CN1124345A - 低温分离空气的方法及装置 - Google Patents
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Abstract
本发明涉及低温分离空气的方法和装置。将经压缩、净化、和冷却的空气至少部分地送入双级精馏设备的压力级。从低压级中提取氧馏份和含氮馏份作为产品流。低压级的下部区域与压力级的上部区域呈热交换关系。在稳定运行时,大体全部流入低压级的回流液是从低压级下部区域抽取的,并将其导入缓冲容器。从缓冲容器流出的液体与从压力级上部区域流出的待冷凝气体进行间接热交换后部分被蒸发,同时,形成的蒸气被引入低压级的下部区域,剩余的液体至少部分地被送回到缓冲容器中。
Description
本发明涉及一种低温分离空气的方法及装置,在所述方法中,空气经压缩、净化、冷却,然后至少部分地被送入两级精馏设备的压力级中,接着,使从压力级流出的至少一种馏份在低压级中进一步分离,提取低压级中的氧馏份和含氮馏份作为产品流,并使低压级的下部区域和压力级的上部区域呈热交换关系。
精馏分离空气的原理已公开在有关的手册[例如由Hausen/Linde编著的“低温技术”(1985年第2版)的4.5章或由Winnacker/Kuechler编著的“化学工艺”第二卷(第3版)的第4章]以及“空气的蒸馏”[化学工程进展63卷35页-59页(Latimer撰写)]的文献中。上述两级精馏在一个双塔中以常规方式进行,双塔的低压级被设置在压力级的上方。(原则上双塔的低压级和压力级也可以分开设置。)通过使从低压级流出的液体蒸发形成用于压力级的回流,同时,在低压级中产生上升的蒸气。这种间接热交换是在一个冷凝蒸发器中进行的,该蒸发器设置在低压塔中,以常规的方式处于低压塔的底部(Sumpf)。原则上这种安排是有利的,因为省掉了一些将冷凝蒸发器的蒸发通道与低压塔连接起来的专用管道。可是也存在缺点。这样一来,冷凝蒸发器对于双塔的总高度而言不是不重要的,因此,装置的成本较高。此外,在装置停止运行时,低压级的全部回流液流入底部,而且被氮所污染。因此,在装置再次启动时,延长了启动时间,直到又能提供纯氧产品为止启动才能结束。
本发明的目的在于提供一种本说明书开始所描述的方法和装置,它们在经济上是有利的,尤其是通过降低成本或者通过提高运行的灵活性使其在经济上具有优越性。
实现上述目的的技术方案是:在稳定运行时,大体全部流入低压级的回流液从低压级的下部区域抽出,并将其送入一个缓冲容器中,从所述缓冲容器中抽取液体,使其与一从压力级上部区域流出的待冷凝的气体进行间接热交换而部分蒸发;将形成的蒸气至少部分地送入低压级的下部区域,并将剩余液体至少部分地送回到缓冲容器中。
此处术语“稳定运行”意指启动结束后空分装置进入正常的运行状态,在这种状态下,在很长的周期内(在可换式存贮装置的情况中,至少10分钟至数天或数周装置内始终保留有需要的产品)原料流和产品流大体维持恒定。
按照本发明,在稳定运行时,大体上将全部回流液送入一个缓冲容器(例如一个贮液罐)中。也就是说,可以将少部分回流液导入另一路,例如作为液态产品抽取或通过一个安全排放口排出。但至少应将在塔中形成上升蒸气的那部分回流液导入上述缓冲容器中。
上述缓冲容器最好是绝热贮液罐。再将液体从上述罐中抽出,使之与从压力塔流出的富氮蒸气进行间接热交换而蒸发。将上述过程中产生的至少部分气体(最好是大部分气体)导入低压塔,并在该塔中形成与回流液逆向流动的上升的蒸气,另一部分气体在需要时可以作为氧气产品被提取。通常,此部分氧气由与其逆流的大体为环境温度的待分离空气加热。从贮液罐提取的液体在进行间接热交换中未被蒸发的部分(例如与从上述塔流出的回流一道)再被送回到缓冲容器中。
上述液体可以费用低廉地用泵进行输送。例如可以将泵设置在缓冲罐的下游,也可在从低压级到缓冲容器的管路上设泵,或者在上述管路上再附设一个泵,此时缓冲容器本身或者设置在使从罐中流出的液体蒸发的热交换器的上方,或者处于超过一个大气压的状态下。
由于未蒸发的回流液与罐内的存留物混合在一起,不需要维持低压塔中液体的高度。按照本发明的方法,或者只需维持极低的液体高度(例如,与迄今公知的方法中液体高度约为300至2000mm水柱相比,只需维持10mm至最高50mm水柱),或者在低压级的底部(Sumpf)完全不存留液体。
由于移出了冷凝蒸发器,更有利于不必在塔内存留污液,因此,相应降低了精馏塔的建筑高度。这对于双塔高度达40m的大型设置尤其有利。此外,因为碳水化合物是在低压级底部而不是在塔中有增加的趋势,就运行可靠性而言也是很有利的,而且容器中有极大的缓冲容积。
此外,整体式缓冲容器可以在塔运行不完全稳定的情况下(出现故障的情况下或空气流通量发生了变化)通过罐内物的蒸发大体可获得始终是纯净的氧气产品。由于从低压塔流出的氧气产品的质量和产量的波动受到缓冲,本发明方法使用起来非常灵活。
再者,缓冲容器中的一体化简化了本方法的控制过程。就此而言,可控变量是罐中液体的高度。此变量可简单地观测出,而且明显处于非临界状态。仅仅必须保证的是罐不能完全排空或全部充满,罐内的盛装量原则上可以在上述两者之间随意变动。(为了能确实利用缓冲效果,实际上常维持中等液体高度。)这对于有时需观察出罐内液体的高度,然后在液体高度下降或升高时增加或减少外界传冷和/或内部产冷而言是足够的。原则上可自动实现上述调节过程。因为在正常运行中只在较长的时间间隔(根据罐的大小,大约10小时至5天结束)内需要匹配产冷量,上述控制也可手动进行。在本方法中,例如借助于空气或氮气在透平中作功膨胀而获取冷量,这样,例如可用人工适当地调节透平的产冷量。
如果为使从缓冲容器中抽出的液体部分蒸发而进行的间接热交换是以沉降膜蒸发(Fallfilmverdampfung)的形式进行的话则更为有利。有关热交换器作为沉降膜蒸发器工作的详情已在Billet编著的“蒸发及蒸发技术的应用”(1981)第3.5.5章作了描述。在这种沉降膜蒸发器中约25%至75%(重量),最好是40%至60%(重量)的从缓冲容器流出的液体被蒸发。剩余物通常又送回到罐中。
在某些应用中,例如炼钢工业中,对空气产品尤其是氧的需求量非常不稳定。如果产品没有其它应用可能性,有时空分设备必须停产。由于白天能源费用多变,空分装置常常断断续续地运行。因上述原因运行中断以后(或者也可能因出现故障运行中断以后),装置需重新启动,由于装置本身还处于冷状态,到精馏作用重又达到稳定状态并且能提供预定纯度的产品往往需要较长时间(直到2小时)。
本发明方法的重要改进是:运行中断开始时,将从低压级流出的回流液送入压力级的下部区域。
贮存回流液在DE-A-3732363文献中早已公开。但该文献所描述的方法中,需要专门的设备接收回流液。本发明的方法几乎不需要附加设备,可以采用本来就装设了的安全排放管道导出回流液,仅仅需要与压力级相连,例如经输入分离空气的管道与压力级相通。
装置损坏时,空压机停转,使将回流液导入缓冲容器的连接断开,并使通往压力塔的管道开通。(如果与罐相通的管道设置在与压力塔相通的管道的上方,则不需要断开与罐相通的管道)。仍留存在低压塔中的回流液由于其重力的影响流入压力塔的底部,因此,可防止含氮的回流液污染留存在罐底部的产品。
在重新启动时,可在最短的时间内再供给纯净的氧产品。空压机开始运转后几分钟分子筛就能纯化空气、压力塔重又达到其工作压力。一旦具有一定压力的气体从压力级的顶部流过热交换器,从罐中流出的氧就开始蒸发,其中,蒸发出的馏份(从罐中流出的氧)可以直接作为具有一般纯度的产品。精馏作用达到稳定运行状态的时间(作为1分钟到5分钟)可以通过使贮存在缓冲罐中的液体蒸发来弥补,而不会影响产品的纯度或产量。
本发明还涉及一种如权利要求4至6所述的低温分离空气的装置。
下面将结合附图所表示的一个实施例对本发明以及本发明的其它内容进行详细描述。至于如流程中的用作膨胀产冷的透平或直接将空气输入低压塔的细节在经大大简化了的示意图中未示出。将经压缩和净化的空气通过管道1送入双级塔2的压力级3中。(部分待分离的空气也可直接被送入低压级4,例如在作功膨胀之后)。压力级顶部的气体经管道5被送入冷凝蒸发器6中并被全部冷凝,同时所形成的液体经管道7流回到压力级3的上部。流入压力级的部分液体用作压力塔3中的回流液,另一部分液体被送入低压塔4中。(与上述低压塔相通的管道8可以与压力塔3相连,也可直接与冷凝蒸发器6的冷凝物管道7相连)。此外,从压力塔流出的底部液体(Sumpfflussigkeit)9在低压塔4的中间位置被节流,从低压塔顶部抽取富氮产品流10。从低压塔的下端经管道11提取低压塔4的回流液。在稳定运行时,上述回流液由含有100ppm至20%的剩余杂质的氧气组成,最好上述剩余杂质含量为0.3%至10%。将管道11安装在比较靠近构成低压塔4的容器的底部,因此,在塔底中很少或者实际上根本没有液体。
液氧12流入用作缓冲容器的贮氧罐13中。需要时可以通过产品流管道14提取一部分作为液态产品。在附图所示的实施例中,由泵15维持罐13中的压力,因此,从上述罐流出、经管道16流入用作沉降膜蒸发器的冷凝蒸发器6的液体具有一定压力。(在贮存容器无压力的情况中,上述泵应设置在管道16上。
从冷凝蒸发器6的蒸发器通道流出的两相混合流经管道17排出,其蒸气部分的一部分经管道18流回低压塔4中,而另一部分作为氧气产品流19被提取。剩余液体部分经管道12再送回到缓冲容器13中。
另一根液体管道20与低压级4的下部区域相通,最好该管道设置在低于管道11的出口之处。在装置正常运行时,上述液体管道不通。(必要时,为安全起见,偶而可使少量液体流经此开口并通过一个末示出的安全排出口排出且弃之)。在中断运行时,空压机复原后管道11上的阀门21关闭,使之与罐13的连接断开,同时,截止件22开启,使流入低压塔底部的回流液流入压力塔中,并保留在压力塔的底部中。(根据管道11及20与低压级4连接位置的安排,也可以使回流液只经管道20流出,在这种情况中,可省去管道11上的阀门21)。
装置重新启动时,在极短的时间内,再将纯净的氧气产品经管道19排出。也就是说,一旦压力级3达到所需的工作压力,顶部气体5则流向冷凝蒸发器6,在上述蒸发器中进行蒸发。因为将从缓冲罐13中流出的纯氧输入蒸发侧,紧接着,管道19中的气体产品又可随时提供使用。起动时间(即直到低压塔中再次出现稳定的产品浓度所经过的时间)也可通过部分蒸发罐内物来调整。由于冷凝蒸发器6开始蒸发后低压级中立即可提供具有适当纯度的氧气,开始运转后从低压塔流出的回流液(11)同样包含常规组分,并能立即经管道12流入罐13中。
低压级4一侧与管道17/12之间的连接18和11也可通过单独的一根横截面大的管子来实现,使液体和蒸气彼此逆向流动,上述管道17/12则处于冷凝蒸发器6的蒸发通路和缓冲罐13的另一侧之间。
Claims (6)
1、低温分离空气的方法,其中空气经压缩、净化、冷却,然后至少部分地被入两级精馏设备(2)的压力级(3)中,在此过程中得到的至少一种馏份(8,9)从压力级(3)流入低压级(4),并在低压级中进一步分离,提取低压级(4)中的氧馏份(11)和含氮馏份(10)作为产品流,低压级(4)的下部区域与压力级的上部区域呈热交换关系,其特征在于在稳定运行时,大体全部流入低压级(4)的回流液(11)从低压级的下部区域抽出,并将其导入一个缓冲容器(13)中,从缓冲容器(13)中提取液流(16),使之与从压力级(3)上部区域流出的待冷凝气体(5)进行间接热交换而被蒸发;将所形成的蒸气(17,18)至少部分地导入低压级(4)的下部区域,并将在间接热交换中剩留的至少部分液体(17,12)送回缓冲容器(13)中。
2、如权利要求1所述的方法,其特征在于使从缓冲容器(13)中提取的液流(16)部分蒸发的间接热交换过程是以沉降膜蒸发的形式进行的。
3、如权利要求1或2所述的方法,其特征在于运行中断开始时,将从低压级(4)流出的回流液(20)导入压力级(3)的下部区域。
4、低温分离空气的装置,它包括一台空压机,一台净化设备,一个热交换器,一个由压力塔(3)和低压塔(4)组成的双级精馏设备(2),以及一台冷凝蒸发器(6),该蒸发器经蒸气流入管道(5)和冷凝液回流管道(7)与压力塔(3)的上部区域相通,并具有使从低压塔(4)下部区域流出的液体蒸发的蒸发通道,其特征在于还包括与低压级下部区域和缓冲容器(13)相连的回流液管道(11,12),从缓冲容器(13)通向冷凝蒸发器(6)的蒸发通道入口的液流管道(16),连接蒸发通道出口与低压塔(4)下部区域的蒸发管道(17,18),以及回送蒸发通道出口与缓冲容器(13)之间的液体的回送管道(17,12)。
5、如权利要求4所述的装置,其特征在于上述冷凝蒸发器(6)是沉降膜蒸发器。
6、如权利要求4或5所述的装置,其特征在于还包括从低压塔(4)的下部区域通向压力塔(3)的液流管道(20),在该管道上装有截止件(22)。
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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DEP4415747.9 | 1994-05-04 | ||
DE4415747A DE4415747C2 (de) | 1994-05-04 | 1994-05-04 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
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CN1124345A true CN1124345A (zh) | 1996-06-12 |
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CN95105025A Pending CN1124345A (zh) | 1994-05-04 | 1995-05-04 | 低温分离空气的方法及装置 |
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EP (1) | EP0681153B1 (zh) |
JP (1) | JPH0842962A (zh) |
KR (1) | KR950033380A (zh) |
CN (1) | CN1124345A (zh) |
DE (2) | DE4415747C2 (zh) |
ES (1) | ES2106594T3 (zh) |
GR (1) | GR3025534T3 (zh) |
PL (1) | PL308454A1 (zh) |
TW (1) | TW288984B (zh) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100436989C (zh) * | 2004-01-29 | 2008-11-26 | 宝山钢铁股份有限公司 | 一种用全低压空分装置制取高纯氧的方法 |
CN108014601A (zh) * | 2016-11-04 | 2018-05-11 | 林德股份公司 | 用于净化气体的方法和设备 |
CN112629160A (zh) * | 2020-12-21 | 2021-04-09 | 华能(天津)煤气化发电有限公司 | 一种空分自然复热检修方法 |
Families Citing this family (9)
Publication number | Priority date | Publication date | Assignee | Title |
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DE19732887A1 (de) * | 1997-07-30 | 1999-02-04 | Linde Ag | Verfahren zur Luftzerlegung |
US6272884B1 (en) | 1998-04-08 | 2001-08-14 | Praxair Technology, Inc. | Rapid restart system for cryogenic air separation plant |
FR2797942B1 (fr) * | 1999-08-24 | 2001-11-09 | Air Liquide | Vaporiseur-condenseur et installation de distillation d'air correspondante |
FR2802825B1 (fr) * | 1999-12-23 | 2002-05-03 | Air Liquide | Appareil de separation par distillation et procede de nettoyage d'un vaporisateur-condenseur de l'appareil |
FR2855598B1 (fr) * | 2003-05-28 | 2005-10-07 | Air Liquide | Procede et installation de fourniture de secours d'un gaz sous pression par vaporisation de liquide cryogenique |
EP2503270A1 (de) * | 2011-03-22 | 2012-09-26 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Erzeugung eines Sauerstoffprodukts durch Tieftemperaturzerlegung von Luft |
CN103537107B (zh) * | 2012-07-11 | 2015-04-22 | 蓝星(北京)化工机械有限公司 | 一种蒸发***及其应用 |
CN108072234B (zh) * | 2016-11-15 | 2020-03-06 | 北大方正集团有限公司 | 空气分离装置的控制方法 |
KR102354278B1 (ko) | 2017-10-12 | 2022-01-21 | 주식회사 엘지에너지솔루션 | 전지 충방전기 |
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LU35441A1 (zh) * | 1956-09-25 | |||
DE1501760A1 (de) * | 1966-12-27 | 1969-11-27 | Rudisleben Chemieanlagenbau | Verfahren zur Luftzerlegung |
DE3732363A1 (de) * | 1987-09-25 | 1989-04-06 | Linde Ag | Verfahren und vorrichtung zum wiederanfahren einer gaszerlegungsanlage |
DE3913880A1 (de) * | 1989-04-27 | 1990-10-31 | Linde Ag | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
JPH0420783A (ja) * | 1990-05-11 | 1992-01-24 | Hitachi Ltd | 空気分離装置 |
JPH05306884A (ja) * | 1992-03-18 | 1993-11-19 | Hitachi Ltd | 空気分離装置及びその運転方法 |
-
1994
- 1994-05-04 DE DE4415747A patent/DE4415747C2/de not_active Expired - Fee Related
-
1995
- 1995-05-03 KR KR1019950011147A patent/KR950033380A/ko not_active Application Discontinuation
- 1995-05-04 CN CN95105025A patent/CN1124345A/zh active Pending
- 1995-05-04 EP EP95106750A patent/EP0681153B1/de not_active Expired - Lifetime
- 1995-05-04 ES ES95106750T patent/ES2106594T3/es not_active Expired - Lifetime
- 1995-05-04 DE DE59500625T patent/DE59500625D1/de not_active Expired - Fee Related
- 1995-05-04 PL PL95308454A patent/PL308454A1/xx unknown
- 1995-05-08 JP JP7132615A patent/JPH0842962A/ja active Pending
- 1995-09-07 TW TW084109352A patent/TW288984B/zh active
-
1997
- 1997-11-28 GR GR970403183T patent/GR3025534T3/el unknown
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100436989C (zh) * | 2004-01-29 | 2008-11-26 | 宝山钢铁股份有限公司 | 一种用全低压空分装置制取高纯氧的方法 |
CN108014601A (zh) * | 2016-11-04 | 2018-05-11 | 林德股份公司 | 用于净化气体的方法和设备 |
CN108014601B (zh) * | 2016-11-04 | 2021-12-17 | 林德股份公司 | 用于净化气体的方法和设备 |
CN112629160A (zh) * | 2020-12-21 | 2021-04-09 | 华能(天津)煤气化发电有限公司 | 一种空分自然复热检修方法 |
Also Published As
Publication number | Publication date |
---|---|
EP0681153B1 (de) | 1997-09-10 |
ES2106594T3 (es) | 1997-11-01 |
EP0681153A1 (de) | 1995-11-08 |
TW288984B (zh) | 1996-10-21 |
DE4415747C2 (de) | 1996-04-25 |
DE59500625D1 (de) | 1997-10-16 |
PL308454A1 (en) | 1995-11-13 |
GR3025534T3 (en) | 1998-02-27 |
KR950033380A (ko) | 1995-12-22 |
DE4415747A1 (de) | 1995-11-16 |
JPH0842962A (ja) | 1996-02-16 |
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