气排放要求。
发明内容[0008] 本发明提供了一种燃煤锅炉SNCR+SCR联合脱硝系统,通过更合理利用锅炉及尾部省煤器空间,将锅炉炉膛内SNCR还原反应残余的还原剂作为SCR反应的还原剂,实现NOx高效还原以降低烟气中NOx排放。
[0009] 本发明的目的具体是通过以下的技术方案来实现的:
[0010] 一种燃煤锅炉SNCR与SCR联合法烟气脱硝系统,包括锅炉和SCR脱硝装置;
[0011] 所述的锅炉包括炉膛,炉膛的烟气出口、旋风分离器、返料装置、尾部烟道;
[0012] 所述炉膛的烟气出口与旋风分离器的入口相连,旋风分离器的下部出口通过返料装置与炉膛的密相区相连;
[0013] 所述尾部烟道与旋风分离器上部出口相连,所述的SCR脱硝装置设置于尾部烟道中;
[0014] 所述的旋风分离器入口处、和/或炉膛出口、和/或旋风分离器上部设有SNCR还原剂喷射装置;
[0015] 所述的SCR脱硝装置包括SCR脱硝催化剂层。
[0016] 尾部烟道内布置有一级省煤器,二级省煤器;所述的SCR脱硝装置设置于一、二级省煤器之间,和/或一级省煤器前,和/或二级省煤器之后。
[0017] 所述的SCR脱硝装置还包括SCR还原剂喷射装置。
[0018] 所述的SCR还原剂喷射装置设置在一级省煤器之后、催化剂层之前、或一级省煤器之前。
[0019] 所述的SCR还原剂喷射装置、和/或SNCR装置分别独立地为双流体雾化喷枪。
[0020] 还原剂选自氨水、液氨和尿素中的任意一种或几种的组合。
[0021] 一种使用燃煤锅炉SNCR与SCR联合法烟气脱硝系统进行烟气脱硝的方法:在锅炉旋风分离器入口烟道设置SNCR还原剂喷射装置,在烟气温度800-11(KTC工况下对锅炉炉膛出口烟气中的NOx先进行还原;
[0022] 在锅炉尾部烟道的两级省煤器间260-400°C温度范围内设置SCR脱硝催化剂层,作为SCR脱硝系统,SCR脱硝系统利用SNCR脱硝系统逃逸出的还原剂作为还原剂,进一步对烟气中的NOx进行脱除。
[0023] 所述的SCR脱硝装置还增设有还原剂喷射装置,以备在需要时及时补充还原剂量。
[0024] 所述的SNCR还原剂喷射装置设置在温度范围为800-1100°C的烟气通道上。
[0025] 所述的SCR脱硝装置设置在温度范围为260_400°C的尾部烟道上。
[0026] 本发明首先采用简单的SNCR脱硝工艺从源头上降低NOx浓度,然后灵活的布置SCR脱硝装置进一步深入脱硝,两者有机结合,优势结合缺陷互补:SNCR脱硝装置不需要对锅炉进行较大改动, 不增加锅炉烟气系统阻力,但脱硝效率相对较低,氨逃逸较高,增加了SCR脱硝装置正好可提高脱硝效率并同时降低氨逃逸问题,同时,由于SNCR作用已经从源头上降低了 NOx的排放浓度,下游SCR脱硝装置所承担的脱硝压力大大减轻,也使SCR脱硝装置在设计上的难度和投资成本大大降低。
[0027] 在锅炉烟气温度范围为800-1100°C的烟气通道上布置还原剂喷枪,在这一温度范围内喷入的还原剂迅速热分解成NH3并与烟气中的NOx进行SNCR反应生成N2。SNCR脱硝装置可设于循环流化床锅炉旋风分离器入口处、锅炉出口及旋风分离器上部至少一处位置的SNCR还原剂喷射装置。由还原剂制备系统制备的还原剂,通过SNCR还原剂喷射装置喷入,与锅炉炉膛出口的高温烟气中的NOx在旋风分离器位置强烈混合,烟气中部分的NOx与还原剂发生还原反应生成无害、无污染的N2和水,从源头上减低锅炉NOx排放。
[0028] SCR脱硝装置可利用SNCR脱硝反应逃逸的氨量作为还原剂,即解决了 SNCR系统氨逃逸对环境的污染,又在保证脱硝效率的前提下减少了还原剂的用量。为确保SCR脱硝需要的还原剂量充足,可在SCR部分增设还原剂喷射装置,以备在需要时及时补充还原剂量。SCR脱硝反应器可行的布置方式也可以灵活多变,根据脱硝效率要求、催化剂布置层数和锅炉方案整体确定最优布置。
附图说明
[0029] 图1是本发明的结构示意图。
[0030] 图中:1-炉膛,2-旋风分离器,3-返料装置,4-炉膛烟气出口,5-转向室过热屏,6-过热器,7-再热器,8-初级过热器,9-一级省煤器,10-二级省煤气,11-水冷风室,12-尾部烟道,21-SNCR还原剂喷射装置,22-SCR脱硝催化剂层。
具体实施方式
[0031] 现结合附图对本发明的具体实施方式进行详细说明。
[0032] 实施例一
[0033] 一种燃煤锅炉SNCR与SCR联合法烟气脱硝系统,包括锅炉和SCR脱硝装置;
[0034] 所述的锅炉包括炉膛1,炉膛的烟气出口 4、旋风分离器2、返料装置3和尾部烟道12 ;
[0035] 炉膛的烟气出口 4与旋风分离器2的入口相连,旋风分离器2的下部出口通过返料装置3与炉膛的密相区相连;
[0036] 旋风分离器入口处2、炉膛的烟气出口 4或旋风分离器2上部设有至少一个SNCR还原剂喷射装置21 ;
[0037] 所述的SCR脱硝装置还包括SCR脱硝催化剂层22。
[0038] 尾部烟道内布置有一级省煤器9,二级省煤器10,SCR脱硝装置设置在一级省煤器9和二级省煤器10之间,和/或一级省煤器9前,和/或二级省煤器10之后,
[0039] SCR脱硝催化剂层22上方设置有吹灰器,吹灰器选用蒸汽吹灰器。
[0040] SCR脱硝装置还包括有还原剂喷射装置,以备在需要时及时补充还原剂量。
[0041] 所述的SCR还原剂喷射装置设置在一级省煤器下方、催化剂层之前、或一级省煤器之前,SCR还原剂喷射装置、和或SNCR装置分别独立地为双流体雾化喷枪。
[0042] 所述的SNCR还原剂喷射装置设置在温度范围为800-1100°C的烟气通道上。
[0043] 所述的SCR脱硝装置设置在温度范围为290_350°C的尾部烟道上。
[0044] 脱硝还原剂选用10%_20%的氨水。
[0045] 在锅炉旋风分离器入口烟道设置SNCR还原剂喷射装置,在烟气温度800-1100°C工况下对锅炉炉膛出口烟气中的NOx先进行还原,在锅炉尾部烟道的两级省煤器间290-350°C温度范围内设置SCR脱硝催化剂层,作为SCR脱硝系统,SCR脱硝系统利用SNCR脱硝系统逃逸出的氨作为还原剂,进一步对烟气中的NOx进行脱除,所述的SCR脱硝装置还增设有还原剂喷射装置,以备在需要时及时补充还原剂量,采用此联合脱硝工艺,可保证锅炉出口烟气NOx排放浓度彡100mg/Nm3,出口 NH3逃逸浓度彡2.5mg/Nm3。
[0046] 实施例二
[0047] 燃煤锅炉SNCR与SCR联合法烟气脱硝系统,包括锅炉和SCR脱硝装置;
[0048] 锅炉包括炉膛1,煤粉在炉膛I内燃烧后,烟气和未完全燃烧的固体颗粒通过炉膛的烟气出口 4进入旋风分离器2中,旋风分离器2入口处、炉膛的烟气出口 4或旋风分离器2上部设有至少一个SNCR还原剂喷射装置,并且SNCR还原剂喷射装置设置在温度范围为800-1100 V的烟气通道上。
[0049] 在烟气温度范围为800-1100°C的工况下,喷入的还原剂迅速热分解成NH3并与锅炉炉膛出口的高温烟气在旋风分离器位置强烈混合,烟气中部分的NOx与还原剂发生还原反应生成无害、无污染的N2和水,经过初步脱硝的烟气从旋风分离器上部出口进入尾部烟道。
[0050] 尾部烟道内布置有一级省煤器,二级省煤器;在锅炉尾部烟道的两级省煤器间290-350°C温度范围内设置SCR脱硝催化剂层,作为SCR脱硝系统,SCR脱硝系统利用SNCR脱硝系统逃逸出的氨作为还原剂,进一步对烟气中的NOx进行脱除,为确保SCR脱硝需要的还原剂量充足,可在SCR部分增设还原剂喷射装置,以备在需要时及时补充还原剂量。
[0051] 脱硝还原剂选用尿素水溶液,尿素水解可以生成NH3,化学反应式如下:
[0052] NH2C0NH2+H20 — 2NH3+C02`
[0053] 在SCR脱硝催化剂层上方设置蒸汽式吹灰器,以防止灰尘在催化剂表面沉积,降低催化剂堵塞的几率。
`[0054] SCR还原剂喷射装置、SNCR装置分别独立地为双流体雾化喷枪。
[0055] 采用此联合脱硝工艺,可保证锅炉出口烟气NOx排放浓度彡100mg/Nm3,出口順3逃逸浓度< 2.5mg/Nm3。
[0056] 以上对本发明的具体实施例进行了详细描述,但其只是作为范例,本发明并不限制于以上描述的具体实施例。对于本领域技术人员而言,任何对本发明进行的等同修改和替代也都在本发明的范畴之中。因此,在不脱离本发明的精神和范围下所作的均等变换和修改,都应涵盖在本发明的范围内。
Claims (10)
1.燃煤锅炉SNCR与SCR联合法烟气脱硝系统,其特征在于,包括锅炉和SCR脱硝装置; 所述的锅炉包括炉膛,炉膛的烟气出口、旋风分离器、返料装置、尾部烟道; 所述炉膛的烟气出口与旋风分离器的入口相连,旋风分离器的下部出口通过返料装置与炉膛的密相区相连; 所述尾部烟道与旋风分离器上部出口相连,所述的SCR脱硝装置设置于尾部烟道中; 所述的旋风分离器入口处、和/或炉膛出口、和/或旋风分离器上部设有SNCR还原剂喷射装置; 所述的SCR脱硝装置包括SCR脱硝催化剂层。
2.根据权利要求1所述的燃煤锅炉SNCR与SCR联合法烟气脱硝系统,其特征在于,尾部烟道内布置有一级省煤器,二级省煤器;所述的SCR脱硝装置设置于一、二级省煤器之间,和/或一级省煤器前,和/或二级省煤器之后。
3.根据权利要求2所述的燃煤锅炉SNCR与SCR联合法烟气脱硝系统,其特征在于,所述的SCR脱硝装置还包括SCR 还原剂喷射装置。
4.根据权利要求3所述的燃煤锅炉SNCR与SCR联合法烟气脱硝系统,其特征在于,所述的SCR还原剂喷射装置设置在一级省煤器之后、催化剂层之前、或一级省煤器之前。
5.根据权利要求1或4所述的燃煤锅炉SNCR与SCR联合法烟气脱硝系统,其特征在于,所述的SCR还原剂喷射装置、和/或SNCR还原剂喷射装置分别独立地为双流体雾化喷枪。
6.根据权利要求1所述的燃煤锅炉SNCR与SCR联合法烟气脱硝系统,其特征在于,还原剂选自氨水、液氨和尿素中的任意一种或几种的组合。
7.一种使用燃煤锅炉SNCR与SCR联合法烟气脱硝系统进行烟气脱硝的方法,其特征在于,在锅炉旋风分离器入口烟道设置SNCR还原剂喷射装置,在烟气温度800-1100°C工况下对锅炉炉膛出口烟气中的NOx先进行还原; 在锅炉尾部烟道的两级省煤器间260-400°C温度范围内设置SCR脱硝催化剂层,作为SCR脱硝系统,SCR脱硝系统利用SNCR脱硝系统逃逸出的还原剂作为还原剂,进一步对烟气中的NOx进行脱除。
8.根据权利要求7所述的使用燃煤锅炉SNCR与SCR联合法烟气脱硝系统进行烟气脱硝的方法,其特征在于,所述的SCR脱硝装置还增设有还原剂喷射装置,以备在需要时及时补充还原剂量。
9.根据权利要求7所述的使用燃煤锅炉SNCR与SCR联合法烟气脱硝系统进行烟气脱硝的方法,所述的SNCR还原剂喷射装置设置在温度范围为800-1100°C的烟气通道上。
10.根据权利要求7所述的使用燃煤锅炉SNCR与SCR联合法烟气脱硝系统进行烟气脱硝的方法,其特征在于,所述的SCR脱硝装置设置在温度范围为260-400°C的尾部烟道上。
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