CN107575308A - 低排放三循环动力产生系统和方法 - Google Patents

低排放三循环动力产生系统和方法 Download PDF

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CN107575308A
CN107575308A CN201710761087.8A CN201710761087A CN107575308A CN 107575308 A CN107575308 A CN 107575308A CN 201710761087 A CN201710761087 A CN 201710761087A CN 107575308 A CN107575308 A CN 107575308A
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R·H·欧尔菲克
M·明特
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ExxonMobil Upstream Research Co
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Abstract

本申请的名称为低排放三循环动力产生系统和方法。提供了用于联合循环动力工厂中的低排放动力产生的方法和系统。一个系统包含燃气涡轮系统，其在压缩的再循环流的存在下化学计量地燃烧燃料和氧化剂，以提供机械动力和气态废气。压缩的再循环流用作稀释剂以调节燃烧工艺的温度。增压器可在气态废气被压缩成为压缩的再循环流之前提高气态废气的压力。净化流从压缩的再循环流流出并且被引导至排出CO2和富氮气体的CO2分离器，CO2和富氮气体可在气体膨胀器中膨胀以产生额外的机械动力。

Description

低排放三循环动力产生系统和方法
本申请是分案申请，原申请的申请日为2011年6月9日、申请号为201180033204X(PCT/US2011/039826)、发明名称为“低排放三循环动力产生系统和方法”。
相关申请的交叉引用
本申请要求于2010年7月2日提交的，名称为“Low Emission Triple-Cycle PowerGeneration Systems and Methods(低排放三循环动力产生系统和方法)”的美国临时专利申请61/361,173的权益，其在此通过引用全文并入。
本申请含有涉及以下的主题：于2010年7月2日提交的，名称为“Systems andMethods for Controlling Combustion of a Fuel(控制燃料燃烧的系统和方法)”的美国专利申请号61/361,169；于2010年7月2日提交的，名称为“Low Emission Triple-CyclePower Generation Systems and Methods(低排放三循环动力产生系统和方法)”的美国专利申请号61/361,170；于2010年7月2日提交的，名称为“Stoichiometric Combustion WithExhaust Gas Recirculation and Direct Contact Cooler(具有废气再循环和直接接触冷却器的化学计量的燃烧)”的美国专利申请号61/361,176；于2010年7月2日提交的，名称为“Stoichiometric Combustion of Enriched Air With Exhaust Gas Recirculation(具有废气再循环的富集空气的化学计量的燃烧)”的美国专利申请号61/361,178，和于2010年7月2日提交的，名称为“Low Emission Power Generation Systems and Methods(低排放动力产生系统和方法)”的美国专利申请号61/361,180。
技术领域
本公开的实施方式涉及联合循环动力系统中的低排放动力产生。更具体地，本公开的实施方式涉及为了增强的CO2制造和捕获以及富氮气体的膨胀或压缩，化学计量地燃烧燃料的方法和装置。
背景技术
本章节意欲介绍本领域的多个方面，其可与本公开的示例性实施方式相关。相信该讨论帮助提供框架，以便于更好地理解本公开的具体方面。因此，应当理解应据此阅读本章节，并不必承认为现有技术。
很多产油国家正经历动力需求的强烈国内增长并对提高采收率法采油(EOR)感兴趣，以提高从他们油藏采油。两种常见的EOR技术包含用于油藏压力保持的氮气(N2)注入和用于EOR的混相驱动(miscible flooding)的二氧化碳(CO2)注入。也存在关于温室气体(GHG)排放的全球关注。该关注连同很多国家中的限制和交易政策的执行使得减少CO2排放成为这些和其他国家以及其中操作烃生产系统的公司优先考虑的事。
一些降低CO2排放的方法包含燃料去碳化或利用溶剂诸如胺类的燃烧后捕获。然而，这两种方案昂贵并降低动力产生效力，导致较低的动力产生、增加的燃料需求和增加的电成本以满足国内动力需求。具体地，氧、SOX和NOX成分的存在使得胺溶剂吸收的使用非常成问题。另一种方法是在结合循环中的含氧燃料(oxyfuel)燃气涡轮(例如，其中来自燃气涡轮布雷顿循环的废热被捕获以制造蒸汽并且在兰金循环中产生额外的动力)。然而，没有可在这样的循环中运转的商业可得的燃气涡轮，并且生产高纯氧要求的动力显著降低了该工艺的总体效力。一些研究已经比较了这些工艺并显示每种方法的一些优势。见例如BOLLAND，OLAV，和UNDRUM，HENRIETTE，Removal of CO2from Gas Turbine Power Plants:Evaluation of pre-and post-combustion methods，SINTEF Group，found at http://www.energy.sintef.no/publ/xergi/98/3/3art-8-engelsk.htm(1998)。
降低CO2排放的其他方法包含诸如在天然气联合循环(NGCC)中的化学计量的废气再循环。在常规NGCC系统中，仅要求大约40％的空气吸入体积，以提供燃料的充分的化学计量的燃烧，而剩余60％的空气体积用于调节温度和冷却烟道气，以便适于引入随后的膨胀器，但也不利地产生难以去除的过量的氧副产品。典型的NGCC产生低压烟道气，其要求一部分产生的动力提取CO2，用于埋存(sequestration)或EOR，由此减少NGCC的热效力。进一步，用于CO2提取的设备大并且昂贵，而且需要数个压缩阶段以便使环境压力气体达到EOR或埋存所需的压力。这样的限制是来自与其他化石燃料诸如煤的燃烧相关的低压烟道气的燃烧后碳捕获的典型特征。
因此，仍然存在对低排放、高效力动力产生和CO2捕获或制造工艺的实质需要。
发明内容
本公开涉及操作系统的三循环动力产生系统和方法。在一个示例性系统中，综合系统包括燃气涡轮系统、废气再循环系统和气体膨胀器。燃气涡轮系统具有第一燃烧室，其被配置用于在压缩的再循环流的存在下化学计量地燃烧第一压缩的氧化剂和第一燃料。燃烧室引导第一排出物流至膨胀器，以产生气态废流和至少部分地驱动主压缩机。废气再循环系统接收来自燃气涡轮系统的膨胀器的气态废流并从其中含有的热能产生动力，诸如通过热回收蒸汽产生单元。废气再循环系统进一步按路线发送废气流至主压缩机，在那里将其压缩以产生压缩的再循环流。压缩的再循环流被引导至燃烧室以用作稀释剂，其被配置用于调节第一排出物流的温度。综合系统进一步包含经净化流流体连接至压缩的再循环流的CO2分离器。CO2分离器从净化流产生富含CO2流和残余流，包括富氮气体。如以上指示的，综合系统也包含气体膨胀器。气体膨胀器经残余流被流体连接至CO2分离器，因为其适于通过使残余流膨胀产生动力。
在操作三循环动力产生系统的示例性方法中，产生动力的方法可包括在第一燃烧室中和在压缩的再循环流的存在下，化学计量地燃烧第一压缩的氧化剂和第一燃料。燃烧可从而产生第一排出物流。压缩的再循环流可用作稀释剂，其被配置用于调节第一排出物流的温度。该方法进一步包含在膨胀器中使第一排出物流膨胀以至少部分地驱动第一压缩机并产生气态废流。第一排出物流的膨胀可产生额外的动力用于其他用途。该方法进一步包含引导气态废流进入第一压缩机，其中第一压缩机压缩气态废流并从而产生压缩的再循环流。仍然进一步地，该方法包含经净化流提取一部分压缩的再循环流至CO2分离器，CO2分离器经源于CO2分离器并主要由富氮气体组成的残余流流体连接至气体膨胀器。示例性方法进一步包含在气体膨胀器中使残余流膨胀，以产生机械动力和废气。
附图说明
本公开的上述和其他优势可在回顾以下详细描述和实施方式的非限制性实施例的附图后变得显而易见，其中：
图1描绘了根据本公开的一种或多种实施方式的用于低排放动力产生和增强的CO2回收的综合系统。
图2描绘了根据本公开的一种或多种实施方式的用于低排放动力产生和增强的CO2回收的另一个综合系统。
图3描绘了根据本公开的一种或多种实施方式的用于低排放动力产生和增强的CO2回收的另一个综合系统。
图4描绘了根据本公开的一种或多种实施方式的用于低排放动力产生和增强的CO2回收的另一个综合系统。
图5描绘了根据本公开的一种或多种实施方式的用于低排放动力产生和增强的CO2回收的另一个综合系统。
图6描绘了根据本公开的一种或多种实施方式的用于低排放动力产生和增强的CO2回收的另一个综合系统。
图7描绘了根据本公开的一种或多种实施方式的用于低排放动力产生和增强的CO2回收的另一个综合系统。
图8描绘了根据本公开的一种或多种实施方式的用于低排放动力产生和增强的CO2回收的另一个综合系统。
发明详述
在以下详述部分，本公开的具体实施方式结合优选实施方式进行描述。然而，对于以下描述对于本公开的特定实施方式或特定用途是特异性的而言，意欲仅用于示例性目的和简单地提供示例性实施方式的描述。因此，本公开不限于以下描述的具体实施方式，而是它包含落入所附权利要求的真实精神和范围内的所有可选方案、更改和等价物。
本文所用的多种术语定义如下。对于在权利要求中使用的术语在以下未定义而言，其应该给予在已经给予该术语的相关领域中的人最广泛的定义，如在至少一个印刷出版物或授权的专利中反映的。
如本文所用的，术语“天然气”指的是从原油井(相关的气体)或从地下含气地层(非相关的气体)获得的多成分气体。天然气的组成和压力可显著变化。典型的天然气流含有甲烷(CH4)作为主要成分，即大于50mol％的天然气流为甲烷。天然气流也可含有乙烷(C2H6)、较高分子量烃(例如，C3-C20烃)、一种或多种酸性气体(例如，硫化氢、二氧化碳)或其任何组合。天然气也可含有少量杂质，诸如水、氮气、硫化铁、蜡、原油或其任何组合。
如本文所用的，术语“化学计量的燃烧”指的是具有一定体积的包括燃料和氧化剂的反应物和一定体积的由燃烧反应物形成的产物的燃烧反应，其中反应物的整个体积用于形成该产物。如本文所用的，术语“基本上化学计量的燃烧”指的是具有燃烧燃料与氧的摩尔比在以下范围中的燃烧反应：从大约化学计量比要求的氧加或减10％，或更优选从大约化学计量比要求的氧加或减5％。例如，对于甲烷，燃料与氧的化学计量比为1:2(CH4+2O2＞CO2+2H2O)。丙烷将具有燃料与氧为1:5的化学计量比。测量基本上化学计量的燃烧的另一种方法为供应的氧与化学计量的燃烧需要的氧的比，诸如从大约0.9:1至大约1.1:1，或更优选从大约0.95:1至大约1.05:1。
如本文所用的，术语“流”指的是一定体积的流体，尽管使用术语流通常表示移动体积的流体(例如，具有速度或质量流速)。然而，术语“流”不要求速度、质量流速或特定类型的用于封闭流的管道。
目前公开的系统和工艺的实施方式可用于生产超低排放电力和CO2，用于提高采收率法采油(EOR)或埋存应用。根据本文公开的实施方式，空气和燃料的混合物可化学计量地燃烧并且同时与再循环的废气流混合。通常包含燃烧产物诸如CO2的再循环的废气流可用作稀释剂以控制或以其他方式调节化学计量的燃烧和进入随后的膨胀器的烟道气的温度。
在接近化学计量的条件下的燃烧(或“轻微富(slightly rich)”燃烧)可证明是有利的，以便消除过量氧去除的成本。通过冷却烟道气和从流冷凝出水，可以产生相对高含量的CO2流。尽管一部分再循环的废气可用于闭合布雷顿循环中的温度调节，但剩余的净化流可用于EOR应用，并且可产生电力，很少或没有SOX、NOX或CO2排放至大气。例如，根据本文公开的实施方式，净化流可在适于排出富氮气体的CO2分离器中被处理，其可随后在气体膨胀器中膨胀，以产生额外的机械动力。本文公开的系统的结果是在三个分开的循环中产生动力，并以更经济有效的水平制造或捕获额外的CO2。在一些实施中，富氮排出物流可通过多种方式进行加热，以便增加在氮气流上通过膨胀器可获得的动力。另外地，在一些实施中，膨胀器后的氮气出口可被冷却并且用于提供制冷，其可用于改善布雷顿循环中和/或回收废气中的压缩机(一个或多个)的效力。冷氮气流也可用于改善工艺效力的其他应用。
可选地，排出的富氮气体可被发送至EOR设施，用于额外的压缩和/或注入井用于采油和/或压力保持。尽管可能完全独立地生产用于油藏压力保持的氮气和用于EOR的CO2，但本文公开的实施方式利用协同作用，当在综合工艺中生产氮气和CO2两者时，有可能以低得多的成本完成这些气体的生产，同时也产生动力。
现在参考图，图1说明了动力产生系统100，其被配置用于提供利用联合循环布置的改善的燃烧后CO2捕获工艺。在至少一个实施方式中，动力产生系统100可包含燃气涡轮系统102，其可以表征为闭合的布雷顿循环。在一个实施方式中，燃气涡轮系统102可具有通过公共轴108或其他机械、电或其他动力连接连接至膨胀器106的第一或主压缩机104，从而允许由膨胀器106产生的机械能的一部分驱动压缩机104。膨胀器106也可产生用于其他用途的动力。燃气涡轮系统102可为标准燃气涡轮，其中主压缩机104和膨胀器106分别形成标准燃气涡轮的压缩机和膨胀器末端。然而，在其他实施方式中，主压缩机104和膨胀器106可为系统102中单独的组件。
燃气涡轮系统102也可包含燃烧室110，其被配置用于燃烧与压缩的氧化剂114混合的燃料流112。在一种或多种实施方式中，燃料流112可包含任何合适的烃气体或液体，诸如天然气、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、氧化烃原料或其组合。压缩的氧化剂114可源于流体连接至燃烧室110并且适于压缩供应氧化剂120的第二或入口压缩机118。在一种或多种实施方式中，供应氧化剂120可包含任何合适的含氧气体，诸如空气、富氧空气、氧耗尽的空气、纯氧或其组合。
如将在以下更详细地描述的，燃烧室110也可接收压缩的再循环流144——其包含主要具有CO2和氮气成分的烟道气。压缩的再循环流144可源于主压缩机104并适于帮助促进压缩的氧化剂114和燃料112中的化学计量的燃烧，并也增加工作流体中CO2的浓度。在压缩的再循环流144的存在下，引导至膨胀器106的入口的排出物流116可作为燃料流112和压缩的氧化剂114的燃烧产物而产生。在至少一个实施方式中，燃料流112可主要为天然气，从而产生包含体积部分的蒸发的水、CO2、氮气、氧化氮(NOX)和氧化硫(SOX)的排出物116。在一些实施方式中，小部分未燃烧的燃料112或其他化合物也可由于燃烧平衡限制存在于排出物116中。当排出物流116通过膨胀器106膨胀时，它产生机械动力，以驱动主压缩机104、发电机或其他设施，并也产生具有提高的CO2含量的气态废流122。
动力产生系统100也可包含废气再循环(EGR)系统124。尽管在图中说明的EGR系统124合并了多种装置，但说明的构造仅是代表性的，并且可使用任何将废气122再循环回主压缩机的系统。在一种或多种实施方式中，EGR系统124可包含流体连接至蒸汽燃气涡轮128的热回收蒸汽发生器(HRSG)126，或类似设备。在至少一个实施方式中，HRSG 126和蒸汽燃气涡轮128的组合可以表征为闭合的兰金循环。结合燃气涡轮系统102、HRSG126和蒸汽燃气涡轮128可形成联合循环动力产生工厂的一部分，诸如天然气联合循环(NGCC)工厂。气态废流122可被发送至HRSG 126，以产生蒸汽的流130和冷却的废气132。在一些实施方式中，蒸汽130可被发送至蒸汽燃气涡轮128以产生额外的电力。
图1说明了任选地可被并入一些实施中的EGR系统124中的额外的装置。冷却的废气132可被发送至至少一个冷却单元134，其被配置用于降低冷却的废气132的温度并且产生冷却的再循环气流140。在一种或多种实施方式中，冷却单元134可为直接接触冷却器、调温冷却器(trim cooler)、机械制冷单元或其组合。冷却单元134也可被配置用于经水排泄流138去除一部分冷凝水，水排泄流138可在至少一个实施方式中经管线141按路线发送至HRSG 126，以提供用于产生额外的蒸汽130的水源。在一种或多种实施方式中，冷却的再循环气流140可被引导至流体连接至冷却单元134的增压器142(如有需要)。在冷却单元134中，冷却冷却的废气132可减少压缩增压器142中冷却的再循环气流140需要的动力或完全消除对它的需要。
增压器142可被配置用于在冷却的再循环气流140被引入主压缩机104之前增加其压力。与常规风扇或鼓风机系统相反，增压器142增加冷却的再循环气流140的总体密度，从而引导相同体积流量至主压缩机104的增加的质量流速。因为主压缩机104通常是体积-流量限制的，引导更多质量流量通过主压缩机104可导致来自主压缩机104的较高排出压力，从而经过膨胀器106转换成较高的压力比。经过膨胀器106产生的较高压力比可允许较高的入口温度，并且因此增加膨胀器106的动力和效力。这可证明是有利的，因为富含CO2的排出物116通常保持较高的比热容。因此，当并入时，冷却单元134和增压器142每一个可适于优化或改进燃气涡轮系统102的操作。
主压缩机104可被配置用于压缩从EGR系统124诸如从增压器142接收的冷却的再循环气流140至稍高于燃烧室110压力的压力，从而产生压缩的再循环流144。在至少一个实施方式中，净化流146可从压缩的再循环流144流出并随后在CO2分离器148中进行处理以在升高的压力下经管线150捕获CO2。管线150中分离的CO2可用于出售，用于需要二氧化碳的另一个工艺，和/或被压缩和注入陆地油藏，用于提高采收率法采油(EOR)、埋存或另一个目的。
基本上耗尽CO2并且主要由氮气组成的残余流151可源于CO2分离器148。在一种或多种实施方式中，残余流151可在气体膨胀器152诸如流体连接至CO2分离器148的产生动力的氮气膨胀器中进行膨胀。如图1-3所描绘的，气体膨胀器152可通过公共轴154或其他机械、电或其他动力任选地连接连接至入口压缩机118，从而允许由气体膨胀器152产生的一部分动力驱动入口压缩机118。在气体膨胀器152中膨胀后，主要由氮气组成的废气156可被排出至大气或在本领域已知的其他下游应用中实施。例如，膨胀的氮气流可用于蒸发冷却工艺，其被配置用于进一步降低废气温度，如在同时提交的名称为“StoichiometricCombustion with Exhaust Gas Recirculation and Direct Contact Cooler(具有废气再循环和直接接触冷却器的化学计量的燃烧)”的美国专利申请中大体描述的，其内容在此通过引用并入至与本公开一致。在至少一个实施方式中，气体膨胀器152、入口压缩机118和CO2分离器的组合可以表征为开放的布雷顿循环，或系统100的第三动力产生部件。
尽管气体膨胀器152和入口压缩机118的组合或连接可类似于开放的布雷顿循环，但气体膨胀器152——不管从入口压缩机118连接或未连接，均提供系统100的第三动力产生部件。例如，气体膨胀器152可用于向其他应用提供动力，并且不直接连接至化学计量的压缩机118。例如，在由膨胀器152产生的动力和压缩机118的要求之间存在大量失配。在这种情况下，膨胀器152可适于驱动需要较少动力的较小的压缩机(未示出)(或驱动入口压缩机118和一种或多种额外的设施)。
还在其他实施方式中，如将在以下参考图8讨论的，气体膨胀器152可用下游压缩机188取代，其被配置用于压缩残余流151和产生适于注入油藏用于压力保持或EOR应用的压缩的废气190。
如本文所述的EGR系统124可被实施以实现动力产生系统100的工作流体中较高浓度的CO2，从而允许更有效的CO2分离，用于随后的埋存、压力保持或EOR应用。例如，本文公开的实施方式可有效增加烟道气废流中CO2的浓度至大约10vol％或更高。为了实现该目标，燃烧室110可适于化学计量地燃烧燃料112和压缩的氧化剂114的进入混合物。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要求，源于压缩的再循环流144的一部分废气可被注入燃烧室110作为稀释剂。因此，本公开的实施方式可基本上消除来自工作流体的任何过量的氧，同时增加其CO2组分。如此，气态废流122可具有小于大约3.0vol％的氧，或小于大约1.0vol％的氧，或小于大约0.1vol％的氧，或甚至小于大约0.001vol％的氧。在一些实施中，燃烧室110，或更具体地燃烧室的入口流可优选被控制为亚化学计量的燃烧，以进一步减少气态废流122的氧含量。
现在将讨论系统100的示例性操作的细节。如可被理解的，在任何本文公开的实施方式的不同部件中实现或经历的具体温度和压力可取决于使用的氧化剂的纯度和膨胀器、压缩机、冷却器等的具体制造和/或型号等等这些因素变化。因此，将理解本文描述的特定数据仅是为了说明性目的并且不应当被理解为其唯一的解释。例如，在本文所述的一个实施方式中，入口压缩机118可被配置为提供在大约280psia和大约300psia之间范围的压力下的压缩的氧化剂114的化学计量的压缩机。然而，同样在本文中考虑的是航改式(aeroderivative)燃气涡轮技术，其可产生和消耗高达大约750psia和更多的压力。
主压缩机104可被配置用于再循环和压缩再循环的废气成为稍高于燃烧室110压力的压力下或在燃烧室110压力下的压缩的再循环流144，并且在燃烧室110中使用一部分再循环的废气作为稀释剂。因为燃烧室110中需要的稀释剂的量可取决于用于化学计量的燃烧的氧化剂的纯度或膨胀器106的型号，热电偶环和/或氧传感器(未示出)可与燃烧室和/或膨胀器相关连。例如，热电偶和/或氧传感器可被放置在燃烧室110的出口、在膨胀器106的入口上和/或在膨胀器106的出口上。在操作中，热电偶和传感器可适于确定一种或多种流的组成和/或温度，用于确定要求作为稀释剂以冷却燃烧产物至要求的膨胀器入口温度需要的废气的体积。另外地或可选地，热电偶和传感器可适于确定将被注入燃烧室110的氧化剂的量。因此，响应于由热电偶检测的热要求和由氧传感器检测的氧水平，压缩的再循环流144和/或压缩的氧化剂114的体积质量流可被操纵或控制以符合需求。体积质量流速可通过任何合适的流量控制系统进行控制。
在至少一个实施方式中，可在化学计量的燃烧期间通过燃烧室110经历大约12-13psia的压力降。燃料112和压缩的氧化剂114的燃烧可产生大约2000℉和大约3000℉之间的温度以及范围从250psia至大约300psia的压力。因为增加的质量流和源于压缩的再循环流144的富含CO2的工作流体的较高比热容，可实现通过膨胀器106的较高的压力比，从而允许较高的入口温度和增加的膨胀器106动力。
离开膨胀器106的气态废流122可具有在或接近环境的压力。在至少一个实施方式中，气态废流122可具有大约15.2psia的压力。在通过HRSG126之前，气态废流122的温度可从大约1180℉至大约1250℉的范围内，以产生管线130中的蒸汽和冷却的废气132。冷却的废气132可具有从大约190℉至大约200℉范围内的温度。在一种或多种实施方式中，冷却单元134可降低冷却的废气132的温度，从而产生具有温度在大约32℉和120℉之间的冷却的再循环气流140，主要取决于在具体的位置和在具体季节期间的湿球温度。
根据一种或多种实施方式，增压器142可被配置用于提高冷却的再循环体流140的压力至范围从大约17.1psia至大约21psia的压力。结果，主压缩机104接收和压缩具有较高的密度和增加的质量流的再循环的烟道气工作流体，从而允许充分较高的排出压力，同时保持相同或相似的压力比。在至少一个实施方式中，从主压缩机104排出的压缩的再循环流144的温度可为大约800℉，压力为大约280psia。
下表提供了具有和不具有增压器142增加的益处的基于联合循环燃气涡轮的测试结果和性能评估，如本文所述的。
表1
如应从表1显而易见的，由于压力比增加，包含增压器142的实施方式可使得膨胀器106功率(即，“燃气涡轮膨胀器功率”)增加。尽管主压缩机104的功率需求可增加，但它的增加不只被膨胀器106的功率输出增加抵消，从而导致大约1％lhv(较低的加热值)的总体热动力性能效力改善。
另外，增加增压器142也可增加氮气膨胀器152的功率输出和净化流146管线中CO2净化压力。尽管增压器142可增加氮气膨胀器152的功率输出，但在表1中可见氮气膨胀器152是对具有或不具有增压器的总体系统100的效力的显著的促进因素。
由于较高的CO2分压，净化流146的净化压力的增加可导致CO2分离器148中改善的溶剂处理性能。这种改善可包含但不限于，以用于溶剂提取工艺的减小的设备尺寸形式的总体资金花费的减少。
现在参考图2，其描绘的是图1的动力产生系统100的可选实施方式，实施并且描述为系统200。如此，参考图1可更好地理解图2。类似于图1的系统100，图2的系统200包含连接至废气再循环(EGR)系统124或以其他方式由废气再循环(EGR)系统124支持的燃气涡轮系统102。然而，图2中的EGR系统124可包含如此实施方式，其中增压器142跟随HRSG 126或可以其他方式被流体连接至HRSG 126。如此，冷却的废气132可在冷却单元134中被降温之前在增压器142中进行压缩。因此，冷却单元134可用作适于去除由增压器142产生的压缩热的后冷却器。与先前公开的实施方式一样，水排泄流138可或可不按路线发送至HRSG 126，以产生额外的蒸汽130。
冷却的再循环气流140可随后被引导至主压缩机104，在那里它如上所讨论的被进一步压缩，从而产生压缩的再循环流144。如可理解的，在增压器142中压缩后，冷却冷却单元134中冷却的废气132可减少在随后的主压缩机104中压缩冷却的再循环气流140至预定压力需要的动力的量。
图3描绘了图1的低排放动力产生系统100的另一个实施方式，实施为系统300。如此，参考图1和2可更好地理解图3。分别类似于图1和2描述的系统100、200，系统300包含由EGR系统124支持的或以其他方式连接至EGR系统124的燃气涡轮系统102。然而，图3中的EGR系统124可包含第一冷却单元134和第二冷却单元136，在其间具有流体连接的增压器142。与先前的实施方式一样，每个冷却单元134、136都可为直接接触冷却器、调温冷却器或类似物，如本领域已知的。
在一种或多种实施方式中，从HRSG 126排出的冷却的废气132可被发送至第一冷却单元134，以产生冷凝水排泄流138和冷却的再循环气流140。冷却的再循环气流140可被引导至增压器142，以便提高冷却的再循环气流140的压力，并随后将它引导至第二冷却单元136。第二冷却单元136可用作后冷却器，其适于去除由增压器142产生的压缩热，并且也经水排泄流143去除额外的冷凝水。在一种或多种实施方式中，每个水排泄流138、143可或可不按路线发送至HRSG 126，以产生额外的蒸汽130。
冷却的再循环气流140可随后被引入主压缩机104，以产生稍高于燃烧室110压力或处于燃烧室110压力下的压缩的再循环流144。如可理解的，在第一冷却单元134中冷却冷却的废气132可减少在增压器142中压缩冷却的再循环气流140需要的动力的量。另外，进一步冷却第二冷却单元136中的废气可减少压缩冷却的再循环气流140至随后的主压缩机104中的预定压力需要的动力的量。
现在参考图4，其描绘了低排放动力产生系统400的另一个实施方式，在一些方面类似于图3的系统300。如此，可参考图1和3更好地理解图4的系统400。然而，应当注意到参考图1-3公开的单独的实施方式或其组合可结合图4的系统400进行实施和/或省略，而不脱离本公开的范围。例如，如本文他处描述的，并入EGR系统124的具体设施和设备可变化。
如上所述，从主压缩机104排出的压缩的再循环流144的温度可为大约800℉，并且显示大约280psia的压力。因此，从压缩的再循环流144流出的净化流146可显示相似的温度和压力。应当再一次注意具体的温度和压力将取决于膨胀器、压缩机、冷却器等的具体的制造和型号不可避免的改变。因为压力比在具有燃烧后CO2回收的常规天然气联合循环(NGCC)系统中发现的那些高得多，它促进了在CO2分离器148中使用更少能量-密集气体处理工艺。例如，这种升高的温度和压力，结合由燃烧室110中进行的化学计量的燃烧引起的大量缺氧，可允许使用热碳酸钾溶剂，以从净化流146提取CO2。在其他实施方式中，CO2选择性吸附剂可包含但不限于，单乙醇胺(“MEA”)、二乙醇胺(“DEA”)、三乙醇胺(“TEA”)、碳酸钾、甲基二乙醇胺(“MDEA”)、活性甲基二乙醇胺(“aMDEA”)、二甘醇胺(“DGA”)、二异丙醇胺(“DIPA”)、哌嗪(“PZ”)、其衍生物、其混合物或其任何组合。其他合适的吸附剂和技术可包含但不限于碳酸丙烯酯物理吸附剂溶剂以及其他碳酸烷基酯、2至12个甘醇单元的聚乙二醇的二甲基醚(SelexolTM工艺)、n-甲基-吡咯烷酮、环丁砜和使用气体处理工艺。
在一个实施方式中，CO2分离器148中的气体处理工艺可要求净化流146的温度冷却至大约250℉-300℉。为了实现该目标，净化流146可被引导通过热交换器158，诸如流体连接至残余流151的交叉交换热交换器。在至少一个实施方式中，在CO2分离器148中从净化流146提取CO2可留下处于净化流146的升高的压力或接近该升高的压力和在大约150℉的温度下的富氮残余流151。在一个实施方式中，与冷却净化流146相关的热能可经热交换器158被提取并用于再加热残余流151，从而产生具有大约750℉温度和大约270-280psia压力的加热的氮蒸气160。尽管与净化流146的热交换是加热残余流的一种方式，但其他方法也位于本公开的范围内。例如，在一种或多种实施方式中，可利用HRSG 126进行补充加热流151，以供应热以及产生蒸汽130。其他示例性方法在本文中进行描述并且不应该被认为是加热残余流151的可用方法的穷尽列举。
在一种或多种实施方式中，加热的氮蒸气160可随后通过气体膨胀器152进行膨胀。因此，热交换器158中的交叉交换热可被配置用于捕获源于主压缩机104的大量压缩能量并且使用其以使从气体膨胀器152提取的动力最大化，和任选地为化学计量的入口压缩机118提供动力。在至少一个实施方式中，主要由大气压下的氮气组成的废气156可被无害地排出至大气或在本领域已知的其他下游应用中实施。示例性下游应用，诸如蒸发冷却工艺，在同时提交的名称为“Stoichiometric Combustion with Exhaust GasRecirculation and Direct Contact Cooler(具有废气再循环和直接接触冷却器的化学计量的燃烧)”的美国专利申请中进行描述，如上所述。
在启动系统400期间和在正常运行期间，当气体膨胀器152可能不能供应所有需要的动力以运行入口压缩机118时，至少一个发动机162，诸如电动机，可与气体膨胀器152协同使用。例如，发动机(一个或多个)162可具有适当(sensibly)的大小，以便在系统400的正常操作期间，发动机(一个或多个)162可被配置用于从气体膨胀器152供应不足的动力。另外地或可选地，在操作期间，有些时候气体膨胀器152产生比入口压缩机118需要的更多的能量。在一些实施中，至少一个发动机162可为发动机/发生器系统，其被可选择地配置用于诸如从电网向压缩机提供动力或从由涡轮152产生的动力产生电。
现在参考图5，其描绘的是低排放动力产生系统500的另一个实施方式，在一些方面类似于图4的系统400。如此，图5的整个系统500将不进行详细地描述，但可参考图1、3和4最好地理解。应当注意参考图1-4公开的任何实施方式可单独实施或结合系统500实施，而不脱离本公开的范围。
在一个实施方式中，一旦净化流146从压缩的再循环流144中流出，它的温度可由催化装置164中进行的催化工艺升高。在操作中，催化装置164可被配置用于减少净化流中的氧和/或一氧化碳含量，并将其转化为残余CO2和热。催化装置164可为单独的设备或多个并联、串联、或并联和串联的组合的设备。在一个实施方式中，催化装置164可为仅需要少量动力运行的小设备。一个示例性催化装置164可包含通常用于HRSG以满足排放要求的氧还原催化剂。这样的系统通常不被设计以去除大量氧，但是如果显著量的氧保留在压缩的再循环流144中，则净化流146可在进一步处理或使用——例如，用于提高采收率法采油(EOR)、CO2分离等的压缩和注入——之前被再循环通过催化装置164多于一次。
另外，净化流146中的任何残余烃也可在催化装置164中燃烧。在至少一个实施方式中，净化流146的温度可通过完全催化转化存在于净化流146中的大约1200ppm氧，从大约785℉升高至大约825℉。可用于催化装置164的说明性催化剂可包含但不限于，镍、铂、铑、钌、钯、或其衍生物、其混合物、其任何组合。该热含量增加可被引入热交换器158并且与富氮残余流151交叉交换，从而导致加热的氮蒸气160的较高温度，并且促进气体膨胀器152中更有效和有力的膨胀工艺。
如包含气体膨胀器152的三循环系统的仍进一步增强，在一种或多种实施方式中，水可经管线166被注入加热的氮蒸气160中，以增加气体膨胀器152的质量通过量并因此增加产生的动力。水可被处理为雾化水或蒸汽。在至少一个实施方式中，通过注入雾化水或蒸汽提供的补充的动力可增加动力输出从大约169MW至大约181MW。如可理解的，动力输出将通常取决于气体膨胀器的制造和型号。应当注意到经管线166将雾化水或蒸汽注入加热的氮蒸气160中以便增加通过气体膨胀器152的质量流可在本文公开的任何实施方式中实施，而不脱离本公开的范围。
参考图6，其描绘的是低排放动力产生系统600的另一个实施方式，类似于图5的系统500。如此，整个系统600将不进行详细地描述，但可参考图5最好地理解。在一个实施方式中，系统600可包含在气体膨胀器152之前放置的额外的化学计量的燃烧室168。燃烧室168可被配置用于化学计量地燃烧燃料170和压缩的氧化剂172的组合，更像上述的燃烧室110，以便在升高的温度和压力下产生排出物流174。在一个实施方式中，燃料170和压缩的氧化剂172可来自分别与被供应进入第一燃烧室110的燃料112和压缩的氧化剂114相同的来源。在并入额外的燃烧室168的实施中，热交换器158可通过其他手段冷却净化流，诸如通过加热在系统600或他处中的一种或多种其他流。例如，对净化流的热交换器可向HRSG或重整工艺提供额外的热。
在其他实施方式中，特别是其中期望或要求零CO2排放的实施方式，燃料170可主要由氢组成。在至少一个实施方式中，氢燃料可通过重整HRSG 126或单独的HRSG(未示出)中的甲烷产生。在甲烷的重整和水煤气转换后，氢产物流中的CO2可在吸收塔(未示出)例如在CO2分离器148中去除。氢可随后与燃烧室168内的加热的氮蒸气160流中的一些氮气混合，以制造可接受的燃气涡轮燃料。
从热交换器158排出的或从CO2分离器148排出的加热的氮蒸气160可用作稀释剂，其被配置用于调节燃烧和排出物流174的温度。在至少一个实施方式中，在气体膨胀器中膨胀以产生机械动力之前，离开燃烧室168的排出物流174可具有大约2500℉的温度。如将理解的，气体膨胀器152、燃烧室168和入口压缩机118的组合可以表征为分开的标准燃气涡轮系统，其中入口压缩机118成为压缩机末端，并且气体膨胀器152成为燃气涡轮的膨胀器末端。
在一种或多种实施方式中，废气156可具有大约1100℉的温度。在至少一个实施方式中，废气156可被引导至HRSG 126，以回收热作为蒸汽燃气涡轮128中的动力。在其他实施方式中，废气156可被引导至外部HRSG和蒸汽燃气涡轮(未示出)，以产生用于其他应用的动力。在任何情况下，富氮残余流151在通过膨胀器152后可以以本文讨论的任何方式进行处理，诸如经氮排出、经埋存、EOR或压力保持操作等。
现在参考图7，描绘的是低排放动力产生系统700的另一个实施方式，类似于图6的系统600。如此，图7的整个系统700将不进行详细地描述，但可参考图6及其所附说明最好地理解。不利用分开的入口压缩机118和氮气膨胀器152(见图1-6)，如图7所描绘的系统700可包含第二燃气涡轮系统702，其具有第二压缩机176和第二膨胀器178。在一种或多种实施方式中，第二压缩机176可接收和压缩第二供应氧化剂180。类似于在以上图1-6中显示和描述的供应氧化剂120，第二供应氧化剂180可包含任何合适的含氧气体，诸如空气、富氧空气或其组合。第二压缩机176可被配置用于压缩第二供应氧化剂180并且产生第二压缩的氧化剂182。如所描绘的，燃烧室110要求的压缩的氧化剂114可从第二压缩的氧化剂182流供应或提取，并起到与以上一般描述的相同的作用。
在操作中，燃烧室168可被配置用于化学计量地燃烧燃料170和第二压缩的氧化剂182的组合，以便产生升高的温度和压力的排出物流174。在一种或多种实施方式中，来自热交换器158的氮蒸气160或来自CO2分离器148的残余流可被用作稀释剂，其被配置用于调节第二燃烧室168中的燃烧温度。在一个实施方式中，燃料170可来自与供应进入第一燃烧室110的燃料112诸如烃燃料相同的来源。在其他期望或要求零CO2排放的实施方式中，燃料170可主要由氢组成，如以上参考图6一般描述的。
如果使用烃燃料，则将自然产生CO2排放。然而，因为使用大体纯的氮气流作为稀释剂，与常规NGCC动力工厂相比，产生的CO2排放将显著地小。例如，在一个实施方式中，与常规NGCC动力工厂的大约400lbs/MWhr相比，由系统700产生的CO2排放将仅为大约80lbs/MWhr。在一种或多种实施方式中，来自第二膨胀器178的废气156可具有大约1100℉的温度。在至少一个实施方式中，废气156可被引导至第二HRSG 184，以回收热作为分开的蒸汽燃气涡轮186中的动力。然而，在可选实施方式中，废气156可被引导至第一HRSG 126，以回收热作为蒸汽燃气涡轮128中的动力。在这里，再次可理解废气156在通过第二HRSG 184后可被排出或以其他方式用于如上所述的烃回收操作(未示出)。
如可理解的，图7的系统700可允许利用商业可得的燃气涡轮，而不是经历昂贵的升级以获得定制的空气压缩机和定制的膨胀器。系统700也可以以更高的效力产生更多的净动力，因为第二膨胀器178的入口温度可达到大约2500℉的温度。
现在参考图8，描绘的是低排放动力产生系统800的另一个实施方式，类似于图3的系统300。如此，图8的整个系统800将不进行详细地描述，但可参考图1和3最好地理解。然而，应当注意到，参考图1-6公开的实施方式可单独实施或结合图8的系统800实施，而不脱离本公开的范围。在示例性实施方式中，源于CO2分离器148的主要由氮气组成的残余流151可被引导至下游压缩机188。下游压缩机188可被配置用于压缩残余流151并产生压缩的废气190，该压缩的废气190具有例如大约3400psi的压力，或另外适于注入油藏用于压力保持应用的压力。
用下游压缩机188压缩残余流151在应用中可证明是有利的，在该应用中甲烷气体通常被重新注入烃井以保持井压。根据本文公开的实施方式，氮气可替代地被注入烃井，并且残余的甲烷气体可被出售或以其他方式用作相关应用中的燃料，诸如为燃料流112，170提供燃料(见图6和7)。
继续参考图5-7，下表基于以下提供了测试结果和性能评估：不具有膨胀循环的系统(例如，图8的系统800)，燃烧室168中不具有额外的点火的系统(例如，图5的系统500)，和燃烧室168中具有额外的点火的系统(例如，分别地图6和7的系统600，700)。数据反映了甲烷燃料170点火用于燃烧。
表2
如应从表2显而易见的，燃烧室168中具有点火的实施方式可产生显著较高的联合循环功率输出；当与在燃烧室168中不实施点火的实施方式相比时，几乎是两倍的功率输出。另外，与不实施这种点火技术的实施方式相反，总体热动力性能效力对于并入如本文公开的点火的系统显示了大约3.3％lhv(较低的加热值)的大量上升或改善。
尽管本公开可易于多种更改和可选形式，但以上讨论的示例性实施方式已经仅以实施例的方式显示。然而，应当再次理解本公开不意欲限于本文公开的特定实施方式。的确，本公开包含所有落入所附权利要求的真实精神和范围内的可选方案、更改和等价物。

Claims (21)

1.综合系统，包括：
具有第一燃烧室的燃气涡轮系统，所述第一燃烧室被配置用于在压缩的再循环流的存在下基本上化学计量地燃烧第一压缩的氧化剂和第一燃料，以便供应的氧与化学计量的燃烧需要的氧的比为0.9:1至1.1:1，其中所述燃烧室引导第一排出物流至膨胀器，以产生气态废流并且至少部分地驱动主压缩机；
放置在所述第一燃烧室的出口上并且适于分别测量所述气态废流的温度或氧浓度的至少一个热电偶或氧传感器，其中来自所述热电偶或氧传感器的至少一个测量用于(i)调节注入所述第一燃烧室的所述第一燃料和所述第一压缩的氧化剂的比，以维持基本上化学计量的燃烧条件；或(ii)修改作为稀释剂以冷却燃烧产物至要求的膨胀器入口温度需要的所述气态废流的体积；或二者；
废气再循环系统，其包括至少一个增压器，所述增压器被配置用于在引导冷却的再循环气体进入所述主压缩机之前接收和提高所述气态废流的压力，其中所述主压缩机压缩所述气态废流并且从而产生所述压缩的再循环流，所述压缩的再循环流用作稀释剂，其被配置用于调节所述第一排出物流的温度；
CO2分离器，其经净化流流体连接至所述压缩的再循环流；
催化装置，其与所述净化流结合放置并且配置用于在所述净化流进入所述CO2分离器之前降低所述净化流中的氧含量；和
第二燃烧室，其经源于所述CO2分离器的主要由富氮气体组成的残余流流体连接至所述CO2分离器，其中所述第二燃烧室被配置用于基本上化学计量地燃烧所述残余流、源自与所述第一燃料相同来源的第二燃料和源自与所述第一压缩的氧化剂相同来源的第二压缩的氧化剂的组合；和
气体膨胀器，其经第二排出物流与所述第二燃烧室流体连接。
2.权利要求1所述的系统，进一步包括流体连接至所述至少一个增压器的第一冷却单元和第二冷却单元，所述第一冷却单元被配置用于在所述气态废流进入所述至少一个增压器之前接收和冷却所述气态废流，和所述第二冷却单元被配置用于接收来自所述至少一个增压器的所述气态废流并且进一步冷却所述气态废流以产生所述冷却的再循环气体。
3.权利要求1所述的系统，进一步包括加热器构件，其适于加热所述残余流产生加热的氮蒸气流。
4.权利要求3所述的系统，其中所述气体膨胀器被配置用于使所述加热的氮蒸气膨胀并且从而产生机械动力和废气。
5.权利要求4所述的系统，进一步包括由通过所述气体膨胀器产生的所述机械动力驱动的入口压缩机，其中所述入口压缩机被配置用于提供所述第一压缩的氧化剂。
6.权利要求3所述的系统，其中所述加热器构件包括流体连接至所述净化流和所述残余流两者的热交换器，所述热交换器被配置用于在所述催化装置中处理之后降低所述净化流的温度并且同时升高所述残余流的温度。
7.权利要求1所述的系统，其中所述气体膨胀器被配置用于使所述第二排出物流膨胀并且从而产生机械动力和废气。
8.产生动力的方法，包括：
在第一燃烧室中并在压缩的再循环流的存在下基本上化学计量地燃烧第一压缩的氧化剂和第一燃料，以便供应的氧与化学计量的燃烧需要的氧的比为0.9:1至1.1:1，从而产生第一排出物流，其中所述压缩的再循环流用作稀释剂，其被配置用于调节所述第一排出物流的温度；
使用放置在所述第一燃烧室的出口上的至少一个热电偶或氧传感器分别地测量所述第一排出物流的温度和氧浓度的一个或两个，
使用来自所述热电偶或氧传感器的至少一个测量(i)调节注入所述第一燃烧室的所述第一燃料和所述第一压缩的氧化剂的比，以维持基本上化学计量的燃烧条件；或(ii)修改稀释剂的体积；或二者；
在膨胀器中使所述第一排出物流膨胀，以至少部分地驱动第一压缩机并且产生气态废流；
引导所述气态废流进入所述第一压缩机，其中所述第一压缩机压缩所述气态废流并且从而产生所述压缩的再循环流；
经净化流提取一部分所述压缩的再循环流至CO2分离器；
在所述CO2分离器之前的所述净化流内放置的催化装置中，通过燃烧氧和剩余的燃料降低所述净化流中的氧含量；
从所述CO2分离器获得主要由富氮气体组成的残余流；
在第二燃烧室中在所述残余流存在的情况下，基本上化学计量地燃烧第二压缩的氧化剂和第二燃料以产生第二排出物流，其中所述第一压缩的氧化剂和第二压缩的氧化剂和所述第一燃料和第二燃料分别来自相同的来源；
在气体膨胀器中，使所述第二排出物流膨胀；和
使用增压器和冷却单元中的至少一个，其适于增加所述气态废流的质量流速，以产生再循环气体。
9.权利要求8所述的方法，包括利用流体连接至至少一个增压器的第一冷却单元冷却所述气态废流，所述第一冷却单元被配置用于在所述气态废流进入所述至少一个增压器之前接收和冷却所述气态废流。
10.权利要求9所述的方法，进一步包括利用流体连接至所述至少一个增压器的第二冷却单元冷却来自所述至少一个增压器的所述气态废流，以产生所述再循环气体。
11.权利要求8所述的方法，进一步包括利用由所述气体膨胀器产生的所述机械动力驱动入口压缩机，所述入口压缩机被配置用于产生所述第一压缩的氧化剂。
12.权利要求8所述的方法，进一步包括加热器构件，其适于升高所述残余流的温度，以产生加热的氮蒸气流。
13.权利要求12所述的方法，其中所述加热器构件包括流体连接至所述净化流和所述残余流两者的热交换器，并且进一步包括利用所述热交换器在所述催化装置中处理之后降低所述净化流的温度和升高所述残余流的温度，从而产生所述加热的氮蒸气流。
14.权利要求8所述的方法，进一步包括将水注入所述加热的氮蒸气流以增加所述气体膨胀器的质量通过量。
15.权利要求12所述的方法，进一步包括利用从所述CO2分离器排出的所述残余流调节所述第二排出物流的温度。
16.权利要求13所述的方法，进一步包括在所述气体膨胀器中使所述第二排出物流膨胀，以产生机械动力从而驱动入口压缩机，所述入口压缩机被配置用于产生所述第一压缩的氧化剂。
17.综合系统，包括：
第一燃气涡轮系统，包括：
第一压缩机，其被配置用于接收和压缩再循环的废气，并且提供第一压缩的再循环流；
第一燃烧室，其被配置用于接收所述第一压缩的再循环流、第一压缩的氧化剂和第一燃料流，所述第一燃烧室适于基本上化学计量地燃烧所述第一燃料流和第一压缩的氧化剂，以便供应的氧与化学计量的燃烧需要的氧的比为0.9:1至1.1:1，其中所述第一压缩的再循环流用作稀释剂以调节燃烧温度；
放置在所述第一燃烧室的出口上并且适于分别测量气态废流的温度或氧浓度的至少一个热电偶或氧传感器，其中来自所述热电偶或氧传感器的至少一个测量用于(i)调节注入所述第一燃烧室的所述第一燃料流和所述第一压缩的氧化剂的比，以维持基本上化学计量的燃烧条件；或(ii)修改作为稀释剂以冷却燃烧产物至要求的膨胀器入口温度需要的所述气态废流的体积；或二者；
第一膨胀器，其连接至所述第一压缩机并被配置用于接收来自所述第一燃烧室的第一排出物，并且产生所述再循环的废气并且至少部分地驱动所述第一压缩机；和
增压器，其被配置用于在注入所述第一压缩机之前增加所述再循环的废气的压力，以提供所述压缩的再循环流；
净化流，其从所述压缩的再循环流获得并且在CO2分离器中被处理，以提供CO2流和残余流，所述残余流基本上包括氮气；
催化装置，其与所述净化流结合放置并且配置用于在所述净化流进入所述CO2分离器之前降低所述净化流中的氧含量；和
第二燃气涡轮系统，其经所述净化流流体连接至所述第一燃气涡轮系统，所述第二燃气涡轮系统包括：
第二压缩机，其被配置用于接收和压缩供应氧化剂并且产生第二压缩的氧化剂，所述第一压缩的氧化剂至少部分源于所述第二压缩的氧化剂；
第二燃烧室，其被配置用于接收所述第二压缩的氧化剂、所述残余流和源自与所述第一燃料流相同来源的第二燃料流，所述第二燃烧室适于基本上化学计量地燃烧所述第二燃料流和第二压缩的氧化剂，其中所述氮气用作稀释剂以调节燃烧温度；和
第二膨胀器，其连接至所述第二压缩机并且被配置用于接收来自所述第二燃烧室的第二排出物并且产生废气和至少部分地驱动所述第二压缩机。
18.权利要求17所述的系统，其中所述第二燃料为氢燃料。
19.权利要求17所述的系统，其中所述第二燃气涡轮系统进一步包括热回收蒸汽发生器，其被配置用于接收来自所述第二膨胀器的废气并且为蒸汽燃气涡轮提供蒸汽。
20.综合系统，包括：
具有第一燃烧室的燃气涡轮系统，所述第一燃烧室被配置用于在压缩的再循环流的存在下基本上化学计量地燃烧压缩的氧化剂和燃料，以便供应的氧与化学计量的燃烧需要的氧的比为0.9:1至1.1:1，其中所述燃烧室向膨胀器提供排出物流，以便产生气态废流并且至少部分地驱动第一压缩机；
放置在所述第一燃烧室的出口上并且适于分别测量所述气态废流的温度和氧浓度的热电偶和氧传感器的至少一个，其中所述至少一个测量用于(i)调节注入所述第一燃烧室的所述燃料和所述压缩的氧化剂的比，以维持基本上化学计量的燃烧条件；或(ii)修改作为稀释剂以冷却燃烧产物至要求的膨胀器入口温度需要的所述气态废流的体积；或二者；
具有至少一个增压器的废气再循环系统，所述至少一个增压器被配置用于在引导冷却的再循环气体进入所述第一压缩机之前接收和提高所述气态废流的压力，其中所述第一压缩机压缩所述冷却的再循环气体并且从而产生所述压缩的再循环流，所述压缩的再循环流用作稀释剂，其被配置用于调节所述排出物流的温度；
CO2分离器，其经净化流流体连接至所述压缩的再循环流；
催化装置，其与所述净化流结合放置并且配置用于在所述净化流进入所述CO2分离器之前降低所述净化流中的氧含量；和
第二燃烧室，其经源于所述CO2分离器并且主要由富氮气体组成的残余流流体连接至所述CO2分离器，其中所述第二燃烧室被配置用于基本上化学计量地燃烧所述残余流、源自与所述第一燃料相同来源的第二燃料和源自与所述第一压缩的氧化剂相同来源的第二压缩的氧化剂的组合；和
下游压缩机，其经第二排出物流与所述第二燃烧室流体连接。
21.权利要求20所述的系统，其中所述下游压缩机被配置用于压缩所述富氮气体用于压力保持。
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