CN115427347A - 用于碳捕获的蒸汽甲烷重整单元 - Google Patents

用于碳捕获的蒸汽甲烷重整单元 Download PDF

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CN115427347A
CN115427347A CN202180027847.7A CN202180027847A CN115427347A CN 115427347 A CN115427347 A CN 115427347A CN 202180027847 A CN202180027847 A CN 202180027847A CN 115427347 A CN115427347 A CN 115427347A
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F·C·扬克
S·乔利
H·格泽尔－阿亚格
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Abstract

一种熔融碳酸盐燃料电池供电的系统，其用于捕获由蒸汽甲烷重整器系统产生的二氧化碳。将来自变压吸附系统的尾气与来自燃料电池阳极的废气混合，然后加压和冷却以提取液化二氧化碳。将残余的低CO2气体引导至阳极气体氧化器、阳极、重整器以用于燃料燃烧，和/或引导至所述变压吸附系统。来自所述重整器的低CO2烟道气可以被排放到大气中或者被引导至所述阳极气体氧化器中。到达燃料电池的CO2量的减少允许根据所述系统的功率需求来设计所述燃料电池的尺寸，并且消除了输出额外电力输出的需要。

Description

用于碳捕获的蒸汽甲烷重整单元
相关专利申请的交叉参考
本申请要求2020年3月11日提交的美国临时申请第62/987,985号的权益和优先权，其全部公开内容通过引用并入本文。
背景技术
本公开涉及一种蒸汽甲烷重整器(SMR)。特别地，本公开涉及一种具有增强的二氧化碳(CO2)捕获的SMR。
蒸汽甲烷重整器(SMR)通常用于从气体原料如天然气或炼厂气生产合成气。产生的合成气可以在工厂内进一步加工，以产生各种最终产物，包含纯化的氢气、甲醇、一氧化碳和氨。然而，在重整过程中产生的烟道气含有污染物，如二氧化碳，已知这些污染物通过造成整体气候变化，从而对环境产生不利影响。众所周知，SMR是炼油厂最大的CO2排放者中的一个。因此，近年来，许多政府监管机构要求减少二氧化碳向大气中的排放。
考虑到对二氧化碳释放的有害影响的认识和最近对其排放的限制，已经努力从蒸汽重整器工厂产生的烟道气中有效地除去纯化形式的二氧化碳。通过从烟道气中除去二氧化碳，二氧化碳可替代地用于其他更安全的目的，如地下储存或石油生产需要。
目前从SMR捕获CO2的方法，如例如使用胺吸收汽提塔系统从烟道气中除去CO2(燃烧后捕获)或在汽提塔系统中使用物理或胺基化学溶剂从SMR尾气中除去CO2(燃烧前捕获)，效率非常低且成本高。汽提系统通常过于耗能，需要大量的蒸汽来使溶剂再生。采用熔融碳酸盐燃料电池(MCFC)技术的最新燃烧后方法在从宿主植物中捕获CO2同时发电。超出系统自身需求产生的额外电力提供了收入来源，其可抵消系统资本和运营成本。在常规的后燃烧系统中，来自SMR的含有高CO2水平的烟道气被引导至MCFC。由于高CO2水平，此方法需要相对大量的MCFC模块，这可能是昂贵的，并且可能产生比期望的更多的电力。因此，常规的基于MCFC的CO2捕获系统可能非常昂贵，并且可能产生不容易卸载的过剩能量。
发明内容
本文描述的实施例提供了从SMR系统的变压吸附(PSA)系统的尾气中捕获CO2的SMR-CO2捕获系统，与一些常规的CO2捕获系统相比，其可以有利地有助于以更高效和成本有效的方式捕获CO2。
在一些实施例中，用于从SMR系统捕获CO2的系统包括压缩机、制冷机和CO2分离器。来自SMR系统PSA的尾气由压缩机压缩，并由制冷机冷却。CO2分离器将液化CO2与残余的未冷凝气体分离。未冷凝的气体然后可以再循环到SMR系统的PSA和/或SMR系统的重整器中作为燃料燃烧。
在一些实施例中，该系统还包括MCFC。来自PSA的尾气可以在被压缩、冷却和分离成液态CO2和残余气体之前与来自MCFC的阳极的废气混合。残余气体可以再循环到SMR系统或用于捕获CO2的系统的各个部分中。例如，在一些实施例中，气体的一部分可以再循环到阳极气体氧化器，然后再循环到MCFC的阴极，而另一部分再循环到MCFC的阳极。在一些实施例中，残余气体的第三部分可以再循环到SMR系统的PSA以产生更多的氢气，或者再循环到SMR系统中的重整器以作为燃料燃烧。残余气体的此第三部分可改为再循环用于SMR系统外的PSA中。在一些实施例中，残余气体的第三部分可以再循环到SMR系统的PSA以产生更多的氢气，并且残余气体的第四部分可以再循环到SMR系统中的重整器以作为燃料燃烧。
在一些实施例中，来自SMR系统的重整器的烟道气可被排放到大气中。因为来自SMR系统的PSA的尾气没有被燃烧来为SMR系统的重整器提供燃料，所以烟道气中的CO2相对低。在其他实施例中，烟道气可被引导至用于捕获CO2的系统中的阳极气体氧化器，然后被引导至MCFC的阴极。
在一些实施例中，MCFC的尺寸可经设计仅为用于捕获CO2的系统、仅为SMR系统或两者供电。因为来自SMR系统的PSA的尾气没有被燃烧来为SMR系统的重整器提供燃料，所以MCFC接收的CO2量减少，从而允许MCFC的尺寸被设计得更小，并且减少了过剩的发电。
在一些实施例中，提供了实施上述系统的捕获CO2的方法。
前述是本公开的概述，因此必然含有细节的简化、概括和省略。因此，本领域的技术人员将了解，概述仅为说明性且并不旨在以任何方式进行限制。如仅通过权利要求书所定义，本文所描述的装置和/或过程的其它方面、特征以及优点将在本文中且结合附图阐述的具体实施方式中变得显而易见。
附图说明
结合附图，从以下详细描述中将更充分地理解本公开，其中相同的附图标记指代相同的元件，其中：
图1显示了常规SMR-CO2捕获系统的示意图。
图2显示了根据本公开的代表性实施例的SMR-CO2捕获系统的示意图。
图3显示了根据另一个代表性实施例的SMR-CO2捕获系统的示意图。
图4显示了根据又一代表性实施例的SMR-CO2捕获系统的示意图。
图5显示了根据又一代表性实施例的SMR-CO2捕获系统的示意图。
图6显示了根据代表性实施例的从SMR捕获CO2的方法。
具体实施方式
总体参考附图，本文公开了与一些常规CO2捕获系统相比，能够以更高效和成本有效的方式捕获CO2的增强的SMR-CO2捕获系统的各种实施例。本文公开的各种实施例可以能够增加捕获的CO2的量，提高捕获CO2的效率，增加产生的氢气的量，和/或降低与捕获CO2相关联的成本。在本文公开的各种实施例中，附图之间相同的附图标记指代相同的元件，但是从一幅图到另一幅图增加200(例如，图2中的PSA 450与图3中的PSA 650相同，等等)。
一般来说，在SMR-CO2捕获系统的典型SMR单元中，天然气与水反应形成氢气和CO2。一些甲烷未被转化，并且在该过程中还产生一些一氧化碳。通常使用PSA系统从氢气中除去这些杂质以及没有通过冷凝分离出来的任何水，该PSA系统可以在大气压下解吸这些杂质以产生通常CO2含量高并且还含有CO、甲烷和氢气的PSA尾气。典型地，PSA尾气作为燃料在SMR单元中再循环，在该SMR单元中气体与空气一起燃烧以提供吸热重整反应所需的热量。此反应产生具有相对高CO2含量的烟道气，该烟道气可以被引导至MCFC用于随后的CO2捕获。在这种类型的系统配置中，MCFC的尺寸部分地由从SMR单元接收的烟道气中转移到MCFC的阳极的CO2的量(或百分比)(例如，70％-90％的CO2)支配。
然而，PSA尾气的成分非常类似于CO2捕获系统中MCFC的经变换阳极废气。因此，申请人有利地确定PSA尾气可以在被压缩和冷却以从气体中分离CO2之前直接与MCFC的阳极废气混合，而不是使PSA尾气在SMR单元中再循环。以这种方式，MCFC的尺寸不受来自SMR单元的PSA尾气的支配，因为通常来自PSA尾气的烟道气中所含有的CO2与MCFC下游的阳极废气混合，用于随后的CO2捕获。因此，可通过选择较小尺寸的MCFC来降低系统的总成本，该较小尺寸的MCFC可例如为CO2捕获系统、SMR系统本身或两者的制冷机和其他电力负载产生刚好足够的电力，如下面更详细讨论的。
在一些实施方式中，该系统还可以被配置成将烟道气从SMR单元引导至MCFC，用于额外的CO2捕获。在一些实施方式中，来自MCFC的阳极的含有氢气和一氧化碳的未使用的燃料可以从CO2捕获尾气被引导至PSA，以增加系统的氢气生产。在一些实施方式中，电力从外部来源购买，而不是使用MCFC来为CO2捕获系统供电。
图1显示了典型的SMR-CO2捕获系统。如图1所示，由蒸汽供应管线210供应的蒸汽和由天然气供应管线220供应的天然气被混合并馈送至重整器系统200的重整器230，用于将甲烷转化为氢气、CO2和CO。重整器流出物可以被输送到重整器系统200的变换组件，在该变换器组件中流出物可以被冷却，并且大部分CO可以根据以下反应被变换成氢气：
Figure BDA0003884099020000042
然后经变换的气体经由变换气体管线240被送到PSA系统250，在该PSA系统中，其中氢气与气体中残余的甲烷和CO以及由重整和变换反应产生的CO2分离。残余气体作为燃料经由再循环管线260再循环到重整器230，其中气体与由空气供应管线270供应的空气一起燃烧，以提供吸热重整反应所需的热量。氢气生产中产生的所有CO2作为N2、CO2和H2O以及一些NOx的混合物在重整器烟道气中被排出。
仍然参考图1，含有CO2的重整器烟道气被送到CO2捕获系统100的AGO(阳极气体氧化器)110，其中烟道气任选地与来自空气供应管线112的空气组合，如果需要将烟道气的氧含量增加到MCFC操作所需的水平。烟道气和空气被加热并被馈送到MCFC120的阴极124。天然气在经由天然气供应管线114被馈送到MCFC 120的阳极122之前被提供给预热器115。由于MCFC的独特性质，在MCFC正常电力产生期间，CO3 ＝从MCFC 120的阴极124转移到阳极122。这种转移从含有阴极进料的烟道气中除去CO2和O2，并且产生CO2含量相对低的阴极废气，从而减少CO2排放。转移到阳极122的CO3 ＝与阳极122中的氢气反应，形成H2O和CO2，同时发电。在碳捕获过程中，来自阳极122的出口流被例如蒸发器125冷却，并且进入变换反应器，使得出口流中的CO利用以下变换反应转化成氢气和CO2：
Figure BDA0003884099020000041
出口流然后被压缩机130压缩，然后被例如制冷机135冷却。经压缩和冷却的出口流然后被转移到CO2分离器140。在经压缩和冷却的出口流中，约60％至约90％的CO2冷凝为液体，并与含有氢气、任何未转化的CO、剩余的未冷凝CO2和甲烷的残余CO2捕获尾气分离。残余CO2捕获尾气经由再循环管线142部分再循环到阳极122，以用作MCFC 120中的燃料。残余CO2捕获尾气的剩余部分被送至AGO 110，以有助于防止惰性气体如氮气的积聚，并通过燃烧残余CO2捕获尾气中的剩余氢气来加热AGO 110中的气体。这种再循环具有增加从阳极废气中回收的CO2量的优点。
在图1的系统中，MCFC 120的尺寸设计部分地基于烟道气中要转移到阳极122的CO2的量(例如，烟道气中CO2的约70％至约90％)。因此，图1的系统配置实现起来可能很昂贵，并且可能产生比期望的更多的电力。
现在参考图2，显示了根据本公开的示例性实施例的包含CO2捕获系统300和SMR系统400的SMR-CO2捕获系统。与图1的系统相比，来自SMR系统400的烟道气不被引导至用于CO2捕获的MCFC，而是被排出，因为其通常具有低CO2含量。相反，SMR系统400被配置成使得来自SMR系统400中的PSA 450的PSA尾气与来自MCFC 320的阳极322的阳极废气直接混合，其中混合物可以被压缩和冷却，使得液化CO2可以从要被捕获的混合物中分离。以这种方式，MCFC 320的尺寸对来自SMR重整器430的烟道气具有非依赖性，使得MCFC 320的尺寸可经设计以仅提供CO2捕获系统300、SMR系统400或两者所需的电力，从而降低系统的总成本，同时仍提供足够的CO2捕获。
仍然参考图2，由蒸汽供应管线410供应的蒸汽和由天然气供应管线420供应的天然气被混合并被馈送至SMR系统400的SMR重整器430，用于将甲烷转化为氢气、CO2和CO。重整器流出物可以被输送到SMR系统400的变换组件，其中流出物可以被冷却并且大部分CO可以被变换成氢气。然后，经变换的气体经由变换气体管线440被送到PSA 450，其中氢气与气体中残余的甲烷和CO以及由重整和变换反应产生的CO2分离。代替在SMR重整器430中再循环PSA尾气中的残余气体作为燃料，如在图1的系统中，PSA尾气通过PSA尾气供应管线460被引导至CO2捕获系统300，以与MCFC 320的阳极322的阳极废气直接混合，用于随后的CO2捕获。以这种方式，MCFC 320的尺寸不受要转移到阳极322的PSA尾气中CO2的量的支配。因此，MCFC 320的尺寸可被设计成任何规格，例如，为CO2捕获系统300、SMR系统400或两者产生足够的电力。
仍然参考图2，阳极废气和PSA尾气的混合物然后被压缩机330压缩，然后被例如制冷机335冷却。经压缩和冷却的出口流然后被转移到CO2分离器340。在经压缩和冷却的出口流中，约60％至约90％的CO2冷凝为液体，并与含有氢气、任何未转化的CO、剩余的未冷凝CO2和甲烷的残余CO2捕获尾气分离。CO2捕获尾气流的一部分经由再循环管线342再循环至阳极322，以用作MCFC 320中的燃料，同时尾气的一小部分也被送至AGO 310，以有助于防止惰性气体如氮气的积聚，并通过燃烧残余CO2捕获尾气中的剩余氢气来加热AGO 310中的气体。
在图2的系统配置中，PSA尾气不再被引导回SMR重整器430用于随后的燃烧。因此，天然气可代替地用于向SMR重整器430提供燃料，并且如法规所允许的，含有相对少量CO2的所得烟道气可作为N2、CO2和H2O以及一些NOx的混合物排出。在这种配置中，通常从SMR排放的约50％至约60％的CO2被捕获。
根据图2所示的另一个代表性实施例，残余CO2捕获尾气的一部分也可以通过CO2捕获尾气供应管线344(由虚线/箭头表示)被引导回SMR重整器430。残余CO2捕获尾气的该部分可以用作SMR重整器430中的燃料，以减少所需天然气的量。如图2所示，残余CO2捕获尾气的该部分也可以再循环到PSA450，以增加PSA的H2生产，而不增加SMR重整器430的尺寸。根据另一个代表性实施例，MCFC 320的尺寸可经设计以仅使用残余CO2捕获尾气作为燃料，从而除了启动和扰乱操作之外，消除了在MCFC 320处对天然气的需求。
现在参照图3，显示了根据本公开的另一个示例性实施例的包含CO2捕获系统500和SMR系统600的SMR-CO2捕获系统。与图2的系统相比，来自SMR系统600的烟道气沿着烟道气供应管线635被引导至MCFC用于CO2捕获，而不是被排出。此外，来自SMR系统600的PSA650的尾气沿着PSA尾气供应管线660被引导，以与来自MCFC 520的阳极522的阳极废气直接混合，用于捕获CO2。以这种方式，MCFC 520的尺寸可经设计小于典型的SMR-CO2捕获系统(如图1的系统)，因为要被MCFC 520捕获的含有通常存在于烟道气中的约50％至60％的CO2的尾气转而被引导至MCFC的阳极废气。因此，与图2的系统相比，此示例性系统可以提供相对较高的CO2捕获，同时与图1的常规系统相比，仍然降低了总成本。
根据另一代表性实施例，MCFC 520的尺寸可配置成补偿由CO2捕获系统500和SMR系统600消耗的功率。在这种配置中，相对大百分比的正常排放的CO2(例如，约60％至约70％)仍将被系统捕获，但是资本成本将显著降低，并且将消除或减少向第三方输出电力的需要。
现在参考图4，显示了根据本公开的另一个示例性实施例的包含CO2捕获系统700和SMR系统800的SMR-CO2捕获系统。如图4所示，来自SMR系统800的烟道气沿着烟道气供应管线835被引导至MCFC 720的阴极724，并且来自SMR系统800的PSA 850的尾气沿着PSA尾气供应管线860被引导以与来自MCFC 720的阳极722的阳极废气直接混合，用于捕获CO2。来自阳极722的含有氢气和一氧化碳(例如，约30％)以及少量甲烷的未使用的燃料可以沿着CO2捕获尾气供应管线744从CO2捕获尾气被引导至PSA 850，以增加系统的氢气生产。在一些实施例中，如果例如PSA 850不具有额外进料所需的容量，则CO2捕获尾气可被送至与PSA 850分离的PSA。以这种方式，此示例性系统可以提供相对高的CO2捕获和增加的氢气生产，同时降低总成本。
现在参考图5，显示了根据本公开的另一个示例性实施例的包含CO2捕获系统900和SMR系统1000的SMR-CO2捕获系统。如图5所示，从外部来源接收功率，而不是使用MCFC来为CO2捕获系统900提供电力。根据各种示例性实施例，外部电源可以是现有的发电厂、公用电网和/或可再生能源如太阳能或风能。来自SMR系统1000的PSA 1050的尾气被压缩机930压缩并被制冷机935冷却，使得液化的CO2可以与用于捕获CO2的气体分离。CO2捕获尾气可以沿着PSA尾气供应管线942被引导至PSA 1050和/或SMR系统1000的重整器1030，以增加系统的氢气生产并有助于防止惰性气体在SMR系统1000中积聚。以这种方式，与其他CO2捕获系统相比，此示例性系统可以提供用于捕获CO2的更低成本的选择。然而，应当理解，当估计利用这种配置的CO2减少量时，应当考虑由外部电源释放的潜在CO2量。
参考图6，根据示例性实施例显示了实现上述系统的方法。该示例性方法包含混合步骤1101，在该步骤中将来自SMR系统的PSA的尾气与来自MCFC阳极的阳极废气混合；压缩步骤1103，在该压缩步骤中，由压缩机压缩混合气体；冷却步骤1105，在该压缩步骤中，例如由制冷机冷却气体，使得大部分CO2作为液体输出；分离步骤1107，在该分离步骤中，通过CO2分离器将液态CO2与残余气体分离；收集步骤1109，在该收集步骤中，收集液态CO2以隔离或用于其他目的；以及再循环步骤1111，在该再循环步骤中，将残余气体再循环用于阳极气体氧化器、MCFC的阳极、作为重整器的燃料源的SMR和PSA中的一个或多个中以产生氢气。在某些实施例中，混合步骤1101被省略，并且SMR尾气在不与阳极废气混合的情况下被处理，特别是当使用外部电源代替MCFC时。
根据代表性实施例，来自SMR系统中的PSA的尾气与来自MCFC阳极的阳极废气直接混合，其中混合物可以被压缩，并且其温度被制冷机降低，使得液化CO2可以从混合物中分离出来以被捕获。与一些常规的SMR-CO2捕获系统相比，来自SMR系统的重整器的燃烧器的CO2，即来自SMR系统的烟道气，不被引导至MCFC用于CO2捕获。以这种方式，MCFC的尺寸对来自SMR重整器的烟道气具有非依赖性，而是由从PSA尾气中捕获的CO2控制，从而降低系统的总成本，同时仍然提供CO2捕获。
根据另一个代表性实施例，来自SMR系统的烟道气被送到MCFC的阴极，并且来自SMR系统的PSA的尾气与来自MCFC阳极的阳极废气直接混合，用于捕获CO2。以这种方式，MCFC的尺寸可以经设计小于典型的SMR-CO2捕获系统，因为要被MCFC捕获的含有通常存在于烟道气中的约50％至60％的CO2的尾气转而被引导至MCFC的阳极废气。因此，此示例性系统可以提供相对高的CO2捕获，同时降低系统的总成本。
根据另一个代表性实施例，来自SMR系统的烟道气被送到MCFC的阴极，并且来自SMR系统的PSA的尾气与来自MCFC阳极的阳极废气直接混合，用于捕获CO2。来自MCFC阳极，除去CO2后，且含有氢气和一氧化碳(CO)的一部分未使用的燃料可以从CO2捕获尾气中被引导至PSA以增加系统的氢气生产。以这种方式，此示例性系统可以提供相对高的CO2捕获和增加的氢气生产，同时降低系统的总成本。
根据另一个代表性实施例，来自SMR系统的PSA的尾气被压缩，并且其温度被使用外部电源(和，在使用吸收式制冷机的情况下，外部热源)的制冷机降低，使得液化CO2可以从用于捕获CO2的气体中分离。来自含有氢气、CO、残余CO2和其他不可冷凝气体的CO2捕获尾气的未使用的燃料可以被引导至PSA以增加系统的氢气生产，和/或被引导至SMR系统的重整器，有助于防止SMR系统中惰性气体的积聚。以这种方式，与一些常规SMR-CO2捕获系统相比，此示例性系统可以提供用于捕获CO2的更低成本的选择。
本文公开了增强的SMR-CO2捕获系统的各种实施例，与使用MCFC的一些常规CO2捕获系统相比，该系统能够以更高效和成本有效的方式捕获CO2。本文公开的各种实施例可以能够增加捕获的CO2的量，提高捕获CO2的效率，增加产生的氢气的量，和/或降低与捕获CO2相关联的成本。
如本文中所使用，术语“大约”、“约”、“大体上”和类似术语旨在具有与由本公开的主题所属的领域的普通技术人员常用和公认的用法相一致的广泛含义。对本公开进行审查的本领域技术人员应理解，这些术语旨在允许对所描述和所要求的某些特征进行描述，而不将这些特征的范围限于所提供的精确数值范围。因此，这些术语应解释为指示对所描述和所要求的主题的非实质性的或无关紧要的修改或改变被视为处于所附权利要求书中所述的本发明的范围内。
如本文中所使用，术语“耦合”、“连接”等意指两个构件直接或间接地彼此接合。这种接合可以是静止的(例如，永久的)或可移动的(例如，可移除的或可释放的)。这种接合可以通过两个构件或两个构件和任何附加的中间构件彼此整体形成为单个整体来实现，或者通过两个构件或两个构件和任何附加的中间构件彼此附接来实现。
本文中对元件的位置(例如，“顶部”、“底部”、“上方”、“下方”等)的引用仅用于描述附图中各个元件的定向。应注意，根据其它示例性实施例，各种元件的定向可以不同，并且此类变化旨在被本公开所涵盖。
重要的是应注意，各种示例性实施例的构造和布置仅是说明性的。虽然在本公开中仅详细描述了几个实施例，但是审阅本公开的本领域技术人员将容易理解，在实质上不脱离本文所述主题的新颖教导和优点的情况下，许多修改是可能的(例如，各种元件的大小、尺寸、结构、形状和比例、参数值、安装布置、材料的使用、颜色、定向等的变化)。例如，示出为整体形成的元件可以由多个部分或元件构成，元件的位置可以颠倒或以其它方式变化，并且离散元件的性质或数量或位置可以改变或变化。任何过程或方法步骤的次序或顺序可根据替代实施例变化或再定顺序。还可以在各种示例性实施例的设计、操作条件和布置中进行其它替换、修改、改变和省略，而不脱离本发明的范围。例如，热回收热交换器可被进一步优化。

Claims (15)

1.一种用于从蒸汽甲烷重整器系统捕获二氧化碳的系统，所述用于捕获二氧化碳的系统包括：
压缩机，其被配置成压缩从所述蒸汽甲烷重整器系统接收的尾气；
制冷机，其被配置成冷却所述尾气；和
二氧化碳分离器，其被配置成将所述尾气分离成液化二氧化碳和残余尾气。
2.根据权利要求1所述的系统，其进一步包括：
熔融碳酸盐燃料电池，其包括阳极和阴极；
其中所述尾气在被压缩和冷却之前与来自所述阳极的阳极废气混合。
3.根据权利要求2所述的系统，其中残余尾气的第一部分被引导至阳极气体氧化器，并且所述残余尾气的第二部分被引导至所述阳极。
4.根据权利要求1至3中任一项所述的系统，其中所述蒸汽甲烷重整器系统包括变压吸附系统，所述变压吸附系统被配置成产生所述尾气。
5.根据权利要求1或2中任一项所述的系统，其中所述残余尾气的一部分被引导至所述蒸汽甲烷重整器系统中的变压吸附系统。
6.根据权利要求1或2中任一项所述的系统，其中所述残余尾气的一部分被引导至所述蒸汽甲烷重整器系统以作为燃料燃烧。
7.根据权利要求1或2中任一项所述的系统，其中所述残余尾气的第一部分被引导至所述蒸汽甲烷重整器系统以作为燃料燃烧，并且所述残余尾气的第二部分被引导至所述蒸汽甲烷重整器系统中的变压吸附系统。
8.根据权利要求3所述的系统，其中所述残余尾气的第三部分被引导至所述蒸汽甲烷重整器系统中的变压吸附系统。
9.根据权利要求3所述的系统，其中所述残余尾气的第三部分被引导至所述蒸汽甲烷重整器系统以作为燃料燃烧。
10.根据权利要求3所述的系统，其中所述残余尾气的第三部分被引导至所述蒸汽甲烷重整器系统作为燃料燃烧，并且所述残余尾气的第四部分被引导至所述蒸汽甲烷重整器系统中的变压吸附系统。
11.根据权利要求2或3中任一项所述的系统，其中来自所述蒸汽甲烷重整器系统中的重整器的烟道气被引导至阳极气体氧化器。
12.根据权利要求2或3中任一项所述的系统，其中来自所述蒸汽甲烷重整器系统中的重整器的烟道气被引导至阳极气体氧化器，并且所述残余尾气的一部分被引导至所述蒸汽甲烷重整器系统中的变压吸附系统。
13.根据权利要求2或3中任一项所述的系统，其中所述熔融碳酸盐燃料电池的尺寸经设计为所述用于捕获二氧化碳的系统或所述蒸汽甲烷重整器系统中的至少一个供电。
14.根据权利要求2或3中任一项所述的系统，其中残余气体混合物的一部分被引导至所述蒸汽甲烷重整器系统外的第二变压吸附系统。
15.一种从根据前述权利要求中任一项所述的蒸汽甲烷重整器系统捕获二氧化碳的方法。
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