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CN1052940A - 粗氩提取方法 - Google Patents

粗氩提取方法 Download PDF

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CN1052940A
CN1052940A CN89107084A CN89107084A CN1052940A CN 1052940 A CN1052940 A CN 1052940A CN 89107084 A CN89107084 A CN 89107084A CN 89107084 A CN89107084 A CN 89107084A CN 1052940 A CN1052940 A CN 1052940A
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crude argon
air
recompression
decompression
heat exchange
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威谦·罗德
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Linde GmbH
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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
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    • 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
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
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    • 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
    • F25J3/04096—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 argon or argon enriched stream
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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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    • F25J3/04—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
    • F25J3/04103—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 using solely hydrostatic liquid head
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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
    • F25J3/04248—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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    • F25J3/00—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
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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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
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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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/58—One fluid being argon or crude argon
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air

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  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

本发明涉及一种低温精馏空气提取气态粗氩的 方法，其中将一部分(18)压缩过的空气。(在19中)再 压缩。使再压缩过的空气部分地(管22)与以液态形 式获得并处于高压下正在汽化的粗氩逆流液化(在 16中)。

Description

本发明涉及一种低温精馏空气提取气态粗氩的方法，其中将空气压缩、预净化、冷却并送向二级精馏的压力级，二级精馏后得到液体状态的粗氩。
这样的方法由联邦德国专利局公开说明书DE-OS  34  28  968已知，其中由粗氩塔顶部采出液态粗氩或从粗氩塔采出后进行液化。利用流体静力学位能使液态粗氩升压，以便将一般约在大气压力下得到的粗氩升至进一步加工所需要的大约3.5至5巴的压力。这种处理方法的优点是可以节省一台例如在以气态采出粗氩时所必需的粗氩压缩机。
处于高压下的粗氩必须汽化才能提取纯氩。在DE-OS  34  28  968的工艺中，将汽化所致的冷通过与氮换热来释出。然而，在将空气压缩到约6巴的低压设备中，这样一种工艺气流不具备足够的高压，以致于不能使该气流在粗氩高压汽化的同时液化，从而只能利用气态氮的热容而不能利用其潜热来释出粗氩汽化所致的冷。因此，用于粗氩汽化的换热器必须构制得比较大。另外，还要向精馏过程加入一种与以液态采出的粗氩量数量相当的液体，因此还必须在其它位置另外制冷。
本发明的任务在于，提供一种本说明书开头所述类型的在高压下提取气态粗氩的改进方法，该方法可以极低的能耗及设备费用获得特别高的产率。
该任务由下述措施完成：在冷却之前从空气中分出一股分流，将其再压缩、冷却、接着使之部分地作功减压，并导入精馏的低压级，在减压前从再压缩后的空气中分出一部分，使之与液态粗氩换热。
空气分流的再压缩本身已由联邦德国专利说明书DE-PS  28  54  508已知。在该专利说明书所述的方法中不包括粗氩的提取，而是将所有的再压缩空气作功减压。在本发明的方法中，也用处于高压下的空气为液态粗氩提供热量，并使其汽化。由于再压缩后的空气处于高压下，它在与汽化的粗氩换热时被液化。所以，空气的潜热也能用于接受粗氩的汽化冷，由此，一方面较少的工艺气流对于汽化即已足够，另一方面还可产生精馏省冷所必需的液体。
有利的是，将再压缩后空气减压时得到的功用于再压缩。这样，可在没有外加能量的情况下提高压力。通过再压缩机和减压机的机械耦合，可最有效地进行能量传递。
在本发明进一步的优选方案中，使再压缩后空气的未减压部分与以液态获取的粗氩换热后送入精馏过程。在粗氩汽化时大部分液化的空气因而可作为回流加入精馏塔，最好加到压力级。
再压缩空气的未减压部分与以液态获取的粗氩换热后也可与粗氩塔顶部的气体进行换热，（由该塔采出粗氩，）以便以有利的方式将最大限度的冷量用于在精馏过程中产生液体。换热时汽化的空气可导入低压塔。
下面借助于附图所示的实施例详细解释本发明。附图示出本发明方法从吸入待分离空气到汽化并加热粗氩的一种实施方式，图中将不太重要且已知的工艺步骤大幅度简化。粗氩汽化后接着的精细提取粗氩的处理步骤没有示出。
空气经管道1吸入，在空气压缩机2中压缩，在提纯级3（例如一个分子筛设备）预提纯，经管4送入总换热器5中，在此空气被产物流逆流冷却。冷空气送往二级精馏塔6的压力级7，该级在5.0至7.0巴压力下工作，并经冷凝-蒸发器9与低压级8以换热方式相联连。
富含氧的液体由压力级7的底部经管道10采出，并在合适的位置节流进入处于1.0至2.0巴压力下的基压级8。由低压级作为产物流导出氮（管11）和氧（管12），随后在总环热器5中预热到接近于环境温度。此外，另一个氩浓度较高的氧气流经管13导出并送入一个粗氩塔14。经同一管线13，也有液体从粗氩塔14回流到低压级8中去。
从粗氩塔14中作为产物采出液态粗氩（管15）。该粗氩也可全部或部分地气态采出并随后液化，如DE-OS  34  28  968所建议的那样。液态粗氩通过利用沿管15约30至40m的流体静力学位压头升压到3.0至5.0巴，最好约4.0巴，在粗氩汽化器16中汽化，在总换热器5中加热到大约环境温度，并经管线17送往另一个提纯级。
按照本发明，将一部分空气在预提纯（3）后经管18分出，在再压缩机19中进一步压缩到7.0至11.0巴的压力，在总换热器5中冷却到中等温度，绝大部分在涡轮发动机20中减压作功，（经管21）导入低压级8中。涡轮发动机20与再压缩机19机械耦合。按照本发明的主要构思，一部分再压缩后的空气经管22在减压（20）前分出，正与汽化的粗氩成逆流方式穿过粗氩汽化器16，由此至少部分地液化，随后经管23和节流阀24作为回流导入压力级7。

Claims (4)

1、低温精馏空气提取气态粗氩的方法，其中对空气(1)进行压缩(2)、预提纯(3)和冷却(5)，并导入二级精馏(6)的压力级(7)，二级精馏(6)后得到液体状态的粗氩(15)，其特征在于，将一部分空气(18)在冷却前分出，再压缩(19)，冷却，随后使之部分地作功减压(20)，并导入精馏的低压的(7)，将再压缩过的空气的一部分(22)在减压(20)前分出，使之与以液态状态得到的粗氩(5)进行换热(16)。
2、权利要求1所述的方法，其特征在于，将再压缩空气减压（20）时获得的功用于再压缩（19）。
3、权利要求1或2所述的方法，其特征在于，将再压缩过的空气的未减压部分（22）在与以液体状态获得的粗氩换热（16）后送入精馏过程。
4、权利要求1至3中任一项所述的方法，其特征在于，使再压缩过空气的未减压部分（22），在与以液体状态获得的粗氩换热（16）后，再与粗氩塔（14）顶气体换热，由该粗氩塔采出粗氩（15）。
CN89107084A 1988-10-12 1989-09-16 粗氩提取方法 Withdrawn CN1052940A (zh)

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DEP3834793.8 1988-10-12
DE3834793A DE3834793A1 (de) 1988-10-12 1988-10-12 Verfahren zur gewinnung von rohargon

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CN113959179A (zh) * 2021-12-22 2022-01-21 杭州制氧机集团股份有限公司 一种用于液氩提纯的装置及方法

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US5255522A (en) * 1992-02-13 1993-10-26 Air Products And Chemicals, Inc. Vaporization of liquid oxygen for increased argon recovery
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CA2000595A1 (en) 1990-04-12
US4932212A (en) 1990-06-12
EP0363861A2 (de) 1990-04-18
DE3834793A1 (de) 1990-04-19

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