CN102721263A - 一种利用深冷技术分离空气的系统及方法 - Google Patents

一种利用深冷技术分离空气的系统及方法 Download PDF

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CN102721263A
CN102721263A CN2012102401799A CN201210240179A CN102721263A CN 102721263 A CN102721263 A CN 102721263A CN 2012102401799 A CN2012102401799 A CN 2012102401799A CN 201210240179 A CN201210240179 A CN 201210240179A CN 102721263 A CN102721263 A CN 102721263A
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heat exchanger
liquid
indirect heat
air
gas
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韩一松
谭芳
艾绍华
瞿晖
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Hangzhou Hangyang Co Ltd
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    • 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
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Abstract

一种利用深冷技术分离空气的系统及方法，所述的系统主要由精馏装置，间接换热器以及对原料空气进行预处理的压缩、预冷和纯化装置组成；原料空气被一低压压缩机或一体机的低压段压缩并被冷却净化，净化气体的一部分经高压压缩机或一体机的高压段压缩至更高压力后至少分成几路：第一路分支气体被压缩机进一步压缩成再高压气体进入间接换热器冷却，并在所述间接换热器底部抽出第一路流体；第二路分支气体直接经所述间接换热器冷却，并在所述间接换热器中部抽出第二路气体；第三路分支气体直接经所述间接换热器冷却，并在所述间接换热器底部抽出第三路流体；所述第一路流体和第三路流体或为全液态或为超临界态流体；所述第二路气体进入一膨胀机膨胀到压力塔的工作压力成全气态或气液两相流体进入精馏系统；从精馏装置抽出的液体以液体的形式被增压并在间接换热器中气化复热并被取出。

Description

一种利用深冷技术分离空气的系统及方法
技术领域
本发明涉及的是一种利用深冷技术分离空气的系统及方法，属于空分制冷技术领域。
背景技术
在空分应用领域中，包括冶金、石化、煤化工等行业的快速发展，对带压产品气体的需求越来越多，相对于产品气在冷箱外以气态形式压缩的外压缩方法，内压缩方法压缩气体以液态的形式增压因其可达压力高、安全性好而获得青睐，其特别是用于获取压力氧，也可用于压力氮和压力氩。
发明内容
本发明的目的在于克服现有技术存在的不足，而提供一种能够解决膨胀机膨胀端流量和增压端流量不匹配的问题，性能先进，能耗低，使用范围广，投资成本低的利用深冷技术分离空气的系统及方法。
本发明的目的是通过如下技术方案来完成的，一种利用深冷技术分离空气的系统，该系统主要由精馏装置，间接换热器以及对原料空气进行预处理的压缩、预冷和纯化装置组成，所述的压缩、预冷和纯化装置包括：
一可将变成压缩空气的低压压缩机或由一体机的低压段构成的低压压缩机构；
一可将压缩空气进行预冷变成预冷空气的空气预冷器；
一可将预冷空气进行净化变成净化气体的纯化机构；
所述的精馏装置至少由压力塔C1和低压塔C2及连接压力塔C1顶部和低压塔C2底部的主冷凝蒸发器K1构成的精馏塔组成；
所述的纯化机构后面配置有一可将净化气体一部分或全部压缩成为高压气体的高压压缩机或由一体机的高压段构成的高压压缩机构；
所述的高压压缩机或高压压缩机构后面相接有至少三条管路，第一管路连接于一可将高压气体进一步压缩成再高压气体的压缩机，该压缩机出口联通于所述可使再高压气体冷却的间接换热器，该路换热通道与所述精馏装置相连通；一与所述压缩机直接机械耦合的膨胀机，第二管路联通于可使高压气体冷却的间接换热器后，在其中部用连管连接于所述膨胀机，并所述膨胀机的出口与所述精馏装置相连通；第三管路直接联通于所述的间接换热器，该路换热通道也与所述精馏装置相连通；
所述的精馏装置至少设置有一路引出液体的液体管路，并通过一加压设备接入所述的可使液体复热后作为气体产品的间接换热器。
    本发明所述的纯化机构后面配置有一可将净化气体一部分压缩成为高压气体的高压压缩机或由一体机的高压段构成的高压压缩机构；净化机构后面配置有一根第四管路连通于所述可将净化气体另一部分冷却成直接流体的间接换热器，并通过该间接换热器直接连通于所述的精馏装置；所述的第一管路通过所述间接换热器后再通过第一节流阀与所述精馏装置相连通；所述的第三管路在通过所述间接换热器后再通过第三节流阀与所述精馏装置相连通。
本发明所述的间接换热器上至少设置有二路液体换热通道，一路液体换热通道为液氧换热通道，该液氧换热通道的进口通过相连通的液氧泵与所述的精馏装置相连通，出口相接有氧气产品管道；另一路为液氮换热通道，该液氮换热通道的进口通过相连通的液氮泵与所述的精馏装置相连通，出口相接有氮气产品管道。
本发明所述的精馏装置中配置有粗氩塔和氩精馏塔；所述的间接换热器上还设置有粗氩换热通道和液氩换热通道，所述的粗氩换热通道直接与粗氩塔相连通，出口相接有引出复热后粗氩气的管道；所述的液氩换热通道的进口通过相连通的液氩泵与所述的精馏装置的氩精馏塔相连通，出口相接有氩气产品管道。
一种利用如上所述系统进行深冷技术分离空气的方法，其特征在于该方法是：
    —原料空气001在空气低压压缩机ATC1或一体机的低压段压缩并经空气预冷系统预冷和纯化系统净化成纯化气体01；     —所述纯化空气01的一部分或全部构成的气体3经高压压缩机ATC2或一体机的高压段压缩为高压气体4，该高压气体4的压力高于纯化气体3的压力；
    —所述高压空气4分成至少三路：第一路分支气体5被压缩机BT进一步压缩成再高压气体8进入间接换热器E1冷却，并在所述间接换热器E1底部抽出第一路流体11；第二路分支气体6直接经所述间接换热器E1冷却，并在所述间接换热器E1中部抽出第二路气体9；第三路分支气体7直接经所述间接换热器E1冷却，并在所述间接换热器E1底部抽出第三路流体12；所述地一路流体11和第三路流体12或为全液态或为超临界态流体；
    所述第二路气体9进入一膨胀机ET1膨胀到压力塔C1的工作压力成全气态或气液两相流体10进入精馏系统49；
    所述第一路流体11或经节流阀V1节流到所述压力塔C1的工作压力成全液态或气液两相流体132或/和经液体膨胀机ET2膨胀成液体131，再经节流阀V8节流到所述压力塔C1的工作压力成全液态或气液两相流体133进入所述精馏系统49；
    所述第三路流体12经节流阀V2节流到所述压力塔C1的工作压力成全液态或气液两相流体14进入所述精馏系统49；
    从精馏装置中抽出的液氧26、液氮35以及液氩39至少一部分分别经液氧泵OP、液氮泵NP及液氩泵AP加压后进入所述间接换热器E1，至少被所述第二路分支气体6、第三路分支气体7、再高压气体8在所述间接换热器E1中间复热后成为氧气产品50、氮气产品51以及氩气产品52。
本发明所述的纯化空气01还有一路分支气体1经所述间接换热器E1冷却成至少部分是气态的流体2进入所述精馏装置49参与气体的精馏过程。
本发明的关键之处是气体4要分成至少三路，气体4的一分支气体7的存在是必须的。受高压压缩机ATC2或一体机的高压段机器级数压比本身限制使得气体4的压力在某些范围内，若此时同已知的方法一样，气体4只有分支气体5和分支气体6，受液体产量和气体产量需要的限制，使得分支气体5的流量相对很小和分支气体6的流量相对很大，此时因膨胀机膨胀端流量和增压端流量不匹配而导致增压膨胀机整机效率极差或相应的增压膨胀机不存在。增压膨胀机整机效率极差或没有相应的增压膨胀机可用使得已知的方法因整体能耗高，性能不先进而没有使用价值或已知的方法不可用。
本发明增加气体4的一分支气体7，使得分支气体5的相对流量和分支气体6的相对流量控制在某范围内，此时膨胀机膨胀端流量和增压端流量匹配而使增压膨胀机整机效率优良，使得本发明的方法性能先进，能耗低，使用范围广，投资成本低。
附图说明
图1是本发明的一个实施例工艺流程示意图。
图2是本发明的另一个实施例工艺流程示意图。
图3是本发明的又一个实施例工艺流程示意图。
图4是本发明所述的一种纯化气体进入间接换热器的换热通道示意图。
具体实施方式
下面将结合附图对本发明作详细的介绍：本发明所述的利用深冷技术分离空气的系统，该系统主要由精馏装置，间接换热器以及对原料空气进行预处理的压缩、预冷和纯化装置组成，其特征在于所述的压缩、预冷和纯化装置包括：
一可将变成压缩空气的低压压缩机或由一体机的低压段构成的低压压缩机构；
一可将压缩空气进行预冷变成预冷空气的空气预冷器；
一可将预冷空气进行净化变成净化气体的纯化机构；
所述的精馏装置至少由压力塔C1和低压塔C2及连接压力塔C1顶部和低压塔C2底部的主冷凝蒸发器K1构成的精馏塔组成；
所述的纯化机构后面配置有一可将净化气体一部分或全部压缩成为高压气体的高压压缩机或由一体机的高压段构成的高压压缩机构；
所述的高压压缩机或高压压缩机构后面相接有至少三条管路，第一管路连接于一可将高压气体进一步压缩成再高压气体的压缩机，该压缩机出口联通于所述可使再高压气体冷却的间接换热器，该路换热通道与所述精馏装置相连通；一与所述压缩机直接机械耦合的膨胀机，第二管路联通于可使高压气体冷却的间接换热器后，在其中部用连管连接于所述膨胀机，并所述膨胀机的出口与所述精馏装置相连通；第三管路直接联通于所述的间接换热器，该路换热通道也与所述精馏装置相连通；
所述的精馏装置至少设置有一路引出液体的液体管路，并通过一加压设备接入所述的可使液体复热后作为气体产品的间接换热器。
本发明所述的纯化机构后面配置有一可将净化气体一部分压缩成为高压气体的高压压缩机或由一体机的高压段构成的高压压缩机构；净化机构后面配置有一根第四管路连通于所述可将净化气体另一部分冷却成直接流体的间接换热器，并通过该间接换热器直接连通于所述的精馏装置；所述的第一管路通过所述间接换热器后再通过第一节流阀与所述精馏装置相连通；所述的第三管路在通过所述间接换热器后再通过第三节流阀与所述精馏装置相连通。
本发明所述的间接换热器上至少设置有二路液体换热通道，一路液体换热通道为液氧换热通道，该液氧换热通道的进口通过相连通的液氧泵与所述的精馏装置相连通，出口相接有氧气产品管道；另一路为液氮换热通道，该液氮换热通道的进口通过相连通的液氮泵与所述的精馏装置相连通，出口相接有氮气产品管道。
本发明所述的精馏装置中配置有粗氩塔和氩精馏塔；所述的间接换热器上还设置有粗氩换热通道和液氩换热通道，所述的粗氩换热通道直接与粗氩塔相连通，出口相接有引出复热后粗氩气的管道；所述的液氩换热通道的进口通过相连通的液氩泵与所述的精馏装置的氩精馏塔相连通，出口相接有氩气产品管道。
所述的一体机是指低压压缩机和高压压缩机因被同一传动装置驱动而为一体的机器。
一种利用如上所述系统进行深冷技术分离空气的方法，该方法是：
    —原料空气001在空气低压压缩机ATC1或一体机的低压段压缩并经空气预冷系统预冷和纯化系统净化成纯化气体01；     —所述纯化空气01的一部分或全部构成的气体3经高压压缩机ATC2或一体机的高压段压缩为高压气体4，该高压气体4的压力高于纯化气体3的压力；
    —所述高压空气4分成至少三路：第一路分支气体5被压缩机BT进一步压缩成再高压气体8进入间接换热器E1冷却，并在所述间接换热器E1底部抽出第一路流体11；第二路分支气体6直接经所述间接换热器E1冷却，并在所述间接换热器E1中部抽出第二路气体9；第三路分支气体7直接经所述间接换热器E1冷却，并在所述间接换热器E1底部抽出第三路流体12；所述地一路流体11和第三路流体12或为全液态或为超临界态流体；
    所述第二路气体9进入一膨胀机ET1膨胀到压力塔C1的工作压力成全气态或气液两相流体10进入精馏系统49；
    所述第一路流体11或经节流阀V1节流到所述压力塔C1的工作压力成全液态或气液两相流体132或/和经液体膨胀机ET2膨胀成液体131，再经节流阀V8节流到所述压力塔C1的工作压力成全液态或气液两相流体133进入所述精馏系统49；
    所述第三路流体12经节流阀V2节流到所述压力塔C1的工作压力成全液态或气液两相流体14进入所述精馏系统49；
    从精馏装置中抽出的液氧26、液氮35以及液氩39至少一部分分别经液氧泵OP、液氮泵NP及液氩泵AP加压后进入所述间接换热器E1，至少被所述第二路分支气体6、第三路分支气体7、再高压气体8在所述间接换热器E1中间复热后成为氧气产品50、氮气产品51以及氩气产品52。
所述的纯化空气01还有一路分支气体1经所述间接换热器E1冷却成至少部分是气态的流体2进入所述精馏装置49参与气体的精馏过程。
实施例：
在图1的实施例中，原料空气001在空气低压压缩机ATC1压缩到如0.6MPaA并经已知的空气预冷系统预冷和纯化系统净化成气体01。空气01的一部分气体3经高压压缩机ATC2压缩到如4.8MPaA的气体4。
空气4分成3路：分支气体5被压缩机BT进一步压缩到如7MPaA的气体8进入间接换热器E1冷却，并在E1底部抽出超临界流体11； 11经节流阀V1节流到压力塔C1的工作压力0.55MPaA成流体132进入精馏系统49参与精馏。替代地，11也可经液体膨胀机ET2膨胀到如压力1MPaA成全液体131再经节流阀V8节流到压力塔C1的工作压力成流体133进入精馏系统49参与精馏。流体132和133一般是含少量汽化的液体，优选为全液体。
空气4的分支气体6直接经间接换热器E1冷却，并在所述间接换热器E1中部抽出温度为167K的气体9进入膨胀机ET1膨胀到压力塔C1的工作压力成流体10进入精馏系统49参与精馏。流体10是全气态或含有少量液体的气体。 
空气4的分支气体7经间接换热器E1冷却，并在E1底部抽出流体12，12经节流阀V2节流成流体14进入精馏系统49参与精馏。 
膨胀机ET1与压缩机BT直接机械耦合，做功膨胀产生的能量经所述压缩机BT用于进一步压缩气体5。
空气01的分支气体1经间接换热器E1冷却成流体2，所述流体2至少部分是气态的，优选为全气态，进入精馏系统49参与精馏。
精馏系统49以已知的方式运行，液氧25从精馏系统49中抽出，一部分液氧26经液氧泵OP加压后进入间接换热器E1，被热流体复热成带压气体取出。
如需替代或附加地产生内压缩氮气，液氮31从精馏系统49中抽出，一部分液氮35经液氮泵NP加压后进入间接换热器E1，被热流体复热成带压气体取出。
粗氩塔C701产生的粗氩气经间接换热器E1复热后出冷箱。
图2中，精馏系统49除了用于氧氮分离的装置外还有一个已知的用于获取液态纯氩的氩精馏系统。同样地如需替代或附加地产生内压缩氩气，液氩37从精馏系统49中抽出，一部分液氩39经液氩泵AP加压后进入间接换热器E1，被热流体复热成带压气体取出。
图3中，精馏系统49对应的是双塔系统，没有增效塔C701、粗氩冷凝器K701及与低压塔和压力塔连接的装置。
    图4与图1至图3的主要区别是气体01需全部进入高压压缩机ATC2压缩，没有了经间接换热器E1冷却成流体2的空气01的分支气体1。

Claims (6)

1.一种利用深冷技术分离空气的系统，该系统主要由精馏装置，间接换热器以及对原料空气进行预处理的压缩、预冷和纯化装置组成，其特征在于所述的压缩、预冷和纯化装置包括：一可将变成压缩空气的低压压缩机或由一体机的低压段构成的低压压缩机构；
    一可将压缩空气进行预冷变成预冷空气的空气预冷器；
    一可将预冷空气进行净化变成净化气体的纯化机构；
所述的精馏装置至少由压力塔C1和低压塔C2及连接压力塔C1顶部和低压塔C2底部的主冷凝蒸发器K1构成的精馏塔组成；
所述的纯化机构后面配置有一可将净化气体一部分或全部压缩成为高压气体的高压压缩机或由一体机的高压段构成的高压压缩机构；
所述的高压压缩机或高压压缩机构后面相接有至少三条管路，第一管路连接于一可将高压气体进一步压缩成再高压气体的压缩机，该压缩机出口联通于所述可使再高压气体冷却的间接换热器，该路换热通道与所述精馏装置相连通；一与所述压缩机直接机械耦合的膨胀机，第二管路联通于可使高压气体冷却的间接换热器后，在其中部用连管连接于所述膨胀机，并所述膨胀机的出口与所述精馏装置相连通；第三管路直接联通于所述的间接换热器，该路换热通道也与所述精馏装置相连通；
所述的精馏装置至少设置有一路引出液体的液体管路，并通过一加压设备接入所述的可使液体复热后作为气体产品的间接换热器。
2.根据权利要求1所述的利用深冷技术分离空气的系统，其特征在于所述的纯化机构后面配置有一可将净化气体一部分压缩成为高压气体的高压压缩机或由一体机的高压段构成的高压压缩机构；净化机构后面配置有一根第四管路连通于所述可将净化气体另一部分冷却成直接流体的间接换热器，并通过该间接换热器直接连通于所述的精馏装置；所述的第一管路通过所述间接换热器后再通过第一节流阀与所述精馏装置相连通；所述的第三管路在通过所述间接换热器后再通过第三节流阀与所述精馏装置相连通。
3.根据权利要求1或2所述的利用深冷技术分离空气的系统，其特征在于所述的间接换热器上至少设置有二路液体换热通道，一路液体换热通道为液氧换热通道，该液氧换热通道的进口通过相连通的液氧泵与所述的精馏装置相连通，出口相接有氧气产品管道；另一路为液氮换热通道，该液氮换热通道的进口通过相连通的液氮泵与所述的精馏装置相连通，出口相接有氮气产品管道。
4.根据权利要求3所述的利用深冷技术分离空气的系统，其特征在于所述的精馏装置中配置有粗氩塔和氩精馏塔；所述的间接换热器上还设置有粗氩换热通道和液氩换热通道，所述的粗氩换热通道直接与粗氩塔相连通，出口相接有引出复热后粗氩气的管道；所述的液氩换热通道的进口通过相连通的液氩泵与所述的精馏装置的氩精馏塔相连通，出口相接有氩气产品管道。
5.一种利用如权利要求1或2或3或4所述系统进行深冷技术分离空气的方法，其特征在于该方法是：
    —原料空气001在空气低压压缩机ATC1或一体机的低压段压缩并经空气预冷系统预冷和纯化系统净化成纯化气体01；     —所述纯化空气01的一部分或全部构成的气体3经高压压缩机ATC2或一体机的高压段压缩为高压气体4，该高压气体4的压力高于纯化气体3的压力；
    —所述高压空气4分成至少三路：第一路分支气体5被压缩机BT进一步压缩成再高压气体8进入间接换热器E1冷却，并在所述间接换热器E1底部抽出第一路流体11；第二路分支气体6直接经所述间接换热器E1冷却，并在所述间接换热器E1中部抽出第二路气体9；第三路分支气体7直接经所述间接换热器E1冷却，并在所述间接换热器E1底部抽出第三路流体12；所述地一路流体11和第三路流体12或为全液态或为超临界态流体；
    所述第二路气体9进入一膨胀机ET1膨胀到压力塔C1的工作压力成全气态或气液两相流体10进入精馏系统49；
    所述第一路流体11或经节流阀V1节流到所述压力塔C1的工作压力成全液态或气液两相流体132或/和经液体膨胀机ET2膨胀成液体131，再经节流阀V8节流到所述压力塔C1的工作压力成全液态或气液两相流体133进入所述精馏系统49；
    所述第三路流体12经节流阀V2节流到所述压力塔C1的工作压力成全液态或气液两相流体14进入所述精馏系统49；
    从精馏装置中抽出的液氧26、液氮35以及液氩39至少一部分分别经液氧泵OP、液氮泵NP及液氩泵AP加压后进入所述间接换热器E1，至少被所述第二路分支气体6、第三路分支气体7、再高压气体8在所述间接换热器E1中间复热后成为氧气产品50、氮气产品51以及氩气产品52。
6.根据权利要求5所述深冷技术分离空气的方法，其特征在于所述的纯化空气01还有一路分支气体1经所述间接换热器E1冷却成至少部分是气态的流体2进入所述精馏装置49参与气体的精馏过程。
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