CN105863844B - 低排放动力产生系统和方法 - Google Patents

低排放动力产生系统和方法 Download PDF

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CN105863844B
CN105863844B CN201610205367.6A CN201610205367A CN105863844B CN 105863844 B CN105863844 B CN 105863844B CN 201610205367 A CN201610205367 A CN 201610205367A CN 105863844 B CN105863844 B CN 105863844B
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CN105863844A (zh
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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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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas- turbine plants for special use
    • F02C6/04—Gas-turbine plants providing heated or pressurised working fluid for other apparatus, e.g. without mechanical power output
    • F02C6/10—Gas-turbine plants providing heated or pressurised working fluid for other apparatus, e.g. without mechanical power output supplying working fluid to a user, e.g. a chemical process, which returns working fluid to a turbine of the plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C7/00—Features, components parts, details or accessories, not provided for in, or of interest apart form groups F02C1/00 - F02C6/00; Air intakes for jet-propulsion plants
    • F02C7/22—Fuel supply systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/34—Gas-turbine plants characterised by the use of combustion products as the working fluid with recycling of part of the working fluid, i.e. semi-closed cycles with combustion products in the closed part of the cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas- turbine plants for special use
    • F02C6/003—Gas-turbine plants with heaters between turbine stages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C7/00—Features, components parts, details or accessories, not provided for in, or of interest apart form groups F02C1/00 - F02C6/00; Air intakes for jet-propulsion plants
    • F02C7/12—Cooling of plants
    • F02C7/14—Cooling of plants of fluids in the plant, e.g. lubricant or fuel
    • F02C7/141—Cooling of plants of fluids in the plant, e.g. lubricant or fuel of working fluid
    • F02C7/143—Cooling of plants of fluids in the plant, e.g. lubricant or fuel of working fluid before or between the compressor stages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F05—INDEXING SCHEMES RELATING TO ENGINES OR PUMPS IN VARIOUS SUBCLASSES OF CLASSES F01-F04
    • F05D—INDEXING SCHEME FOR ASPECTS RELATING TO NON-POSITIVE-DISPLACEMENT MACHINES OR ENGINES, GAS-TURBINES OR JET-PROPULSION PLANTS
    • F05D2260/00—Function
    • F05D2260/60—Fluid transfer
    • F05D2260/61—Removal of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]

Abstract

提供了用于在联合循环动力工厂中的低排放动力产生的CO2分离的方法和系统。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。压缩的再循环流作为稀释剂，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其压力。净化流从压缩的再循环流流出并被引导至被配置用于利用碳酸钾溶剂从净化流吸收CO2的CO2分离器。

Description

低排放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06月09日，申请号为2011800332711(PCT/US2011/039830)，发明名称为“CO2分离系统和分离CO2的方法”。
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 Power GenerationSystems and Methods(低排放动力产生系统和方法)”的美国临时专利申请号61/361,180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“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61/361,173；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和于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。
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。
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 CO2 from 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废气，以便适于引入随后的膨胀器。额外的空气体积也不利地在废气中产生难以去除的过量的氧。典型的NGCC产生低压废气，其要求一部分产生的动力提取CO2，用于埋存(sequestration)或EOR，从而减少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废气的燃烧后碳捕获的典型特征。
本领域中需求的上述讨论意欲为代表性的，而不是穷尽的。解决一种或更多种这样的需求或本领域一些其他相关缺点的技术将有益于联合循环动力系统中的动力产生。
发明内容
本公开提供了利用综合的CO2分离系统产生动力的系统和方法。示例性系统包含燃气涡轮系统、废气再循环系统、热交换器和CO2分离器。燃气涡轮系统可具有燃烧室，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压缩的氧化剂和燃料，以便产生在膨胀器中进行膨胀的排出物流，从而产生气态废流并且至少部分地驱动主压缩机。压缩的再循环流作为被配置用于调节排出物流的温度的稀释剂。废气再循环系统可具有增压器和一个或多个冷却单元中的至少一个，所述一个或多个冷却单元被配置用于提高气态废流的质量流速，以向主压缩机提供冷却的再循环气体。主压缩机压缩冷却的再循环气体并产生压缩的再循环流，再循环流的一部分被引导至燃烧室，并且再循环流的一部分提供净化流。CO2分离器可流体连接至净化流并且可包括吸收器柱、第一阀门和再生柱。吸收器柱可被配置用于接收净化流并且使其中的碳酸钾溶剂循环，以吸收净化流中的CO2。吸收器柱排出富氮残余流和碳酸氢盐溶剂溶液。第一阀门可流体连接至吸收器柱并被配置用于闪蒸碳酸氢盐溶剂溶液至接近大气的压力。再生柱可流体连接至第一阀门并被配置用于接收和煮沸碳酸氢盐溶剂溶液，以从其中去除CO2和水，从而产生再生的碳酸钾溶剂，以便再循环返回吸收器柱。
本公开进一步提供了适于从废气再循环流中去除CO2的相关系统和方法。
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提高采收率法采油的另一个综合系统。
图4描绘了根据本公开的一种或多种实施方式的说明性的CO2捕获系统。
图5描绘了根据本公开的一种或多种实施方式的另一说明性的CO2捕获系统。
图6描绘了根据本公开的一种或多种实施方式的另一说明性的CO2捕获系统。
图7描绘了根据本公开的一种或多种实施方式的另一说明性的CO2捕获系统。
图8描绘了根据本公开的一种或多种实施方式的用于提高采收率法采油的低排放动力产生和氮气膨胀的综合系统。
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。
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被化学计量地或基本上化学计量地燃烧并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温度和进入随后的膨胀器的废气的温度。
通过冷却废气和从流冷凝出水，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。
燃料的化学计量的或基本上化学计量的燃烧，结合压力提高或在被压缩用于再循环之前废气的质量流速的另外增加可使CO2分压比在常规燃气涡轮废气中高得多。结果，CO2分离器中的碳捕获可利用较小能量密集溶剂诸如碳酸钾(K2CO3)或碳酸钠(Na2CO3)进行。废气中氧气(O2)、SOX和NOX的存在使胺溶剂(例如，MEA，DEA，MDEA和相关溶剂)的使用困难——即使利用更高的压力和增加的CO2含量，因为胺溶剂可在它们存在时分解。碳酸钾或碳酸钠溶剂耐受本公开的最小氧含量而不分解。此外，碳酸钾容易吸收SOX或NOX，将其转化成简单的肥料，诸如亚硫酸钾(K2SO3)和硝酸钾(KNO3)。这些肥料可以容易地以环境无害的方式排出。
现在参考附图，图1描绘了根据一种或多种实施方式利用联合循环布置，用于动力产生和CO2回收的说明性综合系统100的示意图。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，其以产生动力的、闭合的布雷顿循环为特征。燃气涡轮系统102可具有经轴108连接至膨胀器106的第一或主压缩机104。轴108可为任何机械、电或其他动力连接的，从而允许由膨胀器106产生的一部分机械能驱动主压缩机104。在至少一个实施方式中，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管线114中压缩的氧化剂混合的管线112中的燃料。在一种或多种实施方式中，管线112中的燃料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。管线114中压缩的氧化剂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和氮气成分的废气。压缩的再循环流144可源于主压缩机104并适于帮助促进管线114中压缩的氧化剂和管线112中燃料的化学计量的或基本上化学计量的燃烧，并也增加废气中CO2的浓度。在压缩的回收流144的存在下，管线116中的废气可作为管线112中的燃料和管线114中压缩的氧化剂的燃烧产物而产生。废气116被引导至膨胀器106的入口。在至少一个实施方式中，管线112中的燃料可主要为天然气，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)的管线116中的废气。在一些实施方式中，小部分未燃烧的燃料或其他化合物也可由于燃烧平衡限制存在于管线116中的废气中。当排出物流116通过膨胀器106扩张时，它产生机械动力，以驱动主压缩机104、电发生器或其他设施，并同时产生具有提高的CO2含量的管线122中的气态废气，导致管线144中压缩的再循环废气的流入。当管线116中的废气通过膨胀器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，并且也产生具有提高的CO2含量的管线122中的气态废气，其由管线144中压缩的再循环废气的流入产生。
动力产生系统100也可包含废气再循环(EGR)系统124。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、HRSG 126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。管线122中的气态废气可被发送至HRSG 126，以产生管线130中的蒸汽流和管线132中的冷却的废气。在一个实施方式中，管线130中的蒸汽可被发送至蒸汽燃气涡轮128以产生额外的电力。
管线132中冷却的废气可被发送至返回主压缩机104的再循环回路中的任何种类装置和/或设施。在说明的实施中，冷却单元和/或增压器以不同的顺序和构造进行显示和描述，其中的每一个都可被理解为适于增加冷却的废气的质量流速。通过增加进入主压缩机的冷却的废气的质量流速，可从主压缩机获得更高的出口压力。
在一些实施中，并如图1所示，再循环回路可包括至少一个冷却单元134，其被配置用于降低管线132中冷却的废气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，以提供用于产生管线130中额外的蒸汽的水源。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。在冷却单元134中，冷却管线132中的冷却的废气可减少压缩增压器142中冷却的再循环气流140需要的动力。
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。这可证明是有利的，因为管线116中富含CO2的废气通常保持较高的比热容。
主压缩机104可被配置用于压缩从增压器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可在流体连接至CO2分离器148的气体膨胀器152诸如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、电或其他动力连接任选地连接至入口压缩机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，主要由氮气组成的管线156中的废气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“Stoichiometric Combustion with Exhaust Gas Recirculation and Direct ContactCooler(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。
然而，在其他实施方式中，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)。另外地或可选地，膨胀器152可适于驱动其他装备，视情况而定。仍在其他实施方式中，如图8描绘的，气体膨胀器152可用下游压缩机188取代，该下游压缩机被配置用于压缩残余流151和产生管线190中的压缩的废气。在一种或多种实施方式中，管线190中压缩的废气可适于注入油藏用于压力保持应用。在甲烷气体通常被重新注入烃井以保持井压的应用中，压缩残余流151可证明是有利的。例如，管线190中加压的氮气可替代被注入烃井，并且任何残余甲烷气体可被出售或以其他方式用作相关应用中的燃料，诸如提供管线112中的燃料。
如本文所述的EGR系统124——特别是增加了增压器142，可被实施以实现动力产生系统100的废气中较高浓度的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废气流中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管线112中的燃料和管线114中压缩的氧化剂的进入混合物。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废气的任何过量的氧，同时增加其CO2组分。如此，管线122中的气态废气可具有小于大约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。
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。在一个实施方式中，入口压缩机118可被配置为化学计量的压缩机，其在大约280psia和大约300psia之间范围的压力下提供管线114中压缩的氧化剂。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/或膨胀器关联放置。例如，热电偶和/或氧传感器可被放置在燃烧室110的出口上、膨胀器106的入口上和/或膨胀器106的出口上。在操作中，热电偶和传感器可适于确定一个或多个流的组成和/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，管线144中压缩的再循环气体的体积质量流和/或管线114中压缩的氧化剂可被操纵或控制以符合要求。体积质量流速可通过任何合适的流量控制系统进行控制，其可与热电偶和/或氧传感器电通信。
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。管线112中的燃料和管线114中压缩的氧化剂的燃烧可产生大约2000°F和大约3000°F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的废气的较高比热容，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的管线122中的气态废气122可具有在或接近环境的压力。在至少一个实施方式中，管线122中的气态废气122可具有大约15.2psia的压力。在通过HRSG 126之前，管线122中的气态废气122的温度可在大约1180°F至大约1250°F的范围内，以产生管线130中的蒸汽和管线132中的冷却的废气。管线132中的冷却的废气可具有从大约190°F至大约200°F范围内的温度。在一种或多种实施方式中，冷却单元134可降低管线132中冷却的废气的温度，从而产生具有温度在大约32°F和120°F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。另外地或可选地，冷却的再循环气流的质量流速可通过其他手段诸如冷却提高。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废气，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°F，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。
此外，增加增压器142或在废气再循环系统中冷却可也增加氮气膨胀器152的功率输出和净化流146管线中的CO2净化压力。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，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可最好地理解图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，管线132中的冷却的废气可在冷却单元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HRSG126，以产生管线130中额外的蒸汽。
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中管线132中的冷却的废气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可最好地理解图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排出的管线132中的冷却的废气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，以产生管线130中额外的蒸汽。
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中冷却管线132中的冷却的废气可减少在增压器142中压缩冷却的再循环气流140需要的动力的量。另外，在第二冷却单元136中进一步冷却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。
燃烧室110中化学计量的燃烧和通过冷却单元134，136去除水的结合允许废气(例如，流122，132，140和/或144)中的CO2含量积累至大约10vol％或更高，其高于常规联合循环系统中的废气。这些作用，加上由增压器142和/或冷却单元的实施和作用引起的更高的质量流速的影响，使得CO2分压比常规燃气涡轮废气高得多。因此，这允许利用较小能量密集溶剂诸如碳酸钾(K2CO3)溶剂技术的CO2分离器148中的碳捕获。
氧气(O2)、SOX和NOX的存在使胺溶剂(例如，MEA、DEA、MDEA和相关溶剂)的使用困难，即使利用更高的压力和增加的CO2含量，因为这些气体可引起胺分解。然而，碳酸钾是非反应性的并对氧的任何作用免疫。尽管在燃烧室110进行的反应意欲为化学计量的，但由于燃烧平衡限制，小部分氧仍然可存在于净化流146中。尽管在该应用中使用MEA溶剂将要求显著的溶剂收回和复杂的处理，但碳酸钾溶剂的使用消除了基于氧的溶剂分解。
碳酸钾容易地吸收废气中的SOX或NOX，将这些化合物转化为简单的肥料，诸如亚硫酸钾(K2SO3)和硝酸钾(KNO3)。具体地，SO2、SO3和NO2都在水中形成相当强的酸，比CO2强得多。因此，它们将优选在溶剂溶液中被吸收，但将成为热稳定的盐(HSS)并且将不被再生作用去除。另一方面，NO和N2O具有低溶解度，并且与NO2相比更难以吸收，并趋于以较低浓度存在。作为简单的肥料，亚硫酸钾和硝酸钾可以容易地以环境无害的方式排出，只要没有其他有毒化合物诸如缓蚀剂、活性剂等被加入至溶剂系统。当去除硫酸盐和硝酸盐化合物时，氢氧化钾(KOH)可被加入用于溶剂组成(makeup)。因为氢氧化钾为相当便宜的化学品，这可被非常经济地完成。
参考图4，描绘的是如本文描述的可采用碳酸钾溶剂技术的CO2分离系统400的示例性实施方式。CO2分离系统400可为或形成CO2分离器148的至少一部分，如本文参考图1-3大体描述的。在一种或多种实施方式中，系统400可被配置用于在大约800°F的温度和在大约270psia至大约280psia的压力下接收从压缩的再循环流144(图1-3)流出的净化流146。
主要含有氮、CO2和多余的燃烧水的净化流146可在热交换器402中被冷却至大约250°F至大约300°F范围内的温度，从而产生管线404中的冷却的净化流。在一个实施方式中，热交换器402可产生蒸汽以与来自HRSG 126的蒸汽流130(图1-3)结合。在CO2分离系统400中从净化流146提取CO2在位于或接近净化流146的升高的压力和在大约150°F的温度下产生富氮残余流151。在至少一种实施方式中，热交换器402可为流体连接至残余流151的交叉交换热交换器，并且其被配置用于提取与冷却净化流146相关的热能，以便重新加热残余流151。一旦重新加热，主要由具有大约750°F的温度和大约270-280psia的压力的氮气蒸气组成的残余流151可随后被膨胀以产生机械动力，如以上大体描述的。
管线404中冷却的净化流可被引导至吸收器柱406，在此使来自管线408的溶剂循环，并且残余流151同时在顶部排出，用于进一步下游处理。在一个实施方式中，溶剂为碳酸钾的基于水的盐溶液。当与竞争的溶剂诸如MEA相比时，碳酸钾溶剂是非常耐受温度的。结果，如需要的，可将净化流146的冷却最小化，并且可允许更高温度的净化流146进入吸收器柱406，而不引起热分解的担心。因此，可更改净化流146的冷却程度以符合工艺热要求，而不是冷却以避免分解。
随着CO2被吸收器柱406中的碳酸钾吸收，它与水反应以形成碳酸(H2CO3)，随后是碳酸氢根(HCO3 -)。碳酸的酸性部分(H+)可与碳酸根离子(CO3 -2)反应以形成另外的碳酸氢根离子。因此，全部反应可为如下：
结果，充足的碳酸氢盐溶剂可经管线410从吸收器柱406的底部排出并且被引导至再生柱412。在一个实施方式中，位于管线410中的第一或中间阀门414可被配置用于在碳酸氢盐溶剂引入再生柱412之前闪蒸碳酸氢盐溶剂至较低的接近大气的压力。在至少一种实施方式中，第一阀门414可为液压涡轮，其被配置用于产生额外的动力。
在至少一种实施方式中，再生柱412可在超过水的标准沸点的温度下操作。例如，再生柱412可在范围从大约220°F、大约230°F或大约240°F至大约280°F、大约290°F或大约300°F的温度下操作。再生柱412可在范围从大约0psig至大约10psig的压力下操作。在至少一种实施方式中，再生柱412可被配置用于在大约3psig的压力下操作。再生柱412可被配置用于使用在其中循环的蒸汽煮沸碳酸氢盐溶剂并逆转在吸收器柱406中进行的反应，从而产生适于经以下管线416再循环的再生的贫(lean)碳酸钾溶剂。在至少一种实施方式中，管线泵418或类似物可经管线420驱动至少一部分贫碳酸钾溶剂返回吸收器柱406。
在向吸收器柱406的途中，一部分贫碳酸钾溶剂可作为热稳定盐(HSS)经管线423去除。如上所述，经管线423提取的说明性的HSS可包含复合肥料诸如但不限于亚硫酸钾和/或硝酸钾。为了弥补经管线423去除的碳酸钾含量的损失，并保持全部溶液浓度(strength)，氢氧化钾流可随后经管线425加入。在一种或多种实施方式中，氢氧化钾用作溶剂组成。管线420中的贫碳酸钾溶剂可随后被任选地引导通过第一冷却单元422。在一种或多种实施方式中，第一冷却单元422可为例如空气冷却器或散热器型热交换器，其被配置用于降低溶剂的温度。如果被使用，第一冷却单元422可被配置用于降低贫碳酸钾溶剂的温度至范围从大约230°F和大约60°F之间的温度。如可理解的，在至少一种实施方式中，HSS可以可选地在第一冷却单元422后作为肥料去除，以及加入氢氧化钾。
为了产生在再生柱412中循环的蒸汽和保持再生需要的热，管线416中的至少一部分贫碳酸钾溶剂可经管线417被引导至再沸器419。再沸器419可被配置用于升高管线417中的贫碳酸钾溶剂的温度，并使加热的再生的碳酸钾溶剂经管线421返回再生柱。在至少一种实施方式中，再沸器419可被供应来自HRSG 126(图1-3)的热。然而，在其他实施方式中，再沸器419可被供应来自蒸汽燃气涡轮128(图1-3)的排出物的热。
包含在净化流146中的水可在吸收器柱406中冷凝进入溶剂溶液，并随后在再生柱412中煮沸。因此，再生柱412可进一步经顶部管线424排出CO2蒸气和任何残余水。在至少一种实施方式中，CO2蒸气和残余水在被引入冷凝器428之前可被引导通过第二冷却单元426，诸如空气冷却器或散热器型热交换器。冷凝器428可被配置用于将残余水与任何回收的CO2分离并且引导分离的水进入下面的管线430，同时供应回收的CO2顶部进入管线150。如可理解的，管线150可为与以上参考图1-3描述的相同的管线150。在至少一种实施方式中，管线150中分离的CO2可随后被压缩用于应用，诸如CO2埋存、提高采收率法采油、CO2出售、碳捕获和/或其组合。
在一个实施方式中，管线430中至少一部分分离的水可利用泵432经管线434再循环返回再生柱412中，以允许系统中的水平衡保持不变。水经流404不断地被引入溶剂，并随后经管线436，150和151去除。为了保持溶剂状态和浓度，水必须在系统400内保持平衡。因此，在管线434中再循环的水可允许水返回，以便管线421中产生的蒸汽可独立于该水平衡而受到控制。换言之，该再循环的水可用作用于再生柱412中蒸汽产生的给水或产生来自供应冷却的低压蒸汽。在其他实施方式中，管线430中一部分残余水可经管线436被处理为新鲜工艺用水。例如，尽管含有一部分溶解的CO2，但管线436中的水可用于灌溉水，被处理用于锅炉给水，和/或其他工艺用水。
现在参考图5，描绘的是CO2分离系统500的另一个说明性的实施方式，在一些方面类似于图4的系统400。如此，整个系统500将不详细进行描述，但可参考图4最好地理解。然而，图4的系统400可表征为单一阶段碳酸钾工艺，图5的系统500可在至少一种实施方式中表征为两阶段碳酸钾工艺。如所描绘的，CO2分离系统500可包含“半贫”溶剂再循环回路，其中一部分溶剂可在完成再生之前经管线502从再生柱412收回。在至少一种实施方式中，经管线502收回的该部分溶剂可为通过再生柱412循环的整个溶剂体积的大约50％或更多。在再生柱412中剩余的溶剂溶液的平衡可被完全再生，如上所述，并经其下面的管线416被排出。
位于管线502内的泵504可引导半贫溶剂溶液至吸收器柱406。在一个实施方式中，半贫溶剂溶液可被向下供应506进入吸收器柱406。作为仅部分再生的，管线502中的半贫溶剂不能从处于吸收器柱406中较高位置的较低浓度的气体吸收CO2。相反，其可被供应进入吸收器柱406，在那里它以吸收最大量的CO2，并不稀释经管线408进入吸收器柱406的全贫溶剂。
系统500中的该变化可要求比图4的系统400更高的溶剂循环流速，但可需要更少的外部热能以去除CO2。以该提高的热效率，与在净化流146中包含的热负荷相比，系统500可需要更少的再沸器419热负荷。换言之，引入的净化流146的热可能能够满足全部再沸器419热要求。因此，如果注入残余流151用于EOR，系统500可为热自给自足的并且不需要来自动力涡轮机HRSG 126的补充热。
现在参考图6，描绘的是CO2分离系统600的另一个示例性实施方式，在一些方面分别类似于图4和5的系统400、500。如此，整个系统600将不详细进行描述，但可参考图4和5最好地理解。如所描绘的，充分的碳酸氢盐溶剂可经管线410从吸收器柱406底部排出，并且在被引入分离器604之前利用第一阀门602降低压力。在一个实施方式中，第一阀门602可被配置用于降低碳酸氢盐溶剂的压力从净化流146压力(例如，在大约270-280psia之间)至中等压力水平。在一种或多种实施方式中，中等压力水平可在范围大约20psia至大约50psia内。
分离器604可被配置用于接收降低压力的溶液并且经顶部管线606去除至少一部分CO2。在一种或多种实施方式中，管线606中去除的CO2可在冷却单元608中冷却，并且随后被供应进入下游压缩系统607。在一种或多种实施方式中，冷却单元608可为直接接触冷却器、调温冷却器、机械制冷单元或其组合。因为管线606中去除部分的CO2处于升高的压力，虽然净化流146和大气的压力之间中等压力，它也可被注入下游压缩系统607的中间阶段，从而降低压缩系统607上要求的压缩负载。
在分离器604中剩余的余量CO2和碳酸氢盐溶剂可经下面的管线610从分离器604排出，并且在被引导入再生柱412之前利用第二阀门612闪蒸至流611中更低的接近大气的压力。在系统600的一些实施方式中，随后可如上参考分别如图4或5所描绘的系统400或系统500所述，发生全部的溶剂再生。例如，如上所述，分离部分的CO2可经管线150在或接近大气压下从冷凝器428提取并且被引导至下游压缩系统607的第一压缩阶段。因此，下游压缩系统607可接收基本上包含捕获的CO2的至少两个供应流；一个供应流具有管线606中的被注入中间压缩阶段的高压CO2，和第二供应流具有管线150中的低压CO2并在第一压缩阶段被注入。如可理解的，这样的布置可在实际上不增加再生器柱412热负载的情况下降低在制备用于EOR或埋存中对CO2压缩的动力要求。
源于系统600的至少一个益处是从再生柱412产生纯的或接近纯的CO2流的能力。存在于管线410中的CO2流的污染物可包含水和溶解在循环溶剂中的一些易挥发气体(例如，N2、CO、Ar等)。系统600可适于去除基本上所有这些易挥发气体，留下仅具有高纯度CO2和水的再生柱412顶部流424。在一种或多种实施方式中，顶部管线424中的CO2浓度可为系统600中全部CO2流量的大约2/3。一旦从水被分离，管线150中的一部分CO2可被引导入净化管线614并且被捕获用于非EOR用途，诸如化学原料、食品生产等。
如可理解的，可结合参考图5-6公开的实施方式和特征，而不脱离本公开。因此，下表和补充信息为上述实施方式和/或特征的结合提供了说明性工艺数据。显示在表中的溶剂流和气流参考数字可参考图5-6。
表2-工艺数据
现在参考图7，描绘的是CO2分离系统700的另一个示例性实施方式。因为系统700在一些方面类似于上述系统400和500，所以整个系统700将不详细进行描述，但可参考图4和5最好地理解。系统700可证明在如此实施方式中是特别有优势的：在这些实施方式中残余流151和在管线150中捕获的CO2在EOR应用中被重新注入。如将在以下描述的，系统700可被配置用于允许净化流146的冷却结合再生柱412和再沸器419中的工艺热要求的较好的集成。
因为系统700中的残余流151可随后被压缩用于EOR，热交换器402不必与残余流151交叉交换，但相反，它的热能可用于其他用途。例如，在一种或多种实施方式中，热交换器402可被配置用于接收至少一部分回收的燃烧水或来自管线436的废水，以在管线702中产生低压蒸汽。管线702中所得的蒸汽可具有大约50psig或更高的压力，并且可被分成管线702a和702b和用作一个或多个引射器(eductor)704a和704b的运动的动力气体。尽管在图7中显示两条管线702a和702b和两个引射器704a和704b，但将理解可具有更多或更少，而不脱离本公开的范围。
在一个实施方式中，引射器704a和704b可被配置为蒸汽喷射器，其适于降低从再生柱412排出进入管线416的贫碳酸钾溶剂上的压力。为了完成该目的，管线416中的贫溶剂可被引导入串联布置并分别流体连接至引射器704a和704b的一个或多个混合室706a和706b中。在一个实施方式中，第一混合室706a可供应第二混合室706b，用于进一步处理。然而，在其他实施方式中，混合室706a和706b可被并联布置，而不脱离本公开的范围。
在操作中，引射器704a和704b可适于使管线702中的蒸汽加速，以在或接近被配置用于闪蒸-煮沸混合室706a和706b中的贫溶剂的真空状态下产生低压区。煮沸贫溶剂可释放不经顶部管线424回收的额外的水和CO2并且抽取所得的气态流出物进入管线708a和708b中。管线708a和708b中所得的流出物可被注入再生柱412中，以便经顶部管线424去除和捕获过量的CO2。因为其蒸汽含量，流出物也可用作汽提用蒸汽，从而补充或完全取代至少一些通常由再沸器419供应的再生的煮沸热负荷。因此，系统700可允许保存在贫溶剂中的一些热驱动混合室706a和706b中的蒸气流动，从而降低溶剂再生需要的净热和再沸器419的整体尺寸。
闪蒸-煮沸混合室706a和706b中额外的水和CO2也可通过降低其压力从大约3psig至大约10psig真空同时冷却剩余的贫溶剂。在一种或多种实施方式中，贫溶剂的温度可从大约240°F、大约230°F或大约220°F降低至大约210°F、大约200°F或大约190°F。冷却的贫溶剂可随后经管线710从混合室706b排出并且随后被引导至管线泵418，该管线泵如上所述可经管线420驱动溶剂返回吸收器柱406。因为贫溶剂的温度可在混合室706a和706b中冷却，因此可减小冷却单元422的尺寸。
因为分别在管线702a和702b中向引射器704a和704b提供的低压蒸汽被注入再生柱412，可导致消耗源于管线434中分离的水的至少一部分给水。因此，任何额外的水可作为额外的废水经顶部管线424从再生柱412中回收。结果，过量的水可连续地在系统700中积累并且可经废水管线436提取。如可理解的，可改变水回流速度以保持溶剂水平衡，或碳酸钾溶液浓度。
如可理解的，可结合参考图5-7公开的实施方式和特征，而不脱离本公开。因此，下表和补充信息为上述实施方式和/或特征的示例性结合提供了说明性工艺数据。显示在表中的溶剂流和气流参考数字可参考图5-7。
表3-工艺数据
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 (20)

1.综合的CO2分离系统，包括：
具有燃烧室的燃气涡轮系统，所述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，以便产生排出物流，所述排出物流在膨胀器中膨胀，从而产生气态废流并且至少部分地驱动主压缩机，其中所述压缩的再循环流用作被配置用于调节所述排出物流的温度的稀释剂；
废气再循环系统，其具有增压器和一个或多个冷却单元中的至少一个，其被配置用于提高所述气态废流的质量流速以向所述主压缩机提供冷却的再循环气体，其中所述主压缩机压缩所述冷却的再循环气体并且产生所述压缩的再循环流，所述压缩的再循环流的一部分被引导至所述燃烧室，并且所述压缩的再循环流的一部分提供净化流；和
流体连接至所述净化流的CO2分离器，所述CO2分离器包括：
吸收器柱，其被配置用于接收所述净化流并且使碳酸钾溶剂在其中循环，以吸收所述净化流中的CO2，其中所述吸收器柱排出富氮残余流和碳酸氢盐溶剂溶液；
第一阀门，其流体连接至所述吸收器柱并被配置用于闪蒸所述碳酸氢盐溶剂溶液至较低的压力，从而产生降低压力的溶液；
分离器，其流体连接至所述第一阀门并被配置用于接收所述降低压力的溶液并且从其中去除第一部分的CO2；
第二阀门，其流体连接至所述分离器并被配置用于接收剩余部分的所述降低压力的溶液和闪蒸所述剩余部分至接近大气压，从而产生接近大气压的碳酸氢盐溶剂溶液；
再生柱，其流体连接至所述第二阀门并被配置用于接收和煮沸所述接近大气压的碳酸氢盐溶剂溶液以从其中去除CO2和水混合物，从而产生再循环返回所述吸收器柱的再生的碳酸钾溶剂；和
冷凝器，其流体连接至所述再生柱，并且被配置用于接收和分离来自从所述接近大气压的碳酸氢盐溶剂溶液中去除的所述CO2和水混合物的第二部分的CO2；
其中所述第一部分的CO2的压力高于所述第二部分的CO2的压力，并且所述第一部分和所述第二部分CO2被分别引导至下游压缩系统。
2.权利要求1所述的系统，进一步包括与所述净化流相关联的热交换器，其中所述热交换器为交叉交换热交换器，其被配置用于降低所述净化流的温度至250℉和300℉之间。
3.权利要求1所述的系统，进一步包括再沸器，其流体连接至所述再生柱，并且被配置用于接收和加热一部分所述再生的碳酸钾溶剂并且产生加热的再生的碳酸钾溶剂。
4.权利要求3所述的系统，其中所述再沸器被配置用于使所述加热的再生的碳酸钾溶剂再循环返回所述再生柱，以产生用于煮沸所述碳酸氢盐溶剂溶液的蒸汽。
5.权利要求1所述的系统，其中所述第二部分的CO2被引导至所述下游压缩系统的第一阶段，并且所述第一部分的CO2被引导至所述下游压缩系统的中间阶段。
6.权利要求1所述的系统，其中与所述CO2和水混合物分离的一部分所述水被用泵输送返回所述再生柱，以产生蒸汽。
7.权利要求1所述的系统，其中一部分所述碳酸氢盐溶剂溶液在完成溶剂再生之前从所述再生柱中收回，并且再循环和向下供应至所述吸收器柱。
8.权利要求7所述的系统，其中碳酸氢盐溶剂溶液总量的50％或更多在完成溶剂再生之前从所述再生柱中收回。
9.综合的CO2分离系统，包括：
具有燃烧室的燃气涡轮系统，所述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，以便在膨胀器中膨胀排出物流，从而产生气态废流并且至少部分地驱动主压缩机，其中所述压缩的再循环流用作被配置用于调节所述排出物流的温度的稀释剂；
废气再循环系统，其具有增压器和流体连接至所述增压器的一个或多个冷却单元，所述增压器被配置用于接收和提高所述气态废流的压力，所述一个或多个冷却单元被配置用于冷却所述气态废流，并且向所述主压缩机提供冷却的再循环气体，其中所述主压缩机压缩所述冷却的再循环气体并且产生所述压缩的再循环流；
净化流，其流体连接至所述压缩的再循环流并且具有热交换器，所述热交换器被配置用于降低所述净化流的温度并产生冷却的净化流；和
CO2分离器，其流体连接至所述热交换器，所述CO2分离器包括：
吸收器柱，其被配置用于接收所述冷却的净化流并且使碳酸钾溶剂在其中循环，以吸收所述冷却的净化流中的CO2，其中所述吸收器柱排出富氮残余流和碳酸氢盐溶剂溶液；
第一阀门，其流体连接至所述吸收器柱并且被配置用于闪蒸所述碳酸氢盐溶剂溶液至较低的压力，从而产生压力降低的溶液；
分离器，其流体连接至所述第一阀门并且被配置用于接收所述压力降低的溶液并且从其中去除第一部分的CO2，以便被注入下游压缩系统的内阶段；
第二阀门，其流体连接至所述分离器并且被配置用于接收剩余部分的所述压力降低的溶液，并且闪蒸剩余部分至接近大气压，从而产生接近大气压的碳酸氢盐溶剂溶液；
再生柱，其流体连接至所述第二阀门并且被配置用于接收和煮沸所述接近大气压的碳酸氢盐溶剂溶液，以去除第二部分的CO2和水，从而产生再生的碳酸钾溶剂，以便再循环返回所述吸收器柱；和
冷凝器，其流体连接至所述再生柱，并且被配置用于接收和分离来自从所述接近大气压的碳酸氢盐溶剂溶液中去除的所述CO2和水混合物的第二部分的CO2；
其中所述第一部分的CO2的压力高于所述第二部分的CO2的压力，并且所述第一部分和所述第二部分CO2被分别引导至下游压缩系统。
10.权利要求9所述的系统，其中所述热交换器为交叉交换热交换器，其被配置用于降低所述净化流的温度至250℉和300℉之间。
11.权利要求10所述的系统，进一步包括高压冷却单元，其被配置用于在注入所述下游压缩系统的所述内阶段之前冷却所述第一部分的CO2。
12.权利要求9所述的系统，其中所述第二部分的CO2被引导至所述下游压缩系统的第一阶段，并且所述第一部分的CO2被引导至所述下游压缩系统的中间阶段。
13.分离CO2的方法，包括：
在燃烧室中且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，从而产生驱动主压缩机并且产生气态废流的在膨胀器中膨胀的排出物流，其中所述压缩的再循环流调节所述排出物流的温度；
用增压器提高所述气态废流的压力并且用流体连接至所述增压器的一个或多个冷却单元冷却所述气态废流，借此将冷却的再循环气体引导至所述主压缩机用于压缩，其中所述主压缩机压缩所述冷却的再循环气体，以产生所述压缩的再循环流；
用热交换器冷却流体连接至压缩的再循环流的净化流，以产生冷却的净化流；
引导所述冷却的净化流至具有碳酸钾溶剂在其中循环的吸收器柱，所述碳酸钾溶剂被配置用于吸收存在于所述冷却的净化流中的CO2；
从所述吸收器柱排出富氮残余流和碳酸氢盐溶剂溶液；
通过第一阀门闪蒸所述碳酸氢盐溶剂溶液至较低的压力，从而产生压力降低的溶液；
使用流体连接至所述第一阀门的分离器以从所述压力降低的溶液去除第一部分的CO2；
通过第二阀门闪蒸剩余部分的所述压力降低的溶液至接近大气压，从而产生接近大气压的碳酸氢盐溶剂溶液；
在再生柱中煮沸所述接近大气压的碳酸氢盐溶剂溶液，以从其中去除CO2和水混合物，从而产生再生的碳酸钾溶剂；
使所述再生的碳酸钾溶剂再循环返回所述吸收器柱；
在流体连接至所述再生柱的冷凝器中分离第二部分的CO2与所述CO2和水混合物，其中所述第一部分的CO2的压力高于所述第二部分的CO2的压力；和
分别引导所述第一部分和所述第二部分的CO2至下游压缩系统。
14.权利要求13所述的方法，进一步包括提高再沸器中一部分所述再生的碳酸钾溶剂的温度，以产生加热的再生的碳酸钾溶剂。
15.权利要求14所述的方法，进一步包括使所述加热的再生的碳酸钾溶剂再循环返回至所述再生柱，以产生用于煮沸所述碳酸氢盐溶剂溶液的蒸汽。
16.权利要求13所述的方法，进一步包括引导所述第二部分的CO2至下游压缩系统的第一阶段，并且引导所述第一部分的CO2至所述下游压缩系统的中间阶段。
17.权利要求16所述的方法，进一步包括引导一部分在所述分离中与所述CO2和水混合物分离的所述水返回至所述再生柱，以产生蒸汽。
18.权利要求13所述的方法，进一步包括在完成溶剂再生之前，从所述再生柱收回一部分所述碳酸氢盐溶剂溶液，并将所述收回的碳酸氢盐溶剂溶液向下供应至所述吸收器柱。
19.权利要求1或9所述的综合的CO2分离系统，其中所述燃烧室仅仅输出由所述燃料、所述压缩的氧化剂在压缩的再循环流的存在下燃烧形成的排放物流。
20.权利要求13所述的方法，其中所述燃烧室仅仅输出由所述燃料、所述压缩的氧化剂在压缩的再循环流的存在下燃烧形成的排放物流。
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