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CN118623558B - 空分系统及空气分离方法 - Google Patents

空分系统及空气分离方法 Download PDF

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Publication number
CN118623558B
CN118623558B CN202411097195.6A CN202411097195A CN118623558B CN 118623558 B CN118623558 B CN 118623558B CN 202411097195 A CN202411097195 A CN 202411097195A CN 118623558 B CN118623558 B CN 118623558B
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air
liquid
liquefier
air separation
outlet
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CN118623558A (zh
Inventor
范小华
任文
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Zhongke Fuhai Hangzhou Gas Engineering Technology Co ltd
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Zhongke Fuhai Hangzhou Gas Engineering Technology Co ltd
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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
    • F25J3/04248—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
    • 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
    • F25J3/04187—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
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
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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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    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—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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    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
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    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0234—Integration with a cryogenic air separation unit
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0251—Intermittent or alternating process, so-called batch process, e.g. "peak-shaving"
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    • F25J3/04339—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air
    • F25J3/04345—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air and comprising a gas work expansion loop
    • 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
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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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    • 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
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
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Abstract

本申请公开了一种空分系统及空气分离方法，空分系统包括液空储能单元和空分单元，液空储能单元包括依次连接的循环增压机、膨胀制冷装置和空气液化器；空分单元包括连接的主换热器和精馏塔，主换热器用于对接收的第二原料气体进行降温处理；空气液化器包括出液口，出液口与精馏塔连通，以将液化空气输入精馏塔中，精馏塔用于对液化空气和降温处理后的第二原料气体一起进行精馏处理。通过上述方案能够拓宽空分产能的调节范围以提高市场适应力，能够实现在适配峰谷电提高电能利用效益的情况下使空分保持工况稳定运行，解决了为适配峰谷电空分需要频繁变负荷或者频繁快速启停的难题，系统综合能效提高，生产成本降低。

Description

空分系统及空气分离方法
技术领域
本申请涉及空分技术领域，特别是涉及一种空分系统及空气分离方法。
背景技术
空分，全称为空气分离，是指从空气中分离出其组分（如氧、氮、氩、氦等稀有气体）的过程。空分设备广泛应用于各行各业，包括重工业和轻工业、食品、医药、机械加工、农业和畜牧业等领域。由于应用广泛，需求量大，空分设备在全国各地均有大量分布。
目前空分设备由于其精馏特性，必须连续生产，大电机的耗电为其主要生产成本，在各地平均电价下的生产成本相对较高。空分设备的大型机组（主要为循环增压机及原料压缩机）均为离心机组，典型的运行范围为80~105%，装置负荷调节能力有限。当大型机组降负荷运行时，其效率衰减严重。
发明内容
本申请主要解决的技术问题是提供一种空分系统及空气分离方法，能够拓宽空分产能的调节范围以提高市场适应力，能够实现在适配峰谷电提高电能利用效益的情况下使空分保持工况稳定运行，解决了为适配峰谷电空分需要频繁变负荷或者频繁快速启停的难题，系统综合能效提高，生产成本降低。
为解决上述技术问题，本申请采用的一个技术方案是：提供一种空分系统，包括液空储能单元和空分单元，所述液空储能单元包括依次连接的循环增压机、膨胀制冷装置和空气液化器，所述循环增压机用于对接收的第一原料气体进行增压处理，所述膨胀制冷装置用于对所述循环增压机输出的高压空气进行降温处理，所述空气液化器用于对所述高压空气进行液化处理以输出液化空气；所述空分单元包括连接的主换热器和精馏塔，所述主换热器用于对接收的第二原料气体进行降温处理；所述空气液化器包括出液口，所述出液口与所述精馏塔连通，以将所述液化空气输入所述精馏塔中，所述精馏塔用于对所述液化空气和降温处理后的第二原料气体一起进行精馏处理。
优选地，所述膨胀制冷装置包括第一膨胀机，所述第一膨胀机 包括第一膨胀端和第一增压端，所述第一增压端的入口与所述循环增压机的出口连通，所述第一增压端的出口与所述空气液化器的入口连通，所述空气液化器包括第一出气口和第二出气口，所述第一出气口与所述循环增压机的入口连通，所述第二出气口与所述第一膨胀端的入口连通，所述第一膨胀端的出口与所述空气液化器的入口连通。
优选地，所述膨胀制冷装置还包括第二膨胀机，所述第二膨胀机连接在所述循环增压机和所述第一膨胀机之间，所述第二膨胀机包括第二膨胀端和第二增压端，所述第二增压端的入口与所述循环增压机的出口连通，所述第二增压端的出口与所述第一增压端的入口连通，所述第二膨胀端的入口与所述循环增压机的出口连通，所述第二膨胀端的出口与所述空气液化器的入口连通。
优选地，所述液空储能单元还包括液空储槽，所述液空储槽两端分别与所述出液口和所述精馏塔连通，用于存储所述液化空气。
优选地，所述液空储能单元还包括依次连接的第一预冷装置和第一纯化装置，所述第一纯化装置通过第一入气通道与所述循环增压机的入口连通；所述液空储能单元还包括节流装置和气液分离装置，所述出液口、所述节流装置、所述气液分离装置和所述液空储槽依次连通，所述气液分离装置还通过第一返流通道与所述第一纯化装置、所述第一预冷装置连通，所述第一返流通道用于使由所述气液分离装置中分离出的气体经所述空气液化器复温后作为所述第一纯化装置的再生气源，所述液空储槽和所述精馏塔之间连接有输送泵。
优选地，所述液空储能单元还包括依次连接的第一预冷装置和第一纯化装置，所述第一纯化装置通过第一入气通道与所述循环增压机的入口连通；所述液空储能单元还包括节流装置和气液分离装置，所述出液口、所述节流装置、所述气液分离装置和所述液空储槽依次连通，所述气液分离装置还通过第三返流通道与所述循环增压机入口连通；所述空分单元还包括依次连接的第二预冷装置和第二纯化装置，所述第二纯化装置通过第二入气通道与所述主换热器连通；所述主换热器还通过第二返流通道与所述第一纯化装置、所述第二预冷装置和所述第二纯化装置连通，所述第二返流通道用于使经所述主换热器复温后作为所述第一纯化装置和所述第二纯化装置的再生气源、以及作为所述第二预冷装置的干燥气冷源。
优选地，所述空分单元还包括氮气压缩机和氮液化器，所述氮液化器连接在液空储槽和所述主换热器之间，所述氮气压缩机连接在所述主换热器和所述氮液化器之间，其中，所述氮液化器用于对液化空气复温后通入所述主换热器，从所述主换热器排出的氮气经所述氮气压缩机加压后再经过所述氮液化器液化形成液氮。
为解决上述技术问题，本申请采用的另一个技术方案是：提供一种空气分离方法，包括:对第一原料气体依次进行增压处理、降温处理和液化处理，得到液化空气；对第二原料气体进行降温处理，对所述液化空气和降温处理后的所述第一原料气体一起进行精馏处理，得到目标产品。
优选地，所述对第一原料气体依次进行增压处理、降温处理和液化处理，得到液化空气的步骤，包括：响应于当前处于谷电时段，对第一原料气体依次进行增压处理、降温处理和液化处理，得到液化空气，并存储所述液化空气。
优选地，所述目标产品包括液氮、液氧和液氩中的至少一种。
本申请的有益效果是：区别于现有技术的情况，本申请提供的空分系统和空气分离方法本采用独立的空分单元和液空储能单元，液空储能单元产生的液化空气灌入精馏塔中用于补充空分所需的冷量并提供一部分原料气，空分单元可以省去常规空分设备的制冷系统并降低原料空气消耗。液空储能单元无精馏装置，便于频繁启停适配峰谷电，液化空气输入至空分单元，使空分单元保持在最佳设计点下全天候24小时高效稳定运行，避免了空分单元为适配峰谷电所需的频繁负荷调整或者频繁启停。液空储能单元可以通过增减运行时间，实现产量的调节，从而调节了空分单元的生产负荷，使空分系统的液体产能调节范围更宽，同时使得液空储能单元能够在电价较低时段运行，因此能够节省电费，整套系统综合效率高且稳定。
附图说明
图1是本申请的空分系统一实施方式的结构示意图；
图2是本申请的空分系统另一实施方式的结构示意图；
图3是本申请的空分系统另一实施方式的结构示意图；
图4是本申请的空分系统另一实施方式的结构示意图；
图5是本申请的空分系统另一实施方式的结构示意图；
图6是本申请的空气分离方法一实施方式的流程示意图。
具体实施方式
为使本申请的目的、技术方案及效果更加清楚、明确，以下参照附图并举实施例对本申请进一步详细说明。显然，所描述的实施例仅是本申请的一部分实施例，而不是全部的实施例。基于本申请中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其它实施例，都属于本申请保护的范围。
参阅图1，图1是本申请的空分系统一实施方式的结构示意图。本申请的空分系统100包括液空储能单元10和空分单元20。
液空储能单元10包括依次连接的循环增压机11、膨胀制冷装置12、空气液化器13，循环增压机11用于对接收的第一原料气体进行增压处理，膨胀制冷装置12用于对循环增压机11输出的高压空气进行降温处理，空气液化器13用于对高压空气进行液化处理以输出液化空气。具体地，膨胀制冷装置12包括第一膨胀机121，第一膨胀机121包括第一膨胀端121a和第一增压端121b，第一增压端121b的入口与循环增压机11的出口连通，第一增压端121b的出口与空气液化器13的入口连通，空气液化器13包括第一出气口13a和第二出气口13b，第一出气口13a与循环增压机11的入口连通，第二出气口13b与第一膨胀端121a的入口连通，第一膨胀端121a的出口与空气液化器13的入口连通。可选地，液空储能单元10还包括依次连接的第一空气过滤器14、第一空压机15、第一预冷装置16和第一纯化装置17，第一纯化装置17通过第一入气通道171与循环增压机11的入口连通。
在本申请中，液空储能单元10的第一原料气体为空气，空气经第一空气过滤器14过滤后，由第一空压机15压缩至所需压力，再经由第一预冷装置16、第一纯化装置17净化后得到洁净干燥的空气。洁净干燥的空气送入第一循环增压机11后被进一步压缩，被压缩的空气送入第一膨胀机121的第一增压端121b再次进行增压，得到高压气体，本实施例中的第一膨胀机121为低温膨胀机。该高压气体被分为体量不同的两路，两路高压气体均通入空气液化器13，其中少部分的一路直接被空气液化器13完全冷却为液化空气；大部分的另一路则被空气液化器13不完全冷却，然后通过第二出气口13b离开空气液化器13进入第一膨胀机121的第一膨胀端121a进行膨胀，气体被减压降温，膨胀后的气体经过空气液化器13为其提供冷量，气体复温后从第一出气口13a离开空气液化器13合并入第一入气通道171中，与前述的经过第一纯化装置17净化的空气一同进入第一循环增压机11中，再次重复前述步骤，得到液化空气。
空分单元20包括连接的主换热器21和精馏塔22，主换热器21用于对接收的第二原料气体进行降温处理。具体地，精馏塔22包括依次连接的双级精馏塔221、第一粗氩塔222、第二粗氩塔223、纯氩塔224和高纯氧塔225，其中，双级精馏塔221包括上塔221a和下塔221b。可选地，空分单元20还包括依次连接的第二空气过滤器23、第二空压机24、第二预冷装置25、第二纯化装置26，第二纯化装置26通过第二入气通道261与主换热器21连通。主换热器21还通过第二返流通道211与第二预冷装置25和第二纯化装置26连通。
空气液化器13包括出液口13c，出液口13c与精馏塔22连通，以将液化空气输入精馏塔22中，精馏塔22用于对液化空气和降温处理后的第二原料气体一起进行精馏处理。可选地，液空储能单元10还包括液空储槽132，液空储槽132两端分别与出液口13c和精馏塔22连通，用于存储液化空气，能够在不生产液化空气的时段仍保证持续不断地向空分单元20输送液化空气。在其他实施例中，液化空气也可以直接输送至空分单元20。
空分单元20用于分离空气各组分，其产品可以为液态或气态，本申请的第二原料气体也为空气，空气经第二空气过滤器23过滤后，由第二空压机24压缩至所需压力，再经由第二预冷装置25、第二纯化装置26净化后得到洁净干燥的空气。洁净干燥的空气通过主换热器21进行降温处理，冷却至接近饱和温度区间，送入双级精馏塔221的下塔221b作为原料上升气，同时，液化空气从空气液化器13的出液口13c离开液空储能单元10后送入双级精馏塔221的上塔221a或下塔221b中，精馏塔22位于冷箱220内，气态空气和液化空气在精馏塔22内经传热传质精馏，最后得到液氧、液氮和液氩等液态产品，或者得到氧气、氮气和氩气等气体产品。剩余物料通过第二返流通道211经主换热器21复温后分别送往第二纯化装置26和第二预冷装置25，作为第二纯化装置26的再生气源以及第二预冷装置25的干燥冷源使用。
本申请采用独立的空分单元20和液空储能单元10，液空储能单元10产生的液化空气灌入精馏塔22中用于补充空分所需的冷量和提供一部分原料气，空分单元20可以省去常规空分设备的制冷系统并降低原料空气消耗。由于液空储能单元10无精馏装置，便于频繁启停适配峰谷电提高电能利用效益，液化空气输入至空分单元20，使空分单元20能够保持在最佳设计点下全天候24小时高效稳定运行，避免了空分单元20为适配峰谷电所需的频繁负荷调整或者频繁启停，空分系统100综合效率高且稳定。液空储能单元10可以通过增减运行时间，实现液化空气的产量的调节，从而调节了空分单元20的生产负荷，使空分系统100的液体产能调节范围更宽。同时使得液空储能单元10能够在电价较低时段运行，因此能够节省电费。
参阅图2，图2是本申请的空分系统另一实施方式的结构示意图。相比于图1所示的实施例，本实施例的膨胀制冷装置12还增设了第二膨胀机122，其中，第一膨胀机121为低温膨胀机，第二膨胀机122为高温膨胀机。第二膨胀机122连接在循环增压机11和第一膨胀机121之间，第二膨胀机122包括第二膨胀端122a和第二增压端122b，第二增压端122b的入口与循环增压机11的出口连通，第二增压端122b的出口与第一增压端121b的入口连通，第二膨胀端122a的入口与循环增压机11的出口连通，第二膨胀端122a的出口与空气液化器13的入口连通。与图1所示实施例不同的是，被循环增压机11压缩的空气被分为两路，其中一路经空气液化器13不充分冷却，预冷后的气体进入第二膨胀机122的第二膨胀端122a进行膨胀，气体被减压降温，膨胀后的气体经过空气液化器13为其提供冷量，气体复温后离开空气液化器13合并入第一入气通道171中，与经过第一纯化装置17净化的空气一同进入第一循环增压机11中；另一路依次经过第二增压端122b、第一增压端121b进行连续二次加压，得到高压空气，高压空气进入空气液化器13之后的路径如图1所示的实施例，此处不再赘述。本实施例相比于图1所示的实施例增设了一台高温膨胀机，能够进一步提升制冷效率，适用于液化空气需求量较大的情况。
继续参阅图1和图2，液空储能单元10还包括节流装置（未标示）和气液分离装置131，出液口13c、节流装置、气液分离装置131和液空储槽132依次连通，气液分离装置131还通过第一返流通道134与第一纯化装置17、第一预冷装置16连通，第一返流通道134用于使由气液分离装置131中分离出的气体经空气液化器13复温后作为第一纯化装置17的再生气源，液空储槽132和精馏塔22之间连接有输送泵133。高压气体被空气液化器13液化形成高压液化空气，高压液化空气通过节流装置后被减压形成常压状态的液化空气和气态空气，气液分离装置131分离液态和气态空气，气态空气通过第一返流通道134返流，经空气液化器13复温后作为第一纯化装置17的再生气源。常压的液化空气被送入液空储槽132中，再通过输送泵133加压后连续稳定地向空分单元20输送液化空气物料，以实现空分单元20全天24小时连续稳定的运行，实现空分产品持续稳定的产出。
参阅图3，图3是本申请的空分系统另一实施方式的结构示意图。本实施例与图2所示的实施例的区别在于，高压液化空气通过节流装置后被减压形成略高于常压状态的低压状态（例如0.5-0.6MPa）的液化空气和气态空气，气液分离装置131分离液态和气态空气，低压的气态空气通过第三返流通道（未标示）返流，经空气液化器13复温后合并入第一入气通道171，从循环增压机11的入口进入循环，此时第一纯化装置17的再生气源由经空分单元20的主换热器21复温的剩余物料提供。低压的液化空气则被送入带压的液空储槽132中，此时液空储槽132直接与精馏塔22连通，无需设置输送泵133。
参阅图4，图4是本申请的空分系统另一实施方式的结构示意图。本实施例与图2所示的实施例的区别在于，空分单元20还包括氮气压缩机和氮液化器，氮液化器连接在液空储槽132和主换热器21之间，氮气压缩机连接在主换热器21和氮液化器之间，其中，氮液化器用于对液化空气复温后通入主换热器21，从主换热器21排出的氮气经氮气压缩机加压后再经过氮液化器液化形成液氮。本实施例将液空储能单元10生产出来的液化空气分出一部分经过氮液化器为其提供冷量，液化空气被氮液化器复温后与前述洁净干燥的空气一同被送入主换热器21，从主换热器21排出的剩余物料（即氮气）经氮气压缩机压缩增压，增压后的氮气通入氮液化器后被液化形成液氮，从而达到增加液氮产量的目的，该工艺适用于氮氧产品比例高的储能型液体空分。
当液空储能单元10所能提供的冷量仍无法使得空分系统100运行在满负荷的最佳效率点时，可以在空分单元20的第二纯化装置26和主换热器21之间增加一台小型增压机，如图5所示，以增压膨胀对冷量进行回收，使得空分系统100运行在最佳效率点。
参阅图6，图6是本申请的空气分离方法一实施方式的流程示意图。该方法包括如下步骤：
步骤S110：对第一原料气体依次进行增压处理、降温处理和液化处理，得到液化空气。该步骤由液空储能单元独立实现，由于液空储能单元无精馏装置，便于频繁启停适配峰谷电提高电能利用效益，液空输入至空分单元，使空分单元保持在最佳设计点下全天候24小时高效稳定运行，避免了空分单元为适配峰谷电所需的频繁负荷调整或者频繁启停。液空储能单元可以通过增减运行时间，实现液化空气的产量的调节，从而调节了空分单元的生产负荷，使空分的液体产能调节范围更宽。
步骤S120：对第二原料气体进行降温处理，对液化空气和降温处理后的第一原料气体一起进行精馏处理，得到目标产品。
可选地，步骤S110可以在谷电时段运行，得到液化空气后将其存储在液空储槽中。上述步骤使得液空储槽能够全天不间断地为空分单元提供液化空气，以执行步骤S120。本方法通过液空储能单元将空分所需要的主要能耗由全天24小时不间断运行转移至谷电时段运行，由于谷电时段所需电费较低，从而大大降低了运行电费，降低生产成本。
本方法可以应用于气体空分，其目标产品可以是气态空气组分，为氮气、氧气和氩气中的至少一种，也可以应用于液体空分，其目标产品可以是液化空气组分，为液氮、液氧和液氩中的至少一种。由于液体空分所需要的主要能耗（即液化功）极大，而本方法可以将做液化功的时段由全天24小时转移至谷电时段，从而显著降低液体空分的生产成本。在其他实施例中，当目标产品的价格较高，能抵消甚至覆盖运行电费时，液空储能单元也可以在平电时段甚至峰电时段运行，以提高目标产品的产量。另外，液空储能单元所产生的液化空气也可以作为一种产品直接出售，由于无需分离空气组分，可以进一步降低能耗，从而降低成本，提高经济效益。
以上仅为本申请的实施方式，并非因此限制本申请的专利范围，凡是利用本申请说明书及附图内容所作的等效结构或等效流程变换，或直接或间接运用在其他相关的技术领域，均同理包括在本申请的专利保护范围内。

Claims (8)

1.一种空分系统，其特征在于，包括：
液空储能单元，所述液空储能单元包括依次连接的循环增压机、膨胀制冷装置和空气液化器，所述循环增压机用于对接收的第一原料气体进行增压处理，所述膨胀制冷装置用于对所述循环增压机输出的高压空气进行降温处理，所述空气液化器用于对所述高压空气进行液化处理以输出液化空气；
空分单元，包括连接的主换热器和精馏塔，所述主换热器用于对接收的第二原料气体进行降温处理；
所述空气液化器包括出液口，所述出液口与所述精馏塔连通，以将所述液化空气输入所述精馏塔中，所述精馏塔用于对所述液化空气和降温处理后的第二原料气体一起进行精馏处理；
所述液空储能单元还包括液空储槽，所述液空储槽两端分别与所述出液口和所述精馏塔连通，用于存储所述液化空气；
所述液空储能单元还包括依次连接的第一预冷装置和第一纯化装置，所述第一纯化装置通过第一入气通道与所述循环增压机的入口连通；所述液空储能单元还包括节流装置和气液分离装置，所述出液口、所述节流装置、所述气液分离装置和所述液空储槽依次连通，所述气液分离装置还通过第一返流通道与所述第一纯化装置连通，所述第一返流通道用于使由所述气液分离装置中分离出的气体经所述空气液化器复温后作为所述第一纯化装置的再生气源，所述液空储槽和所述精馏塔之间连接有输送泵。
2.根据权利要求1所述的空分系统，其特征在于，
所述膨胀制冷装置包括第一膨胀机，所述第一膨胀机包括第一膨胀端和第一增压端，所述第一增压端的入口与所述循环增压机的出口连通，所述第一增压端的出口与所述空气液化器的入口连通，所述空气液化器包括第一出气口和第二出气口，所述第一出气口与所述循环增压机的入口连通，所述第二出气口与所述第一膨胀端的入口连通，所述第一膨胀端的出口与所述空气液化器的入口连通。
3.根据权利要求2所述的空分系统，其特征在于，
所述膨胀制冷装置还包括第二膨胀机，所述第二膨胀机连接在所述循环增压机和所述第一膨胀机之间，所述第二膨胀机包括第二膨胀端和第二增压端，所述第二增压端的入口与所述循环增压机的出口连通，所述第二增压端的出口与所述第一增压端的入口连通，所述第二膨胀端的入口与所述循环增压机的出口连通，所述第二膨胀端的出口与所述空气液化器的入口连通。
4.根据权利要求1所述的空分系统，其特征在于，
所述气液分离装置还通过第三返流通道与所述循环增压机入口连通；
所述空分单元还包括依次连接的第二预冷装置和第二纯化装置，所述第二纯化装置通过第二入气通道与所述主换热器连通；所述主换热器还通过第二返流通道与所述第一纯化装置、所述第二预冷装置和所述第二纯化装置连通，所述第二返流通道用于使经所述主换热器复温后作为所述第一纯化装置和所述第二纯化装置的再生气源、以及作为所述第二预冷装置的干燥气冷源。
5.根据权利要求1所述的空分系统，其特征在于，
所述空分单元还包括氮气压缩机和氮液化器，所述氮液化器连接在液空储槽和所述主换热器之间，所述氮气压缩机连接在所述主换热器和所述氮液化器之间，其中，所述氮液化器用于对液化空气复温后通入所述主换热器，从所述主换热器排出的氮气经所述氮气压缩机加压后再经过所述氮液化器液化形成液氮。
6.一种空气分离方法，其特征在于，应用于权利要求1-5中任一项所述的空分系统，所述空气分离方法包括:
对第一原料气体依次进行增压处理、降温处理和液化处理，得到液化空气；
对第二原料气体进行降温处理，对所述液化空气和降温处理后的所述第一原料气体一起进行精馏处理，得到目标产品。
7.根据权利要求6所述的空气分离方法，其特征在于，
所述对第一原料气体依次进行增压处理、降温处理和液化处理，得到液化空气的步骤，包括：
响应于当前处于谷电时段，对第一原料气体依次进行增压处理、降温处理和液化处理，得到液化空气，并存储所述液化空气。
8.根据权利要求6所述的空气分离方法，其特征在于，
所述目标产品包括液氮、液氧和液氩中的至少一种。
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