CN104501530B - 一种利用多套空分制取的粗氩提取高纯液氩的装置及方法 - Google Patents

一种利用多套空分制取的粗氩提取高纯液氩的装置及方法 Download PDF

Info

Publication number
CN104501530B
CN104501530B CN201410820647.9A CN201410820647A CN104501530B CN 104501530 B CN104501530 B CN 104501530B CN 201410820647 A CN201410820647 A CN 201410820647A CN 104501530 B CN104501530 B CN 104501530B
Authority
CN
China
Prior art keywords
argon
tower
crude
liquid
crude argon
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201410820647.9A
Other languages
English (en)
Other versions
CN104501530A (zh
Inventor
孙健
李玲
韩松
韩一松
王定伟
徐庆
韩帅
谭芳
张华涛
夏鸿雁
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hang Yang Group Co ltd
Original Assignee
Hangzhou Hangyang Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hangzhou Hangyang Co Ltd filed Critical Hangzhou Hangyang Co Ltd
Priority to CN201410820647.9A priority Critical patent/CN104501530B/zh
Publication of CN104501530A publication Critical patent/CN104501530A/zh
Application granted granted Critical
Publication of CN104501530B publication Critical patent/CN104501530B/zh
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • F25J3/0409—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
    • 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
    • F25J3/04248—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
    • 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
    • F25J3/04642—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
    • F25J3/04678—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 cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/04642—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
    • F25J3/04703—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 being arranged in more than one vessel
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/58—Argon
    • 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
    • F25J2230/58—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being argon or crude argon
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

一种利用多套空分制取的粗氩提取高纯液氩的装置及方法，所述的装置包括—用于获得产品液氩的提纯系统，一与所述粗氩Ⅰ塔中部位置相连通的原料粗氩气或粗液氩输入系统，至少—台用于液体回流的循环液氩泵和一台循环液氧泵；利用在一套空分装置中增加氩提取装置，将多套带增效塔空分中的粗氩气或粗液氩提取成纯液氩；它可以有效将粗氩气或粗液氩提取为纯液氩产品，变废为宝；同时对比与每套空分装置增加提氩系统减少了设备，降低投资成本。

Description

一种利用多套空分制取的粗氩提取高纯液氩的装置及方法
技术领域
本发明涉及一种通过低温精馏法，在单套空分设备中增加提氩装置，提纯一套或者多套空分中粗氩气或者粗液氩，将其制取成高纯液氩的装置及方法，属于空分技术领域。
背景技术
近年来随着煤化工行业的崛起，促使空分向大型化不断的跃进。空分中氧气作为煤化工高炉的气化气，氮气作为产品气、输送气等，都为煤化工必不可少原料。而高纯液氩在空分中仅作为副产品输出。所以煤气化设备所配套的空分设备多不带提取氩功能，但为了有效提高氧的提取率来节省能耗，这些空分多采用带增效塔流程。
虽为空分的副产品，高纯氩却广泛应用于工业中。由于它的性质十分不活泼，可应用于飞机制造、造船、原子能工业和机械工业等行业，还可以作为焊接、电子工业的保护气及灯具的填充气等。若有良好的销售渠道，空分设备配备提氩系统产生的经济利益是可观的。
发明内容
本发明的目的在于克服现有技术存在的不足，而提供一种利用多套带增效塔空分中的粗氩气或粗液氩，仅对一套空分设备进行改造增加提氩系统，将多套的粗氩气、粗液氩精馏提取纯液氩，从而变废为宝，增加经济效益的利用多套空分制取的粗氩提取高纯液氩的装置及方法。
本发明的目的是这样实现的：所述的利用多套空分制取的粗氩提取高纯液氩的装置,该装置主要包括：
—用于获得产品液氩的提纯系统，该系统至少包括：利用多套空分中的一套空分，并将该套空分中带有冷凝器的增效塔作为粗氩Ⅱ塔，另配置有一台粗氩Ⅰ塔、一台含有冷凝器和蒸发器的纯氩塔；
一与所述粗氩Ⅰ塔中部位置相连通的原料粗氩气或粗液氩输入系统，该系统至少包括如下装置中的一种：一将远距离布置多套空分装置排放的粗氩气汇集于一体的汇集器、以及将汇集后的粗氩气进行增压的压缩机和将增压后的高温粗氩气冷却的板式换热器；一将近距离布置多套空分装置排放的粗氩气汇集于一体的汇集器；或一将多套空分装置排放的粗液氩作为原料回流液汇总在一起的贮槽、以及将粗液氩进行加压的粗液氩泵；
至少—台用于液体回流的循环液氩泵和一台循环液氧泵。
本发明所述粗氩Ⅰ塔的底部设置有氩馏分气体导入口，该氩馏分气体导入口与空分精馏塔的上塔设置的氩馏分气体出口连接；所述粗氩Ⅰ塔的顶部设置有粗氩气排出口，该粗氩气排出口通过管道连接于粗氩Ⅱ塔的底部导入口；所述粗氩Ⅱ塔上部冷凝器下方的粗液氩出口连接于纯氩塔中上部设置的粗液氩进口；并在纯氩塔的底部设置有纯液氩排出口；
所述的循环液氩泵分别连接于粗氩Ⅱ塔底部氩馏分出口与粗氩Ⅰ塔顶部回流液进口；所述循环液氧泵分别连接于粗氩Ⅰ塔底部粗液氧出口与该粗氩Ⅰ塔上塔回流口。
一种使用上述装置进行提取高纯液氩的方法，该方法使用的是一与所述粗氩Ⅰ塔中部位置相连通的原料粗液氩输入系统，所述的提取方法是：
来自多套空分装置排放的原料粗液氩经管道被集中送入粗液氩贮槽，再从贮槽经泵加压进入粗氩Ⅰ塔中部相应位置进行提纯精馏；
从空分精馏塔的上塔相应部位抽出含氩量约9.18％的氩馏分气体；氩馏分直接从粗氩Ⅰ塔的底部导入，同时将来自多套空分装置的粗液氩送入粗氩Ⅰ塔组份相近的位置；从粗氩Ⅱ塔底部排出的粗液氩经液氩泵加压后进入粗氩Ⅰ塔Ⅰ上部作为回流液；粗氩气自粗氩Ⅰ塔顶部排出，经粗氩Ⅱ塔底部导入；粗氩Ⅱ塔中的粗氩冷凝器采用过冷后的液空作冷源，粗氩Ⅱ塔上升气体在粗氩冷凝器中大部分被冷凝，液体返回粗氩Ⅱ塔顶部作为回流液，其余的粗液氩进入纯氩塔中继续精馏；
粗液氩从纯氩塔中上部进入，与此同时在纯氩塔中的纯氩蒸发器冷凝侧利用下塔压力氮作为热源，使纯氩塔底部的液氩蒸发，成为上升蒸气，而压力氮被冷凝成液氮并节流进入空分精馏塔的上塔；纯氩冷凝器利用过冷液氮作为冷源，冷却纯氩塔顶部的上升蒸气，使纯氩塔顶部产生回流液，以保证塔内的精馏，实现氩氮分离，从而在纯氩塔底部得到纯液氩；同时，在纯氩塔的顶部排放一定量的余气，保证精馏的正常进行。
本发明另一种使用上述装置进行提取高纯液氩的方法，该方法使用的是一与所述粗氩Ⅰ塔中部位置相连通的原料粗氩气输入系统，所述的提取方法是：
来自多套空分装置排放的原料粗氩气经管道被汇集后，经压缩机加压送入冷箱内板式换热器，经冷却后送入粗氩Ⅰ塔中部相应位置进行提纯精馏；
从空分精馏塔的上塔相应部位抽出含氩量约9.18％的氩馏分气体；氩馏分直接从粗氩Ⅰ塔的底部导入，同时将来自多套空分装置的粗氩气送入粗氩Ⅰ塔组份相近的位置；从粗氩Ⅱ塔底部排出的粗液氩经液氩泵加压后进入粗氩Ⅰ塔上部作为回流液；粗氩气自粗氩Ⅰ塔顶部排出，经粗氩Ⅱ塔底部导入；粗氩Ⅱ塔中的粗氩冷凝器采用过冷后的液空作冷源，粗氩Ⅱ塔上升气体在粗氩冷凝器中大部分被冷凝，液体返回粗氩Ⅱ塔顶部作为回流液，其余的粗氩气进入纯氩塔中继续精馏；
粗液氩从纯氩塔中上部进入，与此同时在纯氩塔中的纯氩蒸发器冷凝侧利用下塔压力氮作为热源，使纯氩塔底部的液氩蒸发，成为上升蒸气，而压力氮被冷凝成液氮并节流进入空分精馏塔的上塔；纯氩塔中的纯氩冷凝器利用过冷液氮作为冷源，冷却纯氩塔顶部的上升蒸气，使纯氩塔顶部产生回流液，以保证纯氩塔内的精馏，实现氩氮分离，从而在纯氩塔底部得到纯液氩；同时，在纯氩塔的顶部排放一定量的余气，保证精馏的正常进行。
本发明是对多套空分中的粗氩气或粗液氩进行提取纯液氩的装置和方法，它避免了对每套空分进行改造增加多套提氩系统，有效减少了设备的投资和工程总投资，最小限度的对设备进行改造，充分利用了单套空分设备氩提取系统的分离能力，同时能够变废为宝，有效的增加经济效益。
本发明具有以下特点：
1)本发明的原料气体为空分装置排放的粗氩气或粗液氩，单独对一套带增效塔的空分进行改造，增加提氩装置，避免了对每套空分进行改造增加多套提氩系统，有效减少了设备的投资和工程总投资。最小限度的对设备进行改造，充分利用了单套空分设备提氩系统的分离能力，同时能够变废为宝，有效的增加经济效益；
2)本发明还提供了粗氩气或粗液氩两种形式的原料来提取纯液氩，具有更广的适用性；
3)本发明所采用的制冷方法还可以通过向精馏塔补充液氮的方式来增大液氩产量，在液氩价格高于液氮价格时，可以通过类似置换的方式使得液氩多产。
附图说明
图1是本发明所述采用低温精馏法提取粗液氩获取纯液氩产品的装置流程示意图。
图2是本发明所述采用低温精馏法提取粗氩气获取纯液氩产品的装置流程示意图。
具体实施方式
下面将结合附图及实施例对本发明作详细的介绍：图1、2所示，本发明所述的利用多套空分制取的粗氩提取高纯液氩的装置,该装置主要包括：
—用于获得产品液氩的提纯系统，该系统至少包括：利用多套空分中的一套空分，并将该套空分中带有冷凝器1的增效塔作为粗氩Ⅱ塔，另配置有一台粗氩Ⅰ塔、一台含有冷凝器2和蒸发器3的纯氩塔4；
一与所述粗氩Ⅰ塔中部位置相连通的原料粗氩气或粗液氩输入系统，该系统至少包括如下装置中的一种：一将远距离布置多套空分装置排放的粗氩气5汇集于一体的汇集器6、以及将汇集后的粗氩气进行增压的压缩机7和将增压后的高温粗氩气冷却的板式换热器8；一将近距离布置多套空分装置排放的粗氩气汇集于一体的汇集器；或一将多套空分装置排放的粗液氩9作为原料回流液汇总在一起的贮槽10、以及将粗液氩9进行加压的粗液氩泵11；
至少—台用于液体回流的循环液氩泵12和一台循环液氧泵13。
图中所示，所述粗氩Ⅰ塔的底部设置有氩馏分气体导入口，该氩馏分气体导入口与空分精馏塔的上塔设置的氩馏分气体出口连接；所述粗氩Ⅰ塔的顶部设置有粗氩气排出口，该粗氩气排出口通过管道连接于粗氩Ⅱ塔的底部导入口；所述粗氩Ⅱ塔上部冷凝器下方的粗液氩出口连接于纯氩塔中上部设置的粗液氩进口；并在纯氩塔的底部设置有纯液氩排出口；
所述的循环液氩泵12分别连接于粗氩Ⅱ塔底部氩馏分出口与粗氩Ⅰ塔顶部回流液进口；所述循环液氧泵分别连接于粗氩Ⅰ塔底部粗液氧出口与空分精馏塔14的上塔回流口。
图1所示，本发明所述的一种使用所述装置进行提取高纯液氩的方法，该方法使用的是一与所述粗氩Ⅰ塔中部位置相连通的原料粗液氩输入系统，所述的提取方法是：
来自多套空分装置排放的原料粗液氩9经管道被集中送入粗液氩贮槽10，再从贮槽10经泵11加压进入粗氩Ⅰ塔中部相应位置进行提纯精馏；
从空分精馏塔14的上塔相应部位抽出含氩量约9.18％的氩馏分气体；氩馏分直接从粗氩Ⅰ塔的底部导入，同时将来自多套空分装置的粗液氩汇送入粗氩Ⅰ塔组份相近的位置；从粗氩Ⅱ塔底部排出的粗液氩经液氩泵12加压后进入粗氩Ⅰ塔上部作为回流液；粗氩气自粗氩Ⅰ塔顶部排出，经粗氩Ⅱ塔底部导入；粗氩Ⅱ塔中的粗氩冷凝器1采用过冷后的液空作冷源，粗氩Ⅱ塔上升气体在粗氩冷凝器1中大部分被冷凝，液体返回粗氩Ⅱ塔顶部作为回流液，其余的粗液氩进入纯氩塔4中继续精馏；
粗液氩从纯氩塔4中上部进入，与此同时在纯氩塔4中的纯氩蒸发器3冷凝侧利用下塔压力氮作为热源，使纯氩塔底部的液氩蒸发，成为上升蒸气，而压力氮被冷凝成液氮并节流进入空分精馏塔14的上塔；纯氩冷凝器2利用过冷液氮作为冷源，冷却纯氩塔4顶部的上升蒸气，使纯氩塔4顶部产生回流液，以保证塔内的精馏，实现氩氮分离，从而在纯氩塔4底部得到纯液氩15；同时，在纯氩塔4的顶部排放一定量的余气，保证精馏的正常进行。
图2所示，本发明所述的使用所述装置进行提取高纯液氩的方法，该方法使用的是一与所述粗氩Ⅰ塔中部位置相连通的原料粗氩气输入系统，所述的提取方法是：
来自多套空分装置排放的原料粗氩气5经管道6被汇集后，经压缩机7加压送入冷箱内板式换热器8，经冷却后送入粗氩Ⅰ塔中部相应位置进行提纯精馏；
从空分精馏塔14的上塔相应部位抽出含氩量约9.18％的氩馏分气体；氩馏分直接从粗氩Ⅰ塔的底部导入，同时将来自多套空分装置的粗氩气送入粗氩Ⅰ塔组份相近的位置；从粗氩Ⅱ塔底部排出的粗液氩经液氩泵12加压后进入粗氩Ⅰ塔上部作为回流液；粗氩气自粗氩Ⅰ塔顶部排出，经粗氩Ⅱ塔底部导入；粗氩Ⅱ塔中的粗氩冷凝器1采用过冷后的液空作冷源，粗氩Ⅱ塔上升气体在粗氩冷凝器1中大部分被冷凝，液体返回粗氩Ⅱ塔顶部作为回流液，其余的粗氩气进入纯氩塔4中继续精馏；
粗液氩从纯氩塔4中上部进入，与此同时在纯氩塔4中的纯氩蒸发器3冷凝侧利用下塔压力氮作为热源，使纯氩塔4底部的液氩蒸发，成为上升蒸气，而压力氮被冷凝成液氮并节流进入空分精馏塔14的上塔；纯氩塔4中的纯氩冷凝器2利用过冷液氮作为冷源，冷却纯氩塔4顶部的上升蒸气，使纯氩塔4顶部产生回流液，以保证纯氩塔4内的精馏，实现氩氮分离，从而在纯氩塔4底部得到纯液氩15；同时，在纯氩塔4的顶部排放一定量的余气，保证精馏的正常进行。
实施例：
本发明所述的一种提取多套空分粗氩制取纯氩的方法，它包括以下步骤：
a)来自多套空分装置排放的粗氩气作为原料气体汇总后，经过压缩机增压，得到的高温气体再经过板式换热器冷却为低温(接近粗氩塔温度)。再通入新增的粗氩Ⅰ塔的适当位置；
b)若多套空分距离较近，延程阻力较低，可直接抽取多套空分低温粗氩气汇总通入新增的粗氩Ⅰ塔的适当位置。(此段管道需做好保温，尽量降低冷损)
c)来自多套空分装置排放的粗液氩作为原料回流液汇总到贮槽后，通过粗液氩泵加压节流后送入粗氩Ⅰ塔的适当位置；
d)其中a、b、c作为部分原料气或液，在实施过程中可以三者中选择一种；
e)将原空分装置的增效塔作为粗氩Ⅱ塔，新增粗氩Ⅰ塔、纯氩系统及单独氩冷箱；
f)氩冷箱与主冷箱之间的接管采用隔箱保温；
g)在粗氩Ⅰ塔内，气态氩馏分沿填料盘上升，由于氧的沸点比氩高，故高沸点组分氧被大量地洗涤下来，形成回流液经氩馏分液体泵加压返回上塔。粗氩Ⅱ塔底部粗液氩经粗液氩泵加压返回粗氩Ⅰ塔上部作回流液。上升气体中的低沸点组分氩的含量不断提高，最后在粗氩Ⅱ塔顶部得到含氧≤1.5ppm、含氩～99.6％的粗氩气，粗氩气进入粗氩冷凝器中，一部分被液空冷凝成粗液氩，回流粗氩Ⅱ塔，剩余粗氩气进入粗氩液化器液化后再进入纯氩塔继续参与精馏(或者不采用粗氩液化器，粗氩气直接进入纯氩塔精馏)；
h)由于氮的沸点比氩的沸点低，因此含氮量约为0.4％的粗氩气在纯氩塔中得到进一步分离，最后在纯氩蒸发器底部得到含氩99.999％以上的纯液氩产品；
i)a、b、c中三种方式中任意一种在粗氩Ⅰ塔精馏的组分相近部位送入，在粗氩Ⅰ塔、粗氩Ⅱ塔、纯氩塔内参与精馏，其参与精馏的方式同g、h。原料气或液并入后，使得出粗氩Ⅱ塔的粗氩气量增大，纯氩塔需要处理的负荷也相应增大；
j)在粗氩冷凝器粗氩侧设置气相放空阀，考虑粗氩气放空，防止氮塞或堵塞超压；
k)在纯氩塔顶端设置气相放空阀，考虑余气放空。
一种能够执行本发明方法并具有工业化规模处理能力的提纯多套空分粗氩制取纯氩装置，该装置包含以下几个系统：
a)原料气或液输入系统：可以为1、一台粗氩气压缩机，用于原料粗氩气的增压，能够有足够压力将粗氩气输入到粗氩Ⅰ塔；一台板式换热器，用于冷却增压后的粗氩气。或为2、一台存放粗液氩的贮槽，2台粗液氩泵(一用一备)，用于将粗液氩输入到粗氩Ⅰ塔。
b)制冷系统：由于增加产品液氩的输出，故需要增大主空分膨胀机的膨胀量补充冷量。冷量不足时还需要降低空分本身其他液体产品产量来实现冷量的平衡。空分可以通过调节工况实现不同液体产品的需求。
c)提氩精馏系统：低温全精馏制氩的粗氩液化器(或无)、粗氩Ⅰ塔、纯氩塔组合置于氩冷箱内；粗氩Ⅱ塔(原空分增效塔)和粗氩冷凝器利用原空分设备。
d)循环液体泵：2台循环液氩泵(一用一备)：将粗氩Ⅱ塔底部氩馏分加压送入粗氩Ⅰ塔顶部作为回流液；2台循环液氧泵(一用一备)：将粗氩Ⅰ塔底部粗液氧加压送入到上塔中部作为上塔回流液。
d)自动控制系统：包括增加DCS系统测点；1套阀门，包括各种规格调节阀与手动阀；1套测量仪表，包括温度、压力、流量与液位测量仪表等；1套组分在线分析仪表。

Claims (4)

1.一种利用多套空分制取的粗氩提取高纯液氩的装置,其特征在于该装置主要包括：
—用于获得产品液氩的提纯系统，该系统至少包括：利用多套空分中的一套空分，并将该套空分中带有冷凝器的增效塔作为粗氩Ⅱ塔，另配置有一台粗氩Ⅰ塔、一台含有冷凝器和蒸发器的纯氩塔；
一与所述粗氩Ⅰ塔中部位置相连通的原料粗氩气或粗液氩输入系统，该系统至少包括如下装置中的一种：一将远距离布置多套空分装置排放的粗氩气汇集于一体的汇集器、以及将汇集后的粗氩气进行增压的压缩机和将增压后的高温粗氩气冷却的板式换热器；一将近距离布置多套空分装置排放的粗氩气汇集于一体的汇集器；或一将多套空分装置排放的粗液氩作为原料回流液汇总在一起的贮槽、以及将粗液氩进行加压的粗液氩泵；
至少—台用于液体回流的循环液氩泵和一台循环液氧泵。
2.根据权利要求1所述的利用多套空分制取的粗氩提取高纯液氩的装置,其特征在于所述粗氩Ⅰ塔的底部设置有氩馏分气体导入口，该氩馏分气体导入口与空分精馏塔的上塔设置的氩馏分气体出口连接；所述粗氩Ⅰ塔的顶部设置有粗氩气排出口，该粗氩气排出口通过管道连接于粗氩Ⅱ塔的底部导入口；所述粗氩Ⅱ塔上部冷凝器下方的粗液氩出口连接于纯氩塔中上部设置的粗液氩进口；并在纯氩塔的底部设置有纯液氩排出口；
所述的循环液氩泵分别连接于粗氩Ⅱ塔底部氩馏分出口与粗氩Ⅰ塔顶部回流液进口；所述循环液氧泵分别连接于粗氩Ⅰ塔底部粗液氧出口与该粗氩Ⅰ塔上塔回流口。
3.一种使用权利要求1或2所述装置进行提取高纯液氩的方法，其特征在于该方法使用的是一与所述粗氩Ⅰ塔中部位置相连通的原料粗液氩输入系统，所述的提取方法是：
来自多套空分装置排放的原料粗液氩经管道被集中送入粗液氩贮槽，再从贮槽经泵加压进入粗氩Ⅰ塔中部相应位置进行提纯精馏；
从空分精馏塔的上塔相应部位抽出含氩量约9.18%的氩馏分气体；氩馏分直接从粗氩Ⅰ塔的底部导入，同时将来自多套空分装置的粗液氩送入粗氩Ⅰ塔组份相近的位置；从粗氩Ⅱ塔底部排出的粗液氩经液氩泵加压后进入粗氩Ⅰ塔上部作为回流液；粗氩气自粗氩Ⅰ塔顶部排出，经粗氩Ⅱ塔底部导入；粗氩Ⅱ塔中的粗氩冷凝器采用过冷后的液空作冷源，粗氩Ⅱ塔上升气体在粗氩冷凝器中大部分被冷凝，液体返回粗氩Ⅱ塔顶部作为回流液，其余的粗氩气进入纯氩塔中继续精馏；
粗氩气从纯氩塔中上部进入，与此同时在纯氩塔中的纯氩蒸发器冷凝侧利用下塔压力氮作为热源，使纯氩塔底部的液氩蒸发，成为上升蒸气，而压力氮被冷凝成液氮并节流进入空分精馏塔的上塔；纯氩冷凝器利用过冷液氮作为冷源，冷却纯氩塔顶部的上升蒸气，使纯氩塔顶部产生回流液，以保证塔内的精馏，实现氩氮分离，从而在纯氩塔底部得到纯液氩；同时，在纯氩塔的顶部排放一定量的余气，保证精馏的正常进行。
4.一种使用权利要求1或2所述装置进行提取高纯液氩的方法，其特征在于该方法使用的是一与所述粗氩Ⅰ塔中部位置相连通的原料粗氩气输入系统，所述的提取方法是：
来自多套空分装置排放的原料粗氩气经管道被汇集后，经压缩机加压送入冷箱内板式换热器，经冷却后送入粗氩Ⅰ塔中部相应位置进行提纯精馏；
从空分精馏塔的上塔相应部位抽出含氩量约9.18%的氩馏分气体；氩馏分直接从粗氩Ⅰ塔的底部导入，同时将来自多套空分装置的粗氩气送入粗氩Ⅰ塔组份相近的位置；从粗氩Ⅱ塔底部排出的粗液氩经液氩泵加压后进入粗氩Ⅰ塔上部作为回流液；粗氩气自粗氩Ⅰ塔顶部排出，经粗氩Ⅱ塔底部导入；粗氩Ⅱ塔中的粗氩冷凝器采用过冷后的液空作冷源，粗氩Ⅱ塔上升气体在粗氩冷凝器中大部分被冷凝，液体返回粗氩Ⅱ塔顶部作为回流液，其余的粗氩气进入纯氩塔中继续精馏；
粗氩气从纯氩塔中上部进入，与此同时在纯氩塔中的纯氩蒸发器冷凝侧利用下塔压力氮作为热源，使纯氩塔底部的液氩蒸发，成为上升蒸气，而压力氮被冷凝成液氮并节流进入空分精馏塔的上塔；纯氩塔中的纯氩冷凝器利用过冷液氮作为冷源，冷却纯氩塔顶部的上升蒸气，使纯氩塔顶部产生回流液，以保证纯氩塔内的精馏，实现氩氮分离，从而在纯氩塔底部得到纯液氩；同时，在纯氩塔的顶部排放一定量的余气，保证精馏的正常进行。
CN201410820647.9A 2014-12-25 2014-12-25 一种利用多套空分制取的粗氩提取高纯液氩的装置及方法 Active CN104501530B (zh)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201410820647.9A CN104501530B (zh) 2014-12-25 2014-12-25 一种利用多套空分制取的粗氩提取高纯液氩的装置及方法

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201410820647.9A CN104501530B (zh) 2014-12-25 2014-12-25 一种利用多套空分制取的粗氩提取高纯液氩的装置及方法

Publications (2)

Publication Number Publication Date
CN104501530A CN104501530A (zh) 2015-04-08
CN104501530B true CN104501530B (zh) 2017-05-17

Family

ID=52942956

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201410820647.9A Active CN104501530B (zh) 2014-12-25 2014-12-25 一种利用多套空分制取的粗氩提取高纯液氩的装置及方法

Country Status (1)

Country Link
CN (1) CN104501530B (zh)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023083488A1 (de) * 2021-11-10 2023-05-19 Linde Gmbh Verfahren und anordnung zur erzeugung eines argonprodukts und eines sauerstoffprodukts und verfahren zum umrüsten einer oder mehrerer luftzerlegungsanlagen

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108240733A (zh) * 2018-01-24 2018-07-03 北京拓首能源科技股份有限公司 一种利用液化天然气冷能的空气分离系统
CN108731376A (zh) * 2018-04-18 2018-11-02 衢州杭氧气体有限公司 一种氩气生产工艺及其生产线
CN109489343A (zh) * 2018-10-10 2019-03-19 杭州杭氧股份有限公司 一种提取中压氧气的液体空分的装置及其方法
CN109737689A (zh) * 2018-12-29 2019-05-10 侨源气体（福州）有限公司 空气分离与提纯系统及方法
US11713921B2 (en) * 2019-10-17 2023-08-01 Praxair Technology, Inc. System and method for the production of argon in an air separation plant facility or enclave having multiple cryogenic air separation units
CN113739515B (zh) * 2021-09-06 2022-10-21 乔治洛德方法研究和开发液化空气有限公司 一种通过富氩气提取高纯液氩的方法和装置
CN113959179B (zh) * 2021-12-22 2022-05-03 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

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3364724B2 (ja) * 1993-06-30 2003-01-08 日本酸素株式会社 高純度アルゴンの分離方法及びその装置
DE10040391A1 (de) * 2000-08-18 2002-02-28 Linde Ag Tieftemperaturluftzerlegungsanlage
CN100363699C (zh) * 2005-04-25 2008-01-23 林福粦 回收液化天然气冷能的空气分离系统
CN1884051A (zh) * 2006-07-11 2006-12-27 杭州杭氧股份有限公司 组合式全精馏制氩工艺及制氩设备
CN101782309A (zh) * 2010-01-08 2010-07-21 开封空分集团有限公司 两塔制氩系统及其工艺
CN101846436A (zh) * 2010-05-27 2010-09-29 中国海洋石油总公司 利用lng冷能的全液体空气分离装置
CN104142044A (zh) * 2014-08-06 2014-11-12 杭州杭氧股份有限公司 一种模块化氩回收液化器及氩回收方法
CN204421489U (zh) * 2014-12-25 2015-06-24 杭州杭氧股份有限公司 一种利用多套空分制取的粗氩提取高纯液氩的装置

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023083488A1 (de) * 2021-11-10 2023-05-19 Linde Gmbh Verfahren und anordnung zur erzeugung eines argonprodukts und eines sauerstoffprodukts und verfahren zum umrüsten einer oder mehrerer luftzerlegungsanlagen

Also Published As

Publication number Publication date
CN104501530A (zh) 2015-04-08

Similar Documents

Publication Publication Date Title
CN104501530B (zh) 一种利用多套空分制取的粗氩提取高纯液氩的装置及方法
CN104061757B (zh) 一种液氧及液氮制取装置及方法
CN100565060C (zh) 一种天然气液化的方法及其装置
CN101148252B (zh) 双塔低温精馏制备高纯氧方法
CN104236253B (zh) 深冷法制取纯一氧化碳和富氢气的装置及方法
CN204115392U (zh) 带补气压缩机的全液体空分设备
CN103523751A (zh) 一种深冷分离提纯一氧化碳和氢气的装置及方法
CN104110940A (zh) 一种利用液化天然气冷能的高效空分装置
CN101684983B (zh) 制备高纯度氧的方法和设备
CN204421489U (zh) 一种利用多套空分制取的粗氩提取高纯液氩的装置
CN201028930Y (zh) 一种天然气液化的装置
CN106219495B (zh) 一种小型psa和小型深冷空分的组合装置
CN101943512A (zh) 一种利用液化天然气冷能的空分方法
CN204240703U (zh) 一种利用液化天然气冷能的高效空分装置
CN206094746U (zh) 一种从富甲烷气中提取液态甲烷的新型装置
CN103629894A (zh) 单级精馏设备的空气分离方法
CN101915495A (zh) 利用液化天然气冷能的全液体空气分离装置及方法
CN201876055U (zh) 利用液化天然气冷能的全液体空气分离装置
CN204923686U (zh) 一种低纯度氧空气分离的装置
CN204006964U (zh) 深冷法制取纯一氧化碳和富氢气的装置
CN1038514A (zh) 生产高压氧和高压氮的空气分离流程
CN105482861A (zh) 利用低压塔回流液作为高压塔洗涤液的焦炉气制取lng的方法
CN105115244A (zh) 一种低纯度氧空气分离的装置及方法
CN103773529A (zh) 一种撬装式伴生气液化系统
CN203474449U (zh) 一种深冷分离提纯一氧化碳和氢气的装置

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant
CP03 Change of name, title or address
CP03 Change of name, title or address

Address after: No.799, Xiangfu Road, Qingshanhu street, Lin'an District, Hangzhou City, Zhejiang Province

Patentee after: Hangzhou oxygen generator group Co.,Ltd.

Address before: 311241, No. 99, East Ring Road, Qingshan Lake Street, Hangzhou, Zhejiang, Ling'an

Patentee before: HANGZHOU HANGYANG Co.,Ltd.

CP01 Change in the name or title of a patent holder
CP01 Change in the name or title of a patent holder

Address after: 799 Xiangfu Road, Qingshanhu street, Lin'an District, Hangzhou City, Zhejiang Province

Patentee after: Hang Yang Group Co.,Ltd.

Address before: 799 Xiangfu Road, Qingshanhu street, Lin'an District, Hangzhou City, Zhejiang Province

Patentee before: Hangzhou oxygen generator group Co.,Ltd.