CN1530166A - 具有低压降的间歇混合器 - Google Patents
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Abstract
一热混合器降低供应到织物过滤器的废气的温度。两个喷雾干燥吸收器运行来冷却废气。一混合器的外壳具有一用于来自吸收器的废气的第一和第二入口通道,一用来将废气供应到织物过滤器的出口通道,以及一混合通道。一组阻尼翼片在混合通道内延伸,并具有一混合位置,如果其中一个吸收器不在运行,以便以相对高的压降但低的温度混合来自于入口通道的废气,并将混合气体供应给出口通道。翼片具有一非混合位置,当两个吸收器都在运行时,以便不经混合以低的压降通过废气。本发明也可用来改进起初具有不同的化学成分或颗粒承载量的组合气体流的混合。
Description
技术领域
本发明一般涉及间歇地混合两种或多种气体流,具体来说,涉及一种新颖和有用的装置,在热气体超过织物过滤器的安全操作温度之上时的时间过程中,其用来在相对热和冷的废气供应到一织物过滤器之前将它们彼此混合。
背景技术
干法涤气是对从电站锅炉释放的废气中去除SO2的湿法涤气的最主要的更替。有时干法涤气也称之为喷雾吸收、喷雾干法或半湿法涤气。它包括将一高度雾化的碱性试剂的浆液或水溶液喷雾到热废气中,由此,吸收SO2并绝热地冷却废气。与湿法涤气装置不同,一干法涤气器,或喷雾干燥器吸收器定位在一诸如静电聚尘器或织物过滤器之类的集尘器前。一织物过滤器,或袋式集尘室在冷却的废气通过过滤器材料时收集干的颗粒物质。
由Babcock&Wilcox出版的
STEAM/其产生和应用(第40期)中,在32-9,33-7至33-93和35-11至35-15页,揭示各种涉及织物过滤器和干法涤气器的细节,本文援引在此以作充分的阐述。
喷雾干燥器吸收器的应用一般地限制在从大致200MWe的电厂排放的废气量。较大的电厂要求使用若干个功能块来处理全部的废气流。在一个SDA脱机取出作维护保养其间的过程中,由两个或多个SDA(喷雾干燥器吸收器)输送的袋式集尘室可暴露在超过袋的材料最大允许温度的温度下的气体中。喷雾吸收器必须定期地(例如,两个月)关机,以对必须移去的或至少还可继续工作的雾化器作维护保养。干燥器吸收器也会发生故障。在此异常时间的过程中,通过退役的SDA的废气将不能充分地得到冷却来通过下面的织物过滤器结构,以求取出颗粒,因为气体的高温会损坏织物。
这样的异常时期不应造成整个锅炉或炉子或其它的重要措施的关闭。本发明寻求解决这样的问题。
为了将进入袋式集尘室的高温气体的量减到最小,本发明提出—可调整的热混合、阻尼翼的装置和方法。
在正常运行过程中,两种废气流相同,装置中的混合阻尼器完全打开,且不变化流动的方向。在一个SDA运行中断的过程中,其中,废气温度远高于正常过程,阻尼器移至促进两种气体流混合的一种结构。
在现有技术中,利用水喷雾,空气诱导,或利用废气旁路来进行织物过滤器的热保护。
2002年6月27日出版的授予DeSellem的美国专利申请2002/0079374,公开一用于废气温度控制的锅炉内部废气旁路阻尼器,其允许调整最后一排热交换器表面的热传递效率,以便控制流过废气通道和从废气通道退出以及传输到具有最低运行温度的下游装置的废气的温度。在起动的过程中利用一旁路的模式来防止对织物过滤器的损坏,已公开在授予Roth的美国专利4,322,224中。授予Miller等人的美国专利4,523,931也公开一用于气体旁路的模式。授予Gude等人的美国专利4,372,926公开用来加热供应给袋式集尘室的混合气体的气体的混合。授予Dryden的美国专利5,953,898公开一位于用来控制温度的陶瓷过滤器上游的专用的热交换器。对于其它的废气处理方案可参见授予Peterson等人的美国专利4,452,765,授予Martinelli的美国专利5,599,508和授予Myers等人的美国专利5,651,948,对于用于废气的弧形叶片旁路结构,可参见授予Greene的美国专利6,257,155。
其它对织物过滤器提供热保护的更为通用的方法是使用较高温度等级的袋子。然而,这些袋子比较昂贵且可能不能起到很好的作用。因此,一种能使用廉价的低温度要求的袋子同时将压降降到最低的方法和装置在工业界内是受欢迎的。
发明内容
本发明的目的是提供一呈混合器形式的装置,其减小供应给织物过滤器的废气的温度。操作两个或多个喷雾干燥器吸收器来冷却废气。混合器的外壳具有用于从吸收器出来的气体的第一和第二入口通道,用于到织物过滤器的气体的出口通道,以及一混合通道。一组阻尼翼片沿混合通道延伸,并对混合从入口通道出来的废气具有一混合的位置,如果其中一个吸收器不在工作,其以相对高的压降但低的温度将混合的气体供应到出口通道。当两个吸收器在工作时,它们对不混合气体的通道具有一非混合的位置,并以低的压降供应气体。
本发明的另一目的是提供一种方法,当其中一个吸收器不在运行冷却通过其中的气体时,该方法用来减小从两个喷雾干燥器吸收器供应到一织物过滤器的废气的温度。
本发明的另一目的是提供一种方法,其混合两种气体流,使合成的气体流的气体成分更加均匀。
本发明的另一目的是提供一种方法,其混合载有颗粒的气体和其它的气体,以便获得一具有更加均匀截面颗粒载荷的合成的气体流。
表征本发明新颖性的各种特征在附后的和构成本说明书一部分的权利要求书中特别地予以指出。为了更好地理解本发明,参照附图和其中阐述本发明的优选实施例的描述性的文字,通过本发明的应用达到其运行的诸多优点和特定的目的。
附图的简要说明
在形成本说明书一部分的附图中,全部附图中所示的相同标号表示相同的或对应的零件,其中:
图1是一呈非混合的、低压降结构的根据本发明的混合器的示意的俯视平面图;
图2是一类似于图1的呈混合的、高压降结构的混合器的视图;
图3是一呈非混合结构的本发明的一实施例的示意的立体图;
图4是一呈混合结构的本发明的另一实施例的放大的立体图;
图5是一呈混合结构的图2的实施例的一变体的放大的立体图;以及
图6是一也呈混合结构的图2的实施例的另一变体的放大的立体图。
具体实施方式
现参照诸附图,其中,使用相同的标号来表示相同的或类似的元件,本发明是图1中的一用来混合两种气体流的混合器10,例如,其用来降低供应到一诸如袋式集尘室12的织物过滤器的废气的总的温度。包含有织物的这样的过滤器具有一最大的温度容限,例如,对于低成本的袋子,约为250华氏度。
废气来自于至少两个喷雾干燥器吸收器14和16,它们各自以已知的方式运行来冷却通过其间的废气。
混合器10包括一外壳,它具有一用于来自第一喷雾干燥器吸收器14的废气的第一入口通道18,一用于来自第二喷雾干燥器吸收器16的废气的第二入口通道20,一用来将来自第一和第二喷雾干燥器吸收器的废气供应到织物过滤器或袋式集尘室12的出口通道22,以及一介于入口通道18、20和出口通道22之间的混合通道24。
多个阻尼翼片26至少部分地横贯混合通道而延伸,并具有如图2和4-6所示的一混合位置,以便在混合通道内以相对高的压降将来自于第一和第二入口通道18、20的废气混合在一起,并将混合气体供应给出口通道22。翼片26还具有如图1和3所示的非混合位置,以便不经混合通过来自于第一和第二入口通道18、20的废气,并以相对低的压降将未混合的气体供应给出口通道22。
至少一个致动器30连接到翼片26上,当其中一个喷雾干燥器吸收器不在运行冷却通过其间的废气时,致动器用来将翼片26移动到混合位置,这样,混合的废气的温度是已经冷却的气体和尚未冷却的气体的温度的中间值。当第一和第二入口通道18、20均接收冷却的废气时,致动器30还将翼片26移动到非混合的位置。
如所有附图明显地所示,混合通道具有一纵向轴线,而每个入口通道18、20以与混合通道的纵向轴线相交一锐角的角度延伸,例如,10至90度,但较佳地是45度。
例如,混合通道24的轴线可在如图3所示的入口通道18、20和出口通道22之间垂直地倾斜。一个或多个弧形的折流翼片32也可设置在各个入口通道18、20内,以便将废气转向朝向翼片26,并将压降降到最小。
在非混合位置上的翼片26互相平行和间隔开,例如,在如图3所示的非混合位置中,各翼片位于一平行于混合通道轴线的平面内。在本发明的优选实施例中,诸翼片26从混合通道的底部延伸到顶部,且诸翼片横贯混合通道彼此水平地间隔开。
如图2、4、5和6所示,处于混合位置的翼片26与混合通道的轴线相交一锐角的角度。在图5和6的实施例中,处于混合位置的翼片26设置在至少两个垂直地间隔的水平上,位于一个水平上的翼片的夹角不同于位于另一水平上的翼片夹角。在图5中,翼片26位于两个水平126和226,而在图6中,翼片26位于四个水平126、226、326和426。
在图2中,处于混合位置的翼片26分叉成至少两个交成不同锐角的部分,这样,在垂直的平面图中,成对的翼片形成一X形。
可使用已知设计的致动器来实现混合的位置。例如,各个翼片或翼片部分可安装在一带有伺服电机的垂直轴上,或连接到各轴上,以便转动该轴。
在图4中,诸翼片26沿着混合通道的轴线彼此分隔开地设置成至少两组。然而,当根据数学模型实施试验来验证本发明的有效性时,本发明的该实施例不如其它实施例那样成功。
根据对新的运行单元(Tucson Electric’s Springerville单元#3)提出的SDA-袋式集尘室的废气运行的计算流体动力模型,被开发来评估本发明的有效性。各个模型包括一个在160华氏度的SDA流和另一个在270华氏度的SDA流,废气流量(~6.23Mlb/hr),特性取自KCP&L Hawthorne Station的数据。袋式集尘室的压降假定为6英寸水柱高,并在模型中用一损失因子近似(虽然实际的袋式集尘室结构并未呈现)。为了确定如上所述的混合装置是否可行,检查了十种不同阻尼翼片的混合结构,图3-6是代表性的翼片结构。
对于每个考虑的混合装置,检查废气流的混合和热力曲线。在袋式集尘室入口处,重要的参数是:最大废气温度、平均温度(所有情形均约为215华氏度)的标准偏差,以及进入到250华氏度(对于低成本袋子的最大允许温度)以上的袋式集尘室的流量百分比。
根据气体温度用彩色显示的废气的流线,以及在袋式集尘室入口平面处的气体等温线显示出各实施例的有效性。其中一个这样的绘图(未示出)清楚地证实,在阻尼翼片完全打开的情形中(非混合的位置—基本上等同于无阻尼翼片)冷和热流为层流,且混合非常微乎其微。在袋式集尘室入口平面处的最大温度是267华氏度。温度分布的标准偏差是43华氏度,进入袋式集尘室的大的百分比的气体流(35%)处于大于250华氏度的温度。
图4的实施例的另一温度等温线图显示该两级阻尼翼片结构不是非常有效。流动从一侧推向另一侧,并未很好地混合。在袋式集尘室入口平面处的最大温度是263华氏度。温度分布的标准偏差是40华氏度,进入袋式集尘室的大于27%的气体流处于大于250华氏度的温度。在此结构上的压力损失是1.8英寸水柱,大于在完全打开的结构上的压力损失。
图5中的带有两个水平的单级阻尼翼片显示更为有效。各翼片分裂而允许顶部226倾斜成一方向(45度,完全打开),底部126倾斜成偏离顶部226为90度。当气体的顶层朝向右(从上观看)时,这形成一低压区域,其在朝向左之后允许气体的底层向上运动。以相同的方式,气体的顶层在其朝向右侧运动之后可向下运动。这种类型的结构产生废气的漩涡运动,因此,提供基本上更彻底的混合。在袋式集尘室入口平面处的最大温度是261华氏度。其比上述结构略有改进。在袋式集尘室入口处的温度的标准偏差仅为18华氏度,其表明在该平面内有一更为均匀的温度分布。进入袋式集尘室的仅有5%的气体流处于大于250华氏度的温度,它是得自于上述结构的一根本的改进。此外,压力损失减小到0.65英寸水柱,大于在完全打开的结构上的压力损失。
图6中的带有四个水平的垂直单级阻尼翼片的结构也提供非常良好的混合。在袋式集尘室入口平面处的最大温度已减小到256华氏度。在袋式集尘室入口处的温度的标准偏差是19华氏度,近似与上述情形中相同。处于大于250华氏度温度的进入袋式集尘室的气体流的百分比是6%,它也近似与上述情形中相同。压力损失是0.69英寸水柱,大于在完全打开的结构上的压力损失。
尽管以上已经显示和描述了本发明的特定的实施例和/或细节,以此来说明本发明的原理的应用,但应该理解的是,本发明可体现为如权利要求书中更为完整地描述的,或者,在不脱离这些原理的前提下,如本技术领域内的技术人员所熟知的其它的形式(包括任何的和所有的等价物)。例如,除了提供在不同温度处的气体流的热混合之外,本发明也可用来提供对具有不同化学成分或颗粒载荷的气体流的改进的混合。尽管它们在许多混合应用中是重要的特征,但它们在用一退役的涤气器以使去除袋式集尘室中的附加的SO2的可能性达到最大的操作中,显现尤其重要。
Claims (36)
1.一用来混合两种气体流的混合器,其包括:
一外壳,其具有一对于第一气体的第一入口通道,一对于第二气体的第二入口通道,一对于混合的第一和第二气体的出口通道,以及一介于诸入口通道和出口通道之间的混合通道,混合通道具有一轴线;
多个阻尼翼片,其至少部分地横贯混合通道延伸,并具有一将从第一和第二入口通道出来的废气混合在一起的混合的位置,以便将在混合通道内相对高压降的混合的气体供应给出口通道,翼片具有一非混合的位置,以便使来自第一和第二入口通道的气体未经混合地通过,将相对低压降的未混合的气体供应给出口通道;以及
连接到翼片的致动器装置,当需要混合时,该装置移动翼片到混合的位置,当不需要混合时,致动器装置移动翼片到非混合的位置。
2.如权利要求1所述的混合器,其特征在于,混合通道具有一轴线,各个入口通道与混合通道的轴线相交成一锐角延伸。
3.如权利要求2所述的混合器,其特征在于,混合通道的轴线在入口通道和出口通道之间垂直地倾斜。
4.如权利要求2所述的混合器,其特征在于,在各个入口通道内包括至少一个弧形的折流翼片,用来朝向翼片转向废气。
5.如权利要求1所述的混合器,其特征在于,在非混合位置的诸翼片互相平行并彼此间隔,各翼片在非混合位置位于平行于混合通道的轴线的平面内。
6.如权利要求5所述的混合器,其特征在于,各翼片从混合通道的底部到顶部延伸,诸翼片水平地横贯混合通道彼此间隔。
7.如权利要求5所述的混合器,其特征在于,在混合位置的诸翼片与混合通道的轴线相交成锐角。
8.如权利要求7所述的混合器,其特征在于,在混合位置的诸翼片设置在至少两个水平上,一个水平上的翼片相比另一水平上的翼片处于不同的锐角。
9.如权利要求8所述的混合器,其特征在于,在混合位置的诸翼片仅设置成两个水平高度。
10.如权利要求8所述的混合器,其特征在于,在混合位置的诸翼片设置成四个水平高度。
11.如权利要求7所述的混合器,其特征在于,在混合位置的诸翼片分叉成至少两个部分,它们处于不同的锐角。
12.如权利要求7所述的混合器,其特征在于,诸翼片设置成至少两组,它们沿着混合通道的轴线彼此间隔。
13.一用来降低供应到包含具有一最大温度容限的织物的织物过滤器的废气的总温度的热混合器,废气由至少两个喷雾干燥吸收器供应,吸收器各自运行冷却通过其中的废气,该混合器包括:
一外壳,它具有一用于来自第一喷雾干燥器吸收器的废气的第一入口通道,一用于来自第二喷雾干燥器吸收器的废气的第二入口通道,一用来将来自第一和第二喷雾干燥器吸收器的废气供应到一织物过滤器的出口通道,以及一介于诸入口通道和出口通道之间的混合通道,混合通道具有一轴线;
多个阻尼翼片,它们至少部分地横贯混合通道延伸,并具有一混合位置,以便将来自于第一和第二入口通道的废气混合在一起,并将在混合通道内的相对高压降的混合气体供应给出口通道,翼片具有一非混合位置,以便不经混合通过来自于第一和第二入口通道的废气,并以相对低的压降将未混合的气体供应给出口通道;以及
致动器装置,它连接到翼片上,当其中一个喷雾干燥器吸收器不在运行冷却通过其间的废气时,致动器用来将翼片移动到混合位置,这样,混合的废气的温度是已经冷却的废气和尚未冷却的废气的温度的中间值,当第一和第二入口通道接收冷却的废气时,致动器装置将翼片移动到非混合的位置。
14.如权利要求13所述的热混合器,其特征在于,混合通道具有一轴线,各入口通道与混合通道的轴线相交成一锐角延伸。
15.如权利要求14所述的热混合器,其特征在于,混合通道的轴线在入口通道和出口通道之间垂直地倾斜。
16.如权利要求14所述的热混合器,其特征在于,在各个入口通道内包括至少一个弧形的折流翼片,用来朝向翼片转向废气。
17.如权利要求13所述的热混合器,其特征在于,在非混合位置的诸翼片互相平行并彼此间隔,各翼片在非混合位置位于平行于混合通道的轴线的平面内。
18.如权利要求17所述的热混合器,其特征在于,各翼片从混合通道的底部到顶部延伸,诸翼片水平地横贯混合通道彼此间隔。
19.如权利要求17所述的热混合器,其特征在于,在混合位置的诸翼片与混合通道的轴线相交成锐角。
20.如权利要求19所述的热混合器,其特征在于,在混合位置的诸翼片设置在至少两个水平上,一个水平上的翼片相比另一水平上的翼片处于不同的锐角。
21.如权利要求20所述的热混合器,其特征在于,在混合位置的诸翼片仅设置成两个水平高度。
22.如权利要求21所述的热混合器,其特征在于,在混合位置的诸翼片设置成四个水平高度。
23.如权利要求19所述的热混合器,其特征在于,在混合位置的诸翼片分叉成至少两个部分,它们相交成不同的锐角。
24.如权利要求19所述的热混合器,其特征在于,诸翼片设置成至少两组,它们沿着混合通道的轴线彼此间隔。
25.一用来降低供应到包含具有一最大温度容限的织物的织物过滤器的废气的总温度的热混合方法,废气由至少两个喷雾干燥吸收器供应,吸收器各自运行冷却通过其中的废气,该方法包括:
提供一外壳,它具有一用于来自第一喷雾干燥器吸收器的废气的第一入口通道,一用于来自第二喷雾干燥器吸收器的废气的第二入口通道,一用来将来自第一和第二喷雾干燥器吸收器的废气供应到一织物过滤器的出口通道,以及一介于入口通道和出口通道之间的混合通道;
提供多个阻尼翼片,它们至少部分地横贯混合通道延伸,并具有一混合位置,以便将来自于第一和第二入口通道的废气混合在一起,并将在混合通道内的相对高压降的混合气体供应给出口通道,翼片具有一非混合位置,以便不经混合通过来自于第一和第二入口通道的废气,并以相对低的压降将未混合的气体供应给出口通道;
当其中一个喷雾干燥器吸收器不在运行冷却通过其间的废气时,将翼片移动到混合位置,这样,混合的废气的温度是已经冷却的废气和尚未冷却的废气的温度的中间值;以及
当第一和第二入口通道接收冷却的废气时,将翼片移动到非混合的位置。
26.如权利要求25所述的方法,其特征在于,混合通道具有一轴线,各入口通道与混合通道的轴线相交成一锐角延伸。
27.如权利要求26所述的方法,其特征在于,混合通道的轴线在入口通道和出口通道之间垂直地倾斜。
28.如权利要求26所述的方法,其特征在于,在各个入口通道内包括朝向翼片折流的废气。
29.如权利要求25所述的方法,其特征在于,在非混合位置的诸翼片互相平行并彼此间隔,各翼片在非混合位置位于平行于混合通道的轴线的平面内。
30.如权利要求29所述的方法,其特征在于,各翼片从混合通道的底部到顶部延伸,诸翼片水平地横贯混合通道彼此间隔。
31.如权利要求30所述的方法,其特征在于,在混合位置的诸翼片与混合通道的轴线相交成锐角。
32.如权利要求30所述的方法,其特征在于,在混合位置的诸翼片设置在至少两个水平上,一个水平上的翼片相比另一水平上的翼片处于不同的锐角。
33.如权利要求31所述的方法,其特征在于,在混合位置的诸翼片仅设置成两个水平高度。
34.如权利要求32所述的方法,其特征在于,在混合位置的诸翼片设置成四个水平高度。
35.如权利要求32所述的方法,其特征在于,在混合位置的诸翼片分叉成至少两个部分,它们相交成不同的锐角。
36.如权利要求32所述的方法,其特征在于,诸翼片设置成至少两组,它们沿着混合通道的轴线彼此间隔。
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CN102089064B (zh) * | 2008-07-10 | 2013-07-17 | 阿尔斯托姆科技有限公司 | 喷雾干燥器吸收器的分散器布置 |
CN101954252A (zh) * | 2010-10-27 | 2011-01-26 | 东莞市力宇燃气动力有限公司 | 一种低压降气体混合系统 |
CN101954252B (zh) * | 2010-10-27 | 2012-04-18 | 东莞市力宇燃气动力有限公司 | 一种低压降气体混合系统 |
CN104676862A (zh) * | 2015-01-20 | 2015-06-03 | 森德(中国)暖通设备有限公司 | 混风装置 |
CN104676862B (zh) * | 2015-01-20 | 2017-09-29 | 森德(中国)暖通设备有限公司 | 混风装置 |
Also Published As
Publication number | Publication date |
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CA2459643C (en) | 2008-08-26 |
US20040182052A1 (en) | 2004-09-23 |
US7291194B2 (en) | 2007-11-06 |
US6946011B2 (en) | 2005-09-20 |
US20050274413A1 (en) | 2005-12-15 |
US20050268964A1 (en) | 2005-12-08 |
CN100386137C (zh) | 2008-05-07 |
US7288128B2 (en) | 2007-10-30 |
CA2459643A1 (en) | 2004-09-18 |
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