CN102612549A - 高能发电厂燃料以及co或co2封存方法 - Google Patents

高能发电厂燃料以及co或co2封存方法 Download PDF

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CN102612549A
CN102612549A CN201080038972XA CN201080038972A CN102612549A CN 102612549 A CN102612549 A CN 102612549A CN 201080038972X A CN201080038972X A CN 201080038972XA CN 201080038972 A CN201080038972 A CN 201080038972A CN 102612549 A CN102612549 A CN 102612549A
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hydrogen
melting tank
plasma body
fuel
body melting
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詹姆斯·查尔斯·朱拉尼奇
托马斯·R·朱拉尼奇
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Priority claimed from PCT/US2009/003934 external-priority patent/WO2010002469A1/en
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Abstract

生产集中于约C9的高的氢与碳的比的燃料的系统处理从制造厂过程产生的废气流。废气流在费托反应器中被加工，且含有被封存的CO和/或CO2，且可以是全部烟道的废气流。费托反应器为颗粒型反应器、泡沫反应器或α氧化铝泡沫反应器。等离子体室产生用于在费托反应器中反应的H2。废气流的一部分在等离子体室中消耗。藻类反应器将封存的CO2转化成O2。藻类暴露于废气流，以从废气流提取营养物并且增强其生长。等离子体室在其高温区域接收被还原成其元素状态的CO或CO2。产品流和燃料被冷凝和分离且作为燃料被再烧。

Description

高能发电厂燃料以及CO或CO2封存方法
与其他申请关系
本申请要求于2009年11月19日提交的美国专利临时申请序列号61/281,668，确认号5332(授权的外国申请许可)和于2009年7月3日提交的美国临时专利申请序列号61/270,035，确认号9380(授权的外国申请许可)的申请日的权益，且是2009年7月1日提交的共同未决的国际专利申请序列号PCT/US2009/003934的部分继续申请，其要求2008年7月1日提交的美国临时专利申请序列号61/133,596的申请日的权益；且其还要求2008年11月19日提交的美国临时专利申请序列号61/199,837、2008年11月19日提交的61/199,761、2008年12月10日提交的61/201,464、2008年11月19日提交的61/199,760、2008年11月19日提交的61/199,828和2009年2月24日提交的61/208,483的申请日的权益，所有这些申请的公开内容通过引用并入本文。
背景技术
发明领域
本发明大体涉及用于产生高能量密度的清洁燃烧燃料的系统，所述产生高能量密度的清洁燃烧燃料是作为其自身过程的或是同时具有处理发电厂或其他释放CO或CO2的工业过程的废气输出的另外的益处。在本发明中，当使用碳中性或碳负性原料，例如城市固体废物、生物质和/或藻类来减少温室气体排放至大气时，也产生高能量密度的可再生燃料。
现有技术描述
全世界关注全球气候变化。以前，这称为“全球变暖”，但目前想法引导人类更多地将其看作是全球气候变化。许多人觉得人类，且更具体地温室气体，是造成全球气候变化的重要部分的原因。
存在对比用于处理可再生的或其他的反应物、来自发电厂或其他制造过程的废气流的常规系统更能量有效、更成本有效和尺寸更小的CO2封存系统或可再生能源产生系统的需求。
发明概述
根据本发明的第一方法方面，提供了一种大规模制造燃料的方法。在本发明的该方法方面的有利的实施方式中，燃料可集中于约C9的平均碳数和约3的氢比。该方法包括以下步骤：
将废弃材料供应到等离子体熔化器；
将电能供应到等离子体熔化器；
将水供应到等离子体熔化器；
从等离子体熔化器提取合成气；
从合成气提取氢；以及
由在提取氢的步骤中产生的氢形成燃料。
在一个实施方式中，将水供应到等离子体熔化器的步骤包括将蒸汽供应到等离子体熔化器的步骤。将废弃材料供应到等离子体熔化器的步骤包括将城市废物供应到等离子体熔化器的步骤。另外，将废弃材料供应到等离子体熔化器的步骤包括将城市固体废物供应到等离子体熔化器的步骤，且将废弃材料供应到等离子体熔化器的步骤包括将生物质供应到等离子体熔化器的步骤，生物质是为了供应到等离子体熔化器的目的而专门培育的，且在一些实施方式中为藻类。
在本发明的另外的实施方式中，从合成气提取氢的步骤包括以下步骤：使合成气经历水煤气变换过程以形成氢和二氧化碳的混合物，以及从氢和二氧化碳的混合物提取氢。在一些实施方式中，从氢和二氧化碳的混合物提取氢的步骤包括使氢和二氧化碳混合物的混合物经历变压吸附过程的步骤。在一些实施方式中，从氢和二氧化碳的混合物提取氢的步骤包括使氢和二氧化碳混合物的混合物经历分子筛或膜的步骤。另外，从氢和二氧化碳的混合物提取氢的步骤包括使氢和二氧化碳的混合物经历乙醇胺水溶液的步骤。在另外的实施方式中，在进行使合成气经历水煤气变换过程以形成氢和二氧化碳的混合物的步骤之前，提供预处理等离子体熔化器的输出以进行合成气的清洁的步骤。另外，在本发明的一些实施方式中，在进行使合成气经历水煤气变换过程以形成氢和二氧化碳的混合物的步骤之前，提供预处理等离子体熔化器的输出以进行合成气的分离的步骤。
在本发明的另外的实施方式中，由在提取氢的步骤中产生的氢形成燃料的步骤包括使氢经历颗粒型(pellet style)费托催化过程的步骤。在进行由在提取氢的步骤中产生的氢形成燃料的步骤之前，提供通过调节费托催化过程中的一氧化碳和氢的摩尔比来优化燃料的生产的另外的步骤。此外，调节费托催化过程中的一氧化碳和氢的摩尔比的步骤包括将氢和一氧化碳的混合物供应到费托催化过程的步骤。在一些实施方式中，该步骤包括转移通过等离子体熔化器产生的氢和一氧化碳的一部分的步骤，该步骤在进行清洁通过等离子体熔化器产生的氢和一氧化碳的步骤之后进行。
在本发明的另外的实施方式中，还提供从等离子体熔化器提取熔渣的步骤。等离子体熔化器以热解模式操作。
根据本发明的系统方面，提供了一种用于处理由发电厂排出的废气流的系统，该系统包括在费托催化剂反应器中处理废气流的步骤，费托催化剂反应器被优化以产生具有约3的氢比的平均约C9的燃料。在本发明的单独的实施方式中，废气流含有CO或CO2。另外，在一些实施方式中，废气流为全部烟道的废气流(full stack exhaust stream)。在一些实施方式中，费托催化剂反应器为颗粒型甲醇反应器，其为泡沫反应器或α-氧化铝泡沫反应器。
在本发明的一些实施方式中，另外提供了用于产生用于在甲醇反应器中反应的H2的等离子体室。由发电厂排出的废气流的一部分在等离子体室中被消耗。在另外的实施方式中，提供了用于产生H2的流化床。在一些实施方式中，采用用于产生H2的蒸汽过程，且在一些这样的实施方式中，提供用于产生H2的蒸汽重整过程。在一些实施方式中，使用由等离子体废气中的显热驱动的二级蒸汽重整过程，以产生另外量的H2。
在本发明的一些实施方式中，采用水解过程以产生H2。在另外的实施方式中，还提供了藻类反应器，以将封存的CO2转化成O2。藻类暴露于发电厂的废气流，以从废气流提取营养物来增强藻类的生长。
在一些实施方式中，等离子体室在其高温区域接收被还原成CO的元素状态的CO。在另外的实施方式中，废气流和甲醇被冷却到低于65℃的温度，以使液体燃料沉淀出来。燃料作为能源被再烧。
根据本发明的另外的系统方面，提供了一种用于处理由发电厂排出的废气流的系统。该系统包括等离子体室，其用于在其高温区域接收被还原成CO的元素状态的CO。
在本发明的具体的示例性实施方式的方法方面，提供了在颗粒型、泡沫型或α-氧化铝泡沫型(alpha alumina oxide foam style)费托催化剂中处理原料和废气流的步骤。已开发了具有具体的α型和使其产物输出集中于约C9值的操作条件的催化剂。这种有利的设计可平衡(leverage)其高的冷凝温度，尤其当与泡沫型费托催化剂的有利的高流动、高转化性质组合时。平均C9化合物将在126℃下冷凝。这种高温允许该过程以能量有效的方式捕获CO或CO2。CH比还约为1∶3.4，这形成非常清洁的燃烧燃料。
本发明大体涉及用于封存来自某过程或废气流的CO2和/或CO的有效的方法和系统。然后CO或CO2转化成当前高能量密度的燃料并且用作可输送的燃料或在需要热量的制造过程中燃烧。当使用碳中性或碳负性原料时，例如生物质、城市固体废物和藻类，显著减少温室气体排放至大气。
在另外的实施方式中，提供了等离子体室，其用于在其高温区域接收CO2，CO2从而被变换或还原。
附图简述
通过阅读下面的详述，连同附图，将有助于理解本发明，其中：
图1是排出温室气体废气的多个发电厂和工业过程的简化的示意图，所述温室气体废气在改进的费托反应器和燃料冷凝系统中被处理；
图2是图1示出的系统的进一步的实施方式的简化的示意图，其中多个发电厂和工业过程排出温室气体废气，该温室气体废气在费托反应器和燃料冷凝系统中被处理；和
图3是不使用工业废气流作为原料的燃料制造系统的简化的示意图。详述
图1示出了多个工厂，尤其是常规的发电厂101、O2注入的煤厂102、产生CO2的工厂103(氨、H2、环氧乙烷和天然气)。燃煤常规发电厂101每千瓦时(“kW-h”)释放约两磅CO2。清洁竞争者(cleaner competitor)是常规的天然气发电厂。其看上去基本上与常规的燃煤发电厂相同，然而每千瓦时将仅排放约1.3磅CO2。所有这些工厂为全球温室气体存量的主要贡献者。
工厂102、103和104示出每个工厂废气体积不断增大的CO2浓度。然而，由发电厂101排放的每废气体积中的CO2的低的比使得CO2的封存昂贵且困难。一些发电厂系统已证实能够实现便宜和容易的CO2封存，但它们是资本和能量密集的。在CO或CO2被封存后，其仍必须被保存在常规的封存系统(未示出)中。此外，储存CO2是昂贵的和有争议的。然而，本发明能够在现场处理CO2，并且储存CO2不是必须的。当使用碳中性或碳负性原料，例如藻类时，这是尤其可行的。在藻类反应器，例如藻类反应器137(图2)中，后加工CO2能够进行碳负性操作。
再次参考图1，工厂废气流106被输送到等离子体室130，然后至费托反应器118。通常小的百分比的流被供给到等离子体反应器130。在本发明的一些实施方式中，费托反应器118为泡沫或氧化铝泡沫反应器，但可以是将CO2转化成平均约C9的碳链的任何结构。等离子体室130用作氢发生器。在实施本发明时，可使用任何合适的氢发生器。然而，在现存技术中，等离子体反应器是最有效的一种，因此在本发明的这一实施方式中示出。在其他实施方式中，还可使用常规的气化器(未示出)或流化床(未示出)。
等离子体室130可由若干原料105中的任何一个供应。这些包括化石燃料例如煤、有害废物、医疗废物、放射性废物、城市废物，或碳负性燃料例如藻类。在本发明的这一具体示例的实施方式中，等离子体室将排出主要由处于约1200℃的温度的合成气组成的产品气体。该流含有在流动流110被提取的相当多的显热能量，以使碳为有效的电能或蒸汽能。在图1示出的本发明的具体的示例性实施方式中，蒸汽重整过程135直接在高温等离子体流动流中或间接地在闭合环路热传递系统中操作，以产生另外的H2。
在碳入口107提供的碳，从常规来源如甲醇(未示出)或从非常规来源如半消耗的粉煤灰(semi-spent fly ash)(未示出)获得。然后合成气110通过变压吸附器132和134来处理，以从CO分离H2。在实施本发明时，任何常规形式的分离体系，例如膜/分子筛(未示出)、水溶液(未示出)、变压吸附器(未示出)等，可用于本发明的其他实施方式中，以分离出H2。然后将H2输送到费托催化剂反应器118，在该实施方式中，H2与工厂废气流106合并。
在本发明的单独的实施方式中，费托催化剂反应器118可以是常规的反应器或在理想化应用中其可以是泡沫反应器或α氧化铝泡沫反应器。α氧化铝泡沫反应器比常规的反应器容纳明显更大的流速，在实施本发明时，这种增大的流动是有利的。
工厂废气106和H2在费托催化剂反应器118中进行放热反应。在本发明的这一实施方式中，所产生的热提取为蒸汽117，蒸汽117可用于本文公开的过程的许多部分，例如在等离子体反应器130中(用于输送的连接件未示出)，蒸汽重整室135(用于输送的连接件未示出)，或作为城市蒸汽。在该实施方式中，然后将费托催化剂反应器出口107的合并的燃料和废气递送到热交换器136。在该实施方式中，通过使用冷水，热交换器136使气体混合物的温度低于65℃，这在一个大气压的压力下在液体高能燃料出口112处沉淀出液体形式的产物燃料。出口112处的液体燃料与CO和或CO2耗尽的工厂废气分离，在本发明的这一具体的示例性实施方式中，CO和或CO2耗尽的工厂废气然后从CO2还原废气出口111排到大气。液体高能燃料可被销售或再循环到任何设备，以产生热。
来自合成气的CO，在本发明的这一实施方式中在CO产物出口113可得到，可作为产品被销售，或在本发明的一些实施方式中，可被再引入到等离子体室130的高温区域(未示出)，等离子体室130可在约7000℃下操作，以还原成元素形式的碳和氧。在一些实施方式中，可通过微波能量、磁等离子体成形、UHF能量、电晕放电或激光能量(未示出)来辅助该过程。另外，可将CO再引入到工厂，以作为燃料燃烧，产生约323BTU/cuft。
图2是图1示出的系统的另外的实施方式的简化的示意图，其中多个发电厂排出在费托催化剂反应器和燃料冷凝系统中被处理的温室气体废气。简单示出已在前面讨论的结构元件。在该图中，示出本方法的另外的实例，其中提供布置在产生合成气的等离子体室130的下游的气体变换反应142。在图2的实施方式中，任选地可采用蒸汽重整系统135(图1)。在本发明的这一实施方式中，通过变压吸附器132和134的操作已分离的CO2被藻类反应器137处理。在一些实施方式中，藻类反应器137是光反应器或混合池。另外，工厂废气106的一部分被藻类处理，以提供加速生长的元素，例如氮。在本发明的其他实施方式中，可使用除变压吸附器外的任何常规的过程，来从变换的合成气分离CO2。
在一些情况下，可能需要在无工厂废气流入口的偏远位置制造高能燃料，然后被输送到工厂，用于消耗。在图3中示出这种实例。如果使用生物质、城市固体废物或其他可再生组的原料的组合，本发明是尤其相关的。这将使得消耗燃料的工厂每燃烧的燃料拥有一定百分比的可再生信用(renewable credit)。废气将还被认为具有适当量的碳中性信用。在这种情况下，通过本发明实现前述和其他目的，这包括以下步骤：
将废弃材料供应到等离子体熔化器；
将电能供应到等离子体熔化器；
将水供应到等离子体熔化器；
从等离子体熔化器提取合成气；
从合成气提取氢；以及
由在提取氢的步骤中产生的氢形成集中于约C9的高的氢/碳比的燃料。
在本发明的一个实施方式中，将水供应到等离子熔化器的步骤包括将蒸汽供应到等离子体熔化器的步骤。
在本发明的有利的实施方式中，供应到等离子体熔化器的废弃材料是城市废物。在其他实施方式中，废弃材料是城市固体废物，且在其他实施方式中，废弃材料是生物质。在废弃材料是生物质的一些实施方式中，生物质是专门培育的。
在本发明的一个实施方式中，从合成气提取氢的步骤包括但不限于以下步骤：
使合成气经历水煤气变换过程，以形成氢和二氧化碳的混合物；以及
将一部分CO2流引导到藻类生物反应器或池或在等离子体室中被再处理。
水煤气变换过程主要用于从氢和二氧化碳的产物混合物提取另外的氢。
在另外的实施方式中，从氢和二氧化碳的混合物提取氢的步骤包括但不限于使氢和二氧化碳混合物的混合物经历变压吸附过程的步骤。在一些实施方式中，从氢和二氧化碳的混合物提取氢的步骤包括但不限于使氢和二氧化碳混合物的混合物经历分子筛或膜的步骤。在另外的实施方式中，从氢和二氧化碳的混合物提取氢的步骤包括但不限于使氢和二氧化碳混合物的混合物经历乙醇胺水溶液的步骤。在又一个实施方式中，在进行使合成气经历水煤气变换过程以形成氢和二氧化碳的混合物之前，提供预处理等离子体熔化器的输出，以对合成气进行清洁和分离的步骤。
根据本发明的有利的实施方式中，由在提取氢的步骤中产生的氢形成产物燃料的步骤包括但不限于使氢经历费托催化过程的步骤。在一个实施方式中，在进行由在提取氢的步骤中产生的氢形成燃料的步骤之前，提供通过调节费托催化过程中的CO和氢的摩尔比来优化燃料的生产的另外的步骤。调节费托催化过程中的CO和氢的摩尔比的步骤包括但不限于将氢和一氧化碳的混合物供应到费托催化过程的步骤。
在本发明的有利的实施方式中，将氢和一氧化碳的混合物供应到费托催化过程的步骤包括但不限于转移通过等离子体熔化器产生的氢和一氧化碳的一部分的步骤。在一个实施方式中，在进行清洁通过等离子体熔化器产生的氢和一氧化碳的步骤之后，进行转移通过等离子体熔化器产生的氢和一氧化碳的一部分的步骤。
在本发明的有利的实施方式中，提供从等离子体熔化器提取炉渣的步骤。在另外的实施方式中，将废弃材料供应到等离子体熔化器的步骤包括但不限于将城市废物供应到等离子体熔化器的步骤。
图3是本发明的具体的示例性实施方式的简单的功能块和示意图。如在该图中示出，燃料产生系统300接收化石燃料、城市废物、或可布置在等离子体熔化器312中的专门培育的生物质310。在实施本发明的一些实施方式时，以热解方式(例如，缺氧)操作该过程。在本发明的该具体的示例性实施方式中以蒸汽315的形式使用的水，被输送到等离子体熔化器312，以促进氢和等离子体的产生。同样，电力316被递送到等离子体熔化器312。富氢合成气318在等离子体熔化器312的输出部(未具体示出)产生，炉渣314也同样，炉渣314随后被除去。
在本发明的一些应用中，炉渣314作为建筑材料被销售，且可呈现石纤维、再生金属和硅酸盐的形式，例如建筑块(building block)。在本发明的一些实施方式中，通过添加小量的焦炭或其他添加剂(未示出)，BTU含量、等离子体产生和炉渣产生还可以“脱硫(sweetened)”。
在本发明的一些实施方式中，在预处理步骤320中，合成气被冷却和清洁，且可被分离。在水煤气变换反应322的输出部，CO被处理离开清洁的合成气。可认为随后被汽提的废弃二氧化碳326不是温室气体碳基的添加物。这是由于它可以以其整体从再生能源和可再生的能源获得。例如，在本发明的这一实施方式中，能源可以主要是城市废物310。
在一些实施方式中，二氧化碳再循环到等离子体熔化器312，并且被再处理成CO和氢。在处理步骤324中，使用变压吸附过程、分子筛/膜、乙醇胺水溶液或其他过程，以分离出二氧化碳326。可将该二氧化碳的一部分引导到藻类生物反应器335或再次引导到等离子体熔化器310，用于再处理。藻类可被再次用作等离子体转化器310的原料。来自处理步骤324的氢输送到优化的费托催化剂过程328。
在本发明的这一具体的示例性实施方式中，通过预处理步骤320获得的CO和氢的一部分通过流量控制阀330被转移，并供应到费托催化剂过程328。应用该转移的流，以实现适当CO和氢的摩尔比，从而优化燃料的生产。
预处理步骤320、水煤气变换反应322和费托催化剂过程328产生热，在本发明的一些实施方式中，产生的热被用于将蒸汽供应到等离子体熔化器312，或者涡轮发生器(未示出)，或利用热的任何其他过程(未示出)。
虽然已通过具体的实施方式和应用描述了本发明，但根据本教导，本领域技术人员可产生另外的实施方式，而不超出本文要求保护的本发明的范围或偏离本文要求保护的本发明的精神。因此，应理解本公开内容中的附图和描述被提供，以促进对本发明的理解，且不应理解为限制本发明的范围。

Claims (40)

1.一种大规模制造燃料的方法，所述燃料集中于约C9的平均碳数和约3的氢比，所述方法具有以下步骤：
将废弃材料供应到等离子体熔化器；
将电能供应到所述等离子体熔化器；
将水供应到所述等离子体熔化器；
从所述等离子体熔化器提取合成气；
从所述合成气提取氢；以及
由在所述提取氢的步骤中产生的氢形成燃料。
2.如权利要求1所述的方法，其中所述将水供应到所述等离子体熔化器的步骤包括将蒸汽供应到所述等离子体熔化器的步骤。
3.如权利要求1所述的方法，其中所述将废弃材料供应到所述等离子体熔化器的步骤包括将城市废物供应到所述等离子体熔化器的步骤。
4.如权利要求1所述的方法，其中所述将废弃材料供应到所述等离子体熔化器的步骤包括将城市固体废物供应到所述等离子体熔化器的步骤。
5.如权利要求1所述的方法，其中所述将废弃材料供应到所述等离子体熔化器的步骤包括将生物质供应到所述等离子体熔化器的步骤。
6.如权利要求5所述的方法，其中所述生物质是专门培育用于供应到等离子体熔化器的，例如藻类。
7.如权利要求1所述的方法，其中所述从合成气提取氢的步骤包括以下步骤：
使所述合成气经历水煤气变换过程以形成氢和二氧化碳的混合物，以及
从所述氢和二氧化碳的混合物提取氢。
8.如权利要求7所述的方法，其中所述从氢和二氧化碳的混合物提取氢的步骤包括使所述氢和二氧化碳混合物的混合物经历变压吸附过程的步骤。
9.如权利要求7所述的方法，其中所述从氢和二氧化碳的混合物提取氢的步骤包括使所述氢和二氧化碳混合物的混合物经历分子筛或膜的步骤。
10.如权利要求7所述的方法，其中所述从氢和二氧化碳的混合物提取氢的步骤包括使所述氢和二氧化碳的混合物经历乙醇胺水溶液的步骤。
11.如权利要求7所述的方法，其中在进行所述使合成气经历水煤气变换过程以形成氢和二氧化碳的混合物的步骤之前，提供预处理所述等离子体熔化器的输出以对所述合成气进行清洁的步骤。
12.如权利要求7所述的方法，其中在进行所述使合成气经历水煤气变换过程以形成氢和二氧化碳的混合物的步骤之前，提供预处理所述等离子体熔化器的输出以进行所述合成气的分离的步骤。
13.如权利要求1所述的方法，其中所述由在所述提取氢的步骤中产生的氢形成燃料的步骤包括使氢经历颗粒型费托催化过程的步骤。
14.如权利要求13所述的方法，其中在进行所述由在所述提取氢的步骤中产生的氢形成燃料的步骤之前，提供通过调节所述费托催化过程中的一氧化碳和氢的摩尔比来优化燃料的生产的另外的步骤。
15.如权利要求14所述的方法，其中所述调节所述费托催化过程中的一氧化碳和氢的摩尔比的步骤包括将氢和一氧化碳的混合物供应到所述费托催化过程的步骤。
16.如权利要求15所述的方法，其中所述将氢和一氧化碳的混合物供应到费托过程的步骤包括转移通过所述等离子体熔化器产生的氢和一氧化碳的一部分的步骤。
17.如权利要求16所述的方法，其中所述转移通过所述等离子体熔化器产生的氢和一氧化碳的一部分的步骤是在进行清洁通过所述等离子体熔化器产生的氢和一氧化碳的步骤之后进行。
18.如权利要求1所述的方法，其中还提供了从所述等离子体熔化器提取熔渣的步骤。
19.如权利要求1所述的方法，其中所述等离子体熔化器以热解模式操作。
20.如权利要求1所述的方法，其中所述由在所述提取氢的步骤中产生的氢形成燃料的步骤包括使氢经历α氧化铝泡沫型费托催化过程的步骤。
21.如权利要求1所述的方法，其中所述由在所述提取氢的步骤中产生的氢形成燃料的步骤包括使氢经历泡沫型费托催化过程的步骤。
22.一种处理由发电厂排出的废气流的系统，所述系统包括在费托催化剂反应器中处理废气流的步骤，所述费托催化剂反应器被优化以产生具有约3的氢比的平均约C9的燃料。
23.如权利要求22所述的系统，其中所述废气流含有CO。
24.如权利要求22所述的系统，其中所述废气流含有CO2。
25.如权利要求22所述的系统，其中所述废气流为全部烟道的废气流。
26.如权利要求22所述的系统，其中所述费托催化剂反应器为颗粒型甲醇反应器。
27.如权利要求22所述的系统，其中所述甲醇反应器为泡沫反应器或α氧化铝泡沫反应器。
28.如权利要求22所述的系统，其中还提供了用于产生用于在所述甲醇反应器中反应的H2的等离子体室。
29.如权利要求28所述的系统，其中由所述发电厂排出的废气流的一部分在所述等离子体室中被消耗。
30.如权利要求22所述的系统，其中还提供了用于产生H2的流化床。
31.如权利要求22所述的系统，其中还提供了用于产生H2的蒸汽过程。
32.如权利要求22所述的系统，其中还提供了用于产生H2的蒸汽重整过程。
33.如权利要求32所述的系统，其中还提供了用于产生另外量的H2的通过等离子体废气中的显热驱动的第二蒸汽重整过程。
34.如权利要求22所述的系统，其中还提供了用于产生H2的水解过程。
35.如权利要求22所述的系统，其中还提供了用于将封存的CO2转化成O2的藻类反应器。
36.如权利要求22所述的系统，其中藻类暴露于所述发电厂的废气流，以从所述废气流提取营养物来增强藻类的生长。
37.如权利要求22所述的系统，其中还提供了等离子体室，用于在其高温区域接收CO，该CO被还原成其元素状态。
38.如权利要求22所述的系统，其中所述废气流和甲醇被冷却到低于65℃的温度，以使液体燃料沉淀出来。
39.如权利要求22所述的系统，其中所述燃料作为能源被再烧。
40.一种处理由发电厂排出的废气流的系统，所述系统包括等离子体室，用于在其高温区域接收CO，该CO被还原成其元素状态。
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