CN1362894A - 选择性催化还原的循环流化床反应器 - Google Patents

选择性催化还原的循环流化床反应器 Download PDF

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CN1362894A
CN1362894A CN01800214A CN01800214A CN1362894A CN 1362894 A CN1362894 A CN 1362894A CN 01800214 A CN01800214 A CN 01800214A CN 01800214 A CN01800214 A CN 01800214A CN 1362894 A CN1362894 A CN 1362894A
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flue gas
efflux
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D·L·维茨克
M·玛亚切克
M·L·西尔维
M·J·斯玛尼亚
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Babcock and Wilcox Co
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Abstract

一种CFB反应器或燃烧器(10),在其下游有选择性催化还原(SCR)系统(150)和干式涤气系统(220),以促进NOx的还原。

Description

选择性催化还原的循环流化床反应器
发明领域
本发明广义上涉及循环流化床(CFB)反应器或燃烧器，具体而言，本发明涉及在其下游使用选择催化还原(SCR)系统的CFB反应器或燃烧器，以增强NOx的还原能力。
发明背景
在设计利用通过燃烧矿物燃料产生蒸汽所得到的热量的蒸汽发生系统时，对固体、液体、气体流出物或排出物的环境保护和控制是关键的因素。目前，最显著的排出物是二氧化硫(SO2)、氮氧化物(NOx)和空中浮游的颗粒。
NOx指一氧化氮(NO)、二氧化氮(NO2)和燃烧时产生的其它痕量物质的积累排出物。一旦选择了燃料，可采用低NOx燃烧技术和后燃烧技术，使NOx排出最少。如果燃烧改善还不够，可以采用后燃烧技术如选择性非催化还原(SNCR)或选择性催化还原(SCR)系统。在SNCR或SCR系统中，通过与注入烟道气(flue gas)中的化学试剂的各种反应，NOx还原为氮(N2)和水(H2O)。氨和尿素是SNCR系统最常用的化学试剂，而氨是SCR系统最常用的化学试剂。
流化床燃烧对燃烧固体燃料和回收能量来产生蒸汽方面具备独特的优点；美国对流化床燃烧研究的主要动力是要降低SO2和NOx的排出。通常，这种技术可用于燃烧高硫煤，可达到低的SO2排出量，而不需要额外的后段除硫设备。流化床锅炉的设计应使床操作温度在1500-1600°F，导致低的NOx排出。这样较低的操作温度还可以燃烧低品位燃料(一般具有高渣和发秽臭的特点)，而不会经历燃烧这类燃料时通常发生的许多操作困难。
CFB反应器或燃烧器中，通过上升的气流将反应性和非反应性固体夹带在反应器封闭区(reactor enclosure)内，该气流将固体带到在反应器封闭区上部的出口。在此，固体通常用冲击型或旋风型初级颗粒分离器收集，并直接或通过一个或多个管道回到反应器封闭区底部，。冲击型初级颗粒分离器在反应器封闭区出口，通常收集90-97％的循环固体。如果需要这种方法，可以在冲击型初级颗粒分离器下游安装另一个固体收集器，收集另外的固体，最终返回到反应器封闭区。
CFB反应器或燃烧器是已知的(例如，参阅美国专利5,343,830(Alexander等))，其中两排或多排冲击部件位于炉内或反应器封闭区内，随后是第二排交叉的冲击部件，进一步从气流中分离颗粒，并通过孔洞装置和颗粒返回装置返回颗粒，而不需要外部和内部的循环管道。
SCR和SNCR系统都已用于还原来自燃烧粉煤产生蒸汽系统的NOx排出物。SNCR系统还应用于流化床蒸汽发生器，并已提出将用于燃烧石油焦的CFB蒸汽发生器和SCR系统结合。
发明概述
本发明广义上涉及循环流化床(CFB)反应器或燃烧器领域，提供了以最低操作成本达到低NOx排出的系统。流化床燃烧方法提供的在燃料进入点的燃烧温度比粉煤燃烧系统低得多(1550-1600°F)，粉煤燃烧系统的燃烧温度为2500-3000°F。燃烧温度的这一差异导致从流化床的未受控制的NOx排出有很大差异。粉煤法的未受控制的NOx排出范围在0.3-0.7 lbs/106Btu，但是流化床法的NOx排出要少数倍，一般在0.12-0.2 lbs/106Btu范围。然而，即使遇到更严格的排放规则，一般在0.10 lbs/106Btu数量级。在有SNCR系统的流化床(在气体温为1450-1650°F位置喷入氨)法，以及在有SCR系统的粉煤法(在气体温度为750°F的位置喷入氨)中达到了这种NOx还原程度。然而，SCR法的经验表明对要求的NOx还原只需要更少的氨，离开该系统的未反应氨小于SNCR法(一般，SCR法为5ppm，SNCR法为25ppm)。由于流化床系统中最初的NOx较低，在SCR系统之后的NOx可以更低，同时只使用最少的催化剂和氨。
因此，本发明的第一方面涉及CFB反应器或燃烧器和SCR系统的结合。这种结合包括用于传送烟道气/固体流通过的CFB反应器附件、用于从烟道气/固体流中分离固体颗粒的初级颗粒分离器和将初级颗粒分离器收集的固体颗粒返回到反应器封闭区内的装置。对烟道气/固体流，至少一个过热器和再热器位于初级颗粒收集器的下游。提供位于至少一个过热器和再热器的热交换面下游的复式旋风粉尘收集器，进一步分离从烟道气/固体流中分离固体颗粒，并提供将复式旋风粉尘收集器收集的固体颗粒返回反应器封闭区内的装置。SCR位于复式旋风粉尘收集器的下游，以除去烟道气/固体流中的NOx，干式涤气器位于SCR系统的下游。最后，提供将氨注入SCR系统上游的烟道气/固体流中的装置，发生还原NOx排出物的化学反应。
在后面的权利要求书和本说明书部分中具体揭示本发明的新颖的特征。为更好地理解本发明，参见附图和对本发明较好实施方案的描述，理解本发明具备的操作优点和达到的特别益处。
附图简述
图1是根据本发明第一实施方案，结合循环流化床(CFB)反应器或燃烧器和SCR系统的示意图。
图2是根据本发明第二实施方案，结合循环流化床(CFB)反应器或燃烧器和SCR系统的示意图。
图3是根据本发明第三实施方案，结合循环流化床(CFB)反应器或燃烧器和SCR系统的示意图。
较好实施方案的描述
本文中，术语CFB燃烧器指其中发生燃烧过程的CFB型反应器。虽然本发明特别涉及使用CFB燃烧器作为产生热量的装置的锅炉或蒸汽发生器，但应理解本发明能够容易应用于不同种类的CFB反应器。例如，本发明可以应用于进行化学反应而不是燃烧过程的反应器，或可将来自发生在别处的燃烧过程产生的气体/固体混合物提供给反应器以进一步的加工、或反应器仅提供将颗粒或固体夹带在气体中的封闭区，该气体不必是燃烧过程的副产物。
为描述CFB反应器和燃烧器的常规操作，可参考40th Edition，Stultz andKitto，Eds，Copyright1992，The Babook & Wilcox Company的蒸汽/其发生和使用的第16章，和美国专利5,343,830(Alexander等)，这两篇文献全文参考结合于此。对涉及NOx还原技术和设备的一般背景资料和具体的选择性催化还原(SCR)系统的资料，还可参考上面提到的蒸汽的第34章内容，该内容也全文参考结合于此。
参见附图，这些附图中同样的参考编号表示同样的部件或功能相同的部件，具体参见附图1-3，所示的循环流化床(CFB)反应器或燃烧器编号为10，包括反应器封闭区20，有上部30。反应器封闭区20的截面通常是长方形，由流体冷却封闭区壁界定，通常包括用钢隔膜彼此分开的水和/或蒸汽传送管，获得气密的封闭区20。
采用本领域技术人员已知的方式，在反应器封闭区20内提供燃料40如煤、吸附剂50如石灰和燃烧空气60。在反应器封闭区20下部发生的燃烧过程产生烟道气/固体流70，向上从反应器封闭区20送出，通过数个除去固体颗粒和热量的阶段(如前面所述)，之后传送到环境大气中。
在位于反应器封闭区20的上部30，在烟道气/固体流70方向提供初级颗粒分离器80，从烟道气/固体流70中收集固体颗粒，使它们返回反应器封闭区20的下部。初级颗粒分离器80较好的包括一排交叉的冲击型颗粒分离器(未标出)。交叉的冲击型颗粒分离器是非平面的，对着进入的烟道气/固体70流动，它们可以是U形、E形、W形或任何呈杯形或凹形表面的形状。或者，初级颗粒分离器80可包括已知构造的旋风分离器(未标出)；这种情况下，一般不提供下游的复式旋风粉尘收集器(下面描述)。
通过L-阀、J-阀或如美国专利5,343,830(Alexander等)中所述的内循环，从烟道气/固体流70除去的固体颗粒90返回反应器封闭区20，附图中仅示意地标出这一返回。
然后，将烟道烟道气/固体流70传送通过一排或多排热交换面，包括过热器(SH)和/或再热器(RH)表面100，之后(图1和2中)进行二级颗粒分离，通常使用复式旋风粉尘收集器(MDC)110。MDC 110除去的固体颗粒120通过管道130返回反应器封闭区20，烟道气/固体70传送至SCR系统150之前，传送通过一排或多排省热器(EC)热交换面140。
或者，如图3所示，可调换MDC110和EC140的位置，使烟道气/固体70从SH/RH100传送到EC 140，然后到MDC 110。附图1-3所示的任一实施方案中，如本领域技术人员所知，EC 140使用的具体数量取决于对进入SCR的烟道气要求的温度，以使操作最优化。由此，和前面一样，烟道气/固体流70传送到SCR150。还在SCR150上游位置提供将氨注入烟道气/固体流70的装置160。
如图2所示，可以合适位置(考虑温度，等等)，在烟道气/固体流70中结合注入尿素或氨，达到使NOx进一步还原。
离开SCR 150时，烟道气/固体70通常传送通过另一排EC表面，为了清楚起见，这次编号为170，然后至已知设计的空气加热装置180。空气加热装置180可以是交流换热型或同流换热型。之后，在烟道气/固体流70方向，提供最后的颗粒收集装置190，该装置包括集尘室或静电沉降器。颗粒收集装置190收集的颗粒200通过管道210也返回到反应器封闭区20。颗粒收集装置190下游还提供了一个干式涤气器系统，一般标号为220，用于从烟道气/固体70捕捉硫。对干式涤气器的描述和其基本操作原理可参考40th Edition，Stultz and Kitto，Eds，Copyright1992，The Babook & Wilcox Company的蒸汽/其发生和使用的第35章该内容全文参考结合于此。最后，排烟机250接受烟道气/固体70，并按已知方式将其输送到烟囱260。
本发明认为在CFB反应器或燃烧器床层中产生的CaO极可能对SCR系统150使用的催化剂不利。MDC 110下游的气体固体可望的分析值范围如下：
         气体分析，体积％                    固体分析，重量％
   CO2             14-15              CaO              4-14
   H2O             7-15               CaSO4           8-16
   O2              3-4                C                6-10
   SO2       0.02-0.04(200-400ppm)    灰*              余量
   N2              余量           (*灰主要组成：SiO2、Al2O3、Fe2O3)
然而，如果使用石灰原料还原硫，烟道气/固体中的CaO含量应较低，因为对给定的硫捕捉，在CFB中的Ca/S比例较低。另外，将干式涤气器用于硫捕捉，可以作为单独的方式或和吸附剂一起送入反应器封闭区20，还对降低进入SCR系统150的任何灰颗粒中的CaO含量有利，从而进一步减少NOx排出，因为CaO起了产生NOx的催化剂的作用。而且，在附图中已标明干式涤气器220位于颗粒收集装置190的下游，调换这两个部件190和220的顺序可能是合乎意愿的，这样可以减少颗粒排出到大气环境，还可以使至少部分包含在烟道气/固体70中的未使用的吸附剂(CaO)通入干式大气器220，因而提供在干式涤气器220中发生的氧化硫还原过程中使用的另外吸附剂来源。
虽然详细描述了本发明的具体实施方案以说明本发明的应用原理，但应理解在不偏离这些原则下本发明还包含其它的内容。例如，本发明可应用于涉及CFB反应器或燃烧器的新的结构，或涉及对现有CFB反应器或燃烧器的修改、替换或变动。本发明的一些实施方案中，使用本发明的一些特征有利，相应不使用其它特征。因此，所有这类变化和实施方案都在下面的权利要求书的范围和等同物内。

Claims (11)

1.一种CFB反应器或燃烧器排列与SCR系统的结合，包括：
用于将烟道气/固体流传送通过的CFB反应器封闭区，用于从烟道气/固体流分离固体颗粒的初级颗粒分离器，和将初级颗粒分离器收集的固体颗粒返回到反应器封闭区的装置；
在初级颗粒分离器下游至少有一个相对于烟道气/固体流的过热器或再热器的热交换面；
复式粉尘收集器，位于至少一个过热器和再热器热交换面的下游，用于从烟道气/固体流进一步分离固体颗粒，以及将复式粉尘收集器收集的固体颗粒返回到反应器封闭区的装置：
SCR系统，位于复式粉尘收集器下游，用于从烟道气/固体流中除去NOx；
干式涤气器，位于SCR系统的下游；和
在SCR系统的上游，将氨注入烟道气/固体流的装置。
2.如权利要求1所述的结合，其特征在于所述初级颗粒分离器包括一排交叉的冲击型颗粒分离器，其截面为U形、E形和W形中的一种。
3.如权利要求1所述的结合，其特征在于所述结合还包括位于SCR系统上游的省热器热交换面，使进入SCR系统的烟道气达到要求的温度。
4.如权利要求1所述的结合，其特征在于所述结合包括位于SCR系统的下游的省热器热交换面和空气加热装置中的至少一种。
5.如权利要求1所述的结合，其特征在于所述结合还包括位于SCR下游的空气加热装置和位于空气加热装置下游的颗粒收集器。
6.如权利要求5所述的结合，其特征在于所述结合还包括将颗粒收集器和干式涤气器从烟道气/固体流收集的固体颗粒返回到反应器封闭区的装置。
7.如权利要求5所述的结合，其特征在于所述颗粒收集器位于空气加热装置下游，它包括集尘室或静电沉降器。
8.如权利要求1所述的结合，其特征在于所述结合还包括在SCR系统的上游，在至少一个过热器和再热器热交换面附近，注入在1450-1650°F的要求温度范围的氨或尿素之一种的装置。
9.如权利要求1所述的结合，其特征在于所述结合还包括在反应器封闭区内至少一个过热器、再热器和锅炉热交换面。
10.如权利要求1所述的结合，其特征在于所述初级颗粒分离器包括旋风分离器。
11.一种CFB反应器或燃烧器排列和SCR系统的结合，包括：
用于将烟道气/固体流传送通过的CFB反应器封闭区，用于从烟道气/固体流分离固体颗粒的初级颗粒分离器，和将初级颗粒分离器收集的固体颗粒返回到反应器封闭区的装置；
在初级颗粒分离器的下游至少有一个相对于烟道气/固体流的过热器或再热器的热交换面；
位于CFB反应器封闭区下游的SCR系统，用于从烟道气/固体流除去NOx；
干式涤气器，位于SCR系统的下游；和
在SCR系统的上游，将氨注入烟道气/固体流的装置。
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