CN101029596A - 部分慢化剂旁路的方法和系统 - Google Patents
部分慢化剂旁路的方法和系统 Download PDFInfo
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Abstract
本发明提供了一种具有部分慢化剂旁路的燃气发生器(56)的方法和系统。该燃气发生器包括部分氧化反应器,该部分氧化反应器包括一入口(260)、一出口(262)以及在两者之间延伸的初始反应区,所述部分氧化反应器被构造以引导部分氧化产品的流体,所述部分氧化产品包括燃料气体、气态的部分氧化副产品以及未燃炭;和第二反应室(228),其与所述部分氧化反应器流体连通并连接,所述第二反应室被构造为把慢化剂流体与气态的部分氧化副产品和未燃炭的流体相混合,从而增大燃料气体的浓度。
Description
技术领域
本发明总体上涉及一种集成式气化复合循环(integratedgasification combined-cycle,简称IGCC)发电系统,更具体地说,涉及采用部分慢化剂旁路提高燃气发生器性能的方法。
背景技术
至少一些公知的IGCC系统包括一气化系统,该气化系统与至少一个发电涡轮系统集成在一起。例如,公知的燃气发生器把燃料,空气或氧气,蒸汽和/或石灰石的混合物转化为部分为氧化气体的输出,有时也叫做“合成气”。该合成气被输送到涡轮机的燃烧室中,该涡轮机驱动发电机,该发电机把电力输送给电力网。至少一些公知的燃气涡轮机的排气被输送给热回收蒸气发生器,该热回收蒸气发生器产生的蒸汽用于驱动蒸汽机。蒸汽机产生的动力也用于驱动向电力网提供电力的发电机。
为了获得可泵送的浆状物浓度,至少一些公知的气化系统给燃气发生器提供过量的水慢化剂。在需要氢含量高的合成气时,也采用过量的水慢化剂。另外,供给燃气发生器的再循环CO2也用来为IGCC提高CO含量(合成气较低热值(LHV))和碳的转化。然而,过量的慢化剂会把合成气冷却到炉渣熔点之下,这会导致比最佳情况下更高的氧气消耗,并且降低合成气产量。
发明内容
在一个实施例中,提供了一种具有部分慢化剂旁路的燃气发生器,该燃气发生器包括部分氧化反应器,该部分氧化反应器包括一入口、一出口以及在两者之间延伸的初始反应区,所述部分氧化反应器被构造以引导部分氧化产品的流体,所述部分氧化产品包括燃料气体、气态的部分氧化副产品以及未燃碳;和第二反应室,其与所述部分氧化反应器流体连通并连接,所述第二反应室被构造为把慢化剂流体与气态的部分氧化副产品和未燃碳的流体相混合,从而增大燃料气体的浓度。
在另一个实施例中,提供了一种在燃气发生器中产生燃料气体的方法,该方法包括对燃气发生器中的燃料进行部分氧化,从而产生部分氧化的产品的流体,该部分氧化的产品包括可流动的炉渣,颗粒物组分和气态组分。该方法还包括从部分氧化产品中除掉可流动的炉渣和一部分颗粒物组分,把慢化剂流体喷射到剩余的部分氧化产品的流体中,从颗粒物组分和慢化剂的混合物中产生燃料气体。
在再另一个实施例中,提供了一种气化系统,其包括压力管,该压力管包括部分氧化反应器,该部分氧化反应器被构造为把部分氧化产品引导向出口通道,所述部分氧化产品包括燃料气体、未燃碳和二氧化碳;以及二氧化碳回收系统,其被构造为从部分氧化产品中回收二氧化碳,并把该二氧化碳作为慢化剂喷射到燃气发生器中,其中压力管还包括,与所述部分氧化反应器流体连通并连接的第二反应室,所述第二反应室被构造为接受二氧化碳流体,与第二反应室流体连通的沉降区,该沉降区被构造为有助于使固态的部分氧化产品从气态的部分氧化产品中分离出来。
附图说明
图1是公知的集成式气化复合循环(IGCC)发电系统的示例性示意图;
图2是可与图1中所示系统一起使用的部分慢化剂旁路燃气发生器的示例性实施例的示意图;
图3是燃气发生器产生燃料气体的示例性方法的流程图。
具体实施方式
图1是集成式气化复合循环(IGCC)发电系统50的示例性示意图。IGCC系统大体包括主空气压缩机52,与压缩机52流体连通的空气分离单元54,与空气分离单元54流体连通的燃气发生器56,与燃气发生器56流体连通的燃气轮机10,以及汽轮机58。在运行时,压缩机52压缩环境空气。压缩空气被输送到空气分离单元54。在一些实施例中,除了压缩机52之外或者替代压缩机52的是,来自燃气轮机压缩机12的压缩空气被供给空气分离单元54。空气分离单元54利用压缩空气产生供燃气发生器56使用的氧气。更具体地说,空气分离单元54把压缩空气分为分离开的氧气流和副产品气体流,有时也叫做“过程气体”。空气分离单元54产生的过程气体包括氮气,在此将其称为“氮气过程气体”。该氮气过程气体也可以包括其他气体,例如但不限于氧气和/或氩气。例如,在一些实施例中,氮气过程气体包括大约95%到大约100%的氮气。氧气流输送给燃气发生器56,用于产生部分氧化气体,在此称为“合成气”,其被燃气涡轮机10用做燃料,这将在下文中详细描述。在一些公知的IGCC系统50中,氮气过程气体气流中的至少一些和空气分离单元54的副产品被排向大气。另外,在一些公知的IGCC系统50中,氮气过程气体气流中的一些被喷射到燃气轮机燃烧室14内的初始反应区(未示出),从而有利于控制发动机10的排放,更具体地,有利于降低燃烧温度和减少从发动机10排出的氧化亚氮排放物。IGCC系统50可以包括压缩机60,用于在氮气过程气体气流被喷射到初始反应区之前对其进行压缩。
燃气发生器56把燃料,空气分离单元54提供的氧气,蒸汽和/或石灰石的混合物转化为合成气的输出,该合成气用做燃气轮机10的燃料。尽管燃气发生器56可以采用各种燃料,在一些公知的IGCC系统50中,燃气发生器56采用煤、油焦、残油、乳化油、沥青砂和/或其他类似的燃料。在一些公知的IGCC系统50中,燃气发生器56产生的合成气包括二氧化碳。燃气发生器56产生的合成气可以在输送给燃气轮机燃烧室14燃烧之前被净化装置62所净化。在一些公知的IGCC系统50中,在净化过程中,二氧化碳可以从合成气中被分离出来并被排到大气中。燃气轮机10输出的动力驱动发电机64,该发电机向电力网(未示出)提供电力。燃气轮机10的排出气体被提供给热回收蒸气发生器66,该热回收蒸气发生器产生的蒸汽用于驱动蒸汽机58。蒸汽机58产生的动力驱动向电力网提供电力的发电机68。在一些公知的IGCC系统50中,热回收蒸气发生器66的蒸汽被提供给燃气发生器56用于产生合成气。
图2是可与系统50(示于图1)一起使用的部分慢化剂旁路燃气发生器200的示例性实施例的示意图。在该示例性实施例中,燃气发生器200包括上壳体202,下壳体204和在两者之间延伸的基本圆筒形的管体206。供料喷射器208插入上壳体202从而把燃料流导入燃气发生器200。通过供料喷射器208中的一个或多个通道输送燃料,并通过喷嘴210把燃料以预定模式212排入燃气发生器200内的初始反应区214。燃料在进入喷嘴210之前可以与其他物质混合,或者在从喷嘴210喷射的同时与其他物质混合。例如,燃料在进入喷嘴210之前可以与从系统50的过程回收的细粉(fines)混合,也可以在喷嘴210或喷嘴210的下游处使燃料与氧化剂例如空气或氧气混合。
在该示例性的实施例中,初始反应区214与喷嘴210在垂直方向对齐、基本圆筒形空间联合排列,并串联流体连通。初始反应区214的外周被耐火壁216限定,该耐火壁包括结构基质,例如耐热镍铬铁合金管218和耐火层220,它们被构造以耐受初始反应区214内的相对高温作用和高压作用。耐火壁216的出口端222包括收敛的出口喷嘴224,其被构造为保持初始反应区214内的预定回压,与此同时允许初始反应区214内产生的部分氧化产物和合成气从初始反应区214排出。部分氧化产物包括气态副产品、大体在耐火层220上形成的炉渣、未燃碳以及气态副产品中悬浮夹带的细小颗粒物。
可流动的炉渣和致密炉渣从初始反应区214排出后,在重力作用下降落到下壳体204中的活底料斗(lockhopper)226内。活底料斗226被一定水位的水所保持,所述水使可流动的炉渣骤冷变为脆性固体材料,这样在从燃气发生器200排出后可以被粉碎为较小的颗粒。活底料斗226还从初始反应区214排出的细小颗粒中捕获大约百分之九十的颗粒。
在示例性的实施例中,环形反应室228至少部分地围绕着初始反应区214。第二反应室228被内周上的耐火壁216和该第二反应室228径向外周上的圆筒状壳体230所限定,其中圆筒状壳体230与初始反应区214同轴布置。第二反应室228在其顶部被顶部凸缘232关闭。气态副产品、未燃碳以及剩下的百分之十的细小颗粒物在初始反应区214内沿向下的方向234输送,而在第二反应室228内沿向上的方向236输送。在喷嘴224出口处的快速变向使得细小颗粒物和炉渣从气态副产品中分离出来。
随着气态副产品、未燃碳以及剩下的百分之十的细小颗粒物被输送到第二反应室228内,慢化剂流体被加入到该气态副产品、未燃碳以及剩下的细小颗粒物中。慢化剂可以包括CO2和/或水,它们可以是蒸汽的形式。慢化剂缓和第二反应室228的温度。可以在入口260处以喷射的形式把慢化剂加入第二反应室228内,或者在流体流过第二反应室228的方向236上沿第二反应室228的长度分段加入慢化剂。例如,第一部分慢化剂可以通过第一集管262加入第二反应室228,第二部分慢化剂可以通过第二集管264加入第二反应室228,其中第二集管264位于第一集管262的下游。在各种实施例中,第二反应室228内分布着多于两个的集管,从而允许以各种组合把慢化剂分段引入,从而与燃气发生器200内的不同运行条件相适应。在示例性的实施例中,在第二反应室228内,慢化剂中的CO2与未燃碳在吸热反应中结合生成CO,该吸热反应把第二反应室228内的一部分热能转化为生成的CO中的化学能。例如,气态副产品、未燃碳以及剩下的细小颗粒物从部分氧化反应器214进入第二反应室228的温度是大约2500°华氏度,从第二反应室228排出的温度是大约1800°华氏度。慢化剂中的CO2可以从燃气发生器排出的合成气中被回收,或者可以在系统50的另一过程中被再循环。
气态副产品以及剩下的百分之十的细小颗粒物通过第二反应室228向上被输送到第一通道出口238。在输送通过第二反应室228的气态副产品的过程中,可以从气态副产品和细小颗粒物中回收热量。例如,气态副产品进入第二反应室228的温度是大约2500°华氏度,从第二反应室228排出时该气态副产品的温度是大约1800°华氏度。气态副产品和细小颗粒物通过第一通道出口238排出第二反应室228并进入第二环形通道240,在第一通道出口238处,该气态副产品和细小颗粒物改变方向而向下流动。随着气态副产品和细小颗粒物穿过第二通道240而流动,可以从气态副产品和细小颗粒物的流动中回收热量,例如采用过热管242,该过热管从气态副产品和细小颗粒物的流动中回收热量并把热量传递给流过过热管242的内侧通道的蒸汽。例如,气态副产品进入第二通道240的温度是大约1800°华氏度,从第二通道240排出时的温度是大约1500°华氏度。当气态副产品和细小颗粒物的流体到达第二通道240的底端244时,第二通道240朝着活底料斗226收敛,上述第二通道240的底端244靠着下壳体204。在底端244处,气态副产品和细小颗粒物的流体沿向上的方向穿过水喷雾246,该水喷雾246用于使气态副产品和细小颗粒物的过热流体降温。从气态副产品和细小颗粒物的流体中回收的热量有助于使水喷雾246汽化和使细小颗粒物集结,从而使得细小颗粒物形成相对较大的灰块,该灰块降落到下壳体204内。气态副产品和剩余细小颗粒物的流体沿相反方向被输送,并被引导到带孔板448的下侧,形成环形盘限定的底端244。水位被保持在带孔板448之上,从而为把额外的细小颗粒从气态副产品流体中除去提供接触介质。气态副产品和剩余细小颗粒物的流体向上穿过带孔板448上的穿孔而渗透,细小颗粒物与水接触并在水浴(water bath)中被捕获,并且穿过穿孔而向下被带入下壳体204的水槽中。活底料斗226和下壳体204之间具有间隙250,细小的颗粒物流过该间隙而流向活底料斗226,在活底料斗226处细小颗粒物被从燃气发生器200中除去。
夹带物分离器254围绕着带孔板248上方的下壳体204的上端部以及带孔板248上方的水位。夹带物分离器254可以例如是气旋的或离心的分离器,并包括切向入口或导向叶片,该切向入口或导向叶片给气态副产品和剩余细小颗粒物施加旋涡运动。颗粒物被离心力向外甩到分离器的壁上,细小的颗粒物在分离器壁上聚结并降落到分离器下壳体204的壁上。另外,采用金属丝网形成金属网垫,剩余的细小颗粒物撞击到该金属网垫表面上,与借助重力作用被水喷雾排到下壳体204上的其他颗粒物聚集。另外,夹带物分离器可以是叶片式的,例如人字形分离器或碰撞分离器。在人字形分离器中,气态副产品穿过叶片之间并被迫以之字形的模式运动。夹带的颗粒物和任何液滴无法跟随气流流线,因此它们撞击到叶片表面上、聚结并掉回到下壳体204内。可以给叶片的侧面添加特别的特征,例如钩形和凹形,从而有助于捕获颗粒物和液滴。人字形网格可以一个接一个地堆叠或弯曲,从而提供一系列的分离级。气态副产品和细小颗粒物经过弯曲的叶片时,碰撞分离器产生气旋运动,并且传递旋转运动,该旋转运动使夹带的颗粒物和任何液滴被导向管壁,夹带的颗粒物和任何液滴在管壁上被收集并导向下壳体204。
气态副产品和任何剩余细小颗粒物的流体进入分离器254后,几乎所有剩余的夹带颗粒物和任何液滴都从气态副产品流体中被除掉。气态副产品流体通过出口256从燃气发生器中排出,进行进一步的处理。
图3是燃气发生器产生燃料气体的示例性方法300的流程图。该方法包括对燃气发生器中的燃料进行部分氧化302,从而产生部分氧化的产品的流体,该部分氧化的产品包括可流动的炉渣,颗粒物组分和气态组分。在该示例性实施例中,燃料通常是浆状或液体形式的含碳燃料,例如煤浆或石油。燃料被喷射到部分氧化反应器中,在该反应器中燃料发生不完全燃烧,形成未燃碳。燃料中的矿物形成的可流动炉渣大体上在部分氧化反应器的壁上聚集,并从部分氧化反应器的底部出口流出。部分氧化产品的颗粒物组分被气态组分夹带着离开部分氧化反应器并被带到沉降区。在沉降区,可流动炉渣和一部分颗粒物组分被从部分氧化产品中除掉304。慢化剂流体被喷射306到剩余的部分氧化产品流体中,从颗粒物组分和慢化剂的混合物中产生308燃料气体。在该示例性实施例中,慢化剂包括CO2和/或蒸汽,颗粒物组分包括未燃碳。CO2和未燃碳结合形成CO,其是燃料气体的一种形式。
上文详细描述了气化系统和燃气发生器中产生燃料气体的方法的示例性实施例。文中的气化系统组件并不限于在此描述的具体实施例,每个系统的组件可以单独使用和独立于其他组件而使用。例如,上文描述的气化系统组件也可以与不同的IGCC系统组件组合使用。
尽管以各种具体实施例的方式描述了本发明,但是本领域技术人员将认识到,在权利要求的精神和范围内,可以对本发明进行改进。
Claims (10)
1、一种燃气发生器(200),包括:
部分氧化反应器,其包括一入口(260)、一出口(256)以及在两者之间延伸的初始反应区,所述反应器被构造以引导部分氧化产品的流体,所述部分氧化产品包括燃料气体、气态的部分氧化副产品以及未燃碳;和
第二反应室(228),其与所述部分氧化反应器流体连通地连接,所述第二反应室被构造为把慢化剂流体与气态的部分氧化副产品流体和未燃碳的流体相混合,从而增大燃料气体的浓度。
2、如权利要求1所述的系统(50),还包括至少部分地围绕所述第二反应室(228)延伸的慢化剂喷射集管(262),所述慢化剂喷射集管被构造为引导慢化剂流体,从而有助于慢化剂和部分氧化产品的混合。
3、如权利要求1所述的系统(50),还包括多个慢化剂喷射集管(262,264),每个集管都至少部分地围绕所述第二反应室(228)延伸,每个所述慢化剂喷射集管被构造为引导慢化剂流体,从而有助于慢化剂和部分氧化产品的混合,其中从每个集管对慢化剂的喷射是同时喷射和分段喷射中的至少一种。
4、如权利要求1所述的系统(50),其中所述部分氧化产品包括燃料气体、气态的部分氧化副产品、未燃碳、可流动的炉渣和颗粒物,所述系统还包括与所述部分氧化反应器流体连通的沉降区,所述沉降区被构造以降低部分氧化产品流体的速度,从而有助于从部分氧化产品中除掉可流动的炉渣和至少一部分颗粒物。
5、如权利要求1所述的系统(50),其中通过化学反应提高燃料气体的浓度,所述化学反应把慢化剂中的一部分二氧化碳和部分氧化产品流体中的一部分未燃碳转化为一氧化碳。
6、如权利要求1所述的系统(50),其中通过吸热化学反应提高燃料气体的浓度,所述吸热化学反应把第二反应室(228)中的一部分热能转化为燃料气体的化学能。
7、如权利要求1所述的系统(50),其中,所述第二反应室(228)被构造以接受大约2500°华氏度的处理材料流体,排出大约1800°华氏度的处理材料流体。
8、一种气化系统(50),包括:
压力管,其包括部分氧化反应器,该部分氧化反应器被构造为把部分氧化产品引导向出口通道(238),所述部分氧化产品包括燃料气体、未燃碳和二氧化碳;和
二氧化碳再循环系统,其被构造为从部分氧化产品中回收二氧化碳,并把该二氧化碳作为慢化剂喷射到燃气发生器中;
其中压力管还包括:
第二反应室(228),其与所述部分氧化反应器流体连通地连接,所述第二反应室被构造为接受二氧化碳流体;
与第二反应室流体连通的沉降区,该沉降区被构造为有助于使固态的部分氧化产品从气态的部分氧化产品中分离出来。
9、如权利要求8所述的气化系统(50),还包括至少部分地围绕所述第二反应室(228)延伸的慢化剂喷射集管(262),所述慢化剂喷射集管被构造为引导慢化剂流体,从而有助于慢化剂和部分氧化产品的混合。
10、如权利要求8所述的气化系统(50),其中所述第二反应室(228)还被构造以接受来自沉降区的未燃碳流体,从而使一部分未燃碳与二氧化碳反应形成一氧化碳。
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2005
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2006
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EP1798276A1 (en) | 2007-06-20 |
US8398729B2 (en) | 2013-03-19 |
US20110305609A1 (en) | 2011-12-15 |
JP5137392B2 (ja) | 2013-02-06 |
US20070137103A1 (en) | 2007-06-21 |
US20100043288A1 (en) | 2010-02-25 |
US8038747B2 (en) | 2011-10-18 |
JP2007169151A (ja) | 2007-07-05 |
CN101029596B (zh) | 2011-01-26 |
US7621973B2 (en) | 2009-11-24 |
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