CN1050257A - 流化床蒸汽发生系统和方法 - Google Patents
流化床蒸汽发生系统和方法 Download PDFInfo
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Abstract
一种流化床蒸汽产生系统和方法,其中在炉体部
分附近设有一个外部换热器,来自炉体部分流化床的
烟气和所夹带的颗粒材料混合物被分离,分离后的烟
气通入热回收部分并且分离出的颗粒材料返回炉体
部分的流化床中。炉体部分的流化床中颗粒材料循
环通入外部换热器以对水、蒸汽或蒸汽/水混合物在
材料流回炉体部分之前进一步进行加热,水被通入炉
体部分、热回收部分,外部换热器以使水转变为蒸
汽。
Description
本发明涉及一种流化床蒸汽发生系统及该系统的操作方法,特别是涉及到在系统的炉体部分附近设有一个外部换热器的流化床系统和方法。
流化床蒸汽发生系统是公知的,在这些装置中,为了使燃料能够在流化床上以相当低的温度下燃烧,空气要穿过有颗粒材料的床体,其中包括如煤的矿物燃料以及用于吸附由于煤燃烧产生的硫的吸附剂。通入水与流化床进行热交换以产生蒸汽。燃烧系统中包括一个分离器,用于将夹带来自炉体部分内流化床气体中的固体颗粒材料分离出来并将其送回到床中。这便达到了高燃烧效率、高脱硫率,低氧化氮排放以及燃烧适用性更佳的具有吸引力的综合效果。
在这些种类系统中的炉体内,最典型使用的流化床一般是叫做“鼓泡”流化床,其中床中颗粒材料具有相当高的浓度并且具有分明的或独立的上部表面。其它所用的流化床类型是“循环”流化床,根据这一技术,该流化床的浓度要低于典型的鼓泡流化床。空气速度要等于或大于鼓泡床的空气速度,并且流过流化床的烟气中所夹带的细固体颗粒的量大致处于使烟气基本上饱和的范围内。
同样,循环流化床的特点在于有相对高的固体循环,这使其对燃料放热方式不敏感,减小了温度的变化,有害物排放处于稳定的低水平,这种高固体循环提高了用于将固体从气体中分离的固体循环机械装置的效率,并且增加了脱硫剂和燃料的停留时间,减少了脱硫剂和燃料的消耗。
通常,在循环流化床燃烧系统中,在热的气旋一次固体流中设有一个外部换热器,用于从循环固体中吸收热量以得到相对高的传热率。
但是,在这类设备中,以这种外部换热条件根本不能实现在所有负荷下高温固体循环具有足够高的循环率以满足过热器和/或沸腾工况的需求的设计要求。
因此本发明的目的在于提供一种能克服上述缺点的流化床燃烧系统和方法。
本发明的另一个目的在于提供一种能够满足过热器和/或沸腾工况需求的上述类型的系统和方法。
本发明的又一个目的在于提供一种上述类型的系统和方法,其中在接收来自流化床的热颗粒材料的炉体部分附近设有流化床外部换热器,用于在床材料返回该床这前从中吸收热量。
本发明的再一个目的在于提供一种上述类型的系统和方法,其中外部换热器的换热面是根据工况要求而定。
本发明的更进一步目的在于提供一种上述类型的系统和方法,其中外部换热器的上况可根据其表面流化速度的变化而变化。
为了实现这些和其它目的,本发明的系统包括一个放在系统炉体部分附近的流化床换热器,来自在产生蒸汽的炉体部分内流化床的烟气及所夹带的颗粒材料要被分离,烟气通到热回收区,分离出的颗粒材料被循环回炉体部分,外部换热器接收来自炉床流化的固体,并且在外部换热器内设有用于从流化颗粒中吸热的换热面,外部换热器中的固体随后返回到炉体部分中的流化床中。
上述简要说明,以及本发明的进一步目的、特点和优点在参照下面现有的较佳实施例的详细说明将得到更充分的理解,但根据本发明说明性的实施例,结合附图,仍然仅是对本发明系统的概述性描述。
参照附图,标号10总体表示本发明的流化床蒸汽发生系统,其中包括一个炉体部分12,分离部分14及一个热回收区16。炉体部分12包括一个直角外壳18和一个放在外壳底部末端的风室20,用于接收来自外部气源的气体,如空气。一个空气分配器,或布风板22设在外壳18的下端部和空气风室20之间,用于让压缩空气从风室中向上穿入外壳18内。
颗粒材料被托在空气分配器22上,随着高度而递减其浓度,并沿整个外壳18高度上延伸,一个或多个入口,如入口24,穿过外壳18壁而设置,用于引导颗粒材料进入床体,在空气风室20和压缩空气源之间有管道26,用于将空气置于风室的挡板26a控制下引入风室。来自风室20的空气流化外壳18中的颗粒材料,根据一个优选实施例,空气速度为能形成一个循环流化床的大小,正如以上所述。一个与空气分配22和/或外壳18壁上开口对准的排出管28用于从外壳中排出耗尽的颗粒材料。颗粒材料可以包括煤和吸收材料,如石灰石的相当细的颗粒,用于以众所周知的方式吸收煤燃烧时产生的硫。
应该认为,外壳18的壁包括多个垂直方向延伸布置的水管,并且流动回路(未表示)中管道内通水,以使水转变为蒸汽。由于外壳18的壁是常规的,就不必对其详细说明了。
分离部分14包括一个或多个旋风分离器30,它放在外壳18的附近并通过管32把它们连接在一起,管32从外壳18后壁上形成的开口延伸到分离器30上部形成的开口。分离器30接收来自外壳18内流化床的烟气和所夹带的颗粒材料,并且以常规方式操作利用分离器内产生的离心力将颗粒材料分离。分离过的烟气由分离器30上升并流入热回收区16。
热回收区16包括一个外壳34罩住过热器36、一个再热器38和一个省煤器40,所有这些换热器由一系列沿伸到气体流过外壳34的流道内的换热管42形成。应该认为,构成过热器36,再热器38和省煤器40的管42全部以束状设在入口联箱44a和出口联箱44b之间依次附加到流体回路中,该回路从形成炉体部分12的炉壁的管12起为进一步使加热的水或蒸汽受热而延伸,烟气在流过过热器36,再热器38和省煤器40之后,由壳体34后壁上出口44中排出。
从分离器30中分离出的固体通入漏斗30a,它与分离器底端相连,固体随后进入与漏斗出口相连的浸入管46。它穿过壳18的后壁,用于使分离出的固体排回到流化床中。它有一个为防止固体和/或气体直接由炉体部分12回流到分离器30的U形段46a。
一个外部换热器50被附加在外壳18的前壁,它包括一个容器、或壳体52,其中有换热管54。形成的管束,壳52可以由水冷管壁或耐火金属壳构成,管54在入口联箱54a和出口联箱54b之间延伸,依次以所希望的方式连接到所述流体流动回路中。
为了将来自外壳18内流化床中的固体颗粒输送到壳52中,一个入口管56从外壳18的壁面起延伸到壳52的下部;为了将固体颗粒输回外壳18,一个出口管58从壳52的上部延伸到外壳18的任意壁面上。
为了形成一个空气风室62,在壳52的下部水平延伸方向设有一个空气分配器60。两个管64和66接收来自外部气源的气体,如空气,并且与风室62和入口管56分别连通。外部气源可以是来自炉子下游的烟气。
在管64和66中分别设有控制挡板68a和68b以分别控制进入空气室62和入口管56的空气流。为从壳52中排出粗粒材料,在空气分配器60上设有一排放管70。
热颗粒材料可以经过管56连续地供入壳52中并被经过分配器60的气室62中的空气所流化,为了在颗粒材料和夹带相对细小颗粒的流化空气经过出口管58排出壳52回到外壳18内与其中颗粒混合之前而在壳52中上升时,从中吸热,管54中要通入水。
在运行中,从入口24将颗粒燃料放入外壳18内并且可以根据需要以同样方式导入吸收材料。供入来自外部气源的流化空气,通过管27、气室20,空气分配器22穿过外壳18内的颗粒材料并将其流化。
一个点火燃烧器(未表示),或类似装置被放在管中引向外壳18并且进行点火,以点燃颗粒燃料材料,当材料温度达到可接受的水平时,经过入口管24向外壳18内添加燃料。
外壳18中的材料通过炉体部分12的加热而自燃,并且空气和气体燃烧产物的混合物(以后叫做“烟气”)在外壳18中向上流动,夹带或淘洗外壳中的颗粒材料。经过管26引入气室20流过空气分配器22进入外壳18内部的空气速度根据外壳18内的颗粒材料的尺寸靠调整挡板26a来控制,因此形成循环流化床,例如,颗粒材料被流化到床体的颗粒材料基本上达到夹带和淘洗范围。因此,流入外壳18上部的烟气基本上与颗粒材料达到饱和状态,饱和烟气流到外壳18的上部并且经过管32排出,并流入旋风分离器30中,在分离器30中,固体颗粒材料与烟气分离,前者通入漏斗30a并且经过浸入管46回到外壳18中,在那里与炉体部分12中的颗粒材料混合,由分离器30中来的分离过的清洁烟气向上流并排到热回收区16,以流入外壳34中并在流出出口44到外部设备之前要穿过过热器36、再热器38、省煤器40。
当希望将空气导入管56以使外壳18中的颗粒材料进入壳52中时,打开控制挡板68b。附加空气,在挡板68a的控制下,导入气室62,向上通过空气速度、材料流入壳52中的程度、流化度、在壳52中材料的综合高度均根据需要,分别以变换挡板68a和68b的位置来控制。
在壳52中堆积的颗粒材料至少在充分能盖住管54管束的水平上,被流化空气夹带并带出的一部分颗粒材料,经过管58导回外壳18。
在形成外壳18壁的管中,形成过热器36、再热器38和省煤器40中的换热管42中以及在外部换热器50中的换热管54中通水,以从外壳18中和外部换热器50中的颗粒材料以及从热回收区内烟气中分别吸收热量,把水转变为蒸汽。
通过控制流入壳52中部材料流的比率便可控制通入换热器50的管54中的水或蒸汽的吸热量,而该比率可通过入口管64的挡板64a变化空气流化速度而进行控制。换热管54的联箱54a和54b可以以某种方法连接到流动回路中以向热回收区的水或蒸汽提供热量,例如,过热器36的出口可以连到换热管54的入口联箱54a上以满足对过热器的要求。
Claims (11)
1、一种流化床蒸汽发生系统,包括炉体部分,一个在所述炉体部分内形成的包括有燃料的颗粒材料流动床;一个用于接收夹带的颗粒材料和来自所述炉体部分内的流化床上燃料燃烧形成的烟气混合物并将所述夹带的颗粒材料从所述烟气中分离的分离部分;一个用于连接受所述分离过的烟气的热回收部分;一个用于将从所述分离部分分离出的颗粒材料返回到所述炉体部分流化床中的装置;一个置于所述炉体部分壳体附近的外部换热器;用于将来自所述炉体部分的颗粒材料通入所述外部换热器连接所述炉体部分和所述外部换热器的第一导管装置;用于将来自所述外部换热器中的所述材料流回所述炉体部分而连接所述外部换热器和所述炉体部分的第二导管装置;以及一个以换热关系将水通入与炉体部分和所述外部换热器中颗粒材料及热回收部分经分离的烟气进行换热以使所述水进一步吸热并转变为蒸汽的装置。
2、如权利要求1所述系统,其中还包括有连接所述外部换热器与所述热回收部分的流体流动回路装置。
3、如权利要求1所述系统,其中所述通水装置包含多个在所述炉体部分形成至少一部分壁面的水管。
4、如权利要求1所述系统。其中所述外部换热器组成有:一个外壳,用于分配气体穿过所述外壳内的颗粒材料并将所述颗粒材料流化的装置。
5、如权利要求4所述系统,其中通水装置组成为多个在所述外壳内布置的管子。
6、如权利要求1所述外部换热器,它还包括用于把气体引入用于使所述炉体部分的颗粒材料流入所述外部换热器的所述第一导管装置中的装置。
7、一种产生蒸汽的方法,步骤为:流化在炉体部分内含有燃料的颗粒材料床,将来自所述流化床燃料燃烧的烟气中央夹带的所述颗粒材料从所述烟气中分离出来,将所述经过分离的烟气通入热回收部分,将所述分离出的颗粒材料通回到所述炉体部分的流化床中,把炉体部分与一个外部换热器连接以将所述炉体部分来的颗粒材料通入所述外部换热器,将外部换热器与所述炉体部分连接以将来自所述外部换热器的颗粒材料返回到所述炉体部分,将水以与所述炉体部分和所述外部热交换器的颗粒材料并且以与热回收区的分离过的烟气成换热关系通入,以向所述水供热使之转变为蒸汽。
8、如权利要求7所述方法,还包含将所述外部换热器与所述热回收部分连接的步骤。
9、如权利要求7所述方法,其中所述通水步骤还包括将水通入所述炉体部分的至少一部分壁面中的步骤。
10、如权利要求7所述方法,还包括有将气体分布穿过所述外部换热器中颗粒材料的步骤。
11、如权利要求7所述方法,还包括将气体引入从所述炉体部分到外部换热器去的颗粒材料中以使其流动的步骤。要分别以变换挡板68a和68b的位置来控制。
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US07/386,181 US4947804A (en) | 1989-07-28 | 1989-07-28 | Fluidized bed steam generation system and method having an external heat exchanger |
US386181 | 1989-07-28 |
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Publication Number | Publication Date |
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CN1050257A true CN1050257A (zh) | 1991-03-27 |
Family
ID=23524514
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN90106960A Pending CN1050257A (zh) | 1989-07-28 | 1990-07-28 | 流化床蒸汽发生系统和方法 |
Country Status (7)
Country | Link |
---|---|
US (1) | US4947804A (zh) |
EP (1) | EP0410773B1 (zh) |
JP (1) | JPH0395303A (zh) |
CN (1) | CN1050257A (zh) |
CA (1) | CA1318196C (zh) |
ES (1) | ES2050377T3 (zh) |
PT (1) | PT94830A (zh) |
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CN106052308A (zh) * | 2016-06-15 | 2016-10-26 | 成都昊特新能源技术股份有限公司 | 一种利用汽机乏汽的干燥系统以及干燥方法 |
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US5040492A (en) * | 1991-01-14 | 1991-08-20 | Foster Wheeler Energy Corporation | Fluidized bed combustion system and method having a recycle heat exchanger with a non-mechanical solids control system |
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US5332553A (en) * | 1993-04-05 | 1994-07-26 | A. Ahlstrom Corporation | Method for circulating solid material in a fluidized bed reactor |
US5299532A (en) * | 1992-11-13 | 1994-04-05 | Foster Wheeler Energy Corporation | Fluidized bed combustion system and method having multiple furnace and recycle sections |
US5390612A (en) * | 1993-03-01 | 1995-02-21 | Foster Wheeler Energy Corporation | Fluidized bed reactor having a furnace strip-air system and method for reducing heat content and increasing combustion efficiency of drained furnace solids |
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US5395596A (en) * | 1993-05-11 | 1995-03-07 | Foster Wheeler Energy Corporation | Fluidized bed reactor and method utilizing refuse derived fuel |
US5347954A (en) * | 1993-07-06 | 1994-09-20 | Foster Wheeler Energy Corporation | Fluidized bed combustion system having an improved pressure seal |
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US5735682A (en) * | 1994-08-11 | 1998-04-07 | Foster Wheeler Energy Corporation | Fluidized bed combustion system having an improved loop seal valve |
US5533471A (en) * | 1994-08-17 | 1996-07-09 | A. Ahlstrom Corporation | fluidized bed reactor and method of operation thereof |
US5463968A (en) * | 1994-08-25 | 1995-11-07 | Foster Wheeler Energy Corporation | Fluidized bed combustion system and method having a multicompartment variable duty recycle heat exchanger |
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US5954000A (en) * | 1997-09-22 | 1999-09-21 | Combustion Engineering, Inc. | Fluid bed ash cooler |
FI103582B1 (fi) * | 1997-12-19 | 1999-07-30 | Valtion Teknillinen | Menetelmä metallia sekä orgaanista ainesta sisältävän materiaalin käsittelemiseksi, johon sisältyy metallin erotus |
AT505526B1 (de) * | 2007-08-14 | 2010-09-15 | Univ Wien Tech | Wirbelschichtreaktorsystem |
CN101929672B (zh) * | 2009-06-24 | 2012-10-24 | 中国科学院工程热物理研究所 | 一种u形水冷返料器 |
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ITRM20130029A1 (it) * | 2013-01-18 | 2014-07-19 | Magaldi Power Spa | Impianto e metodo di estrazione e raffreddamento di ceneri con incremento dell'efficienza complessiva di caldaia. |
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US20170356642A1 (en) * | 2016-06-13 | 2017-12-14 | The Babcock & Wilcox Company | Circulating fluidized bed boiler with bottom-supported in-bed heat exchanger |
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KR101984542B1 (ko) * | 2017-12-21 | 2019-06-03 | 한국에너지기술연구원 | 압력과 밀도 차이를 이용하는 유동층 고체순환장치, 및 그 고체순환장치를 갖는 유동층 반응시스템 및 고체순환방법 |
KR102093302B1 (ko) * | 2018-07-19 | 2020-04-23 | 한국생산기술연구원 | 복수의 라이저부를 구비한 유동사 하강형 순환유동층 보일러 및 이의 운전방법 |
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US4227488A (en) * | 1978-10-03 | 1980-10-14 | Foster Wheeler Energy Corporation | Fluidized bed unit including a cooling device for bed material |
JPS581741B2 (ja) * | 1979-07-20 | 1983-01-12 | 株式会社日立製作所 | ミクロセル用マスクを備えたセルホ−ルダ |
DE3112120C2 (de) * | 1981-03-27 | 1986-08-07 | Deutsche Babcock Ag, 4200 Oberhausen | Wirbelschichtfeuerung mit einem Aschekühler |
DE3125849A1 (de) * | 1981-07-01 | 1983-01-20 | Deutsche Babcock Anlagen Ag, 4200 Oberhausen | Dampferzeuger mit zirkulierender atmosphaerischer oder druckaufgeladener wirbelschichtfeuerung sowie verfahren zu seiner regelung |
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-
1989
- 1989-07-28 US US07/386,181 patent/US4947804A/en not_active Expired - Lifetime
- 1989-09-26 CA CA000613274A patent/CA1318196C/en not_active Expired - Fee Related
-
1990
- 1990-07-26 PT PT94830A patent/PT94830A/pt not_active Application Discontinuation
- 1990-07-27 ES ES90308239T patent/ES2050377T3/es not_active Expired - Lifetime
- 1990-07-27 JP JP2198070A patent/JPH0395303A/ja active Pending
- 1990-07-27 EP EP90308239A patent/EP0410773B1/en not_active Revoked
- 1990-07-28 CN CN90106960A patent/CN1050257A/zh active Pending
Cited By (4)
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CN103732316A (zh) * | 2011-05-04 | 2014-04-16 | 南方公司 | 运输氧-燃烧器中的氧燃烧 |
CN103732316B (zh) * | 2011-05-04 | 2016-02-10 | 南方公司 | 运输氧-燃烧器中的氧燃烧 |
CN106052308A (zh) * | 2016-06-15 | 2016-10-26 | 成都昊特新能源技术股份有限公司 | 一种利用汽机乏汽的干燥系统以及干燥方法 |
CN106052308B (zh) * | 2016-06-15 | 2018-11-13 | 成都昊特新能源技术股份有限公司 | 一种利用汽机乏汽的干燥系统以及干燥方法 |
Also Published As
Publication number | Publication date |
---|---|
US4947804A (en) | 1990-08-14 |
JPH0395303A (ja) | 1991-04-19 |
EP0410773A3 (en) | 1991-03-27 |
EP0410773A2 (en) | 1991-01-30 |
ES2050377T3 (es) | 1994-05-16 |
EP0410773B1 (en) | 1994-01-19 |
CA1318196C (en) | 1993-05-25 |
PT94830A (pt) | 1992-03-31 |
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