CN102483301B - 用于操作至少一个空气分离设备和氧消耗单元的方法 - Google Patents

用于操作至少一个空气分离设备和氧消耗单元的方法 Download PDF

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CN102483301B
CN102483301B CN201080040115.3A CN201080040115A CN102483301B CN 102483301 B CN102483301 B CN 102483301B CN 201080040115 A CN201080040115 A CN 201080040115A CN 102483301 B CN102483301 B CN 102483301B
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air
separation unit
gas separation
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CN102483301A (zh
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A·吉亚尔
N·阿拉德
P-E·弗朗
H·穆萨维
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—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
    • F25J3/04—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 for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J3/04515—Simultaneously changing air feed and products output
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    • F25J3/04533—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion"
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
    • F25J3/04545—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels for the gasification of solid or heavy liquid fuels, e.g. integrated gasification combined cycle [IGCC]
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    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—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
    • F25J3/04—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 for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • 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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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—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
    • F25J3/04—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 for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04842—Intermittent process, so-called batch process
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—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
    • F25J3/04—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 for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
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    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
    • 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
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    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
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Abstract

本发明提供了一种用于操作设备的方法，该设备包括至少两个空气分离装置(1)、储存系统(2)和消耗富氧气体的单元(3)，该气体消耗单元能够根据第一步骤发电，在该第一步骤期间电成本大于第一价格阈值，该气体消耗单元从所述空气分离装置或其中的至少一些接收大于第一消耗阈值的富氧气体量，该富氧气体部分地由通过空气分离装置在第二步骤期间供应的、储存在储存系统中的氧组成，部分地由在第一步骤期间通过蒸馏产生的氧组成，根据第二步骤，在该第二步骤期间电的成本低于第二价格阈值，第二价格阈值小于第一价格阈值。气体消耗单元消耗低于第二消耗阈值的富氧气体量，在所述装置或至少一个所述装置中分离空气，并且将富氧液体从至少两个分离装置输送到储存系统。

Description

用于操作至少一个空气分离设备和氧消耗单元的方法
技术领域
本发明涉及一种用于操作至少一个空气分离单元和包括碳燃料燃烧单元或气化(gazéification)单元的富氧气体消耗装置的方法，所述富氧气体消耗装置能够发电。该消耗装置被供应来自一个或多个空气分离单元的富氧气体。
背景技术
通过碳燃料消耗单元来产生能量的CO2捕集技术中的一种(称为氧燃料燃烧)需要通过一系列空气分离单元产生的很大量的氧(从每天10000M公吨至每天20000M公吨，视地点而定)，所述空气分离单元与用于从燃烧单元分离废气的单元相关联，以在一个或多个燃烧单元的出口处产生CO2，CO2之后被输送和存储。这些空气分离单元是很大型的电能消耗装置，从而不利于在能量成本最高时通过该消耗装置产生的电力对电网的输入。
已知切换系统，其允许它们在峰值需求时段消耗的电力被限制(US-A-20080115531或WO-A-09/071833)。
还可设想关闭并重新起动空气分离单元以便节省能量并因此切换到用于消耗装置的空气模式，除了在相对短的时间段之外不捕集CO2，但用于重新起动的时间不必然每天与这种类型的几种操作相兼容。
一些燃烧单元设计成在基础模式下操作，也就是说全年或接近全年(旺季、一般季节和淡季)处于连续稳定的操作下，并且基本接近它们的标称消耗操作，以便连续地将电能输入电网，而其它燃烧单元则设计成更不规律地操作并满足高于特定电能消耗水平的需求(旺季和一般季节)，而再其它燃烧单元则设计成仅对峰值需求(对于旺季每年几百小时或者甚至略多于一千小时)作出响应。
在燃烧单元以相对不规律的方式操作的情况下，为氧燃料燃烧输送氧的空气分离单元设计成以它们的标称水平输送消耗装置在其正常操作时的全部需求，并且当燃烧单元在需求低时每天停机数小时或每周停机数天时不得不向大气排放或者停机，其总体结果是造成相当大的能量损失。
这是因为在氧被分离后向大气排放氧，即使它可在低压力下执行，也意味着约0.2KWh/Nm3至0.35KWh/Nm3的能量损耗量，其取决于所使用的工艺方案。
对于在短时间停机后重新起动空气分离单元，除了其复杂性以外，还将花费大约一小时来获得所需的纯度和压力，这也对应着并非不明显的能量损失。
发明内容
本发明的一方面提供了一种用于操作设备的方法，该设备包括至少两个空气分离单元、储存系统和包括碳燃料燃烧单元或气化单元的富氧气体消耗装置，该消耗装置能够至少在第一操作阶段发电，在该方法中，该设备在多个操作阶段操作：
a)在第一操作阶段，在此期间电的成本高于第一价格阈值，所述消耗装置接收来自空气分离单元中的至少一个的、高于第一消耗阈值的富氧气体量，该富氧气体部分地由通过空气分离单元在第二操作阶段期间供应的、储存在储存系统中的氧组成，部分地由在第一操作阶段期间通过在至少一个空气分离单元中蒸馏产生的氧组成。
b)在第二操作阶段，在此期间电的成本低于第二价格阈值，该第二价格阈值低于第一价格阈值，消耗装置消耗低于第二消耗阈值的富氧气体量，该第二(消耗)阈值低于第一(消耗)阈值，该量可能为零，至少在特定的空气分离单元中分离空气，并且将富氧液体从分离单元或从至少一个分离单元输送到储存系统；和
c)在第一操作阶段期间进行操作的分离单元的数目少于在第二操作阶段期间进行操作的单元的数目。
根据其它可选方面：
-在整个第二操作阶段期间储存的富氧液体中的氧的摩尔数少于在第一操作阶段期间作为富氧气体被输送到消耗装置的氧的摩尔数；
-在第一操作阶段期间的富氧气体消耗基本恒定；
-输送到空气分离单元中的至少一个——其为在第一操作阶段期间操作的一个或多个单元——的空气的量对应于比输送到消耗装置的气态氧的产量低至少15％、优选低至少25％或甚至低40％的氧产量；
-对应于输送到在第一操作阶段期间操作的至少一个分离单元的空气的量的富氧气体的产量与输送到消耗装置的富氧气体的消耗之差对应于在第二操作阶段期间储存的液氧的量的至少一部分；
-在第一操作阶段期间操作的分离单元的数目比在第二操作阶段期间操作的单元的数目少至少两个；
-供应在第一操作阶段期间操作的空气分离单元的空气压缩机的数目优选比供应在第二操作阶段期间操作的空气分离单元的空气压缩机的数目少至少两个；
-在第一操作阶段期间从一个或多个空气分离单元输送到储存系统的液氧的量不超过被输送到空气分离单元的空气流量的1％、优选2％或甚至5％；
-在第二操作阶段期间从储存系统输送到一个或多个空气分离单元的液氧的量不超过被输送到空气分离单元的空气流量的1％、优选2％或甚至5％；
-在第二操作阶段期间从空气分离单元(1)提取的气态氧的量不超过被输送到空气分离单元的空气流量的1％、优选2％或甚至5％；
-在第二操作阶段期间且优选不在第一操作阶段期间，将液氮和/或液态空气输送到空气分离单元，该液氮和/或液态空气由一个或多个空气分离单元在第一操作阶段期间且优选不在第二操作阶段期间产生；
-存在n个空气分离单元，n优选至少为2，并且空气分离单元中的至少一个或所述空气分离单元具有低于消耗装置的标称富氧气体容量除以n的标称富氧气体容量；
-n至少等于三并且空气分离单元中的至少两个具有低于消耗装置的标称富氧气体容量除以n的标称富氧气体容量；
-存在n个空气分离单元，n优选至少为2，并且空气分离单元中的至少一个或所述空气分离单元具有高于消耗装置的标称富氧气体容量除以n的标称富氧气体容量；和
-n至少等于三并且空气分离单元中的至少两个具有高于消耗装置的标称富氧气体容量除以n的标称富氧气体容量。
由于可行性和/或可靠性原因，每台设备一般均包括至少两个空气分离单元。每个分离单元均包括用于净化空气的水/二氧化碳净化器，以及在其中安置蒸馏塔的冷箱。为了压缩空气，设置至少与空气分离单元一样多的空气压缩机，因此，在两个分离单元的情况下，存在至少两个空气压缩机。这些压缩机可选地与空气增压器组合。
该设备还包括用于储存液态产品(液氧、液氮和可能的液态空气)的系统，所述系统由每种产品一个或多个储存罐组成。该储存系统可与这些空气分离单元连通。
空气压缩机和空气增压器可联通以便共同供应所有空气分离单元。
在消耗装置的特定或者甚至全部操作周期(第一操作阶段)期间，消耗装置消耗大致恒定量的氧。
该恒定量永久由一个或多个空气分离单元输送。在该操作阶段期间，电成本高于第一价格阈值并且消耗装置的氧消耗高于第一消耗阈值。整个第一操作阶段，一部分氧仍从在第二操作阶段期间储存和生产的氧产生。来自储存罐的氧可在位于空气分离单元外部的再沸器中被气化，但对于空气分离单元来说经由来自储存罐的氧的潜热而被致冷更加积极有益。
液氮和/或液态空气可通过给分离单元的元件供应液氧而在对电网具有高电能需求(高于第一价格阈值的费用)的时段中产生，而空气分离单元被供应来自储存系统的储存罐、冷箱的储存罐或外部源的液氧。
在燃烧单元停机的时段期间，空气分离单元中的至少一个继续运行并且产生大量液氧，空气分离单元的一个塔可选地被供应来自储存系统的储存罐、冷箱的储存罐或外部源的液氮和/或液态空气。优选地，在消耗装置停机时进行操作的空气分离单元的数目大于在该消耗装置进行操作时运行的空气分离单元的数目。这样，用户受益于在第二操作阶段期间的低电费用来制造将用于当电昂贵时在第一操作阶段期间供应消耗装置的液氧。
附图说明
将参考附图更详细地描述本发明，附图示出了能够根据本发明的方法操作的设备。
具体实施方式
该设备包括四个空气分离单元、储存系统2和可为碳燃料燃烧单元或气化器的富氧气体消耗装置3的组合体1。如果所述消耗装置为燃烧单元，则其也可被供应空气而不是氧气。
每个空气分离单元均包括净化器5A、5B、5C、5D和冷箱7A、7B、7C、7D，这些单元大致相同。
空气分离单元可从四个空气压缩机3A、3B、3C、3D接收空气，所述四个空气压缩机经由公共管路9连接，使得它们能够供应全部空气分离单元。
在第一操作阶段，富氧气体消耗装置3从最多三个空气分离单元接收气体。在该第一操作阶段期间，电成本超过第一价格阈值并且昂贵。因此希望尽可能多地减少在该操作阶段期间的电耗。为此，操作最多三个空气分离单元或甚至最多两个空气分离单元或者优选仅操作最多三个空气压缩机或甚至最多两个空气压缩机，冷箱在简化的操作模式下运行。
来自两个或三个进行操作的压缩机的空气被输送到所述两个或三个空气分离单元并且在被安置在冷箱中的塔内蒸馏以形成低压富氧气体。该压力很少超过5barabs。可从双塔中的低压塔提取气态形式的氧。所述双塔可为在低压塔中具有两个冷凝器的单元，如公知的那样。也可采取对于低压气化而言常见的措施使从塔提取的液体气化。
为了补偿在塔中蒸馏的气态氧与消耗装置3的氧消耗之间的差别，将液氧13从储存系统2输送到进行操作的空气分离单元，使得液氧的致冷被灵活地用于分离单元中。这样形成的气态氧变成被输送到消耗装置3的富氧气体17的一部分。优选地，在该第一操作阶段期间，没有液氧流从空气分离单元被输送到储存系统。可选地，不超过空气的1％、优选2％或甚至5％的液氧流从空气分离单元被输送到储存系统。
在第二操作阶段期间，消耗装置3不运行，因此没有富氧气流被输送到该单元或者被输送到该单元的流量不超过被输送到空气分离单元的空气的2％。在这种情况下，电成本低于第二价格阈值，该第二价格阈值低于第一价格阈值，因此电相对而言不昂贵。
这里，比在第一操作阶段期间操作更多的空气分离单元和/或更多的空气压缩机是有益的。因此，如果在第一操作阶段期间操作两个分离单元，则在第二操作阶段期间，操作三个或四个分离单元，并且如果在第一操作阶段期间操作三个分离单元，则在第二操作阶段期间，操作四个分离单元。同样，关于压缩机，如果在第一操作阶段期间操作两个压缩机，则在第二操作阶段期间，操作三个或四个压缩机，并且如果在第一操作阶段期间操作三个压缩机，则在第二操作阶段期间，操作四个压缩机。
在第二操作阶段，通过分离单元生产的气态氧很少量，或者甚至不存在。气态氧的产量可达供应空气的1％、优选2％或甚至5％，该氧被排放到大气。然而，空气分离单元产生的所有液氧11被输送到储存系统2。储存系统2在第二操作阶段期间但不在第一操作阶段期间被充装液氧，并且在第一操作阶段期间但不在第二操作阶段期间排出液氧。然而，可在第二操作阶段期间从储存罐排出很少量的液体。
在第二操作阶段期间，部分地通过将液氮和/或液化空气输送到一个或多个空气分离单元而维持分离单元的致冷。这种液氮和/或液化空气的供应在第一操作阶段期间不进行，且优选液氮和/或液化空气在第一操作阶段期间产生并被输送到储存系统2。液氮和/或液化空气可被至少部分地输送到分离单元的塔、分离罐或分离单元的热交换器。

Claims (24)

1.一种用于操作设备的方法，所述设备包括至少两个空气分离单元(1)、储存系统(2)和包括碳燃料燃烧单元或气化单元的富氧气体消耗装置(3)，所述消耗装置能够至少在第一操作阶段发电，在所述方法中，所述设备以多个操作阶段进行操作：
a)在第一操作阶段，在此期间电的成本高于第一价格阈值，所述消耗装置接收来自所述空气分离单元中的至少一个的富氧气体量，所述富氧气体量高于第一消耗阈值，并且所述富氧气体部分地由通过空气分离单元在第二操作阶段期间供应的、储存在储存系统中的氧组成，部分地由在第一操作阶段期间通过在至少一个空气分离单元中蒸馏产生的氧组成；和
b)在所述第二操作阶段，在此期间电的成本低于第二价格阈值，所述第二价格阈值低于所述第一价格阈值，所述消耗装置消耗低于第二消耗阈值的富氧气体量，所述第二消耗阈值低于所述第一消耗阈值，所述量可能为零，至少在特定的所述空气分离单元中分离空气，并且将富氧液体从所述分离单元或从所述至少一个分离单元输送到所述储存系统；和
c)在所述第一操作阶段期间进行操作的分离单元(1)的数目少于在所述第二操作阶段期间进行操作的分离单元的数目。
2.根据权利要求1所述的方法，其特征在于，在整个所述第二操作阶段期间储存的所述富氧液体中的氧的摩尔数少于在所述第一操作阶段期间作为富氧气体被输送到所述消耗装置的氧的摩尔数。
3.根据权利要求1所述的方法，其特征在于，在所述第一操作阶段期间的富氧气体消耗恒定。
4.根据前述权利要求中任一项所述的方法，其特征在于，输送到所述空气分离单元中的至少一个、即在所述第一操作阶段期间进行操作的一个或多个分离单元的空气的量对应于比输送到所述消耗装置的气态氧的产量低至少15％的氧产量。
5.根据权利要求1至3中任一项所述的方法，其特征在于，输送到所述空气分离单元中的至少一个、即在所述第一操作阶段期间进行操作的一个或多个分离单元的空气的量对应于比输送到所述消耗装置的气态氧的产量低至少25％的氧产量。
6.根据权利要求1至3中任一项所述的方法，其特征在于，输送到所述空气分离单元中的至少一个、即在所述第一操作阶段期间进行操作的一个或多个分离单元的空气的量对应于比输送到所述消耗装置的气态氧的产量低至少40％的氧产量。
7.根据权利要求4所述的方法，其特征在于，对应于输送到在所述第一操作阶段期间进行操作的所述至少一个分离单元的空气的量的富氧气体的产量与输送到所述消耗装置(3)的富氧气体的消耗之差对应于在所述第二操作阶段期间储存的液态氧的量的至少一部分。
8.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第一操作阶段期间进行操作的分离单元(1)的数目比在所述第二操作阶段期间进行操作的分离单元的数目少至少两个。
9.根据权利要求1至3中任一项所述的方法，其特征在于，用于供应在所述第一操作阶段期间进行操作的空气分离单元的空气压缩机(3A，3B，3C，3D)的数目比用于供应在所述第二操作阶段期间进行操作的空气分离单元的空气压缩机的数目少至少两个。
10.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第一操作阶段期间从一个或多个空气分离单元(1)输送到所述储存系统(2)的液氧的量不超过被输送到所述空气分离单元的空气的流量的1％。
11.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第一操作阶段期间从一个或多个空气分离单元(1)输送到所述储存系统(2)的液氧的量不超过被输送到所述空气分离单元的空气的流量的2％。
12.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第一操作阶段期间从一个或多个空气分离单元(1)输送到所述储存系统(2)的液氧的量不超过被输送到所述空气分离单元的空气的流量的5％。
13.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第二操作阶段期间从所述储存系统输送到一个或多个空气分离单元的液氧的量不超过被输送到所述空气分离单元的空气的流量的1％。
14.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第二操作阶段期间从所述储存系统输送到一个或多个空气分离单元的液氧的量不超过被输送到所述空气分离单元的空气的流量的2％。
15.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第二操作阶段期间从所述储存系统输送到一个或多个空气分离单元的液氧的量不超过被输送到所述空气分离单元的空气的流量的5％。
16.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第二操作阶段期间从所述空气分离单元(1)提取的气态氧的量不超过被输送到所述空气分离单元的空气的流量的1％。
17.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第二操作阶段期间从所述空气分离单元(1)提取的气态氧的量不超过被输送到所述空气分离单元的空气的流量的2％。
18.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第二操作阶段期间从所述空气分离单元(1)提取的气态氧的量不超过被输送到所述空气分离单元的空气的流量的5％。
19.根据权利要求1至3中任一项所述的方法，其特征在于，在所述第二操作阶段期间，将液氮和/或液态空气输送到所述空气分离单元，所述液氮和/或液态空气由一个或多个空气分离单元在所述第一操作阶段期间产生。
20.根据权利要求19所述的方法，其特征在于，在所述第二操作阶段期间且不在所述第一操作阶段期间，将液氮和/或液态空气输送到所述空气分离单元，所述液氮和/或液态空气由一个或多个空气分离单元在所述第一操作阶段期间且不在所述第二操作阶段期间产生。
21.根据权利要求1至3中任一项所述的方法，其特征在于，存在n个空气分离单元，n至少为2，并且所述空气分离单元中的至少一个所具有的标称富氧气体容量低于所述消耗装置的标称富氧气体容量除以n。
22.根据权利要求21所述的方法，其特征在于，n至少等于三并且所述空气分离单元中的至少两个所具有的标称富氧气体容量低于所述消耗装置的标称富氧气体容量除以n。
23.根据权利要求1至3中任一项所述的方法，其特征在于，存在n个空气分离单元，n至少为2，并且所述空气分离单元中的至少一个所具有的标称富氧气体容量高于所述消耗装置的标称富氧气体容量除以n。
24.根据权利要求23所述的方法，其特征在于，n至少等于三并且所述空气分离单元中的至少两个所具有的标称富氧气体容量高于所述消耗装置的标称富氧气体容量除以n。
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CA2771201C (fr) 2017-05-16
AU2010294078A1 (en) 2012-03-29
WO2011030035A2 (fr) 2011-03-17
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FR2949845A1 (fr) 2011-03-11
CA2771201A1 (fr) 2011-03-17
WO2011030035A3 (fr) 2013-12-19
FR2949845B1 (fr) 2011-12-02
AU2010294078B2 (en) 2014-09-18
CN102483301A (zh) 2012-05-30
EP2475944A2 (fr) 2012-07-18
ZA201201567B (en) 2014-03-26

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