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CN203980791U - 一种生产带压氮气产品的装置 - Google Patents

一种生产带压氮气产品的装置 Download PDF

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CN203980791U
CN203980791U CN201420305156.6U CN201420305156U CN203980791U CN 203980791 U CN203980791 U CN 203980791U CN 201420305156 U CN201420305156 U CN 201420305156U CN 203980791 U CN203980791 U CN 203980791U
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nitrogen
heat exchanger
pressure
pressure column
gas
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韩一松
谭芳
翟晖
艾绍华
张猛
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Hangzhou Hangyang Co Ltd
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Hangzhou Hangyang Co Ltd
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    • 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
    • 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
    • F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
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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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • 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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    • 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

一种生产带压氮气产品的装置，该装置主要由一个精馏塔系统、一个换热系统和一个膨胀机制冷系统紧密耦合组成，三者通过管道和阀门相连通，并实现将部分返流污氮气增压送入精馏塔的功能；其中所述的精馏塔系统至少由一个压力塔和一个冷凝蒸发器组成，或由一个压力塔、一个冷凝蒸发器和一个低压塔组成；它提高了氮气产品的提取率，降低了运行能耗，节省了设备投资。

Description

一种生产带压氮气产品的装置
技术领域
本实用新型涉及一种生产带压氮气产品的装置，属于低温技术领域。 
背景技术
随着冶金、石化、煤化工、电子等工业的快速发展，在空分的应用领域中，带压氮气的多用途性使得有时上述工业领域对带压氮气的需求量远比氧气要多。有时为了节约投资和能耗，在项目改造时需要从出空分装置的废氮气中再次提取带压氮气，变废为宝。上述两种情况都需要能够找到一种设备投资便宜，运行能耗低的方法和装置。 
实用新型内容
本实用新型的目的在于克服现有技术存在的不足，而提供一种以纯净空气、特别是废氮气为原料生产以带压氮气作为唯一产品或主要产品的生产带压氮气产品的方法及装置，该方法和装置提高了氮气产品的提取率，降低了能耗，节约了设备投资。 
为了实现上述目的，本实用新型提供了一种返流污氮气部分膨胀制冷和部分增压进压力塔相耦合生产带压氮气产品的方法，它具有一个精馏塔系统，一个换热系统和一个膨胀机制冷系统，其中所述精馏塔系统由至少一个压力塔和一个冷凝蒸发器组成，所述的方法包括如下步骤： 
a将纯化、干燥和带压的原料气冷却至饱和或近饱和状态进入压力塔进行精馏，返流增压冷却后的污氮气也进入压力塔参与精馏； 
b在压力塔顶部获得的压力氮气和在压力塔底部获得液态流体；压力塔顶部的部分压力氮气作为产品氮气抽出，并复热出冷箱，其余氮气进入冷凝蒸发器冷凝成液氮； 
c部分液氮作为液氮产品抽出，其余液氮回流至压力塔顶部作为精馏的回流液；底部的液态流体经节流进入冷凝蒸发器，一部分作为安全排放液体，其余部分蒸发成气体，作为返流污氮气出精馏塔系统； 
d一部分返流污氮气进入换热器系统复热并在中部抽出后去膨胀机膨胀端膨胀制冷后复热出冷箱；另一部分返流污氮气进入换热器系统复热并在中部抽出后去膨胀机增压端增压冷却后进入压力塔继续参与精馏或这部分返流污氮气直接去膨胀机增压端增压冷却后进入压力塔继续参与精馏。 
本实用新型所述的精馏塔系统组成中还包括一低压塔，其中的步骤c是：部分液氮作为液氮产品抽出，部分液氮回流至压力塔顶部作为压力塔精馏的回流液，其余液氮经节流后进入低压塔顶部作为低压塔上段精馏的回流液；塔底的液态流体经节流进入低压塔中部作为低压塔下段提馏的回流液；从低压塔顶部抽出的次压氮气经复热出冷箱可作为次压氮气产品； 返流污氮气从低压塔中部或下部出精馏塔系统。 
所述膨胀机的增压端和所述膨胀端直接机械耦合，所述膨胀端的输出功为所述增压端提供动力；所述污氮气的一部分经膨胀机膨胀端膨胀制冷后复热出冷箱至大气压后离开；所述污氮气的一部分经膨胀机增压端增压冷却后进入压力塔参与精馏。 
所述原料气是空气或氮含量占主要成分的气体；所述压力塔的操作压力不小于0.4MPaA。 
一种生产带压氮气产品的装置，该装置主要由一个精馏塔系统、一个换热系统和一个膨胀机制冷系统紧密耦合组成，三者通过管道和阀门相连通，并实现将部分返流污氮气增压送入精馏塔的功能；其中所述的精馏塔系统至少由一个压力塔和一个冷凝蒸发器组成，或由一个压力塔、一个冷凝蒸发器和一个低压塔组成。 
所述膨胀机制冷系统由一个带膨胀叶轮的膨胀端、一个带增压叶轮的增压端以及其他辅助性部件组成；所述膨胀端和所述增压端通过单轴直接连接或通过齿轮箱间接连接。 
所述膨胀端和增压端的返流污氮气的比例由所述两端入口支管上的阀门或其他调节装置进行调节，并实现流量匹配。 
所述的换热系统至少包括一主换热器，所述主换热器冷端设置有一供从所述精馏系统中出来的返流污氮气部分或全部复热的第一通道，该所述第一通道出口通过管道连通所述膨胀机的膨胀端；所述主换热器冷端设置有一供膨胀后返流污氮气经所述膨胀端ET出口通过管道连通进入所述主换热器的第二通道，所述返流污氮气经所述第二通道复热离开；所述主换热器中部设置有一供返流增压冷却后的污氮气经所述膨胀机增压端出口通过管道连通进入所述主换热器的第三通道，所述第三通道出口由管道连通经所述主换热器E1冷却后的原料气汇合流道后进入或直接进入所述压力塔。 
传统的返流污氮膨胀流程，返流污氮从精馏塔抽出后不再通过任何方式再回到压力塔进行精馏，本实用新型的优点是利用从精馏塔抽出的返流污氮气一方面通过膨胀制冷，另一方面利用增压让部分返流污氮气获得再次进入压力塔参与精馏的能力。 
本实用新型生产的压力氮气压力不小于0.35MPaA，纯度可达99.999％以上，产品提取率大大提高，特别是压力氮气产品提取率可比上述传统方法提高10％到40％，大大降低了产品的单位能耗，同时节省氮气压缩机等的设备投资。 
附图说明
图1是本实用新型所述单塔系统的一个实施例结构原理示意图。 
图2是本实用新型所述单塔系统的另一个实施例结构原理示意图。 
图3是本实用新型所述双塔系统的一个实施例结构原理示意图。 
图4是本实用新型所述双塔系统的另一个实施例结构原理示意图。 
图5是本实用新型所述双塔系统的又一个实施例结构原理示意图。 
图6是本实用新型所述双塔系统的再一个实施例结构原理示意图。 
具体实施方式
下面将结合附图对本实用新型作详细的介绍：附图所示，本实用新型所述返流污氮气部分膨胀制冷和部分增压进压力塔相耦合生产带压氮气产品的方法，它具有一个精馏塔系统，一个换热系统和一个膨胀机制冷系统，其中所述精馏塔系统由至少一个压力塔和一个冷凝蒸发器组成，所述的方法包括如下步骤： 
a将纯化、干燥和带压的原料气冷却至饱和或近饱和状态进入压力塔进行精馏，返流增压冷却后的污氮气也进入压力塔参与精馏； 
b在压力塔顶部获得的压力氮气和在压力塔底部获得液态流体；压力塔顶部的部分压力氮气作为产品氮气抽出，并复热出冷箱，其余氮气进入冷凝蒸发器冷凝成液氮； 
c部分液氮作为液氮产品抽出，其余液氮回流至压力塔顶部作为精馏的回流液；底部的液态流体经节流进入冷凝蒸发器，一部分作为安全排放液体，其余部分蒸发成气体，作为返流污氮气出精馏塔系统； 
d一部分返流污氮气进入换热器系统复热并在中部抽出后去膨胀机膨胀端膨胀制冷后复热出冷箱；另一部分返流污氮气进入换热器系统复热并在中部抽出后去膨胀机增压端增压冷却后进入压力塔继续参与精馏或这部分返流污氮气直接去膨胀机增压端增压冷却后进入压力塔继续参与精馏。 
本实用新型所述的精馏塔系统组成中还包括一低压塔，其中的步骤c是：部分液氮作为液氮产品抽出，部分液氮回流至压力塔顶部作为压力塔精馏的回流液，其余液氮经节流后进入低压塔顶部作为低压塔上段精馏的回流液；塔底的液态流体经节流进入低压塔中部作为低压塔下段提馏的回流液；从低压塔顶部抽出的次压氮气经复热出冷箱可作为次压氮气产品；返流污氮气从低压塔中部或下部出精馏塔系统。 
所述膨胀机的增压端和所述膨胀端直接机械耦合，所述膨胀端的输出功为所述增压端提供动力；所述污氮气的一部分经膨胀机膨胀端膨胀制冷后复热出冷箱至大气压后离开；所述污氮气的一部分经膨胀机增压端增压冷却后进入压力塔参与精馏。 
所述原料气是空气或氮含量占主要成分的气体；所述压力塔的操作压力不小于0.4MPaA。 
一种用于如上所述生产带压氮气产品的方法的装置，该装置主要由一个精馏塔系统、一个换热系统和一个膨胀机制冷系统紧密耦合组成，三者通过管道和阀门相连通，并实现将部分返流污氮气增压送入精馏塔的功能；其中所述的精馏塔系统至少由一个压力塔C1和一个冷凝蒸发器K1组成，或由一个压力塔C1、一个冷凝蒸发器K1和一个低压塔C2组成。 
所述膨胀机制冷系统由一个带膨胀叶轮的膨胀端ET、一个带增压叶轮的增压端BT以及其他辅助性部件组成；所述膨胀端ET和所述增压端BT通过单轴直接连接或通过齿轮箱间接连接。 
所述膨胀端ET和增压端BT的返流污氮气10、11的比例由所述两端入口支管上的阀门或其他调节装置进行调节，并实现流量匹配。 
所述的换热系统至少包括一主换热器E1，所述主换热器E1冷端设置有一供从所述精馏系统中出来的返流污氮气09部分或全部复热的第一通道，该所述第一通道出口通过管道连通所述膨胀机的膨胀端ET；所述主换热器E1冷端设置有一供膨胀后返流污氮气12经所述膨胀端ET出口通过管道连通进入所述主换热器E1的第二通道，所述返流污氮气12经所述第二通道复热离开；所述主换热器E1中部设置有一供返流增压冷却后的污氮气13经所述膨胀机增压端BT出口通过管道连通进入所述主换热器E1的第三通道，所述第三通道出口由管道连通经所述主换热器E1冷却后的原料气01汇合流道后进入或直接进入所述压力塔C1。 
实施例： 
在图1的实施例中，氮含量占主要成分的气体00(如氮体积含量为97％、氧体积含量为2.9％、氩体积含量为0.1％)通过压缩机TC压缩到0.76MPaA，冷却后纯化干燥的原料气01进入换热器系统E1冷却，得到温度为101.3K的气体02后进入压力塔C1，该压力塔C1可以是筛板或填料塔，优选为填料塔，操作压力约为0.745MPaA。气体02和带液量5％的流体03经压力塔C1精馏后，在塔顶得到氮气04和塔底的液态流体08，氮气04从塔顶抽出后至少分成两路：分支05进入换热器系统E1，复热后得到纯度为99.999％、压力约为0.72MPaA的产品压力氮气；分支06进入冷凝蒸发器K1被冷凝成液体后的一部分经过冷器E2过冷后作为产品液氮，其余部分07进入压力塔C1塔顶作为回流液。液体08从塔底抽出经过冷器E2过冷和节流阀V1节流后进入冷凝蒸发器K1蒸发，蒸发后的气体09进入换热器系统E1复热，一部分气体10在换热器系统E1的中部位置如温度为110K处抽出后经膨胀机的膨胀端ET膨胀至约0.127MPaA后又进入换热器系统E1的冷端去复热后出冷箱离开。一部分气体11在换热器系统E1的中部位置如温度为110K处抽出后经膨胀机的增压端BT增压至约0.76MaA后进入换热器系统E1的相应中部位置如温度130K处，又经换热器系统E1冷却后成为带液量5％的流体03进入压力塔C1参与精馏。膨胀端ET与增压端BT通过单轴直接机械耦合，膨胀端膨胀做功产生的输出功被增压端BT利用，用于进一步压缩气体11。 
在图2的实施例中，蒸发后的气体09只有部分气体进入换热器系统E1复热，并在换热器系统E1的中部位置如温度为111K处抽出，气体10经膨胀机的膨胀端ET膨胀至约0.127MPaA，流体12又进入换热器系统E1的冷端去复热后出冷箱离开。气体09的一部分气 体11经膨胀机的增压端BT增压至约0.76MaA后进入换热器系统E1的相应中部位置如温度125K处，又经换热器系统E1冷却后成为带液量5％的流体03进入压力塔C1参与精馏。 
在图3的实施例中，氮含量占主要成分的气体00(如氮体积含量为97％、氧体积含量为2.9％、氩体积含量为0.1％)通过压缩机TC压缩到如0.76MPaA，冷却后的纯化干燥的原料气01进入换热器系统E1冷却，得到温度为102K的气体02进入压力塔C1，该压力塔C1可以是筛板或填料塔，优选为填料塔，操作压力约为0.745MPaA。气体02和带液量10％的流体03经压力塔C1精馏后，在塔顶得到氮气04和塔底的液态流体08，氮气04从塔顶抽出后至少分成两路：分支05进入换热器系统E1复热后得到纯度为99.999％、压力约为0.72MPaA的产品压力氮气；分支06进入冷凝蒸发器K1被冷凝成液体后的一部分07进入压力塔C1塔顶作为回流液，其余部分经过冷器E2过冷后部分经节流阀V4节流后作为产品液氮，部分经节流阀V2节流后进入低压塔C2的塔顶参与精馏。液体08从塔底抽出经过冷器E2过冷和节流阀V1节流后进入低压塔C2中下部参与精馏，该压力塔C2可以是筛板或填料塔，优选为填料塔，操作压力约为0.43MPaA。在低压塔C2的顶部抽出的氮气14经过冷器E2和换热器系统E1复热后得到纯度为99.999％、压力约为0.4MPaA的次压氮气产品。在低压塔C2的底部抽出的气体09进入换热器系统E1复热，一部分气体10在换热器系统E1的中部位置如温度为109K处抽出，进入膨胀机的膨胀端ET膨胀至约0.126MPaA后又进入换热器系统E1的冷端去复热后出冷箱离开。一部分气体11在换热器系统E1的中部位置如温度为109K处抽出，进入膨胀机的增压端BT增压至约0.76MaA后进入换热器系统E1的相应中部位置如温度130K处，又经换热器系统E1冷却后成为带液量10％的流体03进入压力塔C1参与精馏。膨胀端ET与增压端BT通过单轴直接机械耦合，膨胀端膨胀做功产生输出功被增压端BT利用，进一步压缩气体11。 
在图4的实施例中，蒸发后的气体09只有部分气体进入换热器系统E1复热，并在换热器系统E1的中部位置如温度为110K处抽出，气体10经膨胀机的膨胀端ET膨胀至约0.126MPaA，流体12又进入换热器系统E1的冷端去复热，后出冷箱离开。气体09的一部分气体11经膨胀机的增压端BT增压至约0.76MaA后进入换热器系统E1的相应中部位置如温度126K处，又经换热器系统E1冷却后成为带液量10％的流体03进入压力塔C1参与精馏。 
上述两个实施例仅是本实用新型的优选实施方式，但本实用新型并不限制于以上描述的具体实施例。如上述图3和图4对应的双塔系统的例子，低压塔C2可以生产带压的氮气产品，也可以如图5所述的例子，塔底的液体08进入低压塔C2顶部，并在低压塔C2的底部获得液氧和气体14，气体14经过冷器和换热器复热后作为带压氧气产品，该氧气纯度可达99.6％以上。低压塔C2也可以如图6所述的例子，分别在低压塔C2的塔顶和塔底抽出气体14和气 体16，气体14和气体16分别经过冷器和换热器复热后作为次压氮气产品和带压氧气产品。上述带压氧气产品的纯度可以根据需要获得，一般可达80％-99.99％。因此，在本实用新型的范畴下所作的各种变型或优化，也在本实用新型的保护范围内。 

Claims (4)

1.一种生产带压氮气产品的装置，其特征在于该装置主要由一个精馏塔系统、一个换热系统和一个膨胀机制冷系统紧密耦合组成，三者通过管道和阀门相连通，并实现将部分返流污氮气增压送入精馏塔的功能；其中所述的精馏塔系统至少由一个压力塔(C1)和一个冷凝蒸发器(K1)组成，或由一个压力塔(C1)、一个冷凝蒸发器(K1)和一个低压塔(C2)组成。 
2.根据权利要求1所述的生产带压氮气产品的装置，其特征在于所述膨胀机制冷系统由一个带膨胀叶轮的膨胀端(ET)、一个带增压叶轮的增压端(BT)以及其他辅助性部件组成；所述膨胀端(ET)和所述增压端(BT)通过单轴直接连接或通过齿轮箱间接连接。 
3.根据权利要求1所述的生产带压氮气产品的装置，其特征在于所述膨胀端(ET)和增压端(BT)的返流污氮气(10、11)的比例由所述两端入口支管上的阀门或其他调节装置进行调节，并实现流量匹配。 
4.根据权利要求1所述的生产带压氮气产品的装置，其特征在于所述的换热系统至少包括一主换热器(E1)，所述主换热器(E1)冷端设置有一供从所述精馏系统中出来的返流污氮(09部分或全部复热的第一通道，该所述第一通道出口通过管道连通所述膨胀机的膨胀端(ET)；所述主换热器(E1)冷端设置有一供膨胀后返流污氮气(12)经所述膨胀端(ET)出口通过管道连通进入所述主换热器(E1)的第二通道，所述返流污氮气(12)经所述第二通道复热开；所述主换热器(E1)中部设置有一供返流增压冷却后的污氮气(13)经所述膨胀机增压端(BT)出口通过管道连通进入所述主换热器(E1)的第三通道，所述第三通道出口由管道连通经所述主换热器(E1)冷却后的原料气(01)汇合流道后进入或直接进入所述压力塔(C1)。 
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CN104061756A (zh) * 2014-06-09 2014-09-24 杭州杭氧股份有限公司 返流污氮气部分膨胀制冷和部分增压进压力塔相耦合生产带压氮气产品的方法及装置
CN104534812A (zh) * 2015-01-04 2015-04-22 中煤能源黑龙江煤化工有限公司 一种应用于气体深冷分离设备主精馏塔
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CN113405318A (zh) * 2021-06-29 2021-09-17 杭州制氧机集团股份有限公司 一种使用单个精馏塔生产纯氮的装置及其使用方法

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CN104061756A (zh) * 2014-06-09 2014-09-24 杭州杭氧股份有限公司 返流污氮气部分膨胀制冷和部分增压进压力塔相耦合生产带压氮气产品的方法及装置
CN104534812A (zh) * 2015-01-04 2015-04-22 中煤能源黑龙江煤化工有限公司 一种应用于气体深冷分离设备主精馏塔
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CN106196886A (zh) * 2016-07-13 2016-12-07 浙江智海化工设备工程有限公司 一种新型低能耗氧内压缩氮膨胀无空气膨胀机的空分流程
CN113405318A (zh) * 2021-06-29 2021-09-17 杭州制氧机集团股份有限公司 一种使用单个精馏塔生产纯氮的装置及其使用方法
CN113405318B (zh) * 2021-06-29 2024-04-05 杭氧集团股份有限公司 一种使用单个精馏塔生产纯氮的装置的使用方法

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