CN202648306U - 空气分离装置 - Google Patents

空气分离装置 Download PDF

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CN202648306U
CN202648306U CN2012200040467U CN201220004046U CN202648306U CN 202648306 U CN202648306 U CN 202648306U CN 2012200040467 U CN2012200040467 U CN 2012200040467U CN 201220004046 U CN201220004046 U CN 201220004046U CN 202648306 U CN202648306 U CN 202648306U
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air
nitrogen
liquid
pipeline
liquid nitrogen
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夏瑞田
史宏伟
武林
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SUZHOU OXYGEN PLANT CO., LTD.
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
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    • 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
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
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Abstract

本实用新型提供一种空气分离装置，包括：空气压缩机；预冷机组；主换热器；分馏塔系统包括下塔、上塔、冷凝蒸发器、液氮分离罐；液氮分离罐上设有液氮产品出口，其与液氮产品输出端通过管道相连通；所述上塔设有供分离后的液氧流出的液氧出口，其与液氧产品输出端通过管道相连通；所述上塔设有供分离后的纯氮气流出的纯氮气出口，其与氮气产品输出端通过管道相连通。本实用新型通过设置可产出液氮，或可产出液氧和氮气的空气分离系统，满足了气体生产厂家对于各种工况，对液氧、氮气、液氮的产量、纯度和压力的要求的需求。

Description

空气分离装置
技术领域
本实用新型涉及一种空气分离装置，尤其涉及一种采用低温精馏的方法生产氧氮产品的装置。 
背景技术
空分设备是利用空气中氧氮沸点不同的原理，采用低温精馏的方法生产氧氮产品的装置。 
液体空分设备出产的产品为液态空气制品，随着能源的日趋紧张，在气体生产工业中为追求气体生产能获得更高的经济效益，人们正在进行多种生产方法的比较，由于液态空气制品具有良好的品质、低的运输成本、好的性能价格比和使用方便、安全等特点，现越来越受到气体生产商的青睐。 
现在国外的空分设备, 除满足客户工艺用氧气、氮气、氩气需要外, 还设计有液体氧、氮、氩, 主要是供当地及周围市场需求, 以低温液体方式输供。我国地域辽阔，工业气体的生产水平仍属发展中国家，目前我国工业气体的生产供应均以中小型气站为主，并且十分分散。国内大型冶金、化工等企业配置的大型空分设备生产的工业气体产品又是作为内部生产使用，因此我国目前的气体供应远未达到发达国家可以集中供气覆盖上百公里范围的规模。 
液态空气制品能够很好地调配各地区气体产品供求不平衡的状态，所以当前液体产品的销售已成为许多气体销售公司的最好选择，使液体空分设备和气体液化设备的需求量呈逐年上升趋势。然而，目前市场上的空气分离设备功能单一，输出产品为固定的，并且能耗还有提升的空间。 
实用新型内容
本实用新型的目的为提供一种输出产品多样的、能耗低的空气分离设备。 
本实用新型的目的通过提供以下技术方案来实现： 
一种空气分离装置，包括：将外部空气进行压缩的空气压缩机；对空气压缩机输出的空气进行冷却的预冷机组；净化预冷机组输出的空气的纯化器；供空气分离装置中的空气进行热交换的主换热器；将空气成分分离的分馏塔系统，所述分馏塔系统包括相互连通的下塔、上塔、设于下塔和上塔之间的冷凝蒸发器、液氮分离罐；所述分馏塔系统和液氮产品输出端、液氧产品输出端和氮气产品输出端相连通；所述下塔设有供空气进入的空气入口,该空气入口和纯化器通过管道相连通，所述下塔设有供分离后的富氧液空流出的富氧液空出口，其与上塔上设置的富氧液空入口通过管道相连通；所述冷凝蒸发器设有供液化的液氮流出的液氮出口，其与液氮分离罐上的液氮入口通过管道相连通；所述液氮分离罐上设有液氮产品出口，其与液氮产品输出端通过管道相连通；所述上塔设有供分离后的液氧流出的液氧出口，其与液氧产品输出端通过管道相连通；所述上塔设有供分离后的纯氮气流出的纯氮气出口，其与氮气产品输出端通过管道相连通；所述上塔上设有有供分离后的污氮气输出的污氮气出口。
优选的，所述空气分离装置还包括循环压缩机、第一膨胀机和低温冰机；纯化器通过管道连接循环压缩机，循环压缩机和第一膨胀机、低温冰机、主换热器通过管道连接形成环形的通路，管道依次从循环压缩机连接到第一膨胀机，到低温冰机，到主换热器，到第一膨胀机，到主换热器，最后回到循环压缩机。 
优选的，所述纯化器到空气入口之间的管道经过主换热器。 
优选的，所述冷凝蒸发器的液氮出口到液氮分离罐的液氮入口之间的管道经过过冷器。 
优选的，所述液氮分离罐的顶部设有液氮出口，其和上塔的顶部的液氮入口通过管道相连通。 
优选的，所述下塔的富氧液空出口和上塔的富氧液空入口之间的管道经过过冷器。 
优选的，所述空气分离装置还包括第二膨胀机，所述上塔的污氮气出口处的管道依次经过过冷器，主换热器、第二膨胀机和主换热器。 
优选的，所述空气分离装置还包括第三膨胀机，所述上塔的纯氮气出口和氮气产品输出端之间的管道依次经过过冷器，第三膨胀机，过冷器和主换热器。 
优选的，所述纯化器为分子筛纯化器。 
优选的，所述空气分离装置还包括PLC的远程监控系统。 
本实用新型通过设置可产出液氮，或可产出液氧和氮气的空气分离系统，满足了气体生产厂家对于各种工况，对液氧、氮气、液氮的产量、纯度和压力的要求的需求；循环压缩机采用空气循环，原料空气仅需在设备启动时输入到循环制冷系统，正常运行时该部分空气一直处于循环运行状态，降低了原料压缩机和纯化系统的负荷，从而降低整套装置的能耗；本实用新型的制冷系统充分利用了设备工作介质自身的能量，对设备工作介质的冷量加以回收，利用三台膨胀机进行制冷，在满足空气分离所需冷量的同时降低了辅助制冷设备的功耗，达到节能的目的。 
附图说明
下面结合附图对本实用新型作进一步说明： 
图1为本实用新型的具体实施例的结构示意图。
具体实施方式
以下参照附图说明本实用新型的具体实施例。 
如图1，空气分离装置主要包括过滤器1、空气压缩机3，预冷机组5、纯化器7，循环压缩机21，分馏塔系统。空气分离装置还包括基于PLC的远程监控系统。 
外部空气经过过滤器1进行初步过滤去除灰尘及机械杂质后，进入空气压缩机3压缩到1.0Mpa，40℃左右,然后进入预冷机组5冷却到10~12℃，进入纯化器7，纯化器7为自动切换的分子筛纯化器。空气在纯化器7中去除H2O,CO2,C2H2及其他碳氢化合物，出纯化器7的空气温度为约14℃。 
出纯化器7的空气主要分为两路，其一路经循环压缩机21加压后成为循环气体；一路进入冷箱37，经分离后成为液氮产品，或液氧产品和氮气产品输出。除该两路气体外，另有少量空气进入仪表空气系统，作为仪表气和密封气。 
循环压缩机21和第一膨胀机25、低温冰机23、主换热器9通过管道连接形成环形的通路，管道依次从循环压缩机21连接到第一膨胀机25，到低温冰机23，到主换热器9，到第一膨胀机25，到主换热器9，最后回到循环压缩机21。具体的，循环气体一路中的气体在循环压缩机21中加压后，进入第一膨胀机25的增压端，增压后经冷却器冷却，进入低温冰机23降温到约-30℃，再进入主换热器9中冷却，在主换热器9的中部和偏底部抽出，到第一膨胀机25进行膨胀制冷，膨胀后的空气进入主换热器9复热后，再次进入循环压缩机21，如此循环往复。正常运行后，该路空气一直处于循环运行状态。 
冷箱37内主要包括主换热器9，分馏塔系统(包括下塔11，上塔13，分馏塔15，下塔11和上塔13之间的冷凝蒸发器15，液氮分离罐17)，前述的主换热器9，过冷器19，前述的第一膨胀机25，第二膨胀机27，第三膨胀机29以及连接上述各个部件、分馏塔系统、外部系统的管道。 
进入分馏塔系统的空气首先经管道流过主换热器9，在主换热器9中和被返流的氮气和污氮等低温气体进行热交换，被冷却至液化温度（约-170℃）。这些冷却到液化温度的空气从管道流到下塔11下部的空气入口，从空气入口进入下塔11。在下塔11中，空气和下塔11中的回流液进行热质交换，被进一步冷却。由于氧气和氮气的液化点不同，空气分离为富氧液空和氮气，氮气上升到下塔11的上部，富氧液空沉积到下塔11的下部。 
下塔11的下部设有富氧液空出口，其通过管道连接到上塔13的中部的富氧液空入口。富氧液空经由该通路进入上塔13，沉积到上塔13的下部。上塔13和下塔11之间具有冷凝蒸发器，下塔11顶部的氮气进入冷凝蒸发器15冷凝成液氮。 
冷凝蒸发器15设有供液化的液氮流出的液氮出口，其与液氮分离罐17上的液氮入口通过管道相连通。冷凝蒸发器15中形成的液氮一部分返回下塔11，作为下塔11的回流液，另一部分液氮从冷凝蒸发器15从液氮出口流出，管道经过冷器19过冷后节流，大部分从液氮分离罐17的液氮入口进入液氮分离罐17；在液氮分离罐17中，部分液氮从顶部的液氮出口流出，经管道通路流出到上塔13的顶部的液氮入口，作为上塔13的回流液，另一部分液氮从液氮分离罐17的底部的液氮产品出口抽出，经管道输出到液氮产品输出端31，作为液氮产品输出。 
下塔11设有供分离后的富氧液空流出的富氧液空出口，其与上塔13上设置的富氧液空入口通过管道相连通。下塔11底部的富氧液空经过管道通路，流出到过冷器19过冷，经节流后从上塔13的中部的富氧液空入口进入上塔13，参加精馏，分离后，在上塔13的顶部得到纯氮气，在上塔13的上部得到污氮气，在上塔13的底部得到液氧产品。其中，液氧产品从上塔13底部的液氧出口流出，经管道通路连接到液氧产品输出端输出。上塔13顶部的纯氮气从上塔13顶部的纯氮气出口流出，经管道通路流经过冷器19过冷回收冷量后，进入第三膨胀机29制冷，再经过冷器19回收冷量，再经过主换热器9复热，随后经管道通路输出到氮气产品输出端35输出。上塔13上部的污氮气从上塔13上部的污氮气出口，经管道通路被抽出，也经过冷器19过冷，主换热器9回收热量，随后进入第二膨胀机27膨胀制冷，膨胀后污氮气再次进入主换热器9复热后，排出分镏塔系统，排出的污氮气部分输出到纯化器7处作为吹冷气，部分再次经过第二膨胀机27增压后，作为纯化器7的再生气。 
如前所述的，本实用新型中的空气分离装置可以在液氮产品工况和液氧产品工况之间切换。液氮产品工况时，液氮直接从液氮分离罐17底部抽出，经液氮产品输出端31送入用户储存系统；液氧产品工况时，液氧从上塔13的底部抽出，经液氧产品输出端33送入用户储存系统；同时，氮气经第三膨胀机29膨胀后，经氮气产品输出端35送出，进入用户压缩系统。 
本实用新型的空气分离装置为全低压节能型，可变工况的带压力输出的液体空分设备。全低压流程可提高设备安全性和可靠性，能耗较低。 
本实用新型的空气分离装置可出产高纯度液氮产品或高纯度液氧产品和高纯度氮气，两种工况可相互转换，满足用户液氧、氮气、液氮的产量、纯度和压力的要求。与常规的液体空分设备出产的常压液氮产品、液氧产品相比，本设备出产的液氮和液氧产品为带压输出，降低了后续储存系统的加压设备功耗，在用户压力要求不高的情况下甚至可以无须通过液体泵等加压措施来提升产品压力，从而降低了液体产品储运过程中的能耗。 
本实用新型的纯化系统的再生气利用污氮膨胀机的增压段进行增压，回收了膨胀机的膨胀功，提高了再生气进入纯化系统的温度，降低了纯化系统电加热器的装机功率，从而降低整套装置的能耗。 
本实用新型采用PLC 计算机集中控制系统，实行整套装置的集中显示和自动控制。 
本实用新型采用全低压流程，提高设备安全性和可靠性，能耗较低。 
本实用新型采用撬装化设计，占地面积小。 
需要理解到的是：上述说明并非是对本实用新型的限制，在本实用新型构思范围内，所进行的添加、变换、替换等，也应属于本实用新型的保护范围。 

Claims (10)

1.一种空气分离装置，包括：将外部空气进行压缩的空气压缩机；对空气压缩机输出的空气进行冷却的预冷机组；净化预冷机组输出的空气的纯化器；供空气分离装置中的空气进行热交换的主换热器；将空气成分分离的分馏塔系统，其特征在于：所述分馏塔系统包括相互连通的下塔、上塔、设于下塔和上塔之间的冷凝蒸发器、液氮分离罐；所述分馏塔系统和液氮产品输出端、液氧产品输出端和氮气产品输出端相连通；所述下塔设有供空气进入的空气入口,该空气入口和纯化器通过管道相连通，所述下塔设有供分离后的富氧液空流出的富氧液空出口，其与上塔上设置的富氧液空入口通过管道相连通；所述冷凝蒸发器设有供液化的液氮流出的液氮出口，其与液氮分离罐上的液氮入口通过管道相连通；所述液氮分离罐上设有液氮产品出口，其与液氮产品输出端通过管道相连通；所述上塔设有供分离后的液氧流出的液氧出口，其与液氧产品输出端通过管道相连通；所述上塔设有供分离后的纯氮气流出的纯氮气出口，其与氮气产品输出端通过管道相连通；所述上塔上设有有供分离后的污氮气输出的污氮气出口。
2. 根据权利要求1所述的空气分离装置，其特征在于，所述空气分离装置还包括循环压缩机、第一膨胀机和低温冰机；纯化器通过管道连接循环压缩机，循环压缩机和第一膨胀机、低温冰机、主换热器通过管道连接形成环形的通路，管道依次从循环压缩机连接到第一膨胀机，到低温冰机，到主换热器，到第一膨胀机，到主换热器，最后回到循环压缩机。
3. 根据权利要求1所述的空气分离装置，其特征在于，所述纯化器到空气入口之间的管道经过主换热器。
4. 根据权利要求1所述的空气分离装置，其特征在于，所述冷凝蒸发器的液氮出口到液氮分离罐的液氮入口之间的管道经过过冷器。
5. 根据权利要求1所述的空气分离装置，其特征在于，所述液氮分离罐的顶部设有液氮出口，其和上塔的顶部的液氮入口通过管道相连通。
6. 根据权利要求1所述的空气分离装置，其特征在于，所述下塔的富氧液空出口和上塔的富氧液空入口之间的管道经过过冷器。
7. 根据权利要求1所述的空气分离装置，其特征在于，所述空气分离装置还包括第二膨胀机，所述上塔的污氮气出口处的管道依次经过过冷器，主换热器、第二膨胀机和主换热器。
8. 根据权利要求1所述的空气分离装置，其特征在于，所述空气分离装置还包括第三膨胀机，所述上塔的纯氮气出口和氮气产品输出端之间的管道依次经过过冷器，第三膨胀机，过冷器和主换热器。
9. 根据权利要求1所述的空气分离装置，其特征在于，所述纯化器为分子筛纯化器。
10. 根据权利要求1所述的空气分离装置，其特征在于，所述空气分离装置还包括PLC的远程监控系统。
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103196278A (zh) * 2012-01-06 2013-07-10 苏州制氧机有限责任公司 空气分离装置
CN104949471A (zh) * 2015-05-14 2015-09-30 马钢(集团)控股有限公司 一种提高空分装置氮气产量的方法
CN106288657A (zh) * 2016-10-21 2017-01-04 成都深冷液化设备股份有限公司 液氧、液氮互换生产装置及生产工艺

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103196278A (zh) * 2012-01-06 2013-07-10 苏州制氧机有限责任公司 空气分离装置
CN103196278B (zh) * 2012-01-06 2015-06-10 苏州制氧机有限责任公司 空气分离装置
CN104949471A (zh) * 2015-05-14 2015-09-30 马钢(集团)控股有限公司 一种提高空分装置氮气产量的方法
CN106288657A (zh) * 2016-10-21 2017-01-04 成都深冷液化设备股份有限公司 液氧、液氮互换生产装置及生产工艺
CN106288657B (zh) * 2016-10-21 2019-04-12 成都深冷液化设备股份有限公司 液氧、液氮互换生产装置及生产工艺

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