CN102695935A - 用于从剩余流体生产至少一种富氩流体和至少一种富氧流体的方法和装置 - Google Patents

用于从剩余流体生产至少一种富氩流体和至少一种富氧流体的方法和装置 Download PDF

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CN102695935A
CN102695935A CN2010800247790A CN201080024779A CN102695935A CN 102695935 A CN102695935 A CN 102695935A CN 2010800247790 A CN2010800247790 A CN 2010800247790A CN 201080024779 A CN201080024779 A CN 201080024779A CN 102695935 A CN102695935 A CN 102695935A
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carbon dioxide
oxygen
stream
rich
argon
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J-P·特拉尼耶
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication of CN102695935A publication Critical patent/CN102695935A/zh
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
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    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
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    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
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    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
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    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
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    • B01D2256/10—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
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    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
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    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
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Abstract

本发明涉及一种从产生于用于净化氧-燃料燃烧烟气的方法的流体中生产富含氩的流体和富含氧的流体的方法，所述方法包括：通过净化方法净化剩余气体以便产生富含二氧化碳的气体(119)和二氧化碳贫乏的剩余气体(120)，预处理二氧化碳贫乏的剩余气体以便获得富含二氧化碳的流和二氧化碳贫乏的流(123)，通过低温技术处理二氧化碳贫乏的流以便提取至少富含氩的部分(127)、富含氧的部分(126)以及氩和/或氧贫乏的部分(125)。

Description

用于从剩余流体生产至少一种富氩流体和至少一种富氧流体的方法和装置
技术领域
本发明涉及用于从剩余/残余流体生产至少一种富氩流体和至少一种富氧流体的方法，该剩余流体产生于用于净化剩余气体的方法，剩余气体包含二氧化碳以及氩和氧或氩和氧其中之一。特别的例子为，从用于低温分离剩余气体(剩余气体由消耗氧的设备产生)的方法的不可冷凝物中生产氩，所述剩余气体是氧-燃料燃烧烟气。
背景技术
热电站使得可通过燃料燃烧而释放热量，热量可以被用于生产蒸汽和机械能或电能。燃烧烟气将大量的CO2释放到大气中。为了解决该环境问题，目前的解决方案包括，在存在富氧的并且最重要的脱氮的气体的锅炉中进行燃烧。该燃烧产生具有高浓度CO2的燃烧烟气，这是有利的，因为与从具有低浓度CO2的烟气中去除CO2相比，用于从燃烧烟气中去除CO2的现有技术更容易从具有高浓度CO2的烟气中去除CO2。接着，在隔离之前，需要对该CO2进行净化和压缩。
发明内容
本发明的一个目的是提供一种从富含二氧化碳且包含氩和/或氧的剩余气体中生产氩和氧的方法，该氩和氧是用于在低温下除去CO2以净化烟气的单元的不可冷凝物。
本发明的一个主题提供了一种从剩余流体中生产至少一种富含氩的流体和至少一种富含氧的流体的方法，该剩余流体产生于用于净化剩余气体的方法，该剩余气体包含二氧化碳以及氧和/或氩，该剩余气体来自被供给含有氩的氧的设备，该设备是氧-燃料燃烧设备，该方法包括以下步骤：
-回收由烟气组成的剩余气体，烟气产生于锅炉的燃烧室中燃料借助于富含氧和二氧化碳且含有氩的气体的富氧燃烧；
-通过特别是低温下的净化方法净化剩余气体、特别是离开锅炉的烟气，以便产生富含二氧化碳的流体和二氧化碳变得贫乏的剩余流体；
-预处理所述二氧化碳变得贫乏的剩余流体以便获得富含二氧化碳的流和二氧化碳贫乏的流；和
-低温处理二氧化碳贫乏的流以便从该流中提取至少一个富含氩的部分、富含氧的部分和至少一个氩和/或氧变得贫乏的部分。
根据其它可选的方面：
-低温处理二氧化碳贫乏的流包括：在至少一个交换器中、可选地在再沸器中、可选地在冷凝器中、可选地在可逆型或交流换热器型(再生器型)交换器中进行冷却的步骤，和在蒸馏塔中蒸馏的步骤；
-优选地在低温下执行净化方法，尽管可以替代以其它已知的净化方法(例如通过胺进行洗涤)；
-二氧化碳贫乏的流基本不含二氧化碳，并且可含有例如几ppm的二氧化碳；
-在空气分离装置中、优选地通过低温蒸馏分离空气，以便产生富含氧的流，富含氧的流包含最多99％的氧，优选地包含最多98％或最多97mol％的氧，富含氧的流还包括氩，优选地包含至少2mol％的氩，或至少3mol％的氩，并且该富含氧的流被输送至消耗氧的设备，优选地用于氧-燃料燃烧；
-富含氧的部分用于燃料的富氧燃烧和/或用于二氧化碳变得贫乏的剩余气体的预处理；
-处理还使得可回收富含氮的部分；
-来自用于从空气中分离气体的单元或用于分离空气中的气体、输送用于氧-燃料燃烧的氧的至少一部分的单元的一种或更多种流体用于处理二氧化碳贫乏的流；
-二氧化碳贫乏的流在低温处理的上游被冷却，二氧化碳贫乏的流基本不含二氧化碳；
-二氧化碳贫乏的流在低温处理的上游被冷却，并且同时二氧化碳贫乏的流被净化以除去二氧化碳，二氧化碳贫乏的流包含二氧化碳；
-二氧化碳贫乏的流在至少一个可逆型交换器或交流换热器型交换器中被冷却，并且产生的流被输送给低温处理单元的塔；
-这些流体中的一种是富含氮的液体，该富含氮的液体至少部分地保持二氧化碳贫乏的流的低温处理过程的冷却；
-没有用于或来自处理单元的塔的流体在涡轮中膨胀；
-二氧化碳贫乏的流被输送给第一塔(第一塔可选地具有底部再沸器)，并且被分离而形成富含氧的流体和富含氮的流体，并且从第一塔抽取出中间流并输送至第二塔的底部，在第二塔中使该中间流富含氩从而形成富含氩的部分；
-从第二塔抽取出富含氩的部分并输送给脱氮塔，以便形成富氩部分；
-来自用于从空气中分离气体的单元或用于分离空气中的气体、输送用于被供应氧的设备例如用于氧-燃料燃烧的氧的至少一部分的单元的一种或更多种流体用于处理二氧化碳贫乏的流；
-用于从空气中分离气体的单元的至少一个塔和处理单元的至少一个塔容纳在单个冷箱中；
-这些流体中的一种是富含氮的气体，该富含氮的气体将用作低温处理的至少一个再沸器和/或至少一个冷凝器的循环气体；
-在低温处理之前，预处理去除剩余气体中的至少50％、甚至基本100％的二氧化碳；
-至少部分地通过在多个并联交换器中二氧化碳的反升华/升华来进行预处理；
-在有富氧部分存在的情况下进行二氧化碳的升华，从而形成二氧化碳/氧混合物以便用于燃料的富氧燃烧；
-至少部分地通过TSA、PSA或VPSA过程来进行预处理，以便产生富含二氧化碳的部分和二氧化碳变贫乏但是富含氩的部分；
-至少部分地通过吸收过程来执行预处理；
-吸收过程使用碱性PH值的水溶液；
-通过注入NaOH和/或Na2CO3和/或NH3来获得碱性PH值；
-至少部分地通过吸附过程来执行预处理；
-至少部分地通过渗透来执行预处理；
-由预处理产生的富含二氧化碳的流循环至锅炉，优选地循环至燃烧室。
本发明的另一个主题提供了一种从剩余流体中生产至少一种富含氩的流体和至少一种富含氧的流体的装置，该剩余流体产生于用于净化剩余气体的方法，该剩余气体包含二氧化碳以及氧和/或氩，该剩余气体来自被供给含有氩的氧的设备，该设备是氧-燃料燃烧设备，所述装置包括：
-用于净化剩余气体的单元，该剩余气体由离开锅炉的烟气构成，锅炉用于燃料借助于富含氧和二氧化碳的气体的富氧燃烧，在这种情况下净化单元可以是低温净化单元，以便产生富含二氧化碳的流体和二氧化碳变贫乏的剩余流体；
-用于预处理剩余流体的单元，以便获得富含二氧化碳的流和二氧化碳贫乏的流；以及
-用于低温处理二氧化碳贫乏的流的单元，以便从该二氧化碳贫乏的流中提取富含氩的部分、富含氧的部分以及氩和/或氧变贫乏的部分。
根据其它可选方面：
-用于低温处理二氧化碳贫乏的流的单元包括至少一个交换器和至少一个蒸馏塔；
-至少一个交换器是再沸器；
-至少一个交换器是冷凝器；
-处理单元使得可回收富含氩的部分和富含氧的部分；
-装置包括用于将富含氧的部分输送至锅炉和/或预处理单元的器件；
-处理还使得可回收富含氮的部分；
-装置包括用于将一种或更多种流体输送给用于低温处理二氧化碳贫乏的流的器件，该一种或更多种流体来自用于分离空气中的气体、并且输送用于被供应氧的设备例如用于氧-燃料燃烧的氧的至少一部分的单元；
-这些流体中的一种是富含氮的液体，该富含氮的液体用于保持处理过程的冷却；
-这些流体中的一种是富含氮的气体，该富含氮的气体将被用作低温处理二氧化碳贫乏的流的单元的至少一个再沸器和/或至少一个冷凝器的循环气体；
-预处理单元为/包括二氧化碳反升华/升华单元，该二氧化碳反升华/升华单元包括多个并联的交换器；
-升华单元与用于输送富含氧的部分的管道连接，从而形成二氧化碳和氧的混合物，并且可选地包括将混合物输送给燃料富氧燃烧单元的器件；
-预处理单元为/包括TSA、PSA或VPSA型设备，其产生富含二氧化碳的部分和二氧化碳变贫乏但是富含氩的部分；
-预处理单元为/包括吸收设备；
-吸收过程使用碱性PH值的水溶液；
-通过注入NaOH、Na2CO3、NH3来获得碱性PH值；
-吸收过程是甲醇洗涤过程；
-预处理单元为/包括渗透单元；
-装置包含将富含二氧化碳的流从预处理单元循环至锅炉的器件。
由空气分离装置输送给氧-燃料燃烧设备的氧包含最多98mol％的氧、优选地最多97mol％的氧、或者最多96mol％的氧。
由空气分离装置输送给设备、例如氧-燃料燃烧设备的氧包含至少1mol％的氩，优选地至少2mol％的氩，或者至少3mol％的氩。
由空气分离装置产生的富含氩的气体包括至少50mol％的氩、优选地至少70mol％的氩、或者至少90mol％的氩。
附图说明
参考附图更加详细地描述本发明。
图1示出了氧-燃料燃烧设备，其包括用于净化烟气的单元，
图2更详细地示出了用于净化烟气的单元，
图3示出了用于在低温下净化烟气以除去CO2的单元，
图4示出了用于从图4的单元的剩余气体中回收氮和/或氧和/或氩的装置，以及
图5示出了图4的变型。
具体实施方式
图1是氧-燃料燃烧设备的示意图。空气分离装置2产生氧流10以及剩余氮流13，氧流10通常具有95mol％的纯度以便最大化其氩含量。该装置还产生气态氮13，以及用于处理不可冷凝物的液氮159。氧流10被分成两部分11和12。主要烟气循环流15穿过单元3，在单元3中煤14被转变成粉末。部分11与单元3下游的循环流混合，并且混合物被输送到锅炉1的燃烧室。部分12与次要烟气循环流16混合，其使得燃烧器稳定以便将温度保持在可接受的程度。水17被输送到锅炉1以便产生蒸汽18，蒸汽18在涡轮8中膨胀。富含CO2的烟气19——其通常包含大于70mol％(不计算蒸汽)的CO2——经历数个处理以便去除杂质。单元4例如通过催化作用而去除NOx。随后，单元5去除灰尘，并且随后单元6是用于去除SO2和/或SO3的脱硫***。依据需要的产物的成分，单元4和单元6可能是多余的。来自单元6(或单元5，如果不存在单元6)的净化流24被输送给压缩和净化单元7，以便产生相对纯净的CO2流25和剩余流26。
图2是图1的压缩和净化单元7的示意图。流110(对应于图1的流24)进入单元101，在单元101中，流110被制备成压缩单元102的上游流。在单元101中，流110可以被净化以除去灰尘、SO2和/或SO3，和/或被冷却。
由单元101产生的剩余流111可以是冷凝水、灰尘或H2SO4、HNO3、Na2SO4、CaSO4、Na2CO3、CaCO3等等。
压缩单元102将来自单元101的流112从接近大气压的压力压缩至介于15bar abs(绝对压力)和60bar abs之间、优选地大约30bar abs的高压。可以在包括中间冷却的多个步骤中进行该压缩。在本例中，可能产生冷凝物113。压缩的热量可以回收以便预加热水17。热的流114离开压缩单元102并且进入单元103。该单元103使流114冷却、干燥并且可选地对其净化以除去汞，从而产生剩余物115、116和117。
单元104是低温净化单元。在本例中，“低温”表示净化处理循环中的最小温度低于0℃，并且优选地低于-20℃，或者尽可能地接近纯CO2的三相点/三态点温度-56.6℃。在该单元104中，在一个或更多个步骤中冷却并且部分地冷凝流118。使一个或更多个富含CO2的流膨胀并且蒸发以便获得富含CO2的产物119。从单元104回收不可冷凝物的高压流120并输送给预处理单元122。经预处理的流123被输送给处理单元124，在处理单元124中产生一种或更多种流体，其可以是液态和/或气态氮125、和/或液态和/或气态氧126、和/或气态和/或液态氩127。
在压缩单元105中压缩富含CO2的产物119。在单元105中，被压缩的流121被冷凝并且可能被泵送。
图3示出了低温净化装置，该装置相当于图2的单元104。流118包括处于大约30bar的压力下以及介于15℃和43℃之间的温度下的烟气，流118在单元3中被过滤以便形成流5。流118尤其包含二氧化碳和NO2、氧、氩和氮。可通过单元103在高压下直接产生流118，或者流118可被压缩机2(用虚线示出)压缩。流5在交换管线9中冷却并且部分地冷凝。流5的一部分7没有在交换管线9中被冷却，而是与交换管线的下游的流5的剩余部分混合以便改变混合物的温度。部分冷凝的流被输送给第一分相器11并且被分离成气相13和液相17。气相13被分成两部分以便形成流15和流21。流21用于在交换器25中使塔43再沸腾，接着，流21被输送给第二分相器22。流15使再沸器短路(即绕过再沸器)以便调节再沸腾。
来自第一分相器11的液体17在阀19中膨胀并且第二分相器22的液体流29在阀31中膨胀，接着，两个膨胀的流被输送到塔43的顶部。塔43主要用于从供给流118中去除不可冷凝的成分(氧、氮和氩)。
从塔43的顶部抽取二氧化碳变得贫乏(贫含二氧化碳)的流33，并且输送给压缩机35。以此种方式产生的压缩流37循环至流5。
从塔43的底部抽取出富含二氧化碳的流67，并且流67被分成两部分。一部分69被泵71泵送以便形成流85，随后流85被泵87泵送并且接着从***中去除流85。流85相当于图1的流25。流67的剩余部分73用于保持装置冷却。
推荐净化流118以除去NO2。
可以在分离NO2之前或之后分离不可冷凝物。
图3中，在与流69分开之后，富含二氧化碳的流的剩余部分73在交换管线9中蒸发并且被输送给塔105以便净化除去NO2。
该塔可以具有顶部冷凝器和底部再沸器，流73被输送至中间位置。另外，如果没有底部再沸器，流73被输送至底部。
NO2贫乏的流79被从塔105抽出并且返回到交换管线9中。该流79被加热，在压缩机75、77中被压缩，被输送给交换器65，作为流78被抽出，在交换器81、83中被冷却，并且与流69混合，从而形成流85。交换器81可以用于加热待用于锅炉的水。通过制冷剂流185冷却交换器83，制冷剂可以是R134a、氨、水等等，被加热的制冷剂记作187。从塔105的底部抽取出富含NO2的流84。该流84循环至过滤器3的上游的一位置。
来自第二分相器22的顶部气体32在交换器55中被冷却并且被输送给第三分相器133。来自第三分相器133的液体的一部分被输送给塔43并且剩余部分(作为中等纯度的流45)被分成两股流47、141。流47在交换器55中蒸发并被输送到塔43的顶部或者与流33混合。
流141在阀中膨胀，在交换器55、9中被加热，在压缩机59中被压缩，在交换器60中作为流91被冷却、并且与压缩流5混合。用于使流141膨胀的阀可以用液体涡轮取代。
来自第三分相器133的顶部气体在热交换器55中被冷却(可选地在压缩机134中被压缩之后)，并被输送给第四分相器143。来自第四分相器143的二氧化碳贫乏的顶部气体157在热交换器55中被加热、接着在交换器9中被加热、在交换器65中被加热，并且作为流23在与压缩机35联接的交换器63中膨胀。二氧化碳贫乏的气体157包括介于30％和45％之间的二氧化碳以及介于30％和45％之间的氮。该气体157还包括大量的氧和氩。来自分相器143的底部液体51与流47一起被输送给塔43。
在涡轮63中膨胀的流与没有穿过涡轮的流115混合，并且随后在(交换器)89中被再加热。已加热流的一部分97在涡轮61中膨胀并且被作为流99排入大气。
富含不可冷凝物(氧和/或氩和/或氮)并且包含CO2的流120在单元104中被回收从而回收流120的至少一种成分作为产物。该流120可以是来自涡轮61的流101的一部分和/或来自交换器55上游的第四分相器143的顶部气体157的一部分和/或在涡轮63中膨胀的流的一部分和/或交换器9的下游的流157的一部分。
O2、N2、Ar、CO2的摩尔百分比(示例)
Figure BDA0000116138070000091
表1
图4示出了用于预处理的装置和用于通过低温蒸馏对流120进行分离的装置。该流120首先在预处理单元122中被预处理。该预处理单元去除剩余气体120中至少50mol％的二氧化碳，之后，低温处理产生富含CO2的流169，该流169可以与流118一起循环至单元104。
可以通过在多个并联交换器中二氧化碳的反升华/升华来进行预处理。作为替代，可以通过吸收(例如通过甲醇洗涤)、吸附、渗透或若干个这些技术来进行预处理。
例如，在有富氧部分存在的情况下进行二氧化碳的升华，从而形成二氧化碳和用于燃料的富氧燃烧的氧的混合物。通过反升华，被处理气体的温度从-56.6℃(CO2的三态点)下降到-170℃/-175℃，在-170℃/-175℃下，可以在空气中进行气体的低温蒸馏。
另外，可以通过TSA、PSA或VPSA过程来进行预处理，以便产生富含二氧化碳的部分和二氧化碳变得贫乏但是富含氩的部分。
可以通过吸收过程来进行预处理，例如使用碱性PH值的水溶液。可选地，通过注入NaOH和/或Na2CO3和/或NH3来获得碱性PH值。吸收过程也可以采用非水流体，例如甲醇。本例中，在低温下并且优选地在压力下进行吸收。
作为一种替代方式，可以通过渗透或通过已提到的各种过程的组合来进行预处理。
可在预处理单元中除去全部的二氧化碳以便接着输送含有几ppm的二氧化碳的流。这使得可使用板式交换器和带散热片的交换器作为交换器。
另一方面，如果流123仍然含有二氧化碳，必须使用可逆交换器或者如Springer Verlag出版的“Tieftemperaturtechnik(低温技术)”的第475页、第9.4.2.3段和9.4.2.4段描述的交流换热器型交换器来继续进行预处理。这样，可以通过穿过这两种类型之一的交换器130来除去剩余的二氧化碳。清楚地，在塔的入口处，供给流123应当不再含有超过几ppm的二氧化碳。
如图4所示，预处理之后，二氧化碳变得贫乏的流123被输送给低温蒸馏单元124。流123在交换器130中被冷却至低温并且被输送至具有底部再沸器133的塔131的中部。作为一种替代方式，可通过在涡轮中在产生功的情况下膨胀(等熵膨胀)来冷却流123。气态氧GOX从塔131的底部上方抽取出，在交换器130中被加热并且被用作产物126和/或循环至预处理单元122和/或循环至锅炉1。液氧136可以从塔131的底部抽取出，例如作为产物抽取出。富含氩的流141从塔131输送至塔137，并且不纯的氩流145从塔137的冷凝器155下方抽取出。底部液体流143返回至塔131。不纯的氩145在脱氮塔139中被净化，脱氮塔139包括顶部冷凝器153和底部再沸器151。在脱氮塔139的底部产生液氩127。至少部分地通过注入液氮159来保持装置的冷却，液氮159来自供应氧-燃料燃烧的空气分离装置2。液氮159被输送至塔131的顶部。该空气分离装置2还输送气态氮13，气态氮13在交换器130中被冷却并且加热塔131的底部再沸器133以便形成冷凝流。冷凝流的一部分147在膨胀后被输送至脱氮塔139的顶部冷凝器153，一部分165被输送至塔137的顶部冷凝器155，一部分157在膨胀后被输送至塔131的顶部。在冷凝器153中蒸发的氮163与塔131的顶部气体135混合，在过冷却器160和交换器130中被加热，并且形成气态氮165。在冷凝器155中蒸发的氮161形成氮流161。
装置124的至少一个塔可以可选地与装置2的至少一个塔容纳在相同的冷箱中。因此，可以在不需要再加热和冷却氮的情况下进行氮13和/或159的传递。对于图4的情况，如果不必须回收氩，则可以省略塔137、139。
图5示出了图4的冷部分的变型，在该变型中，来自交换器130的冷混合物123被输送至塔163的中间位置，塔163没有再沸器或顶部冷凝器。来自塔163的顶部气体171构成气态氮，并且底部液体173被输送至塔165的中间位置。气体175从塔165的中间位置返回至塔163的底部。塔165具有底部再沸器175和顶部冷凝器177。气态氧126和/或液态氧136在塔165的底部被回收，并且顶部液体145被输送至脱氮塔167，在脱氮塔167的底部形成液态氩127。脱氮塔具有底部再沸器151和顶部冷凝器153。
来自空气分离装置2的液氮159被输送至塔163的顶部。塔163具有顶部冷凝器，像图5的所有再沸器和冷凝器一样，该顶部冷凝器通过来自空气分离装置2的气态氮的循环而运行，该循环没有示出但是其与图4的循环类似。
可选地，液氮159的输送可以构成用于处理过程的唯一冷却源。
当然，可以设想除了图4和图5中示出的方式之外的通过低温蒸馏分离流123的方法。

Claims (17)

1.一种从剩余流体中生产至少一种富含氩的流体和至少一种富含氧的流体的方法，该剩余流体产生于用于净化剩余气体的方法，该剩余气体包含二氧化碳以及氧和/或氩，该剩余气体来自被供给含有氩的氧的设备，该设备是氧-燃料燃烧设备，该方法包括以下步骤：
-回收烟气，所述烟气产生于锅炉(1)的燃烧室中燃料借助于富含氧和二氧化碳且含有氩的气体的富氧燃烧；
-通过低温净化方法净化由离开锅炉的烟气构成的剩余气体，以便产生富含二氧化碳的流体(119)和二氧化碳变得贫乏的剩余流体(120)；
-预处理所述二氧化碳变得贫乏的剩余流体以便获得富含二氧化碳的流(169)和二氧化碳贫乏的流(123)；
-低温处理所述二氧化碳贫乏的流以便从该流中提取至少一个富含氩的部分(127)和至少一个富含氧的部分(126)和至少一个氩和/或氧变得贫乏的部分(125)。
2.根据权利要求1的方法，其特征在于，低温处理所述二氧化碳贫乏的流包括在至少一个交换器(130)中、可选地在再沸器中、可选地在冷凝器中、可选地在可逆型或交流换热器型交换器中进行冷却的步骤，和在蒸馏塔(131、163)中蒸馏的步骤。
3.根据前述权利要求中任一项的方法，其特征在于，在空气分离装置(2)中优选地通过低温蒸馏分离空气，以便产生富含氧的流(10)，所述富含氧的流(10)包含最多99％的氧，优选地包含最多98％的氧或最多97mol％的氧，所述富含氧的流(10)还包含氩，优选地包含至少2mol％的氩或至少3mol％的氩，并且该富含氧的流被输送以用于氧-燃料燃烧。
5.根据前述权利要求中任一项的方法，其特征在于，所述富含氧的部分(126)用于燃料的富氧燃烧和/或用于二氧化碳变得贫乏的剩余气体的预处理。
6.根据前述权利要求中任一项的方法，其特征在于，所述处理还使得可回收富含氮的部分(125)。
7.根据前述权利要求中任一项的方法，其特征在于，在处理二氧化碳贫乏的流的过程中使用来自用于从空气中分离气体的单元(2)或用于分离空气中的气体的单元的一种或多种流体，所述单元输送用于被供应氧的设备、例如用于氧-燃料燃烧的氧的至少一部分，在该情况下，所述用于从空气中分离气体的单元的至少一个塔和所述处理单元的至少一个塔可以被容纳在单个冷箱中。
8.根据权利要求7的方法，其特征在于，这些流体中的一种是富含氮的液体(159)，该富含氮的液体至少部分地保持二氧化碳贫乏的流的低温处理过程的冷却。
9.根据权利要求7或8的方法，其特征在于，这些流中的一种是富含氮的气体(13)，该富含氮的气体用作低温处理的至少一个再沸器和/或至少一个冷凝器的循环气体。
10.根据前述权利要求中任一项的方法，其特征在于，在低温处理之前，预处理去除剩余气体中的至少50mol％的二氧化碳。
11.根据权利要求10的方法，其特征在于，至少部分地通过在多个并联交换器中二氧化碳的反升华/升华来进行预处理。
12.根据权利要求11的方法，其特征在于，在有富氧部分存在的情况下进行二氧化碳的升华，从而形成二氧化碳/氧混合物以便用于燃料的富氧燃烧。
13.根据权利要求10或11或12的方法，其特征在于，至少部分地通过TSA、PSA或VPSA过程来进行预处理，以便产生富含二氧化碳的部分和二氧化碳变得贫乏但是富含氩的部分。
14.根据权利要求10或11或12或13的方法，其特征在于，至少部分地通过吸收过程，可选地通过使用甲醇洗涤，来执行预处理。
15.根据权利要求10-14中任一项的方法，其特征在于，至少部分地通过渗透来执行预处理。
16.根据前述权利要求中任一项的方法，其特征在于，由预处理产生的富含二氧化碳的流(169)循环至消耗氧的设备，优选地循环至氧-燃料燃烧锅炉，优选地循环至燃烧室。
17.一种从剩余流体中生产至少一种富含氩的流体和至少一种富含氧的流体的装置，该剩余流体产生于用于净化剩余气体的方法，该剩余气体包含二氧化碳以及氧和/或氩，该剩余气体来自被供给含有氩的氧的设备，该设备是氧-燃料燃烧设备，所述装置包括：
-用于净化剩余气体、特别是离开锅炉的烟气，以便产生富含二氧化碳的流体和二氧化碳变得贫乏的剩余流体的单元(104)，所述锅炉用于燃料借助于富含氧和二氧化碳的气体的富氧燃烧，其中净化单元可以是低温净化单元；
-用于预处理所述剩余流体，以便获得富含二氧化碳的流和二氧化碳贫乏的流的单元(122)；以及
-用于低温处理所述二氧化碳贫乏的流，以便从该二氧化碳贫乏的流中提取富含氩的部分、富含氧的部分以及氩和/或氧变得贫乏的部分的单元(124)。
18.根据权利要求17的装置，其特征在于，所述用于低温处理二氧化碳贫乏的流的单元包括至少一个交换器(130)和至少一个蒸馏塔(131、139、163、165、167)。
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