CN105579801A - 通过空气的低温蒸馏而制备气态氧的方法和设备 - Google Patents

通过空气的低温蒸馏而制备气态氧的方法和设备 Download PDF

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Publication number
CN105579801A
CN105579801A CN201480049867.4A CN201480049867A CN105579801A CN 105579801 A CN105579801 A CN 105579801A CN 201480049867 A CN201480049867 A CN 201480049867A CN 105579801 A CN105579801 A CN 105579801A
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pressure
air
compressor
temperature
cooled
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CN105579801B (zh
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A·阿塞
I·贝尔托
A·布里格利亚
R·杜贝蒂尔-格勒尼耶
P·勒博
J-M·佩龙
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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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    • 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
    • F25J3/04406—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 using a dual pressure main column system
    • F25J3/04412—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 using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted 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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    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
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    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • 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
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    • 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • 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
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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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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
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    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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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
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    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
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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
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    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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Abstract

通过空气的低温蒸馏制备气态氧的方法，其中借助吸入温度T0为0-50℃的第一压缩机(1)使一部分(15)进料空气流达到压力P1，将在压力P1下的气体冷却以产生在压力P1和5-45℃的温度T1下的空气料流，使在第一压缩机中压缩的一部分(17，19)空气经受起始于温度T1和压力P1至大于P1的压力P2的另一压缩步骤，然后冷却至温度T2，其中T2和T1相差小于10℃。

Description

通过空气的低温蒸馏而制备气态氧的方法和设备
本发明涉及通过空气的低温蒸馏制备气态氧的方法和设备。
本发明的一个主题是通过将从蒸馏塔中取出的液体氧在主交换器中蒸发并借助泵达到高压而改进在20巴以上的绝对压力下制备气体，通常氧气的空气分离装置的能量性能。
在通过液体的蒸发而制备氧气的装置中，装置的能效很大程度上取决于用于产生热加压流体(通常进料空气)的方法，所述热加压流体通过冷凝至交换器的冷端，能够通过热交换而将氧气蒸发。
US-A-5475980描述了空气分离方法，其中将一部分空气在热增压器中压缩，另一部分在冷增压器中压缩直至达到基本相同的压力。冷压缩导致将压缩热引入换热器中。然而，在冷增压器中增压的一部分空气在膨胀式涡轮机中膨胀。为此不能使冷增压流降至特定值以下，因为有效用于膨胀的空气是不足的。
在本发明中，送入涡轮机中的空气料流未在冷增压器中增压，因此可使压缩热的量最小化。
所有提到的压力为绝对压力。
本发明提议通过连续的几个操作而产生该加压气体的特别有效的方法。
根据本发明的一个主题，提供通过空气的低温蒸馏而制备气态氧的方法，其中：
i)借助吸入温度T0为0-50℃，优选5-30℃的第一压缩机使所有或一部分进料空气流达到比中压塔的压力大至少5巴的压力P1，
ii)通常通过与水热交换而将压力P1下的气体冷却以产生在压力P1和5-45℃，优选15-25℃的温度T1下的空气料流，
iii)使在第一压缩机中压缩的一部分空气经受起始于温度T1和压力P1至大于P1的压力P2的另一压缩步骤，然后通常通过与水热交换而冷却至温度T2，其中T2和T1相差小于10℃，通常小于5℃，
iv)然后将该冷却部分引入空气分离装置的换热器中以经受冷却至低于或等于-100℃的温度，
v)将另一部分空气在压力P1下引入任选来自步骤iv)的空气分离装置的换热器中，以在其中经受冷却至-100℃以下的温度，然后将该另一部分的至少一个馏分在第二压缩机(4)中起始于该深冷温度压缩至等于P2或者比P2高或低小于5巴的压力P3，
vi)将因此在第二压缩机中压缩的馏分送回先前交换器中的一个或者交换器中以在其中冷却至-100℃以下的温度，
vii)将在压力P2下的至少一部分空气和在压力P3下的至少一部分空气以及任选在压力P1下的至少一部分料流冷却至它们在其中液化的交换器的冷端，然后在膨胀以后送入空气分离装置的至少一个蒸馏塔中，
viii)在膨胀式涡轮机中膨胀以后将至少50％，优选至少70％的总空气流以气体形式供入装置的至少一个蒸馏塔中，
ix)将空气在塔系统中分离，和
x)将液体氧从一个蒸馏塔中取出，借助泵加压至大于20巴绝对压力的所需压力，通过热交换蒸发，然后再加热以便以气体产物的形式使用，其特征在于将空气在膨胀式涡轮机中起始于压力P1或P2或者P1与P2之间的压力膨胀。
根据本发明另一任选方面：
-将在小于P1的压力下的第三部分空气在交换器中冷却并送去蒸馏，
-第二压缩机与另一膨胀式涡轮机连接，
-分离装置包含中压塔和低压塔，并使来自中压塔的富氮气体在涡轮机中膨胀，
-第二压缩机与涡轮机连接并且用于供应或提取另外或富余功率的系统直接在涡轮机/第二压缩机的共有轴上或者借助齿轮箱结合在涡轮机与第二压缩机之间，
-将在第二压缩机中压缩的馏分和经受另外压缩的部分在空气分离装置的交换器中再混合以便仅形成在压力P2下的单一流，
-压力P3比P2高或低至多2巴，
-将送入蒸馏塔中的至少一部分气态空气在涡轮机中起始于压力P1或者P1与P2之间的中间压力膨胀，
-将送入蒸馏塔中的至少一部分气态空气在涡轮机中起始于压力P2膨胀，
-压力P1为20-25巴，
-压力P2为50-60巴，
-压力P3为50-60巴，
-将在第二压缩机中压缩的一部分空气馏分压缩至压力P2并与在压力P2下的空气部分混合以便在换热器中冷却。
根据本发明另一主题，提供用于通过空气的低温蒸馏制备气态氧的设备，其包含塔系统，第一压缩机，第二压缩机，至少一个换热器，用于将所有或一部分进料空气流送入能使它的压力达到比中压塔的压力大至少5巴的压力P1的第一压缩机中的装置，用于通常通过与水热交换将压力P1下的气体冷却以产生在压力P1和5-45℃，优选15-25℃的温度T1下的空气料流的第一冷却器，用于将在第一压缩机中压缩的在压力P1下的一部分空气压缩至大于P1的压力P2的装置，用于将在P2下的一部分空气冷却至温度T2的第二冷却器，其中T2和T1相差小于10℃，通常小于5℃，用于将该冷却部分送入换热器或者换热器中的一个中以经受冷却至低于或等于-100℃的温度的装置，用于将在压力P1下的另一部分空气引入空气分离装置的换热器或换热器中的一个中以在其中经受冷却至-100℃以下的温度的装置，用于将该另一部分的至少一个馏分送入第二压缩机中的装置，在第二压缩机中起始于该深冷温度至等于P2或者比P2高或低小于5巴的压力P3，用于将因此在第二压缩机中压缩的馏分送回先前交换器中的一个或换热器中以在其中冷却至-100℃以下的温度的装置，用于将在压力P1下和/或在压力P2下和/或在压力P3下的至少一种液化气体送入空气分离装置的至少一个蒸馏塔中的装置，与系统的至少一个塔连接的能够使至少50％，优选至少70％的总空气流膨胀的膨胀式涡轮机，和用于将液体氧从系统的塔中取出的装置，用于将液体加压的泵和用于将泵送液体送入换热器或换热器中的一个中的装置，其特征在于膨胀式涡轮机与第一压缩机的出口连接以接收源自那里的空气，但连接使得它不接收来自第二压缩机的空气。
根据本发明的另一任选方面：
-用于将在压力P2下的一部分空气增压的装置由压缩机组成，
-第二压缩机的出口和用于将压力P2下的一部分空气增压的装置的出口与换热器的至少一个共同通道连接以将在第二压缩机和增压装置增压的两种空气流冷却，
-第二压缩机与不同于空气涡轮机的涡轮机连接，
-第二压缩机与由塔系统提供的氮气涡轮机连接。
借助吸入温度T0为0-50℃，优选5-30℃的压缩机使所有或一部分进料空气流达到比中压塔大至少5巴的压力P1。在压缩机的出口处，通常通过与水热交换将气体冷却以产生在压力P1和5-45℃，优选15-25℃的温度T1下的空气料流。
使一部分该料流经受起始于温度T1和压力P1至大于P1的压力P2的另一压缩步骤，然后通常通过与水热交换冷却至温度T2。T2和T1仅相差小于10℃，通常小于5℃。然后将该流引入空气分离装置的交换器E1中以经受冷却至低于或等于-100℃的温度。
将另一部分该料流在压力P1和温度T1下引入空气分离装置的交换器，任选E1中，以在其中经受冷却至-100℃以下的温度，然后将该部分的至少一个馏分在压缩机中起始于该深冷温度压缩至等于P2或者与P2相差小于5巴的压力。将因此压缩的流送回先前交换器中的一个中以在其中冷却至-100℃以下的温度。
将达到高压的各个流的至少一部分冷却至它们在那里液化的交换器的冷端，然后在膨胀以后送入蒸馏塔中。
任选将在温度T1和压力P1下的第三部分流送入空气分离装置的交换器中。
将至少50％，优选至少70％的总空气流任选在膨胀式涡轮机中由上述压力中的一个膨胀以后，以气体形式供入装置的蒸馏塔中。
将液体从蒸馏塔中取出，借助泵加压至所需压力，通过热交换，特别是在步骤4)期间蒸发，然后再加热以便以气体产物的形式使用。
起始于如下文所述深冷温度将加压料流压缩在与膨胀式涡轮机连接的增压器中进行。
将来自中压塔的富氮气体在涡轮机中膨胀以实现该压缩。
由涡轮机提供的功率明显不同于低温压缩机所需的功率，使得供应(分别地，提取)另外(分别地，富余)功率的系统直接在涡轮机/增压器的共有轴上或者借助齿轮箱结合在涡轮机与增压器之间。
将产生的在压力P2下的流在空气分离装置的交换器中再混合以仅形成在压力P2下的单一流。
参考代表本发明方法的图以更详细的方式描述本发明。
图1和图2表示用于空气分离的低温蒸馏设备的热交换部分。
图3和图4表示布置冷增压器和涡轮机的方法。
为了简化，附图未显示包含至少一个含有中压塔和低压塔双塔的空气分离设备，其中中压塔与低压塔的底部热连接。将空气送入中压塔以及任选低压塔中。将富含氧气和氮气的回流液体从中压塔送入低压塔中。
将富氧液体从低压塔的底部取出，并在将空气冷却的交换器中蒸发。
在图1中，将在压力P0下的空气11提纯。借助吸入温度T0为0-50℃，优选5-30℃的的压缩机1使一部分15进料空气流11达到比中压塔的压力大至少5巴的压力P1。在压缩机1的出口处，将气体在冷却器R2中通常通过与水热交换而冷却，以产生在压力P1和5-45℃，优选15-25℃的温度T1下的空气料流。
使一部分该料流在压缩机2中经受起始于温度T1和压力P1至大于P1的压力P2的另一压缩步骤，然后在冷却器R3中通常通过与水热交换而冷却至温度T2。T2和T1相差小于10℃，通常小于5℃。然后将该冷却流19引入空气分离装置的换热器9中以经受冷却至低于或等于-100℃的温度。
将另一部分17该流在压力P1和温度T1下引入交换器9中，以在其中经受冷却至-100℃以下的温度。然后将该部分17的馏分21在压缩机4中起始于该深冷温度压缩至等于P2的压力P3。将因此压缩的流送回交换器E1中以在其中冷却至-100℃以下的温度。
将一部分43流19和一部分27馏分17、23冷却至它们在其中液化的交换器9的冷端，然后在阀V1、V2中膨胀以后送入双塔中。
至少50％，优选至少70％的总空气流11作为气体形式的流25供入装置的蒸馏塔中。在压力P1下的一部分25空气在膨胀式涡轮机3中膨胀。膨胀式涡轮机具有比压缩机4更低的入口温度。
将液体氧29从低压塔中取出，借助泵31加压至所需压力，通过在交换器9中热交换而蒸发，然后再加热以便以气体产物的形式使用。
将源自中压塔的中压氮气37在交换器9中再加热，在涡轮机7中膨胀并作为流39送去与低压氮气33混合以形成流35。将流35在交换器9中再加热。
在图2中，将空气在交换器中在4个不同的压力下冷却。将在5.5巴的压力P0下的空气分成两部分，一部分13在交换器中冷却。将空气15在压缩机1中冷却，并在其中间水平下发现20-25巴的压力P1和5-45℃，优选15-25℃的温度T1。将该压力和温度下的空气分成两部分。将一部分12在20-25巴的压力P1下送入第二压缩机4中并压缩至50-60的最高压力P3。将在P1和T1下的其余部分13空气送回压缩机1中并在压缩机1的最后阶段中压缩，在冷却器R2中冷却，然后分成两部分。将一部分17送入交换器9中，在那里将它冷却至中间温度。在该温度下，将它分成两部分，将一部分25送入涡轮机3中，将其余部分空气液化并在阀V2中膨胀。将离开冷却器R2的其余部分15空气送入压缩机2中。源自压缩机2的冷却空气在50-60巴的压力P2和温度T2下。T2和T1相差小于10℃，通常小于5℃。将空气21冷压缩并与源自压缩机2的在50-60巴的压力P2下的气体19混合。将待膨胀空气25在比取出送入第二压缩机中的空气更高的另一中间压力下取出。该中间压力为第一压缩机1的出口压力，在P2与P1之间。
在图3中，将空气21压缩的第二压缩机4与将流37膨胀以产生流39的氮气涡轮机7连接。该系统还可包含用于供应或提取另外或富余功率的系统K，其直接在涡轮机/第二压缩机的共有轴上结合在涡轮机与第二压缩机之间。另外，如图4所示，系统K可借助齿轮箱与压缩机和涡轮机连接。

Claims (16)

1.通过空气的低温蒸馏制备气态氧的方法，其中：
i)借助吸入温度T0为0-50℃，优选5-30℃的第一压缩机(1)使所有或一部分(12，15)进料空气流达到比中压塔的压力大至少5巴的压力P1，
ii)通常通过与水热交换而将压力P1下的气体冷却以产生在压力P1和5-45℃，优选15-25℃的温度T1下的空气料流，
iii)使在第一压缩机中压缩的一部分(17，19)空气经受起始于温度T1和压力P1至大于P1的压力P2的另一压缩步骤，然后通常通过与水热交换而冷却至温度T2，其中T2和T1相差小于10℃，通常小于5℃，
iv)然后将该冷却部分(17，19)引入空气分离装置的换热器(9)中以经受冷却至低于或等于-100℃的温度，
v)将另一部分(12，17)空气在压力P1下引入任选来自步骤iv)的空气分离装置的换热器(9)中，以在其中经受冷却至-100℃以下的温度，然后将该另一部分的至少一个馏分(21)在第二压缩机(4)中起始于该深冷温度压缩至等于P2或者比P2高或低小于5巴的压力P3，
vi)将因此在第二压缩机中压缩的馏分送回先前交换器中的一个或者交换器(13)中以在其中冷却至-100℃以下的温度，
vii)将在压力P2下的至少一部分空气和在压力P3下的至少一部分空气(27)以及任选在压力P1下的至少一部分料流冷却至它们在其中液化的交换器的冷端，然后在膨胀以后送入空气分离装置的至少一个蒸馏塔中，
viii)在膨胀式涡轮机(3)中膨胀以后将至少50％，优选至少70％的总空气流以气体形式供入装置的至少一个蒸馏塔中，
ix)将空气在塔系统中分离，和
x)将液体氧(29)从一个蒸馏塔中取出，借助泵(31)加压至大于20巴绝对压力的所需压力，通过热交换蒸发，然后再加热以便以气体产物的形式使用，
其特征在于将空气在膨胀式涡轮机中起始于压力P1或P2或者P1与P2之间的压力膨胀。
2.根据权利要求1的方法，其中将在小于压力P1的压力P0下的第三部分空气送入空气分离装置的一个换热器或换热器中。
3.根据前述权利要求中一项的方法，其中第二压缩机(4)与另一膨胀式涡轮机(，7)连接。
4.根据前述权利要求中一项的方法，其中分离装置包含中压塔和低压塔，并使来自中压塔的富氮气体(37)在涡轮机(7)中膨胀。
5.根据前述权利要求中一项的方法，其中第二压缩机(4)与涡轮机(3，7)连接，并且用于供应或提取另外或富余功率的系统直接在涡轮机/第二压缩机的共有轴上或者借助齿轮箱结合在涡轮机与第二压缩机之间。
6.根据前述权利要求中一项的方法，其中将在第二压缩机(4)中压缩的馏分和经受另外压缩的部分(19)在空气分离装置的交换器(13)中再混合以便仅形成在压力P2下的单一流(43)。
7.根据前述权利要求中一项的方法，其中压力P3比P2高或低至多2巴。
8.根据前述权利要求中一项的方法，其中将送入蒸馏塔中的至少一部分(25)气态空气在涡轮机(3)中起始于压力P1或者P1与P2之间的中间压力膨胀。
9.根据前述权利要求中一项的方法，其中将送入蒸馏塔中的至少一部分气态空气在涡轮机中起始于压力P2膨胀。
10.根据权利要求8或9的方法，其中在涡轮机(3)中膨胀的空气不在具有环境温度以下的入口温度的压缩机中压缩。
11.根据前述权利要求中一项的方法，其中P2为50-60巴，和/或P3为50-60巴。
11.用于通过空气的低温蒸馏制备气态氧的设备，其包含：包含中压塔和低压塔的塔系统，第一压缩机(1)，第二压缩机(2)，至少一个换热器(9)，用于将所有或一部分(12，15)进料空气流送入能使它的压力达到比中压塔的压力大至少5巴的压力P1的第一压缩机中的装置，用于通常通过与水热交换将压力P1下的气体冷却以产生在压力P1和5-45℃，优选15-25℃的温度T1下的空气料流的第一冷却器(R1)，用于将在第一压缩机中压缩的在压力P1下的一部分(19)空气压缩至大于P1的压力P2的装置(1，2)，用于将在P2下的一部分空气冷却至温度T2的第二冷却器(R2，R3)，其中T2和T1相差小于10℃，通常小于5℃，用于将该冷却部分(19)送入换热器(9)或者换热器中的一个中以经受冷却至低于或等于-100℃的温度的装置，用于将在压力P1下的另一部分(12)空气引入空气分离装置的换热器(9)或换热器(9)中的一个中以在其中经受冷却至-100℃以下的温度的装置，用于将该另一部分的至少一个馏分(21)送入第二压缩机中的装置，在第二压缩机(4)中起始于该深冷温度至等于P2或者比P2高或低小于5巴的压力P3，用于将因此在第二压缩机中压缩的馏分送回先前交换器中的一个或换热器中以在其中冷却至-100℃以下的温度的装置，用于将在压力P2下的至少一种液化气体和在压力P3下的一种液化气体(27)和任选在压力P1下的一种液化气体送入空气分离装置的至少一个蒸馏塔中的装置，与系统的至少一个塔连接的能够使至少50％，优选至少70％的总空气流膨胀的膨胀式涡轮机(3)，和用于将液体氧(29)从系统的塔中取出的装置，用于将液体加压的泵和用于将泵送液体送入换热器或换热器中的一个中的装置，其特征在于膨胀式涡轮机与第一压缩机的出口连接以接收源自那里的空气，但连接使得它不接收来自第二压缩机的空气。
12.根据权利要求11的设备，其中用于将在压力P2下的一部分空气增压的装置(1，2)由压缩机(2)组成。
13.根据权利要求11或12的设备，其中第二压缩机的出口和用于将压力P2下的一部分空气增压的装置的出口与换热器的至少一个共同通道连接以将在第二压缩机和增压装置增压的两个空气流冷却。
14.根据权利要求11-13中一项的设备，其中第二压缩机与不同于空气涡轮机(3)的涡轮机(7)连接。
15.根据权利要求14的设备，其中第二压缩机(4)与由塔系统提供的氮气涡轮机(7)连接。
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