CN103958852A - 用于控制低排放涡轮系统中的化学计量燃烧的系统和方法 - Google Patents
用于控制低排放涡轮系统中的化学计量燃烧的系统和方法 Download PDFInfo
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Abstract
提供了用于控制低排放涡轮系统中的氧化剂进料从而维持化学计量的或基本化学计量的燃烧条件的系统、方法和设备。在一个或更多实施例中，这样的控制通过将再循环排气的一部分转向并将其与氧化剂进料组合从而在馈送到燃烧室的组合的氧化剂排气流中维持恒定的氧含量来实现。
Description
相关申请的交叉参考
本申请要求提交于2011年3月22日标题为METHODS FORCONTROLLING STOICHIOMETRIC COMBUSTION ON A FIXEDGEOMETRY GAS TURBINE SYSTEM AND APPARATUS ANDSYSTEMS RELATED THERETO的美国临时申请61/466385以及提交于2011年9月30日标题为SYSTEMS AND METHODS FORCONTROLLING STOICHIOMETRIC COMBUSTION IN LOWEMISSION TURBINE SYSTEMS的美国临时申请61/542031的优先权，这两个申请都以其全部内容包括在此作为参考。
本申请涉及提交于2011年9月30日标题为SYSTEMS ANDMETHODS FOR CARBON DIOXIDE CAPTURE IN LOW EMISSIONTURBINE SYSTEMS的美国临时申请61/542036；提交于2011年9月30日标题为SYSTEMS AND METHODS FOR CARBON DIOXIDECAPTURE IN LOW EMISSION TURBINE SYSTEMS的美国临时申请61/542037；提交于2011年9月30日标题为SYSTEMS ANDMETHODS FOR CARBON DIOXIDE CAPTURE IN LOW EMISSIONCOMBINED TURBINE SYSTEMS的美国临时申请61/542039；提交于2011年9月30日标题为LOW EMISSION POWER GENERATIONSYSTEMS AND METHODS INCORPORATING CARBON DIOXIDESEPARATION的美国临时申请61/542041；提交于2011年3月22日标题为METHODS OF VARYING LOW EMISSION TURBINE GASRECYCLE CIRCUITS AND SYSTEMS AND APPARATUS RELATEDTHERETO的美国临时申请61/466381；提交于2011年9月30日标题为METHODS OF VARYING LOW EMISSION TURBINE GASRECYCLE CIRCUITS AND SYSTEMS AND APPARATUS RELATEDTHERETO的美国临时申请61/542035；提交于2011年3月22日标题为LOW EMISSION TURBINE SYSTEMS HAVING A MAIN AIRCOMPRESSOR OXIDANT CONTROL APPARATUS AND METHODSRELATED THERETO的美国临时申请61/466384；提交于2011年9月30日标题为LOW EMISSION TURBINE SYSTEMSINCORPORATING INLET COMPRESSOR OXIDANT CONTROLAPPARATUS AND METHODS RELATED THERETO的美国临时申请61/542030；这些申请都以其全部内容包括在此作为参考。
技术领域
本公开的实施例涉及低排放发电。更特别地，本公开的实施例涉及用于控制向低排放涡轮系统的燃烧室供应氧化剂从而实现并维持化学计量的或基本化学计量的燃烧条件的方法和设备。
背景技术
本部分意图介绍可以与本公开的示例性实施例关联的本领域的各个方面。该讨论被确信为帮助提供框架，从而促进更好地理解本公开的特定方面。因此，应理解应据此阅读本部分，而不必作为对现有技术的陈述。
许多产油国经历强劲的国内电力需求增长，并且在增加油回收（EOR）中具有改善从其储油层的油回收的兴趣。两种普通EOR技术包括用于储油层压力维持的氮（N2）喷射以及用于EOR的混相驱动（miscible flooding）的二氧化碳（CO2）喷射。还存在关于温室气体（GHG）排放的全球关注。总量管制和交易（cap-and-trade）政策的实施与该关注的组合在许多国家中使得减少CO2排放在这些国家和其中操作烃生产系统的公司中享有优先权。
降低CO2排放的一些途径包括使用溶剂例如胺的燃料脱碳或补充燃烧捕集。然而，这些解决方案都是昂贵的并且降低发电效率，导致较低的电力生产、增加的燃料需求和满足国内电力需求的增加的电力成本。特别地，氧、SOX和NOX组分的存在使得利用胺溶剂吸收非常成问题。另一途径是在组合循环中的增氧燃料气体涡轮（例如，其中捕集源自气体涡轮布雷顿循环的排气热，从而形成蒸汽并且在兰金循环中产生另外的电力）。然而，没有可以在这样的循环中操作的商业上可用的气体涡轮，并且生产高纯度氧所需要的电力显著降低了工艺的总效率。
此外，由于关于全球气候变化和二氧化碳排放影响的日益增长的关注，重点已置于将源自发电厂的二氧化碳排放最小化上。气体涡轮联合循环发电厂是有效的并且具有与核电或煤炭发电技术比较的更低的成本。因为以下原因，从气体涡轮联合循环发电厂的排气捕集二氧化碳是非常昂贵的：（a）在排气器（exhaust stack）中二氧化碳的低浓度，（b）需要处理的气体的巨大体积，（c）排气流的低压，以及在排气流中存在的巨大量的氧。这些因素中的全部导致从联合循环电厂的二氧化碳捕集的高成本。
因此，仍具有对低排放、高效率发电和CO2捕集制造处理的充分需要。
发明内容
在本文中描述的联合循环发电厂中，在通常的天然气联合循环（NGCC）电厂中排放的源自低排放气体涡轮的排气改为被冷却并再循环到气体涡轮主压缩机入口。再循环排气而不是过量压缩的新鲜空气被用来将燃烧产物冷却到膨胀器中的材料限制。本设备、系统和方法使低排放涡轮能够在大范围的环境条件上维持优选的燃烧方式，例如化学计量燃烧。通过将化学计量燃烧与排气再循环组合，在再循环气体中的CO2的浓度提高，同时最小化过量O2的存在，这两者都使得CO2更容易回收。在一个或更多实施例中，在此描述的低排放涡轮系统采用空气作为氧化剂。
本发明涉及用于控制低排放涡轮系统中的氧化物进料以便维持化学计量的或基本化学计量的燃烧条件的系统、方法和设备。在一个或更多实施例中，这样的控制通过确保氧化剂到燃烧室的恒定质量流率的输送的方法或系统实现。示例包括但不限于用于向氧化剂进料添加再循环的排气从而在氧化剂进料中维持希望的氧含量的各种配置。这些配置可以任选地包括一种或更多其他控制方法，例如比率控制器，或除了将再循环的排气添加到氧化剂进料之外还修改进料的温度。
附图说明
本公开的前述和其他优点可以在浏览以下实施例的非限制性示例的具体实施方式和附图后变得明显，其中：
图1示出用于低排放发电和增加CO2回收的集成系统。
图2示出用于低排放发电和增加CO2回收的集成系统，其中再循环的排气的一部分在再循环鼓风机和冷却单元之间从再循环流转向并被添加到入口压缩机进料。
图3示出用于低排放发电和增加CO2回收的集成系统，其中再循环的排气的一部分从主压缩机转向并在级间位置被添加到入口压缩机。
图4示出用于低排放发电和增加CO2回收的集成系统，其中再循环的排气的一部分在再循环鼓风机和冷却单元之间从再循环流转向并被添加到压缩的氧化剂进料。该系统包括在氧化剂和燃料进料上的可选的比率控制器。
图5示出在配置上相似于图3的用于低排放发电和增加CO2回收的集成系统，其中氧化剂进料在进入入口压缩机之前被冷冻。
具体实施方式
在以下具体实施方式部分中，关于优选实施例描述本公开的具体实施例。然而，就以下说明专用于本公开的特定实施例或特定用途来说，这意图仅用于示例性目的并且仅提供示例性实施例的描述。因此，本公开不限于在下面描述的具体实施例，而是其包括落入所附权利要求的真实精神和范围内的全部替换、修改和等价物。
本文使用的各种术语在下面定义。就在权利要求中使用的术语没有在下面定义来说，其应被给予如在至少一部印刷出版物或已公布的专利中反映的相关领域技术人员给予该术语的最广泛定义。
如在此使用的，术语“天然气”涉及从原油井（伴生气）和/或从地下含气层（非伴生气）获得的多组分气体。天然气的成分和压力可以显著变化。通常的天然气流含有作为主要组分的甲烷（CH4），即大于50mol%的天然气流是甲烷。天然气流也可以含有乙烷（C2H6）、更高分子量的烃（例如C3-C20烃）、一种或更多酸性气体（例如硫化氢）或其任意组合。天然气也可以含有较少量的杂质，例如水、氮、硫化铁、蜡、原油或其任何组合。
如在此使用的，术语“化学计量燃烧”指代燃烧反应，该燃烧反应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，其中反应物的全部容量被用来形成所述产物。如在此使用的，术语“基本化学计量燃烧”指代具有范围从约0.9：1到约1.1：1或更优选从约0.95：1到约1.05：1的当量比的燃烧反应。在此术语“化学计量的”的使用意思是除非另行指出否则包括化学计量的和基本化学计量的条件。
如在此使用的，术语“流”指代大量流体，但是该术语流的使用通常意味着大量移动流体（例如具有速度或质量流率）。然而，术语“流”不必是速度、质量流率或用于包围该流的特定类型的导管。
目前公开的系统和处理的实施例可以用来为增加油回收（EOR）或封存（sequestration）应用而生产超低排放电力和CO2。根据在此公开的实施例，空气和燃料的混合物可以化学计量地燃烧并同时与再循环排气流混合。一般包括燃烧产物例如CO2的再循环排气流可以用作稀释剂，从而控制或以其他方式缓和化学计量燃烧和进入随后的膨胀器的烟道气体的温度。
在近化学计量条件的燃烧（或“稍富的”燃烧）可以证明有利于消除过量氧去除的成本。通过冷却烟道气体并将水从流中冷凝出来，可以产生相对高含量的CO2流。当再循环排气的一部分可以在闭式布雷顿循环中用于温度缓和时，剩余净化流可以用于EOR应用，并且可以在极少或没有SOX、NOX或CO2被排放到大气的情况下生产电力。例如，净化流可以在适于排出富氮气体的CO2分离器中处理，该富氮气体可以随后在气体膨胀器中膨胀，从而生成另外的机械功率。在此公开的系统使得以更经济高效的水平进行电力生产和另外CO2的制造或获取。然而，为了避免从化学计量条件的偏离，供应到燃烧室的氧化剂的量必须被密切控制。本发明提供用于实现这样的控制的系统和方法。
在一个或更多实施例中，本发明涉及包括入口压缩机、气体涡轮系统和排气再循环系统的集成系统。气体涡轮系统包括配置为在存在压缩的再循环流的情况下燃烧一种或更多种氧化剂和一种或更多种燃料的燃烧室。入口压缩机压缩一种或更多种氧化剂并将压缩的氧化剂流引导到燃烧室。燃烧室将第一排放流引导到膨胀器，从而生成排气流并且至少部分地驱动主压缩机，并且该主压缩机压缩排气流并由此生成压缩的再循环流。在本发明的一个或更多实施例中，排气的一部分从排气再循环系统转向，并与一种或更多种氧化剂组合，从而形成被引导到燃烧室的组合的氧化剂排气流。转向的排气量可以变化，使得在燃烧室中维持化学计量的或基本化学计量的反应条件。
转向的排气可以取自排气再循环系统中的任何点，并且可以在氧化剂进入燃烧室之前在任何点处与一种或更多种氧化剂组合。例如，在一个或更多实施例中，从排气再循环系统转向的排气的部分在入口压缩机上游与一种或更多种氧化剂组合。可替换地，从排气再循环系统转向的排气的部分可以在入口压缩机下游但在压缩的氧化剂进入燃烧室之前与压缩的氧化剂组合。
在一个或更多实施例中，从排气再循环系统转向的排气的所述部分可以从主压缩机提取并且注入到入口压缩机中。主压缩机和入口压缩机中的每个可以具有一个或更多级。在某些实施例中，主压缩机具有两个或更多级并且转向的排气在级间位置（即在多级之间）从主压缩机抽取。在相同或其他实施例中，入口压缩机具有两个或更多级，并且转向的排气在级间位置被注入到入口压缩机中。
在一些实施例中，排气再循环系统可以包括配置为接收并冷却排气流的至少一个冷却单元，以及配置为在将冷却的再循环气体引导到主压缩机之前接收排气流并提高排气流的压力的至少一个鼓风机。在这样的实施例中，从排气再循环系统转向的排气的所述部分可以从进入鼓风机的排气流转向，或从自鼓风机流动到冷却单元的排气流转向，或从离开冷却单元的排气流转向，并且可以在氧化剂进入燃烧室之前在任何点与一种或更多种氧化剂组合。
在一个或更多实施例中，集成系统可以可选地进一步包括一个或更多控制器，该控制器配置为调整进入到燃烧室的组合的氧化剂排气流与一种或更多种燃料的流量，从而维持选择的流量比率并因此维持氧化剂对燃料的固定比率。一个或更多控制器可以是适合调整到燃烧室的入口流的任何类型的控制器，例如比率控制器。在一个或更多实施例中，比率控制器可以配置为从安装在到燃烧室的入口流中的一个或更多上的一个或更多流量计接收测量值，并且基于从流量计接收的测量值，打开或关闭一个或更多阀，从而相应地改变入口流中的一个或更多的流动。这样，一个或更多控制器提供超过通过将排气的一部分与氧化剂进料组合而提供的控制的另外水平的控制。一个或更多控制器也可以单独用作控制氧化剂进料从而维持化学计量的或基本化学计量的燃烧的唯一方法。
在一个或更多实施例中，集成系统可以进一步包括一个或更多冷却装置，该冷却装置配置为在一种或更多种氧化剂（或在排气的转向部分在入口压缩机上游与氧化剂组合的情况下的组合的氧化剂排气流）被引入到入口压缩机之前将该氧化剂冷却。例如，氧化剂可以被冷却到低于环境空气温度至少约5℉或至少约10℉，或至少约15℉，或至少约20℉，或至少约25℉，或至少约30℉，或至少约35℉，或至少约40℉的温度。在相同或其他实施例中，在进入冷却装置的氧化剂和离开冷却装置的氧化剂之间的温差是至少约5℉，或至少约10℉，或至少约15℉，或至少约20℉，或至少约25℉，或至少约30℉，或至少约35℉，或至少约40℉。在一个或更多实施例中，冷却装置可以是一个或更多热交换器、机械制冷单元、直接接触冷却器、调温冷却器或相似装置及其组合。另外，冷却装置可以采用适合于这样的应用的任何已知的冷却流体，例如冷冻水或海水，或制冷剂，例如非卤化碳氢化合物、碳氟化合物、氢氟碳化合物、氯氟烃、氢化含氯氟烃、无水氨、丙烷、二氧化碳、丙烯等。在某些实施例中，系统可以进一步包括分离器，该分离器配置为从冷却装置接收冷却的氧化剂，并且在氧化剂流被引入到入口压缩机之前从所述氧化剂流去除任何水滴。分离器可以是适合于意图的用途的任何装置，例如叶片组、网垫或其他除雾装置。
在一个或更多实施例中，本发明也提供用于发电的方法。该方法包括在入口压缩机中压缩一种或更多种氧化剂，从而形成压缩的氧化剂；在存在压缩的再循环排气的情况下并在化学计量的或基本化学计量的条件下，在燃烧室中燃烧压缩的氧化剂和至少一种燃料，由此生成排放流；在膨胀器中将排放流膨胀，从而至少部分驱动主压缩机并生成排气流；将排气流引导到排气再循环系统；以及将排气的一部分从排气再循环系统转向，并将排气的转向部分与一种或更多种氧化剂组合，从而形成被引导到燃烧室的组合的氧化剂排气流。转向的排气可以取自排气再循环系统中的任何点，并且可以在氧化剂进入燃烧室之前在任何点处与一种或更多种氧化剂组合。主压缩机压缩排气流并且由此生成压缩的再循环流。在本发明的一些方法中，排气再循环系统可以包括至少一个冷却单元和至少一个鼓风机，以使排气流在至少一个冷却单元中冷却，并且排气流的压力在至少一个鼓风机中增加，由此生成被引导到主压缩机的冷却的再循环气体。
在一个或更多实施例中，本发明的方法可以进一步包括调整进入到燃烧室中的组合的氧化剂排气流和一种或更多种燃料的流量，从而维持固定的氧化剂与燃料的比率。流量可以经比率控制器或相似装置控制。在相同或其他实施例中，本发明的方法可以进一步包括在一种或更多种氧化剂被引入到入口压缩机之前将该氧化剂冷却，并且在冷却的氧化剂流被引入到入口压缩机之前从该冷却的氧化剂流可选地去除水滴。
通过在本文描述的系统和方法中将再循环的排气的一部分转向并与氧化剂进料组合，可以在馈送到燃烧室的氧化剂的量上施加更精确的控制。具体地，允许氧化剂进料的质量密度基于环境温度和压力条件而浮动，但通过改变向氧化剂进料提供的再循环气体的量，在组合的氧化剂排气进料中的每立方英尺氧气量保持在恒定水平。当需要更多氧时，与氧化剂进料混合的再循环气体的量减少，并且当需要更少氧时，与氧化剂进料混合的再循环气体的量增加。这样，可以适应由温度变化、压力变化、空气质量、湿度等导致的氧化剂进料的氧含量的变化，并且化学计量燃烧条件可以无关于在系统中或在外界环境中任何地方的改变而被维持。
现在参考附图，本发明的各种实施例可以参考在图1中示出的基本情况而被最好地理解。图1说明了配置为提供改进的补充燃烧CO2捕集处理的发电系统100。在至少一个实施例中，发电系统100可以包括可以表征为闭式布雷顿循环的气体涡轮系统102。在一个实施例中，气体涡轮系统102可以具有第一或主压缩机104，其通过共用轴108或其他机械、电气或其他动力耦接来耦接到膨胀器106，由此允许由膨胀器106生成的机械能的一部分驱动压缩机104。膨胀器106也可以为其他用途例如向第二或入口压缩机118供电而生成动力。气体涡轮系统102可以是标准气体涡轮，其中主压缩机104和膨胀器106分别形成标准气体涡轮的压缩机和膨胀器端。然而，在其他实施例中，主压缩机104和膨胀器106可以是在系统102中的个体化部件。
气体涡轮系统102也可以包括配置为将与压缩的氧化剂114混合的燃料流112燃烧的燃烧室110。在一个或更多实施例中，燃料流112可以包括任何合适的烃气体或液体，例如天然气、甲烷、石脑油、丁烷、丙烷、合成气、柴油、煤油、航空燃料、煤炭衍生燃料、生物燃料、含氧烃原料或其组合。压缩的氧化剂114可以得自流体耦合到燃烧室110并且适于压缩进料氧化剂120的第二或入口压缩机118。尽管本公开在此假设进料氧化剂120是环境空气，但氧化剂可以包括含氧的任何合适气体，例如空气、富氧空气或其组合。
如在下面更详细描述的，燃烧室110也可以接收包括烟道气体的压缩的再循环流144，该烟道气体主要具有CO2和氮组分。压缩的再循环流144可以得自主压缩机104，并且适于帮助促进压缩的氧化剂114和燃料112的燃烧，并且也提高工作流体中的CO2浓度。在压缩的再循环流144存在的情况下，被引导到膨胀器106入口的排放流116可以作为燃料流112和压缩的氧化剂114的燃烧产物生成。在至少一个实施例中，燃料流112可以主要是天然气，由此生成包含蒸发的水、CO2、氮、氮氧化物（NOX）和氧化硫（SOX）的体积部分的排放物116。在一些实施例中，由于燃烧平衡限制，因此小部分的未燃烧的燃料112或其他化合物也可以存在于排放物116中。当排放流116通过膨胀器106膨胀时，其生成机械动力，从而驱动主压缩机104或其他设施，并且还产生具有增高的CO2含量的排气流122。
发电系统100也可以包括排气再循环（EGR）系统124。尽管在附图中说明的EGR系统124结合了各种设备，但说明的配置仅是代表性的，并且将排气122再循环回到主压缩机从而实现本文陈述的目标的任何系统都可以被使用。在一个或更多实施例中，EGR系统124可以包括热回收蒸汽发生器（HRSG）126或相似装置。排气流122可以发送到HRSG126以便生成蒸汽130的流和冷却的排气132。蒸汽130可以任选地发送到蒸汽气体涡轮（未示出），从而生成另外的电力。在这样的配置中，HRSG126和蒸汽气体涡轮的组合可以表征为闭式兰金循环。与气体涡轮系统102联合，HRSG126和蒸汽气体涡轮可以形成联合循环发电厂（例如天然气联合循环（NGCC）电厂）的部分。
在一个或更多实施例中，离开HRSG126的冷却的排气132可以发送到配置为降低冷却的排气132的温度并生成冷却的再循环气流140的至少一个冷却单元134。在一个或更多实施例中，冷却单元134在此被认为是直接接触冷却器（DCC），但可以是任何合适的冷却装置，例如直接接触冷却器、调温冷却器、机械制冷单元或其组合。冷却单元134也可以配置为经水滴流（未示出）去除冷凝的水的一部分。在一个或更多实施例中，冷却的排气流132可以被引导到流体耦合到冷却单元134的鼓风机或增压压缩机142。在这样的实施例中，压缩的排气流136离开鼓风机142并且被引导到冷却单元134。
鼓风机142可以配置为在冷却的排气流132被引入主压缩机104之前提高该冷却的排气流132的压力。在一个或更多实施例中，鼓风机142提高了冷却的排气流132的总密度，由此将增加的质量流率的相同体积流引导到主压缩机104。因为主压缩机104通常是体积流量受限的，由此引导更多质量流通过主压缩机104可以导致来自主压缩机104的更高的排放压力，因此转换成膨胀器106两端的更高的压力比。膨胀器106两端生成的更高的压力比可以允许更高的入口温度，并因此允许膨胀器106功率和效率的提高。由于富CO2排放物116一般维持较高的特定热容，因此这可以证明是有利的。因此，冷却单元134和鼓风机142在结合时可以每个均适于最优化或改善气体涡轮系统102的操作。
主压缩机104可以配置为将从EGR系统124接收的冷却的再循环气流140压缩到额定高于燃烧室110压力的压力，由此生成压缩的再循环流144。在至少一个实施例中，净化流146可以从压缩的再循环流144捕集并随后在CO2分离器或其他设备（未示出）中处理，从而获取CO2。已分离的CO2可以用于销售，在需要CO2的其他处理中使用和/或为增加油回收（EOR）、封存或其他目的而压缩并注入地下储油层。
EGR系统124如在此描述地可以被实施以在发电系统100的工作流体中实现更高的CO2浓度，由此允许用于随后的封存、压力维持或EOR应用的更有效的CO2分离。例如，在此公开的实施例可以将烟道气体排气流中的CO2的浓度有效提高到约10wt%（重量百分比）或更高。为实现该目的，燃烧室110适于按化学计量燃烧引入的燃料112和压缩的氧化剂114的混合物。为缓和化学计量燃烧的温度从而符合膨胀器106入口温度和部件冷却需求，来自压缩的再循环流144的排气的一部分可以被注入燃烧室110中作为稀释剂。因此，本公开的实施例可以从工作流体中基本消除任何过量的氧，同时增加其CO2成分。这样，排气流122可以具有小于约3.0vol%（体积百分比）的氧，或小于约1.0vol%的氧，或小于约0.1vol%的氧，或者甚至小于约0.001vol%的氧。
在本文未示出的一些实施例中，高压蒸汽也可以在燃烧室中代替再循环的排气或除再循环的排气之外被用作稀释剂。在这样的实施例中，蒸汽的添加降低了EGR系统中的功率和尺寸需求（或一并消除了EGR系统），但需要水再循环回路的添加。
另外，在本文未示出的进一步实施例中，到燃烧室的压缩的氧化剂进料可以包含氩。例如，氧化剂可以包含从约0.1vol%到约5.0vol%的氩，或从约1.0vol%到约4.5vol%的氩，或从约2.0vol%到约4.0vol%的氩，或从约2.5vol%到约3.5vol%的氩，或约3.0vol%的氩。如本领域技术人员将认识到的，将氩结合到压缩的氧化剂进料可以需要在主压缩机和燃烧室之间添加交叉式交换器或相似装置，该交叉式交换器或相似装置配置为从再循环流去除过量的CO2，并在用于燃烧的适当温度下将氩返回到燃烧室。
图2到图5说明了对在图1中示出的参考系统100的修改，该修改意图通过向氧化剂进料添加变化量的再循环的排气从而适应由温度变化、压力变化、空气质量、湿度等导致的氧化剂进料的氧含量变化，从而允许在馈送到燃烧室110的氧化剂的量上的更精确的控制。在氧化剂进料上的增大的控制允许化学计量燃烧条件的恒定维持，而无关于在系统中或在外界环境中任何地方的改变。在包括但不限于在图2到图5中示出的实施例的本发明的一个或更多实施例中，在提供到燃烧室的进料中需要的氧气量和因此与氧化剂进料组合的再循环气体的量可以通过采用传感器（未示出）测量希望的性质来确定，所述性质例如在离开膨胀器的排气中的氧气、二氧化碳和未燃烧的烃的含量。基于这样的测量，计量阀（metering valve）（同样未示出）可以用来控制排气和氧化剂进料的混合物，从而在组合的氧化剂排气进料中确保恰当的比例。
现在参考图2，其示出了实施并描述为系统200的图1的发电系统100的可替换的配置。这样，图2可以参考图1被最好地理解。在图2的系统200中，循环排气的一部分被转向并与进入入口压缩机118的氧化剂进料120组合，使得在到入口压缩机（和因此燃烧室110）的进料中的氧气量可以无关于氧化剂进料120的成分变化而维持在恒定水平。如在图2中示出，压缩的排气流136的一部分经流210转向并被添加到氧化剂进料120，从而形成组合的氧化剂排气进料212。允许氧化剂进料的质量密度基于环境温度和压力条件而浮动，但通过改变经流210向进料提供的再循环气体的量，在组合的氧化剂排气进料212中每立方英尺的氧气量保持在恒定水平。当需要更多氧时，与氧化剂进料混合的再循环气体的量减少，并且当需要更少氧时，与氧化剂进料混合的再循环气体的量增加。这样，不仅化学计量条件在燃烧室中维持，而且主压缩机104的需要的负荷也可以减小，由此进一步提高系统200的效率。组合的氧化剂排气进料212被引导到入口压缩机118并被压缩，从而形成压缩的氧化剂排气流214。在离开入口压缩机118之后，压缩的氧化剂排气流214被馈送到燃烧室110，并且系统200的剩余部分以与先前描述的图1的系统100相同的方式操作。
现在参考图3，其示出了实施并描述为系统300的图1的发电系统100的可替换的配置，其中再循环的排气用来以与以上关于图2的描述相似的方式在到燃烧室的进料中维持恒定水平的氧气。这样，图3可以参考图1和图2被最好地理解。在图3的系统300中，冷却的再循环排气的一部分从主压缩机104经流310抽取，并且在级间位置被注入到入口压缩机118。压缩的氧化剂排气流214然后离开入口压缩机并被引导到燃烧室110，并且系统300的剩余部分以与先前描述的图1的系统100相同的方式操作。与图2的系统200一样，允许氧化剂进料的质量密度基于环境温度和压力条件而浮动，但通过改变经流310向进料提供的再循环气体的量，在压缩的氧化剂排气进料214中每立方英尺的氧气量保持在恒定水平。
现在参考图4，其示出了实施并描述为系统400的图1的发电系统100的可替换的配置，其中再循环的排气用来以与关于图2的描述相似的方式在到燃烧室的进料中维持恒定水平的氧气。这样，图4可以参考图1和图2被最好地理解。在图4的系统400中，压缩的排气流136的一部分经流410转向并且被添加到离开入口压缩机118的压缩的氧化剂114，从而形成压缩的氧化剂排气流214。压缩的氧化剂排气流214被引导到燃烧室110，并且系统400的剩余部分以与先前描述的图1的系统100相同的方式操作。与图2的系统200一样，允许氧化剂进料的质量密度基于环境温度和压力条件而浮动，但通过改变经流410向进料提供的再循环气体的量，在压缩的氧化剂排气进料214中每立方英尺的氧气量保持在恒定水平。
图4也示出了由比率控制器412提供的可选的另外水平的控制。比率控制器412调整燃料进料112和压缩的氧化剂排气进料214中的一个或两个的流量，从而始终维持进入燃烧室110的燃料与氧化剂的恒定比率。流量计416安装在燃料进料和氧化剂排气进料流上。由流量计416提供的测量值被传送到比率控制器412，该比率控制器412然后自动调整阀414，从而增加或减少在燃料112和氧化剂排气214进料的一个或两个中的流量。这样，比率控制器412提供除了通过将再循环的排气与氧化剂进料组合而提供的第一水平控制之外的动态、实时控制的第二种方法。
对本领域技术人员显然的是，一个或更多比率控制器可以如上所述地使用，而无关于排气再循环回路的配置或排气的一部分被添加到氧化剂进料的位置。另外，一个或更多比率控制器可以用作化学计量控制的唯一方法，不需要同样将排气的一部分添加到氧化剂进料。任何这样的配置或修改在此均是可预计的并且被认为在本发明的范围内。
现在参考图5，其示出了实施并描述为系统500的图1的发电系统100的可替换的配置，其中再循环的排气用来以与以上关于图3的描述相似的方式在到燃烧室的进料中维持恒定水平的氧气。这样，图5可以参考图1和图3被最好地理解。在图5的系统500中，与图3的系统300中相同，冷却的再循环排气的一部分从主压缩机104经流310抽取并且在级间位置被注入到入口压缩机118。
图5也示出了由通过在氧化剂被馈送到入口压缩机118之前冷冻进料氧化剂120而提供的可选的另外水平的控制。离开入口压缩机118的氧化剂的质量主要由进入入口压缩机118的氧化剂进料120的密度确定。由于固定的入口几何构形，入口压缩机118一般引入固定体积的气体。通过控制氧化剂进料120的温度，其密度可以受控制，这进而意味着在恒定体积下，该氧化剂进料的质量流率也受控制。当到燃烧室110的氧化剂进料120的质量流率恒定时，化学计量条件可以被更容易地维持。如在图5中示出，氧化剂进料120在入口压缩机118上游的热交换器510中冷冻。氧化剂进料120的冷却由在流514中提供的制冷剂实现。尽管在此描述了采用制冷剂的热交换器，但任何类型的冷却装置均可以用来将氧化剂冷却到希望温度。例如，其他冷却方法包括使用冷冻的水或海水作为冷却流体的一个或更多热交换器、机械制冷单元、直接接触冷却器、调温冷却器及其组合。另外，可以采用适合于意图的用途的任何已知的制冷剂，例如非卤化碳氢化合物、碳氟化合物、氢氟碳化合物、氯氟烃、氢化含氯氟烃、无水氨、丙烷、二氧化碳、丙烯等。进一步地，尽管在图5中示出了一个热交换器510，但两个或更多热交换器或其他冷却装置也可以被采用（未示出），特别是与多级压缩机结合采用。在这样的实施例中，可以希望在压缩机的每级之间并入一个或更多个冷却装置。
在本发明的一个或更多实施例中，离开热交换器510的冷冻的氧化剂进料120可以可选地被引导到分离器512，从而去除可以夹杂其中的任何冷凝的水滴。分离器512可以是适合于去除水滴的任何装置，例如叶片组、网垫或其他除雾装置。氧化剂进料流120从分离器512被引导到入口压缩机118，并且系统500的剩余部分以与先前描述的图3的系统300相同的方式操作。对于本领域技术人员明显的是，一个或更多热交换器或其他冷却装置可以在具有或不具有伴随的分离器的情况下使用，并且无关于排气再循环回路的配置或排气的一部分被添加到氧化剂进料的位置。任何这样的配置或修改在此均是可预计的并且认为在本发明的范围内。
尽管本公开可能易受各种修改和可替换形式的影响，但在上面讨论的示例性实施例仅通过示例的方式示出。在此描述的任何实施例的任何特征或配置可以与任何其他实施例或与多个其他实施例组合（就可行性来说），并且全部这样的组合意图在本发明的保护范围内。此外，应理解本公开不意图限于在此公开的特定实施例。当然，本公开包括落入所附权利要求的真实精神和保护范围内的全部替换、修改和等价物。
Claims (29)
1.一种集成系统，包括：
气体涡轮系统，所述气体涡轮系统包括配置为在存在压缩的再循环流的情况下燃烧一种或更多种氧化剂和一种或更多种燃料的燃烧室，其中所述燃烧室将第一排放流引导到膨胀器，从而生成排气流并且至少部分地驱动主压缩机；
入口压缩机，所述入口压缩机配置为压缩所述一种或更多种氧化剂并将压缩的氧化剂引导到所述燃烧室；以及
排气再循环系统，其中所述主压缩机压缩所述排气流并由此生成所述压缩的再循环流；
其中所述排气的一部分从所述排气再循环系统转向，并与所述一种或更多种氧化剂组合，从而形成被引导到所述燃烧室的组合的氧化剂排气流；以及
其中在所述燃烧室中的反应条件是化学计量的或基本化学计量的。
2.根据权利要求1所述的系统，其中从所述排气再循环系统转向的所述排气的所述部分在所述入口压缩机上游与所述一种或更多种氧化剂组合。
3.根据权利要求1所述的系统，其中在所述压缩的氧化剂进入所述燃烧室之前，从所述排气再循环系统转向的所述排气的所述部分在所述入口压缩机下游与所述压缩的氧化剂组合。
4.根据权利要求1所述的系统，其中从所述排气再循环系统转向的所述排气的所述部分从所述主压缩机提取并且被注入到所述入口压缩机中。
5.根据权利要求4所述的系统，其中所述主压缩机包括两个或更多级，并且所述排气在级间从所述主压缩机提取。
6.根据权利要求4所述的系统，其中所述入口压缩机包括两个或更多个级，并且所述排气在级间被注入到所述入口压缩机。
7.根据权利要求1所述的系统，其中所述排气再循环系统包括配置为接收并冷却所述排气流的至少一个冷却单元，以及配置为在将冷却的再循环气体引导到所述主压缩机之前接收所述排气流并增大所述排气流的压力的至少一个鼓风机。
8.根据权利要求7所述的系统，其中从所述排气再循环系统转向的所述排气的所述部分从自所述鼓风机流动到所述冷却单元的所述排气流转向。
9.根据权利要求1所述的系统，进一步包括一个或更多个比率控制器，所述一个或更多个比率控制器配置为调整进入到所述燃烧室的所述组合的氧化剂排气流与所述一种或更多种燃料的流量，从而维持氧化剂与燃料的固定的比率。
10.根据权利要求1所述的系统，进一步包括一个或更多个冷却装置，所述一个或更多个冷却装置配置为在所述一种或更多种氧化剂被引入到所述入口压缩机之前将所述一种或更多种氧化剂冷却。
11.根据权利要求10所述的系统，进一步包括分离器，所述分离器配置为从所述冷却装置接收冷却的氧化剂，并且在所述氧化剂流被引入到所述入口压缩机之前从所述氧化剂流去除水滴。
12.根据权利要求10所述的系统，其中所述冷却装置是使用制冷剂作为冷却流体的热交换器。
13.一种发电的方法，包括：
在入口压缩机中压缩一种或更多种氧化剂，从而形成压缩的氧化剂；
在存在压缩的再循环排气的情况下，在燃烧室中燃烧所述压缩的氧化剂和至少一种燃料，由此生成排放流；
在膨胀器中将所述排放流膨胀，从而至少部分地驱动主压缩机并生成排气流；
将所述排气流引导到排气再循环系统，其中所述主压缩机压缩所述排气流并且由此生成压缩的再循环流；以及
将所述排气的一部分从所述排气再循环系统转向，并将排气的转向的部分与所述一种或更多种氧化剂组合，从而形成引导到所述燃烧室的组合的氧化剂排气流；
其中在所述燃烧室中的反应条件是化学计量的或基本化学计量的。
14.根据权利要求13所述的方法，其中从所述排气再循环系统转向的所述排气的所述部分在所述入口压缩机上游与所述一种或更多种氧化剂组合。
15.根据权利要求13所述的方法，其中在所述压缩的氧化剂进入所述燃烧室之前，从所述排气再循环系统转向的所述排气的所述部分在所述入口压缩机下游与所述压缩的氧化剂组合。
16.根据权利要求13所述的方法，其中从所述排气再循环系统转向的所述排气的所述部分从所述主压缩机提取并且被注入到所述入口压缩机。
17.根据权利要求16所述的方法，其中所述主压缩机包括两个或更多级，并且所述排气在级间从所述主压缩机提取。
18.根据权利要求16所述的方法，其中所述入口压缩机包括两个或更多级，并且所述排气在级间被注入到所述入口压缩机。
19.根据权利要求13所述的方法，其中所述排气再循环系统包括至少一个冷却单元和至少一个鼓风机，使得所述排气流在所述至少一个冷却单元中冷却，并且所述排气流的压力在所述至少一个鼓风机中增大，由此生成被引导到所述主压缩机的冷却的再循环气体。
20.根据权利要求19所述的方法，其中从所述排气再循环系统转向的所述排气的所述部分从自所述鼓风机流动到所述冷却单元的所述排气流转向。
21.根据权利要求13所述的方法，进一步包括调整进入到所述燃烧室的所述组合的氧化剂排气流与所述一种或更多种燃料的流量，从而维持氧化剂与燃料的固定的比率。
22.根据权利要求21所述的方法，其中所述氧化剂排气流与所述一种或更多种燃料的流量由比率控制器调节。
23.根据权利要求13所述的方法，进一步包括在所述一种或更多种氧化剂被引入到所述入口压缩机之前将所述一种或更多种氧化剂冷却。
24.根据权利要求23所述的方法，进一步包括在冷却的氧化剂流被引入到所述入口压缩机之前从所述冷却的氧化剂流去除水滴。
25.根据权利要求23所述的方法，其中以使用制冷剂作为冷却流体的热交换器冷却所述一种或更多种氧化剂。
26.根据权利要求1所述的系统，其中所述压缩的再循环流包括补充或代替所述排气流的蒸汽冷却剂。
27.根据权利要求26所述的系统，进一步包括水再循环回路，从而提供所述蒸汽冷却剂。
28.根据权利要求13所述的方法，进一步包括向所述压缩的再循环流添加蒸汽冷却剂，从而补充或代替所述排气流。
29.根据权利要求28所述的方法，进一步包括水再循环回路，从而提供所述蒸汽冷却剂。
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- 2012-03-05 AU AU2012231388A patent/AU2012231388B2/en not_active Ceased
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Also Published As
| Publication number | Publication date |
|---|---|
| EP2689122A4 (en) | 2015-05-06 |
| AR088726A1 (es) | 2014-07-02 |
| TWI564474B (zh) | 2017-01-01 |
| SG192901A1 (en) | 2013-10-30 |
| JP6348416B2 (ja) | 2018-06-27 |
| CA2828768A1 (en) | 2012-09-27 |
| WO2012128925A2 (en) | 2012-09-27 |
| US20140000271A1 (en) | 2014-01-02 |
| EP2689122A2 (en) | 2014-01-29 |
| MX2013009833A (es) | 2013-10-03 |
| US9599021B2 (en) | 2017-03-21 |
| EA201391363A1 (ru) | 2014-02-28 |
| EA029181B1 (ru) | 2018-02-28 |
| AU2012231388B2 (en) | 2016-05-12 |
| CN103958852B (zh) | 2017-04-26 |
| WO2012128925A3 (en) | 2014-04-24 |
| TW201247998A (en) | 2012-12-01 |
| MY168249A (en) | 2018-10-16 |
| JP2014517180A (ja) | 2014-07-17 |
| MX361603B (es) | 2018-12-11 |
| CA2828768C (en) | 2017-09-05 |
| SG10201602189PA (en) | 2016-04-28 |
| AU2012231388A1 (en) | 2013-10-03 |
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