CN102959203A - 通过排气再循环的浓缩空气的化学计量燃烧 - Google Patents
通过排气再循环的浓缩空气的化学计量燃烧 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，其设置为当存在压缩的再循环排气时化学计量燃烧来源于浓缩空气的压缩的氧化剂和燃料，并且在膨胀器中使排出物膨胀以产生再循环排气流和驱动主压缩机。再循环排气流在设置为产生压缩的再循环排气的压缩机中被压缩之前，增压压缩机接收和提高所述再循环排气流的压力。为了促进燃料的化学计量燃料和增加再循环排气中的CO2含量，浓缩空气具有增加的氧气浓度。
Description
相关申请的交叉参考
本申请要求2010年7月2日提交的，题为“通过排气再循环的浓缩空气的化学计量燃烧(Stoichiometric Combustion of Enriched Air WithExhaust Gas Recirculation)”的美国临时专利申请号61/361,178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，题为“用于控制燃料燃烧的系统和方法(Systems and Methods for Controlling Combustion of aFuel)”的美国专利申请号61/361,169；2012年7月2日提交的，题为“低排放三循环发电系统和方法(Low Emission Triple-Cycle PowerGeneration Systems and Methods)”的美国专利申请号61/361,170；2012年7月2日提交的，题为“低排放三循环发电系统和方法”的美国专利申请号61/361,173；2012年7月2日提交的，题为“通过排气再循环和直接接触冷却器的化学计量燃烧(Stoichiometric Combustion WithExhaust Gas Recirculation and Direct Contact Cooler)”的美国专利申请号61/361,176以及2012年7月2日提交的，题为“低排放发电系统和方法”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(power)系统中的低排放发电。更具体地，本公开的实施方式涉及用于提高二氧化碳(CO2)制造和捕集的燃烧燃料的方法和装置。
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，应该从这个角度进行阅读，而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控制与交易（cap-and-trade）政策使得减少CO2排放成为对于这些和其它国家以及在那里操作烃生产系统的公司优先考虑的事。
相比于其它技术，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成本下操作。然而，由于若干原因，从燃气轮机联合循环装置的排气(exhaust)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捕集系统中的再沸器任务。其它常见的因素可以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的高成本。
在联合循环系统中降低CO2排放的至少一个途径包括化学计量燃烧和排气再循环。在传统的排气再循环系统中，例如在天然气联合循环（NGCC）中，排气的再循环成分和环境空气混合，并被引导入燃气轮机的压缩机部分中。NGCC的排气中CO2浓度通常为大约3%-4%，但是通过排气再循环能够增加到4%以上。在操作中，传统的NGCC系统只需要大约40%的进气容积来提供对燃料的足够的化学计量燃烧，而剩余的60%空气容积充当稀释剂来调节温度并将排气冷却到适于引入到随后的膨胀器的温度。将部分排气再循环提高了排气中CO2的浓度，其随后可以在燃烧系统中用作稀释剂。
然而，由于CO2的分子量、比热、马赫数效应等，在对压缩机或者膨胀器部分没有进行显著修改的情况下，针对排气中燃气轮机的压缩部分能够容许的CO2的浓度，标准的燃气轮机受到限制。例如，再循环到标准燃气轮机的压缩部分的排气中CO2含量限制为大约20wt%CO2。
此外，典型的NGCC系统产生低压排气，其需要经排气膨胀产生的部分电力来提取(extract)CO2，用于封存(sequestration)或者提高原油采收率（EOR），从而降低NGCC的热效率。进一步，用于CO2提取的设备大且昂贵，并且需要若干阶段的压缩以使环境压力气体具有EOR或者封存所需要的压力。这些限制是从与其它化石燃料例如煤的燃烧有关的低压排气中燃烧后碳捕集具有的特征。
对于本领域中的需要的上述讨论意图是代表性的而不是穷尽性的。解决一种或多种这样的需要或者本领域一些其它相关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，本公开提供燃气轮机系统，其包括第一压缩机、第二压缩机、燃烧室和膨胀器。第一压缩机可以设置为接收再循环的排气，并将其压缩成压缩的再循环排气。第二压缩机可以设置为接收并压缩浓缩的空气以产生压缩的氧化剂。燃烧室可以设置为接收压缩的再循环排气和压缩的氧化剂，并化学计量燃烧燃料流。压缩的再循环排气充当稀释剂，以调节燃烧温度。膨胀器可以设置为接收来自燃烧室的排出物(discharge)以产生再循环的排气。膨胀器进一步可以结合(couple)到第一压缩机，以至少部分地驱动第一压缩机。
另外或者可替代地，本公开提供发电的方法。示例性方法包括：a）在主压缩机中压缩再循环的排气以产生压缩的再循环排气；b）在进气压缩机(inlet compressor)中压缩浓缩的空气以产生压缩的氧化剂；c）当存在压缩的再循环排气时，在燃烧室中化学计量燃烧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；d）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再循环的排气并至少部分地驱动主压缩机。
仍然另外地或者可替代地，本公开提供集成的发电系统。示例性的集成发电系统包括燃气轮机系统和排气再循环系统。燃气轮机系统可以包括第一压缩机、第二压缩机、燃烧室和膨胀器。第一压缩机可以设置为接收再循环的排气，并将其压缩成压缩的再循环排气。第二压缩机可以设置为接收并压缩浓缩的空气以产生压缩的氧化剂，该浓缩的空气的氧气浓度在大约30wt%到大约50wt％之间。燃烧室可以设置为接收压缩的再循环排气和压缩的氧化剂，并化学计量燃烧燃料流，其中压缩的再循环排气用作调节燃烧温度的稀释剂。膨胀器可以设置为接收来自燃烧室的排出物以产生再循环的排气流。膨胀器可以进一步结合到第一压缩机，并适于至少部分地驱动第一压缩机。排气再循环系统可以包括热量回收蒸汽发生器、一个或更多冷却单元和增压压缩机。热量回收蒸汽发生器可以可连通地结合到蒸汽燃气轮机。热量回收蒸汽发生器可以设置为接收来自膨胀器的排气以产生蒸汽，该蒸汽在蒸汽发生器中产生电力。一个或更多冷却单元可以设置为使接收自热量回收蒸汽发生器的再循环排气冷却，并从再循环排气中除去冷凝水。增压压缩机可以设置为在将再循环排气注入到第一压缩机以提供压缩的再循环排气之前，增加再循环排气的压力。
附图简介
在回顾对实施方式的非限制性实例的详细描述和附图后，本公开的上述和其它优点会变得显而易见，其中：
图1描述根据描述的一个或更多实施方式的、用于低排放发电和提高CO2回收的集成系统的示意图。
图2描述根据描述的一个或更多实施方式的、用于低排放发电和提高CO2回收的集成系统的另一示意图。
图3描述根据描述的一个或更多实施方式的、用于低排放发电和提高CO2回收的集成系统的另一示意图。
发明详述
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的实施方式。然而，就下面的描述是针对本公开的具体实施方式或者具体用途而言，其仅仅是为了示例性的目的，并且简单地提供对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，其包括落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。
本文使用的各种术语定义如下。就权利要求中使用的术语没有在下面定义而言，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，如在至少一个印刷的出版物或者出版的专利中反映的。
如本文所使用的，术语“天然气”指从原油井获得的多成分气体（伴生气）或者从地下的含气层获得的多成分气体（非伴生气）。天然气的组成和压力可显著地变化。通常的天然气流包括甲烷（CH4）作为主要成分，即天然气流中50mol%以上是甲烷。天然气流也可以包括乙烷（C2H6）、较高分子量的烃（例如，C3-C20烃）、一种或更多种酸性气体（例如，硫化氢、二氧化碳）或者其任意组合。天然气也可以包括较少量的杂质，例如水、氮气、硫化铁、蜡、原油或者其任意组合。
如本文所使用的，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。如本文所使用的，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需要的氧气的大约正或负10%，或者更优选地为化学计量比需要的氧气的大约正或负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）。丙烷的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作为供应的氧气与化学计量燃烧所需要的氧气的比例，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。
如本文所使用的，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速）。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。
本公开系统和工艺的实施方式可以用来产生超低排放电力和CO2，用于提高原油采收率（EOR）和/或封存应用。在一个或更多实施方式中，浓缩的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，并且同时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，可以用作稀释剂来控制、调整或者另外调节燃烧以及进入随后的膨胀器中的排气的温度。由于使用浓缩的空气的原因，再循环的排气的CO2含量可以增加，从而对于相同入口和排出温度，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）可以证明是有利的，以消除过量氧气去除的成本。通过冷却排气和冷凝出自冷却的排气流中的水，可以产生相对高含量的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（Brayton cycle）中的温度调节，但是剩余的清除流能够用于EOR应用中和/或可以产生电力，同时排放微量或不排放硫氧化物（SOX）、氮氧化物（NOX）和/或CO2到大气中。该工艺的结果是在三个独立的循环中生产电力并制造额外的CO2。
现在参考图，图1描述根据一个或更多实施方式的、使用联合循环装置用于发电和CO2回收的示例性集成系统100的示意图。在至少一个实施方式中，发电系统100可以包括燃气轮机系统102，其特征是发电的闭合的布雷顿循环。燃气轮机系统102具有第一或者主压缩机104，其通过轴108结合到膨胀器106。轴108可以是任何机械的、电的或者其它电力结合装置（coupling），从而允许由膨胀器106产生的部分机械能驱动主压缩机104。在至少一个实施方式中，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分别形成压缩机端和膨胀器端。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(line)112引入的、并且与经管线114引入的氧化剂混合的燃料。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、氧化的烃类原料或者其任何组合。经管线114的氧化剂可以来源于第二或者进气压缩机118，其流动地结合到燃烧室110，并且适于压缩经管线120引入的进料氧化剂。在一个或更多实施方式中，管线120中的进料氧化剂可以包括大气、浓缩的空气或者其组合。当管线114中的氧化剂包括大气和浓缩的空气的混合物时，在浓缩的空气与大气混合之前或之后，浓缩的空气可以由进气压缩机118压缩。浓缩的空气的总氧气浓度为大约30wt%、大约35wt%、大约40wt%、大约45wt%或者大约50wt%。
浓缩的空气可以来源于若干源，包括实施进气压缩机118上游的各种技术以产生浓缩的空气。例如，浓缩的空气可以来源于这样的分离技术，如膜分离、变压吸附、变温吸附、氮气装置副产物流(plant-by-product stream)和/或其组合。浓缩的空气也能够来自于空气分离单元（ASU），例如低温ASU，用于产生氮气以进行压力维持或其它目的。来自于ASU的排泄流(reject stream)可以富含氧气，其总的氧气含量为大约50wt%到大约70wt%。该排泄流可以用作至少部分浓缩的空气，并且如果需要，其随后可以用未处理的大气稀释以获得应用所需要的氧气浓度。
如下面更详细地描述的，燃烧室110也可以接收管线144中的压缩的再循环排气，包括主要具有CO2和氮成分的排气再循环。在管线144中的压缩的再循环排气来源于主压缩机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。如可以理解地，再循环排气可以用来提高排气中的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中的排气可以作为管线112中的燃料和管线114中的压缩的氧化剂的燃烧产物而产生。在至少一个实施方式中，管线112中的燃料主要是天然气，从而经管线116产生排出物或者排气，其可以包括容积部分(volumetric portion)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它化合物也可以存在于管线116中的排气中。随着管线116中的排气通过膨胀器106膨胀，其产生机械力驱动主压缩机104，发电机或者其它设施，并且也在管线122中产生气态排气，其由于管线144中压缩的再循环排气的流入而具有提高的CO2含量。在一些实施中，膨胀器106可以适于产生用于其它目的的额外的机械力。
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可以包括热量回收蒸汽发生器（HRSG）126或类似的装置，其流动地结合到蒸汽燃气轮机128。在至少一个实施方式中，HRSG126和蒸汽燃气轮机128的组合可以被表征为产生电力的闭合的郎肯循环(Rankin cycle)。与燃气轮机系统102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。管线122中的气态排气能够引入HRSG126中，以经管线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中的蒸汽可以被发送到蒸汽燃气轮机128中以产生额外的电力。
管线132中的冷却排气可以被发送到第一冷却单元134中，其适于冷却管线132中的冷却排气并且产生冷却的再循环气流140。第一冷却单元134可以包括，例如一个或更多个接触冷却器、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(water dropout stream)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被发送到HRSG126中，以提供用于在管线130那里产生额外蒸汽的水源。在其它实施方式中，经水滴流138回收的水可以用于其它下游的应用，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的体积流量具有提高的质量流速。这可以证明是有利的，因为主压缩机104可以是体积流量限制的，并且，引导更多的质量流量经过主压缩机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，因此允许提高膨胀器106的电力和效率。如可以理解的，因为管线116中富含CO2的排气通常维持较高的比热容，因此这证明是有利的。
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来操作主压缩机104。结果，管线145中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130产生额外的蒸汽。
虽然本文仅描述了第一和第二冷却单元134、136，但是应该理解，在没有背离本公开的保护范围的情况下，可以使用任何数目的冷却单元以适合各种装置。事实上，本文中考虑的是其中管线132中冷却的排气被进一步引导入与排气再循环回路联合的蒸发冷却单元的实施方式，例如在同时提交的题为“通过排气再循环和直接接触冷却器的化学计量燃烧”的美国专利申请中一般描述的，其内容通过参考并入本文，达到与本公开一致的程度。如本文所描述的，排气再循环系统可以包括任何种类的这样的设备，其适于给主压缩机提供排气用于注入到燃烧室中。
主压缩机104可以设置为接收管线145中加压的再循环气体，并将其压缩为压力额定地等于或高于燃烧室100的压力，从而在管线144中产生压缩的再循环排气。如可以理解的，在增压压缩机142中压缩后，在第二冷却单元136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中的排气的体积质量流量。因此，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。
在至少一个实施方式中，清除流146可以从管线144中压缩的再循环排气中被回收，并随后在CO2分离器148中被处理，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的其它工艺中，和/或进一步压缩并注入到陆相储层中用于提高原油采收率（EOR）、封存或另外的目的。由于与来自增压压缩机142的增加的压力结合的管线112中燃料的化学计量或者大体上化学计量燃烧，清除流146中的CO2分压会比常规燃气轮机排气中的高得多。结果，可以使用低能量分离工艺，例如应用能耗较少的(lessenergy-intensive)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）和其它单纯肥料。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题为“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。
实质上去除了CO2并主要由氮组成的剩余流151，也可以来源于CO2分离器148。在一个或更多实施方式中，剩余流151可以引入到气体膨胀器152中，以经管线156提供电力和膨胀的减压气体或者排气。膨胀器152可以是，例如产生电力的氮气膨胀器。如所描述的，气体膨胀器152可以任选地通过共同轴154或者其它机械的、电的或者其它电力结合装置结合到进气压缩机118，从而允许由气体膨胀器152产生的部分电力驱动进气压缩机118。然而，在系统100启动期间和/或在正常操作期间，当气体膨胀器152不能供应所有需要的电力以操作进气压缩机118时，至少一个马达158，例如电动机，可以与气体膨胀器152协同使用。例如，马达158可以灵敏地使尺寸适合，以便在系统100的正常操作期间，马达158可以设置为供应气体膨胀器152缺少的电力。然而，在其它的实施方式中，气体膨胀器152可以用来给其它应用提供电力，并且不直接结合到进气压缩机118。例如，在由膨胀器152产生的电力和压缩机118的需要之间可能存在实质上的不匹配。在这样的情况下，膨胀器152可以适于驱动需要较少（或者较多）电力的较小（或者较大的）的压缩机（没有显示）。
主要由干燥的氮气组成的管线156中膨胀的减压气体可以从气体膨胀器152中排出。在至少一个实施方式中，气体膨胀器152、进气压缩机118和CO2分离器148的组合可以表征为开放的布雷顿循环，或者是发电系统100的第三产生电力的部件。使剩余流151中的氮气膨胀的示例性系统和方法以及其变体可以在同时提交的，题为“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，其描述了根据一个或更多实施方式的、使用联合循环装置用于发电和CO2回收的示例性集成系统200的另一示意图。图2中的系统200实质上类似于图1中的系统100，因此不再详细地讨论，其中相同的元件对应于相同的数字。然而，图2中的系统200可以用下游压缩机158替换系统100中的气体膨胀器152，该下游压缩机158设置为压缩剩余流151并且经管线160产生压缩的排气。在一个或更多实施方式中，管线160中压缩的排气可以适合于注入到储层中用于压力维持应用。在其中甲烷气体通常被再注入到烃井中以维持井的压力的情况下，压缩剩余流151可以证明是有利的。例如，管线160中加压的氮气可以代替注入到烃井中，并且任何剩余甲烷气体均可以售出，或者另外用作相关应用中的燃料，例如提供管线112中的燃料。
参考图3，其描述了根据一个或更多实施方式的、使用联合循环装置用于发电和CO2回收的示例性集成系统300的另一示意图。图3中的系统300实质上分别类似于图1和2中的系统100和200，因此不再详细地讨论，其中相同的元件对应于相同的数字。如所描述的，系统300可以表征为如参考图1所讨论的产生电力的氮气膨胀器152以及如参考图2所讨论的压力维持下游压缩机158的混合装置。在一个或更多实施方式中，剩余流151可以分开，从而将剩余流151的第一部分引导至气体膨胀器152中，同时将剩余流151的第二部分经管线162引导至下游压缩机158中。在至少一个实施方式中，可以操纵第一部分和第二部分的各自的体积质量流量，以便提供预定的和/或要求量的剩余流151到任一个位置中以使产量最大化。
通过使用浓缩的空气作为管线114中压缩的氧化剂，并且在增压压缩机142中使排气加压，发电系统100能够达到排气中更高浓度的CO2，从而允许更有效的CO2分离和捕集。本文公开的实施方式能够有效地将管线116中排气中的CO2浓度增加到范围为大约10wt%到大约20wt%的CO2浓度。为了达到这样的CO2浓度，燃烧室110能够适于化学计量燃烧或者大体上化学计量燃烧管线112中燃料和管线114中压缩的氧化剂的进料混合物，其中管线114中压缩的氧化剂包括浓缩的空气，其总氧气浓度为大约30wt%、大约35wt%、大约40wt%、大约45wt%或者大约50wt%。
为了调节化学计量燃烧的温度并且满足膨胀器106入口温度和成分冷却需要，来自于管线144中压缩的再循环排气的、具有增加的CO2含量的部分排气可以注入到燃烧室110中作为稀释剂。因此，本公开的实施方式可以基本上消除管线116排气中的过量氧气，并且也将其CO2浓度增加到大约20wt%。如此，管线122中的气态排气可以具有少于大约3.0wt%的氧气，或者少于大约1.0wt%的氧气，或者少于大约0.1wt%的氧气，或者甚至少于大约0.001wt%的氧气。
CO2浓度增加的至少一个益处是对于相同的入口和排出温度，膨胀器106可以在甚至较高的膨胀比下操作，从而产生增加的电力。这是由于相对于在环境空气中发现的氮气CO2的较高热容。在一个或更多实施方式中，膨胀器106的膨胀比可以从大约17.0增加到大约20.0，其分别对应于大约10wt%和大约20wt%CO2再循环流。可以应用使用具有大约35wt%氧气的浓缩空气的实施方式，以在CO2再循环流中达到大约20wt%。
在再循环气体中CO2浓度增加的其它益处包括用于CO2分离的提取的清除流146中CO2浓度的增加。由于其CO2浓度的增加，清除流146不需要很大以提取需要量的CO2。例如，操作提取以进行CO2分离的设备可以较小，包括其管系、热交换器、阀门、吸收塔等。此外，增加浓度的CO2可以提高CO2去除技术的性能，包括使用低能量分离工艺，例如使用能耗较少的溶剂，否则这是站不住脚的。因此，可以显著地降低用于捕集CO2的资本支出。
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个部件中达到或者经受的具体温度和压力可以根据——除了其它因素之外——使用的氧化剂的纯度和/或膨胀器、压缩机、冷却器等的特定构造(makes)和/或模型而改变。因此，应该理解，本文描述的具体数据仅仅是为了说明性的目的，而不应该解释为其唯一解释。在一个实施方式中，进气压缩机118可以提供管线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，本文还考虑航空衍生的燃气轮机技术，其可以产生和消耗的压力高达大约750psia和更大。
主压缩机104可以设置为将再循环的排气再循环并在额定地高于或等于燃烧室110压力的压力下压缩成管线144中压缩的再循环排气，并且使用该再循环排气的部分作为燃烧室110中的稀释剂。因为燃烧室110中所需要的稀释剂的量取决于用于化学计量燃烧的氧化剂的纯度或者膨胀器106的具体模型或设计，所以可以在膨胀器106的出口布置一圈的热电偶(aring ofthermocouple)和/或氧传感器（没有显示）。在操作中，热电偶和传感器可以适于调整和测定作为稀释剂——将燃烧产物冷却为需要的膨胀器入口温度所需要的——所需要的排气的体积，并且也调整注入到燃烧室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传感器检测的氧水平，管线144中压缩的再循环排气和管线114中压缩的氧化剂的体积质量流量可以被操纵或者可以波动，以与需要相匹配。对于用于控制通过燃烧燃料产生的排气的组成的系统和方法的示例性实施方式和更详细的描述可以在同时提交的，题为“用于控制燃料燃烧的系统和方法”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。
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，在燃烧室110中可以经受大约12-13psia的压力下降。管线112中的燃料和管线114中压缩的氧化剂的燃烧可以产生大约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。如上所述，由于来自于管线144中压缩的再循环排气的富含CO2排气的增加的质量流量和较高的比热容，在膨胀器106中可以达到较高的压力比，从而允许较高的入口温度和提高的膨胀器106电力。
离开膨胀器106的管线122中的气态排气可以表现出等于或接近于环境的压力。在至少一个实施方式中，管线122中气态排气的压力为大约13-17psia。在经过HRSG126之前，管线122中气态排气的温度可以为大约1225°F到大约1275°F，以产生管线130中的蒸汽和管线132中的冷却排气。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体流140。如可以理解的，这样的温度能够波动，这主要取决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的压力提高为范围为大约17psia到大约21psia的压力。结果，压缩机104最后接受和压缩具有较高密度和增加的质量流量的再循环排气，从而允许实质上较高的排出压力同时维持相同或类似的压力比。为了进一步提高再循环排气的密度和质量流量，从增压压缩机142排出的管线145中的加压再循环气体然后进一步在第二冷却单元136中冷却。在一个或更多实施方式中，第二冷却单元136可以设置为在管线145中加压的再循环气体被引导至主压缩机104之前，将其温度降低至大约105°F。
在至少一个实施方式中，从主压缩机104排出的管线144中压缩的再循环排气的温度，以及因此清除流146的温度可以为大约800°F，压力为大约280psia。增压压缩机142的加入和浓缩空气的化学计量燃烧可以增加清除流146中的CO2清除压力，由于较高的CO2分压，这可以导致在CO2分离器148中的溶剂处理性能提高。
通过下列的仿真实例可以进一步描述本公开的实施方式。虽然仿真实例涉及具体的实施方式，但是不应该认为其将本公开限制在任何具体的方面。
为了说明使用浓缩的空气作为管线114中压缩的氧化剂的优良性能，模拟了系统100，其使用标准的空气，然后在相同的环境条件下对于相同的燃气轮机系统102使用氧气浓度大约为35wt%的浓缩空气。下表提供了这些测试结果以及性能估测。
表1
如表1显而易见地，包括浓缩空气作为管线114中压缩的氧化剂的实施方式可以导致膨胀器106电力的增加，这是由于通过膨胀器106增加的膨胀压力比和增加的质量流量。此外，部分由于从空气中除去部分N2成分，虽然主压缩机104可以经历电力需要的轻微增加，但是该增加多于通过在进气压缩机118中减少的空气压缩电力进行的补偿，从而导致需要的总压缩电力的总体减少。如可以理解的，由于对于相同量的氧气减少的气流，进气压缩机118可以表现出需要的压缩机电力的相当大的减少。重要地，表1暗示了在联合循环电力输出中大的增加，其反映了联合循环效率中大约1.0%的提高。
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举例的方式显示的。然而，还应该明白，本公开并不意图限制于本文公开的具体实施方式。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 (20)
1.燃气轮机系统，其包括：
第一压缩机，其设置为接收再循环的排气，并将其压缩成压缩的再循环排气；
第二压缩机，其设置为接收并压缩浓缩的空气以产生压缩的氧化剂；
燃烧室，其设置为接收所述压缩的再循环排气和所述压缩的氧化剂，并且化学计量燃烧燃料流，其中所述压缩的再循环排气用作稀释剂以调节燃烧温度；和
膨胀器，其结合到所述第一压缩机并且设置为接收来自所述燃烧室的排出物以产生再循环的排气并至少部分地驱动所述第一压缩机。
2.权利要求1所述的系统，其中所述浓缩空气的氧气浓度在大约30wt%和大约50wt%之间。
3.权利要求2所述的系统，其中所述浓缩空气与大气混合以获得大约30wt%和大约50wt%之间的氧气浓度。
4.权利要求1所述的系统，其中所述浓缩空气来源于膜分离、变压吸附、变温吸附和其任意组合。
5.权利要求1所述的系统，其中所述浓缩空气来源于空气分离单元的排泄流。
6.权利要求5所述的系统，其中所述排泄流的氧气浓度在大约50wt%和大约70wt%之间。
7.权利要求1所述的系统，其中所述再循环排气的CO2浓度在大约10wt%和大约20wt%之间。
8.权利要求1所述的系统，其中所述燃料流选自天然气、甲烷、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、氧化的烃类原料和其任何组合。
9.权利要求1所述的系统，进一步包括清除流，所述清除流来自压缩的再循环排气并且在CO2分离器中被处理以产生CO2流和大体上包括氮气的剩余流。
10.产生电力的方法，其包括：
在主压缩机中压缩再循环的排气以产生压缩的再循环排气；
在进气压缩机中压缩浓缩的空气以产生压缩的氧化剂；
当存在所述压缩的再循环排气时，在燃烧室中化学计量燃烧所述压缩的氧化剂和燃料，从而产生排出流，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出流的温度；和
在膨胀器中使所述排出流膨胀，以至少部分地驱动所述主压缩机并产生所述再循环的排气和至少部分地驱动所述主压缩机。
11.权利要求10所述的方法，其中所述浓缩空气的氧气浓度在大约30wt%和大约50wt%之间。
12.权利要求11所述的方法，进一步包括混合所述浓缩空气与大气以获得大约30wt%和大约50wt%之间的氧气浓度。
13.权利要求10所述的方法，其中所述再循环排气的CO2浓度在大约10wt%和大约20wt%之间。
14.权利要求10所述的方法，其中所述浓缩空气来源于空气分离单元的排泄流，所述排泄流的氧气浓度在大约50wt%和大约70wt%之间。
15.集成系统，其包括：
燃气轮机系统，其包括：
第一压缩机，其设置为接收再循环的排气，并将其压缩成压缩的再循环排气；
第二压缩机，其设置为接收并压缩浓缩的空气以产生压缩的氧化剂，所述浓缩空气的氧气浓度在大约30wt%和大约50wt%之间；
燃烧室，其设置为接收所述压缩的再循环排气和所述压缩的氧化剂，并且化学计量燃烧燃料流，其中所述压缩的再循环排气用作稀释剂以调节燃烧温度；和
膨胀器，其结合到所述第一压缩机并且设置为接收来自所述燃烧室的排出物以产生所述再循环的排气流和至少部分地驱动所述第一压缩机；和排气再循环系统，其包括：
热量回收蒸汽发生器，其可连通地结合到蒸汽燃气轮机，所述热量回收蒸汽发生器设置为接收来自所述膨胀器的所述再循环排气以产生蒸汽，所述蒸汽在所述蒸汽发生器中产生电力；
一个或更多冷却单元，其设置为使接收自所述热量回收蒸汽发生器的所述再循环排气冷却，并从所述再循环排气中除去冷凝水；和
增压压缩机，其设置为在将所述再循环排气注入到所述第一压缩机以提供所述压缩的再循环排气之前，增加所述再循环排气的压力。
16.权利要求15所述的系统，其中所述增压压缩机将所述再循环排气流的压力增加到在大约17psia和大约21psia之间的压力。
17.权利要求15所述的系统，其中所述再循环排气的CO2浓度在大约15wt%和大约20wt%之间。
18.权利要求15所述的系统，其中所述浓缩空气与大气混合以获得大约30wt%和大约50wt%之间的氧气浓度。
19.权利要求15所述的系统，其中所述浓缩空气来源于膜分离、变压吸附、变温吸附、空气分离单元和其任意组合。
20.权利要求19所述的系统，其中所述空气分离单元具有氧气浓度在大约50wt％和大约70wt％之间的排泄流，所述排泄流大体上提供所述浓缩空气。
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| US36117810P | 2010-07-02 | 2010-07-02 | |
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| US20130091854A1 (en) | 2013-04-18 |
| AU2011271635B2 (en) | 2015-10-08 |
| WO2012003079A1 (en) | 2012-01-05 |
| EP2588728A4 (en) | 2017-11-01 |
| EP2588728A1 (en) | 2013-05-08 |
| BR112012031505A2 (pt) | 2016-11-01 |
| JP2013530376A (ja) | 2013-07-25 |
| EA029336B1 (ru) | 2018-03-30 |
| EA201390058A1 (ru) | 2013-05-30 |
| SG186157A1 (en) | 2013-01-30 |
| US9903316B2 (en) | 2018-02-27 |
| SG10201505280WA (en) | 2015-08-28 |
| CN102959203B (zh) | 2018-10-09 |
| AR081786A1 (es) | 2012-10-17 |
| AU2011271635A1 (en) | 2013-01-10 |
| MY160833A (en) | 2017-03-31 |
| TW201215820A (en) | 2012-04-16 |
| MX354587B (es) | 2018-03-12 |
| CA2801494C (en) | 2018-04-17 |
| TWI579507B (zh) | 2017-04-21 |
| MX2012014458A (es) | 2013-02-07 |
| CA2801494A1 (en) | 2012-01-05 |
| EP2588728B1 (en) | 2020-04-08 |
| JP5906555B2 (ja) | 2016-04-20 |
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