CN103443403A - 用于在低排放联合涡轮机系统中捕获二氧化碳的系统和方法 - Google Patents

用于在低排放联合涡轮机系统中捕获二氧化碳的系统和方法 Download PDF

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CN103443403A
CN103443403A CN2012800138097A CN201280013809A CN103443403A CN 103443403 A CN103443403 A CN 103443403A CN 2012800138097 A CN2012800138097 A CN 2012800138097A CN 201280013809 A CN201280013809 A CN 201280013809A CN 103443403 A CN103443403 A CN 103443403A
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waste gas
gas streams
gaseous state
compression
cooling
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F·F·米特瑞克
R·A·亨廷顿
O·A·斯特斯
S·K·达安卡
D·M·奥戴
R·H·欧尔菲克
R·D·登顿
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ExxonMobil Upstream Research Co
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Abstract

本发明提供用于在联合低排放涡轮机系统中发电以及捕获并回收废气中二氧化碳的系统、方法和装置。在一种或多种实施方式中，来自多个涡轮机系统的废气经结合、冷却、压缩以及分离，产生含二氧化碳的流出流和含氮的产物流。回收的废气流和产物流的部分可用作稀释剂，调节涡轮机系统中每个燃烧器的燃烧。

Description

用于在低排放联合涡轮机系统中捕获二氧化碳的系统和方法
相关申请的交叉引用
本申请要求以下申请的优先权：2011年9月30日提出的美国临时申请61/542,039，名称为SYSTEMS AND METHODS FOR CARBONDIOXIDE CAPTURE IN LOW EMISSION COMBINED TURBINESYSTEMS（用于在低排放联合涡轮机系统中捕获二氧化碳的系统和方法）；2011年3月22日提出的美国临时申请61/466,384，名称为LOWEMISSION TURBINE SYSTEMS HAVING A MAIN AIRCOMPRESSOR OXIDANT CONTROL APPARATUS AND METHODSRELATED THERETO（具有主压缩空气压缩机氧化剂控制装置的低排放涡轮机系统以及相关方法）；2011年9月30日提出的美国临时申请61/542,030，名称为LOW EMISSION TURBINE SYSTEMSINCORPORATING INLET COMPRESSOR OXIDANT CONTROLAPPARATUS AND METHODS RELATED THERETO（结合了入口压缩机氧化剂控制装置的低排放涡轮机系统以及相关方法）；2011年3月22日提出的美国临时申请61/466,385，名称为METHODS FORCONTROLLING STOICHIOMETRIC COMBUSTION ON A FIXEDGEOMETRY GAS TURBINE SYSTEM AND APPARATUS ANDSYSTEMS RELATED THERETO（在固定几何形状的燃气轮机系统上控制化学计量燃烧的方法以及相关装置和系统）；2011年9月30日提出的美国临时申请61/542,031，名称为SYSTEMS AND METHODS FORCONTROLLING STOICHIOMETRIC COMBUSTION IN LOWEMISSION TURBINE SYSTEMS（在低排放涡轮机系统中控制化学计量燃烧的系统和方法）；2011年3月22日提出的美国临时申请61/466,381，名称为METHODS OF VARYING LOW EMISSIONTURBINE GAS RECYCLE CIRCUITS AND SYSTEMS ANDAPPARATUS RELATED THERETO（改变低排放涡轮机气体循环回路的方法以及相关的系统和装置）；2011年9月30日提出的美国临时申请61/542,035，名称为METHODS OF VARYING LOW EMISSIONTURBINE GAS RECYCLE CIRCUITS AND SYSTEMS ANDAPPARATUS RELATED THERETO（改变低排放涡轮机气体循环回路的方法以及相关的系统和装置）；所有这些申请通过引用以其整体并入本文。
本申请与下述申请相关：2011年9月30日提出的美国临时申请61/542,036，名称为SYSTEMS AND METHODS FOR CARBONDIOXIDE CAPTURE IN LOW EMISSION TURBINE SYSTEMS（在低排放涡轮机系统中捕获二氧化碳的系统和方法）；2011年9月30日提出的美国临时申请61/542,037，名称为SYSTEMS AND METHODS FORCARBON DIOXIDE CAPTURE IN LOW EMISSION TURBINESYSTEMS（在低排放涡轮机系统中捕获二氧化碳的系统和方法）；2011年9月30日提出的美国临时申请61/542,041，名称为LOW EMISSIONPOWER GENERATION SYSTEMS AND METHODSINCORPORATING CARBON DIOXIDE SEPARATION（结合了二氧化碳分离的低排放发电系统和方法）；所有这些申请通过引用以其整体并入本文。
技术领域
本公开的实施方式涉及低排放发电。更具体地，本公开的实施方式涉及捕获二氧化碳以便提高低排放联合涡轮机系统的效率并降低成本的方法和装置。
背景技术
本节旨在介绍本领域的各个方面，所述各个方面可能与本公开的示范性实施方式相关。相信这种讨论有助于提供一个框架，以促进更好地理解本发明的具体方面。因此，应当理解，本节应该从这个角度理解而不一定是作为现有技术的承认。
许多产油国正在经历强劲的国内电力需求增长，并且对提高采收率法采油（EOR）感兴趣以改进从其储油层采油。两种通常的EOR技术包括氮（N2）注入用于维持储层压力和二氧化碳（CO2）注入用于EOR的混相驱动。全球也在关注温室气体（GHG）排放。这种关注结合在许多国家执行总量管制与排放交易政策使得减少CO2排放成为这些国家以及其中运转烃生产系统的公司的当务之急。
降低CO2排放的一些方法包括使用溶剂如胺进行燃料脱碳或者燃烧后捕获。然而，这两种方案都昂贵而且降低了发电效率，导致较低的电力生产，燃料需求增大，以及电成本增大以满足国内电力需求。具体地，氧气、SOX和NOX成分的存在使得使用胺溶剂吸收很成问题。另一种方法是在联合循环中的含氧燃料燃气轮机（比如，其中捕获来自燃气轮机布雷顿循环的废气热量以在兰金循环中用于产生蒸汽和产生额外电力）。但是，商业上可得的燃气轮机没有可以在这样的循环内运转的并且用于产生高纯度氧气所需的电力显著降低了该方法的总体效率。
另外，随着日益关注全球气候变化和二氧化碳排放的影响，重点已经放在使发电厂的二氧化碳排放量最小化。燃气轮机发电厂是有效的并且与核能或煤发电技术相比具有更低成本。然而，因为排气管中的二氧化碳浓度低，大体积的气体需要处理，以及废气流的压力低，捕获来自燃气轮机发电厂的废气中的二氧化碳是很昂贵的。这些因素以及其他因素导致二氧化碳捕获的高成本。
因此，仍然显著需要结合了降低成本的CO2捕获和回收的低排放、高效率的发电方法。
发明内容
在本文描述的低排放发电系统中，来自低排放燃气轮机的、排入到典型天然气联合循环（NGCC）厂中的废气改为被分离和回收。本发明的装置、系统和方法结合并再循环两个燃气轮机的废气流，以有效地发电同时浓缩且回收二氧化碳。
在本发明的系统和方法中，两个燃气轮机系统——每一个包括压缩机、燃烧室以及膨胀机——流体连接以串联操作，并且将来自每个系统的废气结合。结合的废气然后被冷却、压缩和再循环。再循环废气流的一部分被供应到一个燃烧室，充当稀释剂，以控制或者另外方式调节燃烧温度和进入后面膨胀机的废气(flue gas)。再循环废气流的另一部分被分离以捕获一个流中的CO2并产生分离的产物流，其包括氮气、氧气、氩气或者它们的组合。来自CO2分离器的产物流的一部分之后被类似地供应到另一燃烧室，充当稀释剂，同时产物流的其余部分可用于产生额外的电力或者用于其他目的，不管在本系统之内还是之外。通过这种方式结合废气，来自整个系统中每个燃气轮机的燃烧产物被浓缩且CO2可以更容易捕获并去除，因此导致更有效的发电。
附图说明
在阅读以下详细描述和实施方式的非限制性示例的附图之后，本公开的上述和其他优势可变得明显，其中：
图1描绘包括两个流体连接的燃气轮机系统而且结合了CO2分离的联合低排放发电系统。
图2描绘图1中联合低排放发电系统的一种变型，其中将来自每个涡轮机的废气流结合，然后从所述流回收热。
图3描绘图1中联合低排放发电系统的一种变型，其中从来自每个涡轮机的废气流独立地回收热并且在热回收之后将所述流结合。
具体实施方式
在以下的具体实施方式部分中，将本公开的具体实施方式结合优选实施方式进行描述。然而，在以下描述特定于本公开的具体实施方式或具体用途的方面，这旨在仅用于示范性的目的并且仅提供示范性实施方式的描述。因此，本公开不限于下述的具体实施方式，而是包括落入所附权利要求书的真正精神和范围之内的所有替代方案、改型和等同物。
本文所用的各种术语如下定义。对于下文中没有定义的权利要求中使用的术语，应给予相关领域人员给予该术语的最宽泛定义，如在至少一个印刷出版物或授权专利中反映的。
如本文中使用的，术语“天然气”指从原油井（伴生气）和/或从地下气层（非伴生气）中获取的多组分气体。天然气的组成和压力可以显著不同。一般天然气流包含甲烷（CH4）作为主要成分，即天然气流中多于50mol%的是甲烷。天然气流也可包含乙烷（C2H6）、更高分子量的烃（比如C3-C20烃）、一种或多种酸性气体（比如硫化氢）、或者它们的任何组合。天然气也可包含少量的污染物，例如水、氮、硫化铁、蜡、原油、或者它们的任何组合。
如本文中使用的，术语“化学计量燃烧”指这样的燃烧反应，其具有包含燃料和氧化剂的反应物体积和通过燃烧反应物形成的产物体积，其中反应物的全部体积用于形成产物。如本文中使用的，术语“基本化学计量的”燃烧指这样的燃烧反应，其当量比率在约0.9:1到约1.1:1的范围内，或者更优选地在约0.95:1到约1.05:1的范围内。本文使用术语“化学计量的”意思是既包括化学计量条件也包括基本化学计量条件，除非另外指出。
如本文中使用的，术语“流”指一定体积的流体，尽管术语流的使用通常指移动的一定体积的流体（比如，具有速度或者质量流速）。然而，术语“流”不要求速度、质量流速或者包围流的具体类型的管道。
本公开的系统和方法的实施方式可用于生产低排放电力和CO2，用于提高采收率法采油（EOR）或者封存应用。根据本文公开的实施方式，将压缩的氧化剂（一般是空气）和燃料的混合物在两个独立但流体连接的燃气轮机中燃烧，并且使来自每一个的废气膨胀以发电。然后废气被结合、冷却、压缩并分离以捕获CO2并产生包括氮气的产物流。在EOR应用中，将回收的CO2注入到生产油井内或者其附近，通常在超临界条件下进行。CO2既充当加压剂，也在溶解到地下原油中时显著减小油的粘度，使得油能够更迅速地流经土壤至移除井(remove well)中。包括氮气（并且经常也包括氧气和氩气）的产物流可用于产生额外的电力，也可以用于多种目的，包括压力维持应用。在压力维持应用中，惰性气体如氮气被压缩并被注入到烃储层中以维持储层中的原始压力，因此允许提高烃的回收。本文公开的系统的结果是发电以及以更加经济有效的方式浓缩和捕获CO2。
在本发明的一种或多种实施方式中，提供发电系统，其包括第一压缩机，配置来接收并压缩一种或多种氧化剂，产生压缩的氧化剂；第一燃烧室，配置来接收并燃烧第一部分的压缩的氧化剂、至少一种第一燃料以及第一稀释剂，产生第一废气流；以及第一膨胀机，配置来接收第一废气流并产生第一气态废气流。所述系统进一步包括第二压缩机，配置来接收并压缩冷却的循环流，产生压缩的循环流；第二燃烧室，配置来接收并燃烧第二部分的压缩的氧化剂、至少一种第二燃料以及第二稀释剂，产生第二废气流；以及第二膨胀机，配置来接收第二废气流并产生第二气态废气流。所述系统还包括一个或多个热回收蒸汽发生器，配置来接收并冷却第一和第二气态废气流，产生蒸汽和结合的废气流；循环冷却单元，配置来接收并冷却结合的废气流并产生冷却的循环流；以及分离器，配置来接收一部分压缩的循环流并将其分离成分离器流出流和分离器产物流。
一种或多种氧化剂可包括任何含氧流体，如环境空气、富氧空气、基本纯的氧气、或者它们的组合。在本发明的一种或多种实施方式中，作为整体供应到联合系统中的氧化剂的全部或者基本上全部在第一压缩机中被压缩并由第一压缩机供应。从第一压缩机排出的压缩的氧化剂然后分成两个流，以便将第一部分的压缩的氧化剂引入第一燃烧室和将第二部分的压缩的氧化剂引入第二燃烧室。这种分离可以是等分的或不等分的，也可在操作期间改变以适应过程中的变化。
第一和第二燃料可以相同或者不同，并且每种燃料可包括天然气、伴生气、柴油、燃料油、气化煤、焦炭、石脑油、丁烷、丙烷、合成气、煤油、航空燃料、生物燃料、氧化的烃原料、任何其它合适的含烃气体或液体、氢气或者它们的组合。另外，燃料可包括惰性成分，包含但不限制于N2或者CO2。在一些实施方式中，第一和/或第二燃料可至少部分由通过本文描述的方法经注入捕获的CO2正受益于提高采收率法采油的烃储层供应。在某些实施方式中，第一和第二燃料包括天然气。
第一和第二燃烧室的每一个中的燃烧条件可以是贫的、化学计量的或者基本上化学计量的、或者富的。在一种或多种实施方式中，第一和第二燃烧室中的燃烧条件是化学计量的或者基本上化学计量的。将第一和第二稀释剂供应到第一和第二燃烧室中以控制或者另外方式调节燃烧温度和废气(flue gas)以满足后面膨胀机的材料要求。然而，也可调整第一和第二稀释剂的流量，以帮助维持各燃烧室的化学计量条件，调节氧化剂和燃料流中的组成、体积流量或者其他变量的变化。在一种或多种实施方式中，提供到第一燃烧室的第一稀释剂包括至少部分分离器产物流。在相同或者其他实施方式中，提供到第二燃烧室的第二稀释剂包括至少部分压缩的循环流。
在一些实施方式中，也可采用高压蒸汽作为第一和第二燃烧室中一个或两个的冷却剂。在这些实施方式中，蒸汽的加入会降低系统中的电力和尺寸要求，但是需要添加一个或多个水循环回路。另外，在进一步的实施方式中，输送到一个或两个燃烧室的压缩的氧化剂进料可包括氩气。比如，氧化剂可包括约0.1到约5.0vol%的氩气，或者约0.1到约4.5vol%的氩气，或者约2.0到约4.0vol%的氩气，或者约2.5到约3.5vol%的氩气，或者约3.0vol%的氩气。
第一和第二压缩机可以各自是单个压缩机或者可以是并联或串联操作的两个或更多压缩机。每个压缩机可包括单个阶段或者多个阶段。在多个阶段的压缩机中，可以任选地采用级间冷却以允许更高的总体压缩比率和更高的总体电力输出。当使用多于一个的压缩机压缩过程流时，放在一起的压缩机在本文若合适被认为是“第一压缩机”或“第二压缩机”。每个压缩机可以具有适合于本文所述方法的任何类型。这些压缩机包括但不限制于轴流式、离心式、往复式、或者双螺杆式压缩机以及它们的组合。在一种或多种实施方式中，第一和第二压缩机是轴流式压缩机。
在第一和第二燃烧室的每一个中的氧化剂和燃料的燃烧分别产生第一废气流和第二废气流。第一废气流和第二废气流包括燃烧的产物，且它们各自的组成将取决于每个燃烧室中使用的燃料和氧化剂的组成发生变化。在一种或多种实施方式中，第一和第二废气流可各自包括汽化的水、CO2、一氧化碳（CO）、氧气（O2）、氮气（N2）、氩气（Ar）、氮氧化物（NOx）、硫氧化物（SOx）、硫化氢（H2S）、或者它们的组合。
可使第一废气流在第一膨胀机中膨胀，形成第一气态废气流，可使第二废气流在第二膨胀机中膨胀，形成第二气态废气流。第一和第二膨胀机可以各自是单个膨胀机或者可以是并联或串联操作的两个或更多膨胀机。每个膨胀机可包括单个阶段或者多个阶段。当使用多于一个膨胀机使废气流膨胀时，放在一起的膨胀机在本文若合适被认为是“第一膨胀机”或“第二膨胀机”。每个膨胀机可以是适用于本文描述方法的任意类型的膨胀机，包括但不限制于轴流式或离心式膨胀机或它们的组合。第一和第二废气流的膨胀产生电力，其可用于驱动一个或多个压缩机或发电机。在本发明的一种或多种实施方式中，第一膨胀机通过共用轴或者其他机械、电气或者其他动力连接，连接至第一压缩机，以便第一压缩机至少部分由第一膨胀机驱动。在相同或者其他实施方式中，第二膨胀机通过共用轴或者其他机械、电气或者其他动力连接，连接至第二压缩机，以便第二压缩机至少部分由第二膨胀机驱动。在其他实施方式中，第一或第二压缩机或两者可机械连接至电动机，具有或者没有速度增加或者减小设备如齿轮箱。当第一压缩机、第一燃烧室和第一膨胀机放在一起时可以表现为布雷顿循环。类似地，当第二压缩机、第二燃烧室和第二膨胀机放在一起时也可表现为布雷顿循环。
膨胀之后，第一和第二气态废气流在一些实施方式中可以在热回收蒸汽发生器（HRSG）中冷却。尽管本文涉及单个HRSG，但实际上可使用两个或更多HRSG。可选地，可代替HRSG使用设计来冷却或回收来自第一和第二气态废气流的热的任何设备，比如一个或多个热交换器、再生器、冷却单元等。HRSG可配置来接收第一和第二废气流并利用流中的余热产生蒸汽。由HRSG产生的蒸汽可用于多种目的，如驱动兰金循环中的蒸汽涡轮发电机或用于水脱盐。
在本发明的一种或多种实施方式中，第一和第二气态废气流分别供应到HRSG并在HRSG中结合以形成结合的废气流。在其他实施方式中，第一和第二气态废气流可在HRSG的上游或者下游结合。当流在下游结合时，第一和第二气态废气流中的每一个可在单独的HRSG中冷却，然后结合形成结合的废气流。
在本发明的一种或多种实施方式中，可将结合的废气流输送至一个或者更多冷却单元，该冷却单元配置来降低结合的废气流的温度并产生冷却的循环流。冷却单元可以是适合于降低废气温度的任意类型的装置，比如直接接触冷却器（DCC）、调温冷却器(trim cooler)、机械制冷单元、或者它们的组合。在一些实施方式中，冷却单元是DCC。冷却单元也可以配置来通过水排泄流(water dropout stream)将一部分冷凝水从冷却循环流中移除。在一些实施方式中，可任选地将水排泄流送至HRSG，以提供产生额外蒸汽的水源。
在一些实施方式中，可将从冷却单元排出的冷却循环流输送到第二压缩机并压缩，产生压缩的循环流。将废气冷却和压缩有助于解决与必须处理的气体的大体积以及通常导致高CO2捕获成本的废气流的低压相关的问题，从而使本系统中CO2的捕获和回收更有效率且更加成本有效。
从第二压缩机排出后，压缩的循环流被分离，且可将第一部分的压缩的循环流提供到第二燃烧室用作稀释剂，如前面描述。在这些情况下，未引入第二燃烧室的第二部分压缩的循环流可送到一个或者更多分离器，其中从压缩的循环流中分离出CO2和其他温室气体。尽管未在本文详细描述，但本领域技术人员将认识到，第二压缩机和分离器之间可需要中间加热、冷却或者其他工艺操作，以便循环流在对于采用的具体分离方法优化的条件下进入分离器。在一种或多种实施方式中，比如，冷却单元可用于在压缩的循环流进入分离器之前将其冷却。
在一个或多个分离器中采用的CO2分离方法可以是设计来分离压缩的循环气体并形成包括CO2的分离器流出流和包括氮气的分离器产物流的任何合适方法。在一些实施方式中，产物流也可包括氧气、氩气或两者。分离压缩循环流的成分允许废气中的不同成分以不同的方式处理。理想地，分离方法将废气中所有的温室气体如CO2、CO、NOx、SOx等分离在流出流中，留下其余废气成分如氮气、氧气和氩气在产物流中。然而，实际上，分离方法可以不收回产物流中所有的温室气体，并且一些非温室气体可保留在流出流中。
任何合适的设计来实现预期结果的分离方法都可以被使用。在一种或多种实施方式中，分离方法是氧气不敏感方法。合适的分离方法的实例包括但不限制于热碳酸钾（“热罐(hot pot)”）分离方法、胺分离、分子筛分离、膜分离、吸附动力学分离、受控冷冻区分离、以及它们的组合。在一些实施方式中，分离器使用热罐分离方法。在本发明的一种或多种实施方式中，分离方法可在升高的压力（即，高于环境压力）下操作并且配置来保持产物流被加压。以这种方式维持过程上的压力允许更小的分离设备，提供提高的分离效率，并且允许提高从产物流中提取能量。在一些实施方式中，CO2分离方法被选择并配置来使产物流的出口压力或者出口温度或者两者最大化。
分离器流出流可用于多种应用。比如，流出流可被注入到烃储层中用于提高采收率法采油（EOR）或者可以被引入储层中用于碳封存或者存储。分离器流出流也可以出售、排出或燃烧。
在一种或多种实施方式中，分离器产物流包括氮气，也任选地包括氧气或氩气（二者）。分离器产物流可以被分离，第一部分产物流可被提供到第一燃烧室，用作稀释剂，如前面描述。在这些情况下，未引入第一燃烧室的第二部分分离器产物流可被引入第三膨胀机。在一种或多种实施方式中，第三膨胀机可配置来接收分离器产物流并在大致环境压力下输出同一气体。本领域技术人员将理解，第三膨胀机产生电力且产生的电力可用于驱动任何配置的一个或多个压缩机或发电机，无论在所描述的系统之内还是之外。
在一种或多种实施方式中，产物流在膨胀之后经过一个或多个另外的热回收蒸汽发生器（HRSG）。一个或多个HRSG可配置来使用流中的余热产生蒸汽。由一个或多个HRSG产生的蒸汽可用于多种目的，比如驱动兰金循环中的蒸汽涡轮发电机或者用于水脱盐。进一步地，如果从一个或多个HRSG排出的产物流中仍有任何余热，系统可进一步包括一个或多个热交换器，其配置来将该热转移至非蒸汽工作流体。在这些实施方式中，非蒸汽工作流体可任选地用于驱动兰金循环中的膨胀机。
分离器产物流可全部或者部分用于多种应用。比如，可将产物流注入到烃储层中用于维持压力。产物流也可销售或者排出。在一种或多种实施方式中，当压力维持不是可行的选择时（或者压力维持只需要部分产物流时），产物流可通过膨胀或者其他方法冷却，并用于提供本文描述的系统中的制冷。比如，冷却的产物流可用于提供制冷以降低本系统内一个或多个压缩机的抽吸温度，或者用于冷却本系统内一个或多个冷却单元使用的水。
在其他实施方式中当产物流的全部或者部分不用于压力维持时，可改为加热产物流以便可产生额外的电力用于系统中其他地方或者用于出售。加热产物流的一些方法包括在热交换器中使产物流与其他过程流交叉交换，或者使用辅助燃烧器向产物流供应额外的热。应当理解，额外燃烧器的使用将需要额外的燃料。如果燃烧器中使用含碳燃料，将产生额外的无法从产物流中回收的CO2。因此，在一些实施方式中，燃烧器中使用的燃料是无碳燃料源，如氢气。辅助燃烧器需要的氧化剂可通过单独的氧化剂流供应，或者产物流中可存在足够的氧化剂，从而不需要额外供应氧化剂。加热分离器产物流的其他可能的方法包括在HRSG中使用加热线圈加热产物流，使用催化以燃烧产物流中存在的任何CO，或者作为使用产物流进行冷却的结果加热所述流（即，因为产物流向其他流或者装置提供冷却，流本身被加热）。
现在参看图，图1示出联合发电系统100，其配置来在燃烧之后提供CO2的分离和捕获。在至少一个实施方式中，发电系统100可具有第一压缩机118，其通过共用轴108或者其他机械、电气或者其他动力连接，连接至第一膨胀机106，从而允许第一膨胀机106产生的机械能的一部分驱动第一压缩机118。第一膨胀机106也可以发电用于其他用途，比如向另一个压缩机、发电机等供电。第一压缩机118和第一膨胀机106可以分别形成标准燃气轮机的压缩机端和膨胀机端。然而，在其他实施方式中，第一压缩机118和第一膨胀机106在系统中可以是独立的组件。
系统100也可包括第一燃烧室110，其配置来燃烧与第一部分压缩的氧化剂114混合的第一燃料流112。在一个或多个实施方式中，第一燃料流112可包括任何合适的烃气体或液体，比如天然气、甲烷、石脑油、丁烷、丙烷、合成气、柴油、煤油、航空燃料、煤来源燃料、生物燃料、氧化的烃原料、或者它们的组合。第一燃料流112也可以包含氢气。供应至第一燃烧室110的第一部分压缩的氧化剂114可以来自流体连接至第一燃烧室110并且适于压缩氧化剂进料120的第一压缩机118。虽然本文中的讨论假定氧化剂进料120是环境空气，但氧化剂可包括任何合适的含氧气体，比如空气、富氧空气、基本纯的氧气、或者它们的组合。在一个或多个实施方式中，第一压缩机118、第一燃烧室110、和第一膨胀机106放在一起可以表现为布雷顿循环。
产生第一废气流116作为第一燃料流112和第一部分压缩的氧化剂114的燃烧产物并且被引导至第一膨胀机106的入口。在至少一个实施方式中，第一燃料流112可以主要是天然气，因此产生包括体积份的蒸发的水、CO2、CO、氧气、氮气、氩气、氮氧化物（NOx）和硫氧化物（SOx）的第一废气流116。在一些实施方式中，由于燃烧平衡限制，小部分未燃烧的第一燃料112或者其他化合物也可存在于第一废气116中。随着第一废气流116通过第一膨胀机106膨胀，它产生机械能以驱动第一压缩机118或者其他设备，也产生第一气态废气流122。
发电系统100也可具有第二压缩机180，其通过共用轴188或其他机械、电气或其他动力连接，连接至第二膨胀机170，从而允许由第二膨胀机170产生的一部分机械能驱动第二压缩机180。第二膨胀机170也可发电用于其他用途，例如向另一压缩机、发电机等供电。第二压缩机180和第二膨胀机170可分别形成标准燃气轮机的压缩机端和膨胀机端。然而在其他实施方式中，第二压缩机180和第二膨胀机170在系统中可以是独立的组件。
系统100也可包括第二燃烧室150，其配置来燃烧与第二部分压缩的氧化剂114混合的第二燃料流152。在一种或多种实施方式中，第二燃料流152可包含任何合适的烃气体或液体，比如天然气、甲烷、石脑油、丁烷、丙烷、合成气、柴油、煤油、航空燃料、煤衍生燃料、生物燃料、氧化的烃原料、或者它们的组合。第二燃料流152也可包括氢气。供应到第二燃烧室150的第二部分压缩的氧化剂114可来自流体连接至第二燃烧室150的第一压缩机118。在一种或多种实施方式中，第二压缩机180、第二燃烧室150和第二膨胀机170放在一起可以表现为布雷顿循环。
第二废气流156作为第二燃料流152和第二部分压缩的氧化剂114的燃烧产物产生，并被引至第二膨胀机170的入口。在至少一个实施方式中，第二燃料流152可主要包括天然气，因此产生包含体积份的蒸发的水、CO2、CO、氧气、氮气、氩气、氮氧化物（NOx）和硫氧化物（SOx）的第二废气流156。在一些实施方式中，由于燃烧平衡限制，第二废气156中也存在小部分未燃烧的第二燃料152或者其他化合物。随着第二废气流156通过第二膨胀机170膨胀，其产生机械能以驱动第二压缩机180或者其他设备，也产生第二气态废气流172。
从第一膨胀机106和第二膨胀机170，分别将第一和第二气态废气流122和172引入热回收蒸汽发生器（HRSG）126，该HRSG配置来使用气态废气流122和172中的余热产生蒸汽130和结合的废气流132。由HRSG126产生的蒸汽130可具有多种用途，比如用于通过驱动兰金循环中的蒸汽涡轮发电机产生额外的电力或者用于水脱盐。
结合的废气132可输送至至少一个冷却单元134，其配置来降低结合的废气132的温度并产生冷却的循环流140。在一种或多种实施方式中，冷却单元134在本文中被认为是直接接触冷却器（DCC），但可以是任意合适的冷却设备，比如直接接触冷却器、调温冷却器、机械制冷单元、或者它们的组合。冷却单元134也可配置来通过水排泄流136移除部分冷凝水。
在一种或多种实施方式中，冷却的循环流140可被引入流体连接至冷却单元134的第二压缩机180。第二压缩机180可配置来增加冷却的循环流140的压力，因此产生压缩的循环流182。从第二压缩机180排出后，压缩的循环流182可被分离，以便将一部分压缩的循环流182引入第二燃烧室150，在此其可用作稀释剂调节第二燃烧室150内的燃烧条件。
在一种或多种实施方式中，未引入第二燃烧室的剩余部分压缩的循环流182被引入分离器162。分离器162可采用设计来将压缩循环流182分离成包括CO2的分离器流出流166和一般包括氮气并在一些情况下包括氧气和/或氩气的分离器产物流164的多种分离方法中的任一种。比如，分离器162可设计来使用化学分离方法分离压缩的循环流182，如热碳酸钾（“热罐”）分离、胺分离、或者使用分子筛的分离。其他分离方法包括使用膜的物理分离，或者例如吸附动力学分离或控制冷冻区分离的方法。在一些实施方式中，可以使用上述分离方法的组合。在一种或多种实施方式中，CO2分离方法可配置来将产物流164的温度或压力最大化。分离器流出流166可用于多种下游应用，如注入到烃储层中用于提高采收率法采油（EOR）、碳封存、存储、或出售。流出流166也可排出或燃烧。
在一种或多种实施方式中，从分离器162排出的产物流164的一部分可被转移并在循环产物流184中引入第一燃烧室110。以这种方式，循环产物流184可作为稀释剂调节第一燃烧室110内的燃烧条件。产物流164的剩余部分之后可用于产生额外电力。比如，产物流164可被引入第三膨胀机190。由第三膨胀机190产生的电力可用于多种目的，如至少部分驱动一个或多个额外压缩机（未示出）或者驱动发电机。在一些实施方式中，当产物流被注入储层中用于维持压力时，第三膨胀机190可用于驱动管道或注射压缩机。
在一种或多种实施方式中，可将从第三膨胀机190排出的膨胀产物流192引入热回收蒸汽发生器（未示出）中用于额外发电。与流出流166一样，产物流192也可用于多种其他应用，包括维持压力、存储或排出。
现在参考图2，其描绘图1中发电系统100的可选配置，具体化为并描绘为系统200。因此，图2可通过参考图1最好地理解。在图2的系统200中，第一气态废气流122和第二气态废气流172在HRSG126的上游结合，形成结合的废气流132。结合的废气流132之后被引入HRSG126以冷却结合的废气流132并产生蒸汽130，系统的剩余部分如对图1在前面描述的操作。
现在参考图3，其描绘图1中发电系统100的可选配置，具体化为并描绘为系统300。在图3的系统300中，每个气态废气流在结合前分别冷却。具体地，第一气态废气流122在HRSG126中冷却，同时第二气态废气流172在额外的HRSG326中冷却。第一和第二气态废气流122和172分别从HRSG126和326排出，然后在HRSG的下游结合，形成结合的废气流132。系统的剩余部分如对图1在前面描述的操作。
尽管本公开可进行各种修改和可选形式，但上面讨论的示范性实施方式仅通过示例示出。本文中描述的任何实施方式的任何特征或配置均可结合任何其他任何实施方式或者多个其他实施方式（可行的情况下），并且所有的这些结合都意欲在本发明的范围内。另外，应当理解，本公开不意欲限于本文公开的具体实施方式。事实上，本公开包括落入所附权利要求的真正精神和范围之内的所有可选物、修改物和等同物。

Claims (31)

1.发电系统，其包括：
第一压缩机，其配置来接收并压缩一种或多种氧化剂，产生压缩的氧化剂；
第一燃烧室，其配置来接收并燃烧第一部分所述压缩的氧化剂、至少一种第一燃料以及第一稀释剂，产生第一废气流；
第一膨胀机，其配置来接收来自所述第一燃烧室的所述第一废气流并产生第一气态废气流；
第二压缩机，其配置来接收并压缩冷却的循环流，产生压缩的循环流；
第二燃烧室，其配置来接收并燃烧第二部分所述压缩的氧化剂、至少一种第二燃料以及第二稀释剂，产生第二废气流；
第二膨胀机，其配置来接收来自所述第二燃烧室的所述第二废气流并产生第二气态废气流；
热回收蒸汽发生器，其配置来接收并冷却所述第一气态废气流和所述第二气态废气流，产生结合的废气流和蒸汽；
冷却单元，其配置来接收并冷却所述结合的废气流且产生所述冷却的循环流；以及
分离器，其配置来接收一部分所述压缩的循环流并将其分离成分离器流出流和分离器产物流。
2.根据权利要求1所述的系统，其中所述第一稀释剂包括至少部分所述分离器产物流。
3.根据权利要求1所述的系统，其中所述第二稀释剂包括至少部分所述压缩的循环流。
4.根据权利要求1所述的系统，其中所述冷却单元是直接接触冷却器。
5.根据权利要求1所述的系统，其中所述分离器产物流包括氮气、氧气、氩气或者它们的组合。
6.根据权利要求1所述的系统，其中所述分离器流出流包括二氧化碳。
7.根据权利要求1所述的系统，其中所述分离器使用选自以下的分离方法：热碳酸钾分离、胺分离、分子筛分离、膜分离、吸附动力学分离、控制冷冻区分离或者它们的组合。
8.根据权利要求7所述的系统，其中所述分离器使用热碳酸钾分离方法。
9.根据权利要求1所述的系统，其中所述分离器流出流用于在烃储层中的提高采收率法采油。
10.根据权利要求1所述的系统，其中所述分离器产物流用于在烃储层中维持压力。
11.根据权利要求1所述的系统，进一步包括第三膨胀机，其配置来接收并且膨胀至少部分所述分离器产物流。
12.根据权利要求11所述的系统，进一步包括产物加热单元，其配置来接收并加热引入所述第三膨胀机的所述部分的所述分离器产物流。
13.根据权利要求11所述的系统，进一步包括产物冷却单元，其配置来接收并冷却引入所述第三膨胀机的所述部分的所述分离器产物流。
14.根据权利要求1所述的系统，进一步包括分离器冷却单元，其配置来接收并冷却引入所述分离器的所述部分的所述压缩的循环流。
15.发电方法，其包括：
在第一压缩机中压缩一种或多种氧化剂，产生压缩的氧化剂；
向第一燃烧室供应第一部分所述压缩的氧化剂、至少一种第一燃料以及第一稀释剂；
在所述第一燃烧室中燃烧所述第一部分所述压缩的氧化剂和所述至少一种第一燃料，产生第一废气流；
在第一膨胀机中使所述第一废气流膨胀，产生第一气态废气流；
在第二压缩机中压缩冷却的循环流，产生压缩的循环流；
向第二燃烧室供应第二部分所述压缩的氧化剂、至少一种第二燃料以及第二稀释剂；
在所述第二燃烧室中燃烧所述第二部分所述压缩的氧化剂和所述至少一种第二燃料，产生第二废气流；
在第二膨胀机中使所述第二废气流膨胀，产生第二气态废气流；
从所述第一气态废气流和所述第二气态废气流回收热；
结合所述第一气态废气流和所述第二气态废气流，形成结合的废气流；
冷却所述结合的废气流，产生所述冷却的循环流；以及
分离至少部分所述压缩的循环流，产生流出流和产物流。
16.根据权利要求15所述的方法，其中在一个或多个热回收蒸汽发生器中从所述第一气态废气流、所述第二气态废气流或者从二者回收热。
17.根据权利要求15所述的方法，其中所述第一气态废气流和所述第二气态废气流在从所述第一气态废气流和所述第二气态废气流回收热之前结合。
18.根据权利要求15所述的方法，其中所述第一气态废气流和所述第二气态废气流在从所述第一气态废气流和所述第二气态废气流回收热之后结合。
19.根据权利要求15所述的方法，其中所述第一稀释剂包括至少部分所述产物流。
20.根据权利要求15所述的方法，其中所述第二稀释剂包括至少部分所述压缩的循环流。
21.根据权利要求15所述的方法，其中所述结合的废气流在直接接触冷却器中冷却。
22.根据权利要求15所述的方法，其中所述产物流包括氮气、氧气、氩气或者它们的组合。
23.根据权利要求15所述的方法，其中所述流出流包括二氧化碳。
24.根据权利要求15所述的方法，其中所述至少部分所述压缩的循环流使用选自以下的方法分离：热碳酸钾分离、胺分离、分子筛分离、膜分离、吸附动力学分离、控制冷冻区分离或者它们的组合。
25.根据权利要求24所述的方法，其中所述至少部分所述压缩的循环流使用热碳酸钾分离方法分离。
26.根据权利要求15所述的方法，进一步包括压缩至少部分所述流出流并将所述流出流注入烃储层中用于提高采收率法采油。
27.根据权利要求15所述的方法，进一步包括将至少部分所述产物流注入烃储层中用于维持压力。
28.根据权利要求15所述的方法，进一步包括使至少部分所述产物流膨胀以发电。
29.根据权利要求28所述的方法，进一步包括在膨胀之前加热所述至少部分所述产物流。
30.根据权利要求28所述的方法，进一步包括在膨胀之前冷却所述至少部分所述产物流。
31.根据权利要求15所述的方法，进一步包括在分离之前冷却所述至少部分所述压缩的循环流。
CN2012800138097A 2011-03-22 2012-03-05 用于在低排放联合涡轮机系统中捕获二氧化碳的系统和方法 Pending CN103443403A (zh)

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CN1959085A (zh) * 2005-07-08 2007-05-09 通用电气公司 二氧化碳分离的发电系统和方法
CN101187338A (zh) * 2006-11-07 2008-05-28 通用电气公司 具有二氧化碳隔离的发电系统和方法
CN101324203A (zh) * 2007-06-13 2008-12-17 通用电气公司 带排气再循环的用于发电的系统和方法

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CN108368750A (zh) * 2015-09-01 2018-08-03 八河流资产有限责任公司 使用嵌入式co2循环发电的系统和方法
CN108368750B (zh) * 2015-09-01 2020-08-18 八河流资产有限责任公司 使用嵌入式co2循环发电的系统和方法
CN108291767A (zh) * 2015-12-14 2018-07-17 埃克森美孚上游研究公司 在储存液氮的lng运输工具上的天然气液化的方法
CN108779685A (zh) * 2016-03-16 2018-11-09 斯特凡诺·布里奥拉 用于供应电功率和/或机械功率、加热功率和/或冷却功率的设备和方法
CN111655976A (zh) * 2017-11-28 2020-09-11 韩华压缩机株式会社 超临界二氧化碳发电系统
CN111655976B (zh) * 2017-11-28 2023-12-22 韩华压缩机株式会社 超临界二氧化碳发电系统
CN110425569A (zh) * 2019-08-27 2019-11-08 华能国际电力股份有限公司 一种采用烟气余热深度利用与烟气再循环的联合循环热电系统及方法

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