CN101424478A - 用于低温空气分馏的方法 - Google Patents

用于低温空气分馏的方法 Download PDF

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CN101424478A
CN101424478A CNA2008101667977A CN200810166797A CN101424478A CN 101424478 A CN101424478 A CN 101424478A CN A2008101667977 A CNA2008101667977 A CN A2008101667977A CN 200810166797 A CN200810166797 A CN 200810166797A CN 101424478 A CN101424478 A CN 101424478A
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heat exchanger
remaining fraction
tower
main heat
discharge
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S·洛赫纳
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Linde GmbH
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Abstract

用于低温空气分馏的方法。进料空气(8)在主热交换器(9)中冷却，并引入用于氮氧分离的蒸馏塔系统(11，43)中，该系统具有至少一个用于获得氮的单塔(12)。从该用于氮氧分离的蒸馏塔系统排出至少一种富含氮或富含氧的产物流(15，16，17；53；51，56，57；19，60)，并在该主热交换器(9)中加热。至少偶尔将来自外部来源的流体送入液体罐(70)中。至少偶尔从该液体罐(70)以液态排出流体(71)，在该主热交换器(9)中蒸发，并获得额外的气态产物(72，73)。

Description

用于低温空气分馏的方法
技术领域
本发明涉及用于低温空气分馏的方法。
背景技术
例如从Hausen/Linde，Tieftemperaturtechnik[Cryogenic engineering]，1985年第2版，第4章(第281至337页)已知用于低温分馏空气的方法和装置。EP 412 793 B2、EP 773 417 B1、EP 780 648 B1、EP 807 792 B1、EP 932 004 A2以及US 2007/204652 A1的导言(SPECTRA)描述了空气分馏方法类型的实施例。已知在这些方法中，从单塔排出第一富含氧的残余馏份，使其蒸发，并在膨胀机中以做功的方式使已蒸发的残余馏份的至少一部分膨胀，从而产生弥补交换损失所需的冷冻，若需要则用于产物液化。在膨胀机的出口压力下排出第一残余馏份，通常大约在大气压下，通常仅可用作用于提纯进料空气的吸附装置的再生气体。在SPECTRA方法中，在此情况下，将第二残余馏份与第一残余馏份一起从单塔排出，并至少部分地蒸发；选择性地，两种残余馏份在单塔的不同位置排出，并彼此独立地蒸发，例如在单塔的顶部冷凝器的不同通道中。
发明内容
本发明的目的是在经济上特别有利地实施该方法和操作该设备。
该目的是通过本发明实现的。
来自液体罐的外部流体并不是按照惯例借助外部热交换器(例如水浴蒸发器或空气加热的蒸发器)进行加热，而是在主热交换器中加热，在该主热交换器中将用于蒸馏塔系统的进料空气冷却。由此，通过将存在于外部流体中的冷量传输至主热交换器中的进料空气从而可以回收以用于分馏过程。
该流体源自“外部来源”，换而言之，并非来自用于氮氧分离的蒸馏塔系统的一个分离塔，也非来自与用于氮氧分离的蒸馏塔系统的下游相连的分离塔。优选地，例如借助储液罐(tanker)从用于产生液化气体的另一个装置进行输送。在此情况下，可以是具有用于氮氧分离的蒸馏塔系统的一种产物流的化学组成的流体。然而，优选地该流体具有不同于这些产物流的组成，而是例如由氩或氢组成。因此，根据本发明的方法特别适合于向半导体工业的工厂供应工业用气。这通常要求少量的氩和/或纯氧，从而不值得连接用以在氮氧分离蒸馏塔系统的下游获得氩的区段。此外，并非在空气分馏设备中获得的诸如氢的气体的冷量用于空气分馏，并由此减少分馏的能量消耗。
该“主热交换器”优选由单独的热交换区段(block)形成。在相对较大的设备中，可以有利地通过与温度过程(temperature course)平行地连接的多个联动装置(trains)实现热交换器，该联动装置是由彼此分离的构件形成的。原则上，用于各个联动装置的热交换器可以由两个或更多个串联的区段形成。
若在液体罐与主热交换器之间流体压力不升高，则是有利的。
优选在不高于液体罐的操作压力的压力下将该流体引入主热交换器中。液体罐的操作压力可以是恒定的或者上下波动，例如在维持该罐和排气系统内的压力的范围内。在液体罐的操作压力上下波动的情况下，在此是指瞬时操作压力。
有利的是液体罐的操作压力比大气压高至少1巴，优选比气态副产物的产物压力高至少1巴，在该压力下该副产物被释放至一种应用(application)或再压缩单元。液体罐的操作压力例如为2至36巴，优选为5至16巴。超过大气压的压力可以通过任何已知的措施形成，例如通过用对应压力下的流体装载或者通过增压蒸发。
平行提交的德国专利申请102007051184.3(申请人的内部文件编号：P07164-DE/AVA＝EM-GTG1267a)以及与其对应的申请中所述特征的更详细的描述也适用于此处所述的方法及对应的设备。
此外，本发明还涉及一种设备。
下面参考附图中所图示的实施例更详细地阐述本发明以及本发明的其他细节。
附图说明
附图所示为根据本发明的实施方案的示意图。
具体实施方式
实施例的蒸馏塔系统具有单塔12及纯氧塔38(本发明同样适用于不包括纯氧塔的类似方法)。借助空气压缩机抽吸大气空气1通过过滤器2，并在此压缩至绝对压力6至20巴，优选约为9巴。在流过后冷却器4和水分离器5之后，在具有一对用优选为分子筛的吸附材料填充的容器的提纯装置7内提纯经压缩的空气6。在主热交换器9内将经提纯的空气8冷却至约为露点，并部分液化。经由节流阀51将经冷却的空气10的第一部分11引入单塔12中。优选将所述经冷却的空气送入底部上方的一些实际或理论的塔板。
单塔12(位于顶部)的操作压力为6至20巴，优选约为9巴。它的顶部冷凝器通过第二残余馏份18及第一残余馏份14加以冷却。从该单塔12的底部排出第一残余馏份14，从空气进料口上方的一些实际或理论的塔板的中间点或者在与此相同的高度排出第二残余馏份18。
作为单塔12的主要产物，在顶部排出气态氮15、16，在主热交换器9内加热至约为环境温度，并最终经由管线17作为受压的气态产物(PGAN)排出。来自顶部冷凝器13的冷凝物52的一部分53可以作为产物液氮(PLIN)获得；残余物54作为回流送回单塔的顶部。
在2至9巴，优选约为4巴的压力下，在顶部冷凝器13中使第二残余馏份18蒸发，并以气态经由管线19流至制冷压缩机30，于其中被再压缩至约为单塔的操作压力。将该经再压缩的残余馏份31冷却回至主热交换器9中的塔温，并最终经由管线32送回至底部的单塔12。
在2至9巴，优选约为4巴的压力下，在顶部冷凝器13中使第一残余馏份14蒸发，并以气态经由管线19流至主热交换器9的冷端。在中间温度下再次排出(管线20)第一残余馏份的第一部分20。第二部分残留在主热交换器9中，在此再次加热至约为环境温度，并经由管线60作为不纯的气态氧产物(GOX-Imp.)排出该设备。第一残余馏份的第一部分20膨胀至高于大气压约300毫巴，从而在实施例中作为透平膨胀机构成的膨胀机21内做功。膨胀机以机械方式连接至制冷压缩机30以及在实施例中通过油制动器形成的阻断装置22。在主热交换器9中加热已膨胀的第一残余馏份23至约为环境温度。若适合在加热装置28中加热之后，将热的第一残余馏份24吹出至大气(管线25)和/或在提纯装置7中用作再生气体26、27。选择性地或者额外地，不纯的氧产物可以从再压缩的第二残余馏份31分出，并在主热交换器9中加热至约为环境温度。
从单塔12的中间点以液态排出基本上不含低挥发性杂质的含氧流36，该中间点设置在空气进料口上方的5至25个理论或实际的塔板。若合适，在纯氧塔38的底部蒸发器37中使该含氧流36过冷，并经由管线39及节流阀40送至纯氧塔38的顶部。纯氧塔38(顶部)的操作压力为1.3至4巴，优选约为2.5巴。
额外地借助经冷却的进料空气10的第二部分42冷却纯氧塔38的底部蒸发器37。在此情况下，至少部分地，例如完全地，使进料空气流42冷凝，并经由管线43流至单塔12，其中大约在残余进料空气11的进料高度处引入。
从纯氧塔38的底部以液态排出纯氧产物流41，借助泵55施加至2至100巴，优选约为12巴的提高的压力，经由管线56送至主热交换器9的冷端，在此于提高的压力下蒸发，并加热至约为环境温度，并最终经由管线57作为气态产物(GOX-IC)获得。
纯氧塔38的塔顶馏出气体58混合至经膨胀的第一残余馏份23。若合适，一部分进料空气经由侧流管线59用于泵保护该制冷压缩机30至其入口(防喘振控制)。
若需要，液态氧可以作为液态产物于该泵55(图中未示出)上游和/或下游从该设备排出。此外，在与用进料空气(图中未示出)间接热交换的情况下，来自液体罐的外部液体，例如液态氩、液态氮或液态氧可以在主热交换器9中蒸发。
用作为“流体”偶尔来自储液罐的液态氩填充该液体罐70。在约12巴，即液体罐的操作压力下引入该流体。经由管线71在约12巴下连续排出液态流体，在该压力下于主热交换器9中蒸发，加热，并最终作为额外的气态产物经由管线72和73排出。
此外，可以从液体罐70排出受压的液态流体的其他流74，在借助外部热载体(例如大气空气或水)加热的蒸发器75中蒸发，并经由管线76添加至额外的气态产物。然而，该蒸发器75还可以在主热交换器9损坏的情况下用于应急供应。借助阀门77和78调节流速。
根据本发明的方法及对应的装置可以特别有利地用于半导体工业中或者用于火成硅酸制造，其要求氮和不纯的氧，若需要则将纯氧作为产物。

Claims (12)

1、用于低温空气分馏的方法，其中
-进料空气(8)在主热交换器(9)中冷却，并引入用于氮氧分离的蒸馏塔系统(11，43)中，该系统具有至少一个用于获得氮的单塔(12)，
-从该用于氮氧分离的蒸馏塔系统排出至少一种富含氮或富含氧的产物流(15，16，17；53；51，56，57；19，60)，并在该主热交换器(9)中加热，
-该单塔(12)具有顶部冷凝器(13)，于该顶部冷凝器中将来自该单塔的上部区域的蒸汽至少部分地冷凝，
-从该单塔(12)的下部区域以液态排出第一残余馏份(14，19)，并在该顶部冷凝器(13)中至少部分地蒸发，
-在该顶部冷凝器(13)的下游在膨胀机(21)中使该第一残余馏份(19)的至少第一部分(20)膨胀以做功，及其中
-从该单塔(12)的下部区域或中间区域排出第二残余馏份(18，29)，再压缩(30)，随后将至少第一部分送回(32)至该单塔(12)，
其特征在于，
-至少偶尔将来自外部来源的流体送入液体罐(70)中，及
-至少偶尔从该液体罐(70)以液态排出流体(71)，在该主热交换器(9)中蒸发，并获得额外的气态产物(72，73)，其中该来自外部来源的流体和该额外的气态产物(72，73)均不与来自该蒸馏塔系统的产物混合。
2、根据权利要求1的方法，其特征在于，所述流体(71)在所述液体罐(70)与所述主热交换器(9)之间并不升高压力。
3、根据权利要求1或2的方法，其特征在于，在不高于所述液体罐(70)的操作压力的压力下将所述流体(71)引入所述主热交换器(9)。
4、根据权利要求1、2或3的方法，其特征在于，所述液体罐(70)的操作压力高于大气压至少1巴。
5、根据权利要求1至4之一的方法，其特征在于，借助制冷压缩机(30)再压缩所述第二残余馏份(18，29)。
6、根据权利要求1至5之一的方法，其特征在于，在做功膨胀(21)中产生的机械能至少部分地被用于对所述第二残余馏份实施再压缩(30)。
7、根据权利要求1至6之一的方法，其特征在于，不将所述第一残余馏份(19)的第二部分在所述顶部冷凝器(13)的下游引入所述膨胀机(21)中，而是作为不纯的气态氧产物(60)排出，和/或于再压缩(30)的下游将所述第二残余馏份的第二部分作为不纯的气态氧产物(160)排出。
8、根据权利要求1至7之一的方法，其特征在于，
-含氧流(36)从所述单塔(12)于中间点排出，并送至(39)纯氧塔(38)，及
-从所述纯氧塔(38)的下部区域以液态排出纯氧产物流(41)，
-若需要在压力上升(55)之后，使处于液态的纯氧产物流(41，56)蒸发，并在所述主热交换器(9)中与所述进料空气(8)相对地进行加热，以及
-最终获得气态产物(57)。
9、根据权利要求1至8之一的方法，其特征在于，于所述单塔(12)的底部排出所述第一残余馏份(14)。
10、根据权利要求1至9之一的方法，其特征在于，从所述单塔(12)的中间点排出所述第二残余馏份(18)，该中间点设置在底部上方，特别是在排出所述第一残余馏份(14)的位置的上方。
11、根据权利要求1至10之一的方法，其特征在于，所述主热交换器(9)和所述顶部冷凝器(13)是通过彼此分离的装置形成的。
12、用于低温空气分馏的设备，其具有
-用于氮氧分离的蒸馏塔系统，该系统具有至少一个用于获得氮的单塔(12)，
-用于冷却进料空气(8)的主热交换器(9)，
-将经冷却的进料空气引入该用于氮氧分离的蒸馏塔系统的进料空气管线(11，43)，
-从该用于氮氧分离的蒸馏塔系统将富含氮或富含氧的产物流(15，16，17；53；51，56，57；19，60)送至该主热交换器(9)的装置，
-至少部分地冷凝来自该单塔的上部区域的蒸汽的顶部冷凝器(13)，
-从该单塔(12)的下部区域将第一液态残余馏份(14，19)送至该顶部冷凝器(13)的装置，
-在该顶部冷凝器(13)的下游使该第一残余馏份(19)的至少第一部分(20)做功膨胀的膨胀机(21)，
-用于再压缩来自该单塔(12)的下部区域或中间区域的第二残余馏份(18，29)的再压缩机(30)，
-及具有将经再压缩的第二残余馏份的至少第一部分引入该单塔(12)内的装置，
其特征在于，
-用于储存来自外部来源的流体的液体罐，及
-至少偶尔从该液体罐(70)以液态排出流体(71)并使其在该主热交换器(9)内蒸发并获得额外的气态产物(72，73)的装置，
-其中该设备不具有用于将该来自外部来源的流体或该额外的气态产物(72，73)与来自该蒸馏塔系统的产物混合的装置。
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