CN102959202B - 集成系统、发电的方法和联合循环发电系统 - Google Patents
集成系统、发电的方法和联合循环发电系统 Download PDFInfo
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Abstract
提供了在烃回收工艺中用于低排放发电的方法和系统。一个系统包括燃气轮机系统,其设置为在压缩的再循环排气存在下化学计量燃烧压缩的氧化剂和燃料,并且在膨胀器中使排放物膨胀以产生气态排气流和驱动主压缩机。增压压缩机能够接收和增加所述气态排气流的压力,并将其注入到蒸发冷却塔中,其设置为使用具有低相对湿度的排放氮气作为蒸发冷却介质。所述冷却的气态排气流然后通过该系统压缩和再循环,作为稀释剂以调节所述化学计量燃烧的温度。
Description
相关申请的交叉参考
本申请要求2010年7月2日提交的,名称为具有排气再循环和直接接触冷却器的化学计量燃烧(STOICHIOMETRICCOMBUSTIONWITHEXHAUSTGASRECIRCULATIONANDDIRECTCONTACTCOOLER)的美国临时专利申请号61/361,176的权益,其全部内容以参考的方式并入本文。
本申请包含与2010年7月2日提交的,名称为“用于控制燃料燃烧的系统和方法(SystemsandMethodsforControllingCombustionofaFuel)”的美国专利申请号61/361,169;2012年7月2日提交的,名称为“低排放三循环发电系统和方法(LowEmissionTriple-CyclePowerGenerationSystemsandMethods)”的美国专利申请号61/361,170;2012年7月2日提交的,名称为“低排放三循环发电系统和方法(LowEmissionTriple-CyclePowerGenerationSystemsandMethods)”的美国专利申请号61/361,173;2012年7月2日提交的,名称为“具有排气再循环的浓缩空气的化学计量燃烧(StoichiometricCombustionofEnrichedAirWithExhaustGasRecirculation)”的美国专利申请号61/361,178以及2012年7月2日提交的,名称为“低排放发电系统和方法(LowEmissionPowerGenerationSystemsandMethods)”的美国专利申请号61/361,180相关的主题。
技术领域
本公开的实施方式涉及在联合循环电力系统中的低排放发电。
背景技术
该部分目的是介绍该技术的各个方面,其可以与本公开的示例性实施方式有关。该讨论被认为有助于提供促进更好地理解本公开的特定方面的框架。因此,应该理解的是该部分应当这样阅读,不必作为对现有技术的承认。
随着对全球气候变化和CO2排放的影响逐渐增长的关注,已经把重点放在从电力装置捕集CO2。该关注结合在许多国家实施总量管理和交易(cap-and-trade)政策使得减少CO2排放成为对于这些和其他国家以及在那里操作烃生产系统的公司优先考虑的事。
相比于其他技术,例如煤和核技术,燃气轮机联合循环电力装置是相当高效的,并且可以在相对较低的费用下操作。然而,由于若干原因,从燃气轮机联合循环装置的排气中捕集CO2存在困难。例如,相比于必须处理的大体积气体,通常排气中CO2浓度较低。同时,在将排气引入CO2捕集系统之前,经常需要额外的冷却,并且冷却后的排气会充满水,从而增加了在CO2捕集系统中的再煮沸任务。其他常见的因素包括低压以及经常包含在排气中的大量的氧气。所有这些因素导致从燃气轮机联合循环电力装置捕集CO2的高费用。
降低CO2排放的一些途径包括燃料脱碳或者使用溶剂例如胺类进行燃烧后捕集。然而,这些方案都很昂贵并且降低发电功效,这导致较低的电力产生、增加的燃料需求以及增加的发电成本以满足国内电力需求。特别地,氧气、SOX和NOX成分的存在使胺类溶剂吸收的使用非常成问题。另一个途径是在联合循环中的含氧燃料燃气轮机(例如,其中捕集来自燃气轮机布雷顿循环(Braytoncycle)的排气热量以在郎肯循环(Rankincycle)中制造蒸汽和生产额外的电力)。然而,没有商业上可利用的燃气轮机能够以这样的循环操作,并且生产高纯度氧需要的电力显著地降低了工艺的整体效率。若干研究比较了这些工艺,并且显示每种途径的一些优点。见,例如Bolland,Olav和Undrum,Henriette,从燃气轮机电力装置中除去CO2:评估前燃烧和后燃烧方法(RemovalofCO2fromGasTurbinePowerPlants:Evaluationofpre-andpost-combustionmethods),SINTEFGroup,http://www.energy.sintef.nO/publ/xergi/98/3/3art-8-engelsk.htm(1998)。
降低CO2排放的其他途径包括化学计量的排气再循环,例如在天然气联合循环(NGCC)中。在传统的NGCC系统中,只需要大约40%的进气容积以提供足够的燃料的化学计量燃烧,而剩余的60%空气容积用于调节温度和冷却排气,以适合于引入到随后的膨胀器中,但是也不利地产生了难以去除的过量的氧气副产物。通常的NGCC产生低压排气,其需要部分所生产的电力提取CO2用于吸收或者EOR,从而降低了NGCC的热效率。进一步,用于CO2提取的设备大且昂贵,并且需要若干步骤的压缩以使环境压力的气体变为EOR或者吸收所需要的压力。这些限制是从与其他化石燃料例如煤的燃烧相关的低压排气中燃烧后碳捕集具有的特征。
在联合循环发电装置中排气压缩机的容量和效率直接受到进气温度和再循环排气的组成的影响。按照惯例,通过在直接接触冷却器中直接接触再循环水,冷却排气。再循环水可以通过若干方法冷却,包括使用热交换器将热量排到再循环的冷却水中、使用空气散热片热交换器、或者通过用传统冷却塔的蒸发冷却。然而,通过这些方法的冷却受到大气状况的限制,特别是在较热的气候下。
对于本领域中需要的上述讨论意图是代表性的而不是详尽的。解决一种或多种这样的需要或者本领域一些其他相关的缺点的技术,有利于在联合循环电力系统中的发电。
发明内容
本公开涉及用于改进发电系统的集成系统和方法。在一些实施中,本公开提供了集成系统,其包括有利地集成的燃气轮机系统、排气再循环系统和CO2分离器。燃气轮机系统可以具有燃烧室,其设置为在压缩的再循环排气的存在下,化学计量燃烧压缩的氧化剂和燃料。压缩的再循环排气用于调节燃烧室中的燃烧温度。燃烧室引导排放物到膨胀器,其设置为产生气态排气流并至少部分地驱动主压缩机。将来自膨胀器的气态排气流引导到具有至少一个集成冷却单元的排气再循环系统。在将其注入到主压缩机以产生压缩的再循环排气之前,至少一个集成冷却单元使气态排气(gaseousexhaust)冷却。CO2分离器经清除流,流动地耦合到压缩的再循环排气中,并且设置为排放主要由富含氮气的气体组成的剩余气流。富含氮气的气体可以在气体膨胀器中膨胀以产生氮气排气。将氮气排气注入到至少一个集成的冷却单元中以冷却气态排气。至少一个集成的冷却单元被集成,原因在于通过氮气排气的集成使用,至少提高了一些冷却效应。
另外或者可替代地,本公开提供了发电的方法。示例性方法包括:a)在压缩的再循环排气存在下在燃烧室中化学计量燃料压缩的氧化剂和燃料,从而产生排出流,其中压缩的再循环排气起稀释剂的作用,其设置为调节排出流的温度;b)在膨胀器中使排出流膨胀,以至少部分地驱动主压缩机并产生气态排气流;c)引导气态排气流进入至少一个集成的冷却单元;d)在将气态排气流注入到主压缩机以产生压缩的再循环排气之前,在至少一个集成的冷却单元中冷却气态排气流;e)引导部分压缩的再循环排气经清除流进入到CO2分离器中,CO2分离器设置为排放主要由富含氮气的气体组成的剩余气流以在气体膨胀器中膨胀并产生氮气排气;以及f)将氮气排气注入至少一个集成的冷却单元中以冷却气态排气流。
仍然另外地或者可替代地,本系统可以包括燃烧室、蒸发冷却塔和CO2分离器。燃烧室可以设置为在压缩的再循环排气存在下,化学计量燃烧压缩的氧化剂和燃料。燃烧室引导排放物到膨胀器,其设置为产生气态排气流并驱动主压缩机。蒸发冷却塔可以具有第一柱和第二柱。第二柱可以设置为在主压缩机中压缩以产生压缩的再循环排气之前,接收和冷却气态排气流。CO2分离器可以经清除流,流动地耦合到压缩的再循环排气中,并且设置为排放主要由富含氮气的气体组成的剩余气流以在气体膨胀器中膨胀并产生氮气排气,其中氮气排气注入到第一柱中以蒸发和使冷却水供应冷却,以排放冷却水,并且其中冷却水注入到第二柱中以冷却气态排气流。
附图说明
在检阅了下面的详细描述和实施方式的非限制性实施例的图后,本公开的上述和其他优点会变得显而易见,其中:
图1描述了根据本公开的一个或更多实施方式的用于低排放发电和提高CO2回收的例证性集成系统。
图2描述了根据本公开的一个或更多实施方式的用于在压缩之前冷却排气的例证性冷却单元。
详细描述
在下面的详细描述部分,结合优选的实施方式描述了本公开的具体实施方式。然而,就下面的描述是针对本公开的特定实施方式或者特定用途来说,其意欲仅仅是为了示例性的目的,并且简单地提供了示例性实施方式的描述。因此,本公开不限于下面描述的具体实施方式,反而,其包括在所附的权利要求的实质精神和范围内的所有备选方案、修改和对等物。
本文所用的各种术语定义如下。就权利要求中使用的术语不是如下定义来说,其应该被给予相关技术人员已经对该术语给出的最广泛的定义,如至少在一个印刷的出版物或者颁发的专利中反映的。
如本文所用,术语“化学计量燃烧”指具有包括燃料和氧化剂的大量反应物以及通过燃烧反应物形成的大量产物的燃烧反应,其中所有量的反应物用于形成产物。如本文所用,术语“大体上化学计量燃烧”指燃烧反应,其燃烧燃料和氧气的摩尔比范围为化学计量比要求的氧气大约正或负10%,或者更优选地为化学计量比要求的氧气大约正或负5%。例如,对于甲烷,燃料和氧气的化学计量比为1:2(CH4+2O2>CO2+2H2O)。对于丙烷,燃料和氧气的化学计量比为1:5。测量大体上化学计量燃烧的另一种方式是所供应的氧气与化学计量燃烧所需要的氧气之间的比例,例如从大约0.9:1到大约1.1:1,或者更优选地从大约0.95:1到大约1.05:1。
如本文所用,术语“流”指大量流体,虽然该术语流的使用通常意味着移动量的流体(例如,具有速度或者质量流率)。然而,术语“流”不要求速度、质量流率或者包围住该流的导管的特定类型。
本公开的系统和工艺的实施方式可以用来产生超低排放的电力和CO2,用于提高原油采收率(EOR)和/或螯合应用。在一个或更多实施方式中,空气和燃料的混合物能够按化学计量或者大体上按化学计量燃烧,并且可以与再循环的排气流混合。再循环的排气流,通常包括燃烧的产物例如CO2,可以用作稀释剂以控制、调整或者另外调节燃烧的温度以及进入随后的膨胀器中的排气。由于使用浓缩空气的原因,再循环的排气CO2含量增加,从而对于相同入口和排气温度,允许膨胀器甚至在较高的膨胀比下操作,从而产生显著增加的电力。
在商业燃气轮机中在化学计量条件或者大体上化学计量条件下的燃烧(例如“稍微充足的”燃烧)能够证明是有利的,以消除过量氧气除去的费用。仍然进一步,稍微稀薄的燃烧可以进一步减少排气流中的氧气含量。通过冷却排气和冷凝出自冷却排气流中的水,可以产生较高含量的CO2排气流。虽然部分再循环的排气可以用于闭合的布雷顿循环中的温度调节,但是剩余的清除流能够用于EOR应用中和/或能够产生电力,而较少或者没有硫氧化物(SOX)、氮氧化物(NOX)和/或CO2排放到环境中。当清除流或者其部分被发送用于生产电力时,结果是在三个分离的循环中发电和制造额外的CO2。
因为排气压缩机的容量和效率直接受到再循环排气的入口温度的影响,因此它可以证明在压缩前降低再循环排气的温度是有利的。因此,本公开的实施方式使用具有低的相对湿度的氮气放气流作为在排气压缩机之前的冷却单元中的蒸发冷却介质。干燥的氮气可被设置为蒸发和冷却适于冷却再循环排气的水流,从而将更冷的排气注入到压缩机中,并通过允许在那里增加容量而提高其效率。如可以理解的,由于若干原因证明这是有利的。例如,较低的吸入温度等同于较低的排放温度,其可以减少低能量CO2分离工艺需要的冷却。此外,额外的冷却单元能够从再循环排气中除去额外量的水,从而减少在任何CO2分离系统中的再煮沸任务。
现在参考图,图1描述了根据一个或更多实施方式,使用联合循环装置用于发电和CO2回收的例证性集成系统100的图解。在至少一个实施方式中,发电系统100包括燃气轮机系统102,其特征是发电的封闭布雷顿循环。燃气轮机系统102可具有第一或者主压缩机104,其通过共同轴108或者其他机械的、电的或者其他电力耦合装置而耦合到膨胀器106上,从而允许由膨胀器106产生的部分机械能驱动主压缩机104。燃气轮机系统102可以是标准的燃气轮机,其中主压缩机104和膨胀器106分别形成压缩机和膨胀器末端。然而,在其它实施方式中,主压缩机104和膨胀器106可以是系统102中个别化的部件。
燃气轮机系统102也可以包括燃烧室110,其设置为燃烧经管线112引入的与管线114中的压缩氧化剂混合的燃料。在一个或更多实施方式中,在管线112中的燃料可以包括任何合适的烃气体或液体,例如天然气、甲烷、乙烷、石脑油、丁烷、丙烷、合成气、柴油、煤油、航空燃料、煤衍生的燃料、生物燃料、氧化的碳氢原料或者其任何组合。在管线114中的压缩的氧化剂可以来源于第二或者进气压缩机118,其流动地耦合到燃烧室110上,并且适应于压缩经管线120引入的进料氧化剂。在一个或更多实施方式中,在管线120中的进料氧化剂可以包括包含氧气的任何合适的气体,例如空气、富含氧气的空气、氧气消耗的空气、纯的氧气或者其组合。
如下面更详细地描述的,燃烧室110也可以接收在管线144中的压缩的再循环排气,包括主要具有CO2和氮气成分的排气再循环。在管线144中的压缩的再循环排气可来源于主压缩机104,并且适于通过调节燃烧产物的温度,帮助促进在管线114中的压缩的氧化剂和管线112中的燃料的化学计量或者大体上化学计量燃烧。如可以理解的,再循环排气能够用来增加排气中的CO2浓度。
当在管线144中存在压缩的再循环排气时,引导至膨胀器106入口的管线116中的排气,能够作为在管线112中的燃料和管线114中的压缩的氧化剂的燃烧产物产生。在至少一个实施方式中,管线112中的燃料主要是天然气,从而产生经管线116的排气或者排气,其包括部分容积的蒸发的水、CO2、氮气、氮氧化物(NOX)和硫氧化物(SOX)。在一些实施方式中,由于燃烧平衡限制,管线112中的小部分未燃烧的燃料或其他化合物也可以存在于管线116中的排气中。因为在管线116中的排气经过膨胀器106膨胀,所以其产生机械动力以驱动主压缩机104,发电机或者其他设施,并且也产生气态排气流122,其具有由管线144中压缩的再循环排气的汇集而产生的增加的CO2含量。膨胀器106可以产生电力,用于除了主压缩机104之外的使用或者用于主压缩机104的替代装置。例如,膨胀器106可以产生电。
发电系统100也可以包括排气再循环(EGR)系统124。在一个或更多实施方式中,EGR系统124可以包括热回收蒸汽发生器(HRSG)126或类似的装置,其流体耦合到蒸汽燃气轮机128上。在至少一个实施方式中,HRSG126和蒸汽燃气轮机128的组合的特征是产生电力的封闭的郎肯循环。与燃气轮机系统102相组合,HRSG126和蒸汽燃气轮机128能够形成部分联合循环发电装置,如天然气联合循环(NGCC)装置。气态排气流122能够引入HRSG126中,以便经管线130产生蒸汽以及在管线132中的冷却排气。在一个实施方式中,管线130中的蒸汽可发送到蒸汽燃气轮机128中以产生额外的电力。
管线132中的冷却排气可以发送到在返回到主压缩机104的再循环回路中的任何种类的装置和/或设施。在一些实施中,如图1所示,再循环回路可以包括第一冷却单元134,其适于冷却管线132中的冷却排气并产生冷却的再循环气流140。第一冷却单元134包括,例如,一个或更多接触冷却器、调温冷却器、蒸发冷却单元或者其任意组合。第一冷却单元134也可以适于经水滴流(waterdropoutstream)138从管线132的冷却排气中除去任何冷凝水部分。在至少一个实施方式中,水滴流138可以经管线141发送到HRSG126中,以提供用于在管线130那里产生额外的蒸汽的水源。在其他实施方式中,经水滴流138回收的水用于其他下游的应用,如补充的热交换工艺。
在一个或更多实施方式中,冷却的再循环气流140可以引导至增压压缩机142中。在第一冷却单元134中使管线132中的冷却排气冷却可以减少在增压压缩机142中压缩冷却的再循环气流140所需要的电力。与传统的鼓风机或者鼓风系统相反,增压压缩机142可以设置为压缩和增加冷却的再循环气流140的总密度,从而引导管线145中加压的再循环气体进入下游,其中管线145中加压的再循环气体对于相同容积的流量具有增加的质量流率。这证明是有利的,因为主压缩机104可以是容积流量限制的,并且引导更多的质量流量穿过主压缩机104可以导致较高的排出压力,从而转化为穿过膨胀器106的较高压力比。经过膨胀器106产生的较高的压力比能够允许较高的入口温度,因此增加了膨胀器106的电力和效率。如可以理解的,这证明是有利的,因为管线116中富含CO2的排气通常维持较高的比热容。
因为主压缩机104的吸入压力是其吸入温度的函数,所以对于相同的质量流量,冷却器吸入温度将需要较低的电力以操作主压缩机104。结果,管线145中的加压的再循环气体可任选地引导入第二冷却单元136中。第二冷却单元136可以包括,例如一个或更多个直接接触冷却器、调温冷却器、蒸发冷却单元或者其任意组合。在至少一个实施方式中,第二冷却单元136可以用作后冷却器,其适于除去由增压压缩机142在管线145中的加压的再循环气体上产生的至少部分压缩热量。第二冷却单元136也可以经水滴流143提取额外的冷凝水。在一个或更多实施方式中,水滴流138、143能够汇聚到流141中,并可以发送或可以不发送到HRSG126中以经过在那里的管线30产生额外的流。在经受第二冷却单元136的冷却之后,管线145中加压的再循环气体能够引导至第三冷却单元200。虽然这里仅描述了第一、第二和第三冷却单元134、136、200,但是应该理解的是在没有违背本公开的保护范围时,可以使用任何数目的冷却单元以适合各种应用。例如,在一些实施方式中可以实施单个冷却单元。
如下面将更详细描述的,第三冷却单元200,如同第一和第二冷却单元,可以是蒸发冷却单元,其设置为在经流214注入到主压缩机104之前进一步降低管线145中加压的再循环气体的温度。然而,在其他的实施方式中,冷却单元134、236、200中的一个或更多个可以是机械制冷系统,这没有违背本公开的保护范围。主压缩机104可以设置为将接收自第三冷却单元200的管线214中的加压的再循环气体压缩为额定地等于或高于燃烧室压力的压力,从而产生管线144中压缩的再循环气体。如可以理解的,在增压压缩机142中压缩后,在第二和第三冷却单元136、200中冷却管线145中加压的再循环气体,可以允许增加进入主压缩机104中的排气的容积质量流量。结果,这可以降低将管线145中加压的再循环气体压缩为预定压力所需要的电力的量。
虽然图1图解了排气再循环回路中的三个冷却单元和增压压缩机,但是应该明白的是这些单元中的每一个适于降低管线132中冷却排气的质量流率。如上所述,例如通过增压压缩机质量流率的降低,以及温度的降低是有利的。本公开涉及在发电系统100内的集成,以提高在排气再循环回路中排气的冷却,其在一些实施中可以将排气再循环回路简化为HSRG系统126和主压缩机104之间的单个冷却单元,如本文进一步所描述的。
在至少一个实施方式中,清除流146可以从管线144中压缩的再循环气体中回收,随后在CO2分离器148中处理以经管线150在升高的压力下捕集CO2。管线150中分离的CO2可用于出售、用在需要CO2的其他工艺中,和/或进一步压缩并注入到陆地储藏中用于提高原油采收率(EOR)、螯合或另外的目的。因为在与排气再循环系统124上的装置结合的管线112中燃料的化学计量或者大体上化学计量燃烧,所以在清除流146中的CO2分压会比传统的燃气轮机排气高得多。结果,可以使用低能量分离工艺例如低能量强度的溶剂在CO2分离器148中进行碳捕集。至少一种合适的溶剂是碳酸钾(K2CO3),其吸收SOX和/或NOX,并将它们转化为有用的化合物,如亚硫酸钾(K2SO3)、硝酸钾(KNO3)和其他单纯肥料。使用碳酸钾用于CO2捕集的示例性系统和方法可以在同时提交的名称为“低排放三循环发电系统和方法”的美国专利申请中找到,其内容通过参考并入本文,达到与本公开一致的程度。
基本上去除了CO2并主要由氮气组成的剩余流151,也可以来自于CO2分离器148中。在一个或更多实施方式中,剩余流151可以引导入气体膨胀器152中以经管线156提供电力和膨胀的减压气体。膨胀器152可以是,例如产生电力的氮气膨胀器。如所描述,气体膨胀器152可以任选地经过共同轴154或者其他机械的、电的或者其他电力耦合装置耦合到入口压缩机118上,从而允许由气体膨胀器152产生的部分电力驱动入口压缩机118。然而,在其他的实施方式中,气体膨胀器152能够用来提供给其他应用电力,并且不直接耦合到化学计量压缩机118上。例如,在由膨胀器152产生的电力和压缩机118的需要之间可能实质上不匹配。在这样的情况下,膨胀器152能够适于驱动需要较少电力的较小的压缩机(没有显示)。或者,膨胀器能够适于驱动需要较多电力的较大的压缩机。
主要由干燥的氮气组成的管线156中膨胀的减压气体,能够从气体膨胀器152中排出。如下面将更详细描述的,生成的干燥氮气能够帮助促进第三冷却单元200中的水流的蒸发和冷却,从而冷却管线145中加压的再循环气体。在至少一个实施方式中,气体膨胀器152、入口压缩机118和CO2分离器的组合的特征是开放的布雷顿循环,或者是系统100的第三产生电力的部件。
如本文描述的发电系统100,特别是具有来自增压压缩机142的附加的排气排放增压(exhaustgasexhaustpressurization)的发电系统100,能够实施以达到排气中较高浓度的CO2,从而允许更有效的CO2分离和捕集。例如,本文公开的实施方式能够有效地用纯的甲烷燃料将排气排放流(exhaustgasexhauststream)中CO2的浓度增加为大约10vol%或者用更丰富的气体可以提高到更高。为了达到这一点,燃烧室110能够适于化学计量燃烧管线112中燃料和管线114中压缩的氧化剂的引入混合物。为了调节化学计量燃烧的温度以满足膨胀器106入口温度和成分冷却需要,来自于管线144中的压缩的再循环气体中的部分排气可以注入到燃烧室110中作为稀释剂。与在燃烧室中引入过量空气或氧化剂以调节温度的传统实践相比较,使用再循环的排气大大降低了离开燃烧室110的氧气的量。因此,本公开的实施方式能够本质上消除来自排气中的任何过量氧气,并且同时增加其CO2组成。因此,气态排气流122可以具有少于大约3.0vol%的氧气,或者少于大约1.0vol%的氧气,或者少于大约0.1vol%的氧气,或者甚至少于大约0.001vol%的氧气。
现在讨论系统100的示例性操作的细节。如可以理解的,本文公开的任何实施方式的各种部件中经受或者达到的特定温度和压力能够根据——除了其他因素之外——使用的氧化剂的纯度,和/或膨胀器、压缩机、冷却器等的特定制作和/或模型而改变。因此,应该理解的是本文描述的特定数据仅仅是为了例证性目的,不应该理解为其唯一解释。例如,在本文描述的一个实施方式中,入口压缩机118可以设置为提供管线114中压缩的氧化剂,其压力范围在大约280psia和大约300psia之间。然而,本文还考虑了航空衍生的燃气轮机技术,其能够产生和消耗的压力高达大约750psia和更大。
主压缩机104能够设置为将再循环的排气再循环和压缩为管线144中的压缩的再循环气体,其压力额定地高于或等于燃烧室110的压力,并且使用部分再循环的排气作为燃烧室110中的稀释剂。因为燃烧室110中所需要的稀释剂的量可依赖于用于化学计量燃烧的氧化剂的纯度、或者膨胀器106的特定模型或设计,所以可以布置与燃烧室和/或膨胀器联合的一圈热电偶和/或氧气传感器(没有显示)。例如,热电偶和/或氧气传感器可以布置在燃烧室110的出口处、膨胀器106的入口处和/或膨胀器106的出口处。在操作中,热电偶和传感器能够适于测定一个或更多流的组成和/或温度,以用于测定作为稀释剂将燃烧产物冷却为所需膨胀器入口温度所需要的排气的容积。另外或者可替代地,热电偶和传感器可以适于测定待注入到燃烧室110中的氧化剂的量。因此,响应由热电偶检测的热量需要和由氧气传感器检测的氧气水平,可以操作或者控制管线144中压缩的再循环气体和/或管线114中压缩的氧化剂的容积质量流量以与需要相匹配。容积质量流率可以通过任何合适的流动控制系统控制,其可以与热电偶和/或氧气传感器电连通。
在至少一个实施方式中,在化学计量或者大体上化学计量燃烧期间,穿过燃烧室110能够经受大约12-13psia的压降。管线112中的燃料和管线114中的压缩的氧化剂的燃烧能够产生大约2000°F和大约3000°F之间的温度以及范围为250psia到大约300psia的压力。由于来自于管线144中压缩的再循环气体的富含CO2的排气增加的质量流量和较高的比热容,所以穿过膨胀器106可以达到较高的压力比,从而允许较高的入口温度和增加的膨胀器106电力。
离开膨胀器106的气态排气流122可呈现等于或接近大气的压力。在至少一个实施方式中,气态排气流122压力可为大约13-17psia。在穿过HRSG126以产生管线130中的蒸汽和管线132中的冷却排气之前,气态排气流122的温度可以为大约1225°F到大约1275°F。
接下来的若干段落描述了图1中显示的示例性实施。如上所述,图1图解了与排气再循环回路联合的多个装置,为了说明各种可能的组合。然而,应该明白的是本文描述的发明不需要所有这些元件的组合。例如,虽然在图1中图解了多个冷却单元,但是应该明白的是使用与氮气排气流联合的冷却剂的直接接触冷却单元(下面描述为冷却单元200)可以通过单个冷却单元提供充足的冷却。在一些实施中,冷却单元200可以提供充足的冷却以提供和增压压缩机一样的优点。
继续讨论图1中的示例性实施,在一个或更多实施方式中,冷却单元134可以降低管线132中冷却的排气的温度,从而产生温度在大约32°F和大约120°F之间的冷却的再循环气流140。如可以理解的,这样的温度能够波动,这主要依赖于世界各地特定位置的特定季节期间的湿球温度。
根据一个或更多实施方式,增压压缩机142可以设置为将冷却的再循环气体流140的压力升高为范围为大约17psia到大约21psia的压力。增压压缩机的增加压缩是除了使用冷却单元之外的另外的方法,以提供较高密度和增加质量流量的再循环的排气到主压缩机104中,从而当维持相同或类似的压力比时,允许实质上较高的排出压力。为了进一步增加排气的密度和质量流量,从增压压缩机142排出的管线145中的加压的再循环气体然后可进一步在第二和第三冷却单元136、200中冷却。在一个或更多实施方式中,第二冷却单元136可设置为在将管线145中加压的再循环气体引导至第三冷却单元200之前使其温度降低为大约105°F。如下面更详细讨论的,第三冷却单元200可以设置为将管线145中加压的再循环气体的温度降低为大约100°F以下的温度。
在至少一个实施方式中,从主压缩机104和清除流146排出的管线144中压缩的再循环气体的温度可以为大约800°F,压力为大约280psia。如可以理解的,增压压缩机142和/或一个或更多冷却单元的加入能够增加清除流管线146中的CO2清除压力,其导致由于较高的CO2分压在CO2分离器148中的溶剂处理性能提高。在一个实施方式中,在CO2分离器148中的气体处理工艺可能需要清除流146的温度冷却到大约250°F-300°F。为了达到该要求,清除流146能够经过热交换器158,如交叉交换热交换器引导。在CO2分离器148中从清除流146中提取CO2可以留下了饱和的富含氮气的剩余流151,其等于或接近清除流146的升高压力,温度为大约150°F。热交换器158可以如图解与剩余流151耦合,或者与集成系统中的其他流或者设施耦合。当与剩余流151耦合时,剩余流能够被加热以增加可从气体膨胀器152获得的电力。
如上所陈述,随后膨胀为管线156中膨胀的减压气体的剩余流151中的氮气可以随后用于使设置为冷却管线145中加压的再循环气体——注入到第三冷却单元200——的水蒸发和冷却,所述第三冷却单元200可以是排气再循环回路中唯一的冷却单元。作为蒸发冷却催化剂,氮气应该尽可能干燥。因此,剩余流151能够引导穿过设置为冷却剩余流151的第四冷却单元160或者冷凝器,从而经管线162冷凝和提取额外部分的水。在一个或更多实施方式中,第四冷却单元160可以是用标准冷却水冷却的直接接触冷却器,以便将剩余流151的温度降低至大约105°F。在其他的实施方式中,第四冷却单元160可以是调温冷却器或者直型热交换器。剩余流151的所得水含量可以为大约0.1wt%到大约0.5wt%。在一个实施方式中,经流162除去的水可以发送至HRSG126中以产生额外的蒸汽。在其他的实施方式中,流162中的水可以经处理并用作农业用水或者软化水。
干燥的氮气可以经流164从第四冷却单元160中排出。在一个实施方式中,与冷却清除流146相关的热能经热交换器158提取,热交换器流体耦合到干燥的氮气流164中,并设置为在膨胀前再加热氮气。再加热氮气能够产生干燥的加热的氮气流166,其温度范围为大约750°F到大约790°F,压力为大约270-280psia。在热交换器158是气体/气体热交换器的实施方式中,在清除流146和干燥的氮气流164之间将实现“节点”温差,其中干燥的氮气流164通常比清除流146的温度低大约25°F。
在一个或更多实施方式中,干燥的加热的氮气流166然后可以经过气体膨胀器152膨胀,并且任选地供给化学计量入口压缩机118电力,如上所述。因此,在热交换器158中交叉交换热量可以设置为捕集来自主压缩机104的大量压缩能量,并且使用其使从气体膨胀器152中提取的电力最大化。在至少一个实施方式中,气体膨胀器152在管线156中排出氮气膨胀的减压气体,其等于或接近大气压力并且温度范围为大约100°F到大约105°F。如能够理解的,管线156中氮气膨胀的减压气体的所得温度通常是在气体膨胀器152中膨胀之前的排气的组成、清除流146的温度和干燥氮气流164的压力的函数。
因为在第四冷却单元160中能够从剩余流151中除去可测量量的水,因此减少的量的质量流量随后在气体膨胀器152中膨胀,从而导致减少的电力产生。结果,在系统100启动期间以及在正常操作期间,当气体膨胀器152不能供应所有需要的电力以操作入口压缩机118时,至少一个马达168,例如电机,可以与气体膨胀器152协同使用。例如,马达168可以敏感地使尺寸适合,以致于在系统400的正常操作期间,马达168可以设置为供应气体膨胀器152电力缺口。另外或者可替代地,当燃气轮机152产生的电力比入口压缩机118需要的多时,马达168可以设置为可以转换为发电机的马达/发电机。
膨胀在剩余流151中的氮气的例证性系统和方法以及其变体可以在同时提交的名称为“低排放三循环发电系统和方法”的美国专利申请中找到,其内容通过参考并入本文,达到与本公开一致的程度。
现在参考图2,其描述的是如图1中图解的第三冷却单元200的示意图。如上所述,所图解的第三冷却单元200可以是设置在排气再循环回路中的唯一单元。另外或者可替代地,第三冷却单元200和其他设备部件,如图1中所图解的一个或更多部件,可以以任何合适的排列设置,以致于第三冷却单元200在顺序上实际上是第一(或者第二等)而不是第三。因此,应该明白的是顺序指示“第三”是参考图1中的特定实施,并且不需要将图2中冷却单元200的特征实施为在系统中的第三冷却单元,但是其可以布置在排气再循环回路中的任何合适位置。
在一个或更多实施方式中,冷却单元200可以包括第一柱202,其流体耦合到第二柱204上。在一个或更多实施方式中,第一柱202可以是蒸发冷却塔,并且第二柱204可以是直接接触冷却塔。第一柱202能够设置为接收来自气体膨胀器152(图1)的管线156中氮气膨胀的减压气体。在一个实施方式中,管线156中氮气膨胀的减压气体注入到第一柱202的底部或者接近底部,并且通过塔上升直到其经过氮气出口流206在顶部或接近顶部排出。在至少一个实施方式中,氮气出口流206能够将其包容物排到大气中或者作为惰性气体售出。在其他实施方式中,在流206中的氮气可以加压用于压力维持或者EOR应用。
因为管线156中氮气膨胀的减压气体能够等于或接近大气压力,所以第一柱202能够适于在等于或接近大气压力下操作。当氮气在第一柱202中上升时,管线208中的水流或者冷却水供应可以注入到第一柱202的顶部或接近顶部。在一个或更多实施方式中,管线208中的冷却水供应可以从局部水体中获得,例如湖、河或者海洋。因此,依赖于系统100位于的特定地理位置的一年中的时间以及环境温度,管线208中冷却水供应可以在不同的温度注入,但是更可能是在大约50°F到大约100°F之间。当水在第一柱202中上升时,一部分水通过吸收来自干燥氮气的热能而蒸发,从而使水冷却并经流210排出冷却水。蒸发的水能够用氮气收集,从而导致饱和的氮气经管线206排出。依赖于管线206中氮气流的预期用途,其中的水蒸气可以通过任何合适的方法除去。
第二柱204能够设置为在其顶部或接近顶部接收冷却水流210。如描述的,第二柱204也可以在其底部或接近底部,接收从第二冷却单元136(图1)排出的管线145中的加压的再循环气体。管线145中加压的再循环气体的图解代表了在排气再循环回路中的任何排气流。因为加压的再循环流145能够在压力范围为大约17psia到大约21psia时注入,如上所述,当合适时,可以使用至少一个泵212或者类似的机构相应地加压冷却水流210。当冷却水流210和管线145中的加压的再循环气体经过第二柱204时,使管线145中的加压的再循环气体冷却并且最后经流214离开,随后引导到主压缩机104(图1)的吸入口。在一些实施中,柱204可以包括多级或者接触表面以增加再循环流145和冷却水流210之间的相互作用。另外或者可替代地,如果需要,可以在第一柱202、第二柱204的位置或者两个位置上连续地或者并行地使用多个塔。
在通常比管线210中的水温暖的温度中返回的冷却水,经管线216离开第二柱204。如能够理解的,冷却管线145中加压的再循环气体,能够导致来自于管线145中的加压的再循环气体的更多水冷凝。该冷凝水可以被收集并随着管线216中返回的冷却水排出,从而产生管线145中甚至更干燥的加压的再循环气体,其经流214离开。在至少一个实施方式中,返回的冷却水能够经管线208再发送并再引导入第一柱。然而,在其他实施方式中,返回的冷却水能够无害地排放到局部水体中或者用作灌溉用水。
如上关于图1的讨论,在引入到第三冷却单元200之前,管线145中的加压的再循环气体能够事先在第二冷却单元136(图1)中冷却到大约105°F的温度。在第三冷却单元200中,管线145中的加压的再循环气体经受的总冷却量可取决于来自于经过第二柱204的流210中冷却水的流动速度。
用下列的模拟实施例能够进一步描述本公开的实施方式。虽然模拟的实施例涉及具体的实施方式,但是其不应该认为是在任何具体的方面限制本公开。下列表1提供了在流210中水的例证性流动速度以及其对第三冷却单元200的冷却工艺的影响。
表1
从表1可明显看出,当管线210中水的流动速度增加时,经管线206的氮气流的出口温度也增加,其是通过增加的水量热交换加热的直接结果。相同地,管线210中水的流动速度的增加导致管线210中水的出口温度增加。因此,相对于管线210中增加的水流动速度,经管线214离开的加压的再循环气体的温度降低。如能够理解的,若干变量能够影响经管线214离开的加压的再循环气体的温度,包括但不限制于,管线156中引入的氮气排气的温度、管线208中冷却水供应的温度、在塔中阶段的配置和数目等。在至少一个实施方式中,管线208中冷却水供应能够在大约80°F到大约85°F的温度下注入到第一柱202中。
下列表2提供了使用了冷却单元200,如本文描述的蒸发冷却单元,的系统和没有这样的冷却单元200的系统之间的性能比较。
表2
如表2显而易见地,包括循环入口冷却的实施方式,例如利用第三冷却单元200,能够增加联合循环电力输出。虽然可能经历来自氮气膨胀器中电力输出的减少,但是其减少多于通过净燃气轮机电力(即,膨胀器106)的增加所补偿的,其转换为CO2清除压力(即,主压缩机104排出压力)的增加。此外,通过实施如本文所述的入口冷却,总的联合循环电力输出能够增加大约0.6%lhv(低热值)。
本公开也考虑使用机械制冷系统(没有显示)作为第三冷却单元200,以替代本文描述的蒸发冷却单元。虽然使用机械制冷系统可能适度地降低主压缩机104的总体需要的压缩电力,但是通过主压缩机104的质量流量可能相应地降低,这将不利地影响产生的电力。必须考虑主压缩机104电力减少与膨胀器106电力产生之间的权衡以得到最佳的工艺循环性能。而且,应该针对额外费用方案考虑额外的冷却设备的费用。
虽然本公开可容易进行各种修改和可替代的形式,但是上面讨论的示例性实施方式仅仅是通过实施例的方式显示的。然而,应该再次明白的是本公开的目的不是限制于本文公开的特定实施方式。事实上,本公开包括落在所附权利要求的真正精神和范围内的所有备选方案、修改和对等物。
Claims (21)
1.集成系统,其包括:
燃气轮机系统,其具有燃烧室,所述燃烧室设置为在压缩的再循环排气存在下,大体上化学计量燃烧压缩的氧化剂和燃料,其中所述压缩的再循环排气用来调节所述燃烧室中燃烧的温度,并且所述燃烧室引导排放物到膨胀器中,所述膨胀器设置为产生气态排气流并至少部分地驱动主压缩机;
排气再循环系统,其具有至少一个冷却单元,其中所述至少一个冷却单元在所述气态排气流注入到所述主压缩机以产生所述压缩的再循环排气之前使所述气态排气流冷却;和
CO2分离器,其经清除流流体耦合到所述压缩的再循环排气,并且设置为排放主要由富含氮气的气体组成的剩余流以在气体膨胀器中膨胀并产生氮气排气,其中所述氮气排气注入到所述至少一个冷却单元中以冷却所述气态排气流。
2.权利要求1所述的系统,进一步包括至少一个额外的冷却单元,其中所述额外的冷却单元流体耦合到所述至少一个冷却单元上,并且其中所述额外的冷却单元将所述气态排气流冷却到大约105°F的温度。
3.权利要求1所述的系统,进一步包括剩余的冷却单元,其流体耦合到所述剩余流,并且设置为降低所述剩余流的温度并从那里提取冷凝水。
4.权利要求3所述的系统,其中所述至少一个冷却单元是蒸发冷却单元,其包括:
第一柱,其设置为接收所述氮气排气和冷却水供应,其中所述氮气排气蒸发部分所述冷却水供应以使所述冷却水供应冷却并产生排出的冷却水;和
第二柱,其设置为接收所述排出的冷却水和所述气态排气流,其中所述排出的冷却水和所述气态排气流之间相互作用使所述气态排气流冷却。
5.权利要求4所述的系统,其中所述至少一个冷却单元将所述压缩的再循环排气的温度降低到100°F以下。
6.权利要求4所述的系统,其中冷却水在引入到所述第二柱之前用泵加压。
7.权利要求4所述的系统,其中所述第二柱进一步设置为从所述压缩的再循环排气中冷凝和提取一定量的水。
8.权利要求1所述的系统,进一步包括热交换器,其流体耦合到所述清除流上,并且设置为在所述清除流引入到所述CO2分离器之前降低所述清除流的温度。
9.权利要求1所述的系统,进一步包括增压压缩机,其适于在所述气态排气流注入到所述主压缩机之前,将所述气态排气流的压力增加到17psia和21psia之间的压力。
10.发电的方法,其包括:
在压缩的再循环排气存在下,在燃烧室中大体上化学计量燃烧压缩的氧化剂和燃料,从而产生排气流,其中所述压缩的再循环排气起稀释剂的作用,其设置为调节所述排气流的温度;
在膨胀器中使所述排气流膨胀以至少部分地驱动主压缩机并且产生气态排气流;
将所述气态排气流引入至少一个冷却单元;
在所述气态排气流注入到所述主压缩机以产生所述压缩的再循环排气之前,在所述至少一个冷却单元中冷却所述气态排气流;
将部分所述压缩的再循环排气经清除流引到CO2分离器,所述CO2分离器设置为排放主要由富含氮气的气体组成的剩余流以在气体膨胀器中膨胀并且产生氮气排气;和
将所述氮气排气注入到所述至少一个冷却单元中以冷却所述气态排气流。
11.权利要求10所述的方法,进一步包括在布置在最后的冷却单元之前的至少一个预冷却单元中将所述压缩的再循环排气冷却到大约105°F的温度,其中所述至少一个预冷却单元流体耦合到所述最后的冷却单元上。
12.权利要求10所述的方法,进一步包括:
用流体耦合到所述CO2分离器上的剩余冷却单元冷却所述剩余流;以及
从所述剩余流中提取冷凝水。
13.权利要求12所述的方法,进一步包括:
在所述至少一个冷却单元的第一柱中接收所述氮气排气和冷却水供应;
蒸发部分所述冷却水供应以使所述冷却水供应冷却并且产生排出的冷却水;
在所述至少一个冷却单元的第二柱中接收所述排出的冷却水和所述气态排气流;
用所述排出的冷却水将所述气态排气流冷却到100°F以下的温度。
14.权利要求13所述的方法,进一步包括在所述排出的冷却水引入所述第二柱之前,用泵使所述排出的冷却水加压。
15.权利要求13所述的方法,进一步包括在所述第二柱中从所述压缩的再循环排气中冷凝并提取一定量的水。
16.权利要求10所述的方法,进一步包括在热交换器中降低所述清除流的温度,所述热交换器流体耦合到所述清除流上,并且设置为在所述清除流引导入所述CO2分离器之前降低所述清除流的温度。
17.联合循环发电系统,其包括:
燃烧室,其设置为在压缩的再循环排气存在下,大体上化学计量燃烧压缩的氧化剂和燃料,其中所述燃烧室将排放物引导入膨胀器中,所述膨胀器设置为产生气态排气流和驱动主压缩机;
蒸发冷却塔,其具有第一柱和第二柱,其中所述第二柱设置为在所述主压缩机中压缩所述气态排气流以产生所述压缩的再循环排气之前,接收和冷却所述气态排气流;和
CO2分离器,其经清除流流体耦合到所述压缩的再循环排气上,并且设置为排放主要由富含氮气的气体组成的剩余流以在气体膨胀器中膨胀并且产生氮气排气,其中所述氮气排气注入到所述第一柱中以使冷却水供应蒸发和冷却而排出冷却水,并且其中所述冷却水注入到所述第二柱中以冷却所述气态排气流。
18.权利要求17所述的系统,进一步包括冷凝器,其流体耦合到所述剩余流上,并且设置为降低所述剩余流的温度和从那里提取冷凝水。
19.权利要求17所述的系统,其中蒸发冷却塔进一步包括泵,所述泵设置为使所述冷却水加压,并将所述冷却水注入到所述第二柱中,以便冷却所述压缩的再循环排气。
20.权利要求19所述的系统,其中所述第二柱是直接接触冷却器。
21.权利要求20所述的系统,其中所述第二柱是多级直接接触冷却器。
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PL2588727T3 (pl) | 2019-05-31 |
EA026404B1 (ru) | 2017-04-28 |
BR112012031499A2 (pt) | 2016-11-01 |
EP2588727A4 (en) | 2017-11-01 |
TWI564476B (zh) | 2017-01-01 |
SG186156A1 (en) | 2013-01-30 |
US9732673B2 (en) | 2017-08-15 |
EP2588727A1 (en) | 2013-05-08 |
AU2011271634B2 (en) | 2016-01-28 |
CN102959202A (zh) | 2013-03-06 |
MX2012014459A (es) | 2013-02-11 |
JP2013537596A (ja) | 2013-10-03 |
AR081785A1 (es) | 2012-10-17 |
MX341981B (es) | 2016-09-08 |
TW201213650A (en) | 2012-04-01 |
JP5759543B2 (ja) | 2015-08-05 |
US20130091853A1 (en) | 2013-04-18 |
EA201390056A1 (ru) | 2013-05-30 |
EP2588727B1 (en) | 2018-12-12 |
CA2801492A1 (en) | 2012-01-05 |
AU2011271634A1 (en) | 2013-01-10 |
WO2012003078A1 (en) | 2012-01-05 |
MY160832A (en) | 2017-03-31 |
CA2801492C (en) | 2017-09-26 |
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