CN1045656C - 为使用空气组分的设备提供加压气体的方法和装置 - Google Patents

为使用空气组分的设备提供加压气体的方法和装置 Download PDF

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CN1045656C
CN1045656C CN94106533A CN94106533A CN1045656C CN 1045656 C CN1045656 C CN 1045656C CN 94106533 A CN94106533 A CN 94106533A CN 94106533 A CN94106533 A CN 94106533A CN 1045656 C CN1045656 C CN 1045656C
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gas
liquid
basin
pressure
air
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CN1108698A (zh
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R·阿金斯
A·贵拉德
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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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • 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
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
    • C21C7/00—Treating molten ferrous alloys, e.g. steel, not covered by groups C21C1/00 - C21C5/00
    • C21C7/04—Removing impurities by adding a treating agent
    • C21C7/068—Decarburising
    • C21C7/0685—Decarburising of stainless steel
    • 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
    • F25J3/04078—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
    • F25J3/04084—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 nitrogen
    • 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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    • F25J3/02—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
    • F25J3/04078—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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    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
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    • 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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    • F25J3/044—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 single pressure main column system only
    • 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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    • 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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    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
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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
    • F25J3/04551—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the metal production
    • F25J3/04557—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the metal production for pig iron or steel making, e.g. blast furnace, Corex
    • 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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    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
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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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    • 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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Abstract

本发明涉及为消耗空气组分的装置提供加压气的方法及装置。该方法包括在与热交换导管组(11)相连的蒸馏设备(13)中蒸馏空气，加压产热流体在热交换导管组(11)中循环；至少间歇地将液态气体供给贮罐(23)；使从贮罐抽出的液态气体达到汽化压力并在该汽化压力下将其于热交换导管组(11)中汽化。本发明也涉及供应氧气、氮气和氩气给生产不锈钢的装置如利用氩氧脱碳法的电弧炉。

Description

为使用空气组分的设备提供加压气体的方法和装置
本发明涉及一种从在深冷温度和一定压力下可液化的带压气体为耗气设备提供至少一种空气组分的方法。
本发明特别适用于为某些冶金设备提供氧气和/或氮气和/或氩气。
下文中的压力是绝对压力。
某些冶金设备同时消耗加压的气态氧、加压的气压氮和加压的气态氩，例如适用于生产不锈钢的电弧炉(氩氧脱碳法)。这些气体使用的压力通常约为25巴，其消耗量很不同，这就需要使用能提供约30-40巴压力的“缓冲罐”或辅助罐。
氧气和氮气通常使用空气蒸馏设备就地生产，而所需的氩气量比该蒸馏设备的氩气生产能力要大得多，氩气的生产能力不可能超过氧气流量的5％。所以，必须由外部氩气源提供给该耗气设备。在先有技术中，这一氩气在辅助设备如热水浴中汽化。
此外，由于技术的发展以及生产的需要，逐渐提高了电弧炉中氧气的消耗量，这一氧气耗量最终会大大超过该蒸馏设备的就地分离能力。
本发明的目的是提供一种能以特别经济的方式满足耗气设备气体需要量的方法，这一气体需要量甚至可有很大的变化。
为此，本发明提供上述类型的方法，其特征在于：
——空气在与热交换导管组相联的蒸馏设备中蒸馏，至少一种比蒸馏设备的操作压力高得多的产热流体在热交换导管组中循环；
——以间歇方式给贮罐提供处于液相的所述气体；
——使从贮罐中抽出的液相气体处于比贮罐压力高的汽化压力，并使它在与蒸馏设备相联的热交换导管组内在该汽化压力下汽化生产至少一部分加压的气体。
该法可有以下的一个或多个特征：
——至少一部分贮量由外部来源提供；
——所述气体的汽化/再加热热量至少部分通过产生另外的液体氧和/或液体氮的方法进行回收；
——使从蒸馏设备中抽出液相空气组分处于比抽出压力高的汽化压力下，并使该液相空气组分在这一汽化压力下，在热交换导管组内汽化同时生产至少一种加压的该空气组分；
——所述的气体是空气，其流速大于当时通过蒸馏设备生产的该气体流速；
——所述的汽化过程连续进行；
——在某一时期，将处于液相的气体从蒸馏设备送到贮罐，而在另一时期则进行所述的汽化过程。
本发明另一目的是提供适合于实施这种方法的装置。该装置包括与热交换导管线相联的空气蒸馏设备，热交换导管组包括至少一种比蒸馏设备的操作压力高得多的高压产热流体的通道，该装置的特征在于，它包括一个适用于至少间歇提供处于液相的所述气体的贮罐和与该贮罐上游和在热交换导管组内加压气体汽化通道下游相连的所述液态气体的压缩设备。
该装置可有一个或多个如下的特征：
——压缩设备也可与辅助汽化设备的下游相连；
——所述的气体是空气，压缩设备仅与贮罐相连，如果需要的话，将贮罐与蒸馏设备相连；
——该装置有一台用来传输处于液相的所述气体的泵，其入口与蒸馏设备相连；
——泵的出口连接到热交换导管组的汽化通道上，它与连接压缩设备的热交换导管组分开。
现在参照附图描述本发明的实施方案的一些例子，其中：
——图1是本发明的装置示意图；
——图2和3是两个改进装置示意图。
适用于为耗气设备1(它通常是实现氩氧脱碳法冶金的典型设备)提供以下气体的设备示于图1：一方面通过管线2提供加压的气态氧，另一方面通过管线3提供加压的气态氮，以及通过管线4提供氩气。这一设备也生产低压气态氮(也就是说接近常压的气态氮)以及液体氧和液体氮，这些液体也处于约常压下。
该装置主要有：常压空气压缩机5；致冷设备组6；用吸附法干燥并从空气中脱除二氧化碳的设备7；鼓风机8以及膨胀透平9(它们的转子同轴键合，鼓风机装有空气或水致冷器12，蒸馏设备13；相分离器17；液体氮贮罐18；液体氧泵19；液体氧贮罐20；液体氮泵21；液体氩泵22和液体氩贮罐23。蒸馏设备13由叠形双塔构成，它包括在约5至6巴下操作的中压塔14，其顶上有在约1.2巴下操作的低压塔15，塔14的顶部通过汽化-冷凝器16与塔15的底部相连。三个贮罐18、20和23处于接近常压下。
在操作中，要蒸馏的空气在5中压缩，然后在6中冷却，在7中净化除去水和二氧化碳，然后全部在8中进一步压缩，并在10中使温度达到常温左右。处于比塔14的中压高得多的高压下的进一步压缩后的空气全部在热交换导管组11中冷却到中等温度下。在这一温度下，部分空气被冷却和液化，如果需要的话，通过热交换导管组的冷端过冷，然后在膨胀阀24和25中膨胀后，在塔14和15之间分配。
在温度T下，其余的空气在9中膨胀到中压，然后送入塔14底部。
图中还示出传统的管线和双叠式管线，也就是说在低压塔顶生产在此低压下的纯氮气。分别用于提升“富液”(富氧的空气)、“下贫液”(不纯的氮)和“上贫液”(实际上是纯氮)的管线26-28分别从塔14的底部及塔14上段的中部引出，并通过冷却器12，并各自装有膨胀阀。
导入设备1的氧以液体的形式从塔15的底部抽出，用泵19达到使用压力，并在热交换导管组内汽化和再加热到大约常温。
同样，导入设备1的氮以液体的形式从塔14的顶部抽出，用泵21达到使用压力，并在热交换导管组内汽化和再加热。
导入设备1的氩以液体的形式贮存在贮罐23中，用槽车29供料。从该贮罐中抽出液体氩，用泵22达到使用压力，并在热交换导管组内汽化和再加热。
通常，形成设备的残留气体的不纯氮气和塔15顶部的纯氮产物先在12中然后在11中再加热，然后分别经管线30和31离开装置。
此外，该装置还生产液体氮，在送入相分离器17以前通过管线28抽出并在膨胀阀32中膨胀。将该相分离器的液体送到贮罐18，而使其气相与塔15顶部的气态氮流合并。该装置还生产液体氧，从塔15的底部抽出，并通过管线33送入贮罐20。正如将看到的那样，通过液体氩的汽化和再加热引入到热交换导管组的外加冷量被回收，以生产液体氧和/或液体氮。
作为改进，空气蒸馏设备可包括以通常的方式与塔15结合的氩生产塔，以便生产一部分供设备1的氩气。
图2和3涉及以大于蒸馏设备13的分离能力的流速为设备1提供加压的气态氧。在这两张图中，所示的是双塔13和氧的回路；除了氩回路不同外，设备的其余部分与图1相同，氩回路被省去。
在图2的情况下，一方面由塔15的底部给贮罐20供料，另一方面用槽车34供料，而泵19的入口连接到贮罐20的底部。因此，可将要汽化和再加热的液体氧以所需的流速提供给热交换导管组。汽化的过量液体氧(也就是说由槽车提供的数量)提供冷量，它可如前那样以送到贮罐18的外加的液体氮的形式被回收。
如图3所示，作为改进，图2中可增加一个第二液体氧泵36，其入口连接到塔15的底部，两台泵的出口连接到热交换导管组的相同一汽化通道上，或甚至连接到分开的汽化通道。
正如混合管线表明的那样，在必要的情况下，例如为了安全，泵19和/或泵36的出口也可连接到常用的辅助汽化设备35如浴上。在这一操作方式中，在汽化的液体氧中所含的冷量当然就损失了。
在图2和3的每种情况下，在耗气设备对氧的需要量低时和/或在电能费用低时，蒸馏设备的产品可逐渐装满贮罐20，而在高需要量和/或高电能费用时，逐渐抽空这一贮罐，如果需要的话，可由槽车供给。如果氧的需要量持续高于蒸馏设备的生产能力，当然必须定期由槽车供给。
作为改进，图3中的贮罐20可不连接到双塔13上，并且可只由槽车供给。在这种情况下，由槽车供给的氧的纯度可能与双塔生产的氧的纯度不同。
本发明也可适用于有单塔的空气蒸馏设备，例如氩汽化方案，如图1的方案，但其中设备13是单一的高纯氮型的氮生产塔，与上述的方案类似的克劳德空气循环相连。在这种情况下，氩的汽化可生产优质液体氮。

Claims (13)

1．一种为消耗至少一种空气组分的设备(1)提供加压气体的方法，该加压气体在深冷温度下于该加压下是可液化的，其中
空气在包括至少一个与热交换导管组相连的蒸馏塔的蒸馏设备(13)中蒸馏，其中至少一种由欲蒸馏的空气组成的加热流体在明显高于蒸馏设备的操作压力下循环；
至少以间歇方式给贮罐(23；20)提供液态形式的所述气体；和
通过从所述的贮罐抽出处于液相的气体使它处于比贮罐压力高的汽化压力下，并使它在与蒸馏设备相连的热交换导管组(11)内在该汽化压力下汽化，生产至少一部分所述的加压气体，
其特征在于在蒸馏设备之外的贮罐(23；20)至少一部分由外源(29,34)而不是蒸馏设备本身供料；和
汽化/再加热所述气体的热量至少部分被生产另外的液体氧和/或液体氮流所回收且液体不从贮罐送到蒸馏塔。
2．根据权利要求1的方法，其特征在于，通过从蒸馏设备(13)中抽出处于液相的一种空气组分，使它处于比抽出压力高的汽化压力下，并使该液体在该汽化压力下，在热交换导管组(11)内汽化，同时生产至少一种空气组分。
3．根据权利要求1或2的方法，其特征在于，所述的气体是空气中的气体，其流速大于同时用蒸馏设备(13)生产的气体流速。
4．根据权利要求1或2的方法，其特征在于，所述的汽化连续进行。
5．根据权利要求3的方法，其特征在于，在某一时期处于液相的气体从蒸馏设备(13)送到贮罐(20)，而在另一时期则进行所述的汽化过程。
6．根据权利要求1或2的方法，其中液体的组成与蒸馏设备的产品不同。
7．一种为消耗至少一种空气组分的设备提供加压气体的装置，该加压气体在深冷温度下于该加压下是可液化的，该装置包括一种空气蒸馏设备(13)，该蒸馏设备包括至少一个与热交换器导管组(11)相连的蒸馏塔，热交换导管组包括至少一种处于比蒸馏设备的操作压力高得多压力的由欲蒸馏的空气组成的加热流体；一种用作处于液态的所述气体的贮罐(23；20)，该贮罐适合至少以间歇方式供料；和与贮罐上游和在用于汽化该加压气体的热交换导管组(11)的通道下游相连的用于压缩处于液态的该气体的压缩设备(22；19)，其特征在于贮罐在蒸馏塔之外并且至少部分由外源(29；34)而不是蒸馏设备本身供料且没有用来从贮罐输送液体到蒸馏塔的设备。
8．根据权利要求7的装置，其特征在于，压缩设备(19)也可与辅助汽化设备(35)的下游相连。
9．根据权利要求7或8的装置，其特征在于，所述的气体是空气，压缩设备(19)仅与贮罐(20)相连，如果需要的话，贮罐与蒸馏设备(13)相连。
10．根据权利要求9的装置，其特征在于，该装置有一台用于处于液相的所述气体的泵(36)，其入口与蒸馏设备(13)相连。
11．根据权利要求10的装置，其特征在于，泵(36)的出口与热交换导管组(11)的汽化通道相连，该通道与压缩设备(19)的出口是分开的。
12．根据权利要求7或8的装置，其中液体的组成与蒸馏产品的组成不同。
13．根据权利要求12的装置，其中液体是液态氩。
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DE69406192T3 (de) 2001-09-20
CA2125230A1 (fr) 1994-12-08
EP0628778B1 (fr) 1997-10-15
CA2125230C (fr) 2002-12-10
FR2706195B1 (fr) 1995-07-28
DE69406192T2 (de) 1998-07-30
EP0628778B2 (fr) 2001-03-21
EP0628778A1 (fr) 1994-12-14
FR2706195A1 (fr) 1994-12-16
ES2109627T5 (es) 2001-06-16
US5505052A (en) 1996-04-09
CN1108698A (zh) 1995-09-20
JPH06347163A (ja) 1994-12-20
ES2109627T3 (es) 1998-01-16
US5566556A (en) 1996-10-22

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