CN203068914U - 高纯氮制取设备 - Google Patents

高纯氮制取设备 Download PDF

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CN203068914U
CN203068914U CN2013200382223U CN201320038222U CN203068914U CN 203068914 U CN203068914 U CN 203068914U CN 2013200382223 U CN2013200382223 U CN 2013200382223U CN 201320038222 U CN201320038222 U CN 201320038222U CN 203068914 U CN203068914 U CN 203068914U
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nitrogen
air
pipeline
liquid
evaporator
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李松涛
张二国
吴海涛
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Henan Kaili Air Separation Plant Co., Ltd.
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KAIFENG KAI LI AIR SEPARATION PLANT CO Ltd
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  • Engineering & Computer Science (AREA)
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Abstract

本实用新型涉及高纯氮制取设备，包括空气压缩机和分馏塔系统，分馏塔系统包括精馏塔和冷凝蒸发器，空气压缩机为变频空气压缩机，精馏塔包括塔体，塔体内间隔设置有至少一层填料层，填料层上方设置有液体分布器，塔体于填料层下方设置有用于使原料空气进入塔体的原料空气入口、用于将塔体底部的富氧液空抽送进冷凝蒸发器的富氧液空接口、与液体分布器连通用于将液氮输送进塔体内部的塔体液氮进口和用于将分馏出的高纯氮气输出的高纯氮出口。本实用新型采用变频空气压缩机和填料精馏塔，可根据需要减少原料空气的用量，减小进入分馏塔系统的原料空气量，填料精馏塔能够实现大范围变负荷的能力，因此可控制氮气产量，避免电能的损耗，节约能源。

Description

高纯氮制取设备
技术领域
本实用新型涉及高纯氮制取设备。 
背景技术
近年来随着社会的发展和技术的进步，对能源的需求越来越严重。现有可利用直接能源越来越紧张，国家号召发展循环经济，充分发挥和利用能源的价值，对高品质的能源利用率和利用效果做到充分利用。 
氮气广泛应用于石油、炼铝、化学、橡胶、电子、玻璃、纺织、钢铁等工业。不同的工业对氮气产品的要求显著不同。针对于不同的工业对于氮气产品纯度、压力、用量的要求显著不同。市场上出现了各种各样的低温制氮生产的工艺。现有的制氮设备如申请公布号为CN 101929790 A的中国专利申请“高纯氮设备”，包括管线连接的空气压缩系统、预冷系统、分子筛纯化系统和分馏塔系统，分馏塔系统包括透平膨胀机、用于热交换的主换热器和过冷器，精馏塔和冷凝蒸发器，所述纯化系统包括分子筛吸附器和电加热器，所述纯化系统的出口经管路连接至精馏塔的原料空气入口，该管路上串接有主换热器，所述精馏塔下方设有用于供精馏产生的富氧液空流出的富氧液空出口，所述精馏塔上方设有氮气出口，精馏塔的氮气出口分别与冷凝蒸发器和主换热器连通，精馏塔的氮气出口与冷凝蒸发器连通用于使分馏处的高纯氮气被流经冷凝蒸发器的富氧液空冷凝成为液氮而作为回流液回流入精馏塔中，精馏塔的氮气出口与主换热器连通使流经该路径的高纯氮气输出；精馏塔的富氧液空出口经透平膨胀机的膨胀制冷，一部分进入纯化系统中的分子筛吸附器后作为再生气体，另一部分多余的富氧气经消音器排入大气中。在该装置中采用的空气压缩机为普通空气压缩机，原料空气进入该设备的量为定量，不能根据实际需要调节，当所需的氮气量小于额定用量时，经过空气压缩机进入设备的原料空气仍为额定用量，空气压缩机耗费功率处理的一部分原料空气所分离出的氮毫无用处的被排放如空气中，不利于电能的节约；并且该设备所使用的精馏塔为板式精馏塔，板式精馏塔不具有大范围变负荷的能力，不能根据实际输入的原料空气进行调节。 
实用新型内容
本实用新型的目的是提出一种可根据实际需要调节氮气产量的高纯氮制取设备。 
为解决上述问题，本实用新型采用的技术方案是： 
高纯氮制取设备，包括空气压缩机和分馏塔系统，所述分馏塔系统包括精馏塔和冷凝蒸发器，所述空气压缩机为用于调节原料空气使用量的变频空气压缩机，所述精馏塔包括塔高沿上下方向延伸的塔体，所述塔体内沿塔高方向间隔设置有至少一层填料层，所述填料层上方设置有对用于润湿填料层的液体进行均匀分布的液体分布器，所述塔体于所述填料层下方设置有用于使变频空气压缩机压缩后的原料空气进入塔体内的原料空气入口、用于将塔体底部的富氧液空抽送进所述冷凝蒸发器的富氧液空接口、与所述液体分布器连通用于将作为回流液的液氮输送进塔体内部的塔体液氮进口和用于将分馏出的高纯氮气输出的高纯氮出口。
所述变频空气压缩机为变频螺杆式空气压缩机。 
还包括分子筛吸附器，所述冷凝蒸发器顶部开设有将污氮气排出冷凝蒸发器的污氮气排出口，周壁上开设有通过管道与所述富氧液空接口连接而使富氧液空进入冷凝蒸发器的富氧液空进口、与所述高纯氮出口管道连接用于使部分氮气进入冷凝蒸发器的氮气进口和用于与所述塔体液氮进口通过管道连通以将氮气与流经冷凝蒸发器的富氧液空进行热交换而形成的液氮输出冷凝蒸发器的液氮出口，所述污氮气排出口通过管道与所述分子筛吸附器的再生气入口连通。 
所述冷凝蒸发器一体设置于所述精馏塔上方。 
还包括主换热器，所述主换热器中设有原料空气管道和用于与原料空气管道中的原料空气热交换而对原料空气进行冷却的污氮气管道，所述污氮气管道具有与所述分子筛吸附器的再生气入口通过管道连通的出口端和与污氮气排出口通过管道连通的入口端。 
所述主换热器与污氮气排出口连接的管道上设置有对污氮气进行膨胀冷却的透平膨胀机，透平膨胀机的入口通过管道与污氮气排出口连通，透平膨胀机的出口通过管道与主换热器的污氮气管道的入口端连通。 
所述富氧液空接口与所述富氧液空进口的连接管道上串接有过冷器。 
所述冷凝蒸发器的液氮出口的管路分为两个分支，其中一个支路与所述塔体液氮进口连通，另一个支路上连接有液体量筒。 
本实用新型提出的高纯氮制取设备，当氮气的实际用量小于额定用量时，通过变频空气压缩机减少原料空气的用量，使进入分馏塔系统的原料空气量减小，分馏塔系统中采用的精馏塔为填料式精馏塔，填料式精馏塔能够实现大范围变负荷的能力，因此可控制氮气产量，避免不必要的电能的损耗，节约能源。 
进一步的，将精馏塔与冷凝蒸发器一体设置，并将冷凝蒸发器设置于填料式精馏塔上方，利用物料的重力即可实现自然回流，省去了回流罐与回流泵等回流装置，使整个装置结构简单，便于安装，降低成本。 
进一步的，主换热器同时设置原料空气管道和用于污氮气通过的冷却管路，使污氮气的冷量得到充分利用、节能环保。 
进一步的，采用透平膨胀机对污氮气进行绝热膨胀，为装置补偿冷量。 
附图说明
图1是本实用新型实施例的结构示意图； 
图2是图1中填料式精馏塔和冷凝蒸发器的结构示意图。
具体实施方式
本实用新型的实施例如图1～图2所示，下面结合附图对本实施例的具体实施方式进行详细说明： 
高纯氮制取设备，包括通过管线连通的空气压缩系统1、预冷系统2、分子筛纯化系统3和分馏塔系统4，空气压缩系统1包括空气压缩机5，所述空气压缩机5采用变频螺杆式空气压缩机，预冷系统2包括冷气机组6，分子筛纯化系统3包括管线连接的电加热器7、分子筛吸附器8和第一消音器9，分子筛吸附器8用于去除原料空气中的H2O、CO2及C2H2等碳氢化合物，在本系统中共设置有两台，一台用于对流入的原料空气进行吸附纯化，另一台用于对经过透平膨胀机回流入其中的废气再生，分馏塔系统4包括通过管线连接的透平膨胀机10、第一主换热器12、第二主换热器13、过冷器15、填料式精馏塔16和冷凝蒸发器17，冷凝蒸发器一体设置于填料式精馏塔16上方。所述第一主换热器12内同时设置有原料空气管道、污氮气管道和高纯氮气输出管道。
填料式精馏塔和冷凝蒸发器的结构如图2所示，填料式精馏塔包括塔高沿上下方向延伸的塔体，塔体内通过填料支撑板支撑有三层填料层1602，也可根据需要设置一层或两层以上的多层填料层，底部开设有用于将塔底沉积的富氧液空排出塔外的排放口1606，最底层填料层下方的塔体的一侧开设有原料空气入口1605，另一侧开设有使富氧液空通过管道抽送入冷凝蒸发器的富氧液空接口1601；最顶层填料层上方的塔体一侧上开设有与塔体内最上层的填料层上方的液体分布器连通的用于将回流的液氮作为回流液输送进塔体内部的塔体液氮进口1604，另一侧开设有用于将分馏出的氮气输出的高纯氮出口1603。填料式精馏塔16的上方设置的冷凝蒸发器17的顶部开设有污氮气排出口1702，冷凝蒸发器上部一侧开设有与富氧液空接口通过管道连接而使富氧液空进入冷凝蒸发器的富氧液空进口1703，冷凝蒸发器一侧开设有使部分氮气进入冷凝蒸发器的氮气进口1701，另一侧开设有用于将氮气与流经冷凝蒸发器的富氧液空进行热交换而形成的液氮输出冷凝蒸发器的液氮出口1705和用于将不凝气体输出的不凝气体出口1704，冷凝蒸发器底部开设有将冷凝蒸发器中的富氧液空排出的富氧液空排放口1706。 
所述原料空气管道入口与分子筛纯化系统3连通、原料空气管道出口通过串接有第二主换热器13的管道与所述填料式精馏塔16的原料空气入口1605连通；所述高纯氮气输出管道入口通过串接有第二主换热器13的管道与所述填料式精馏塔16的高纯氮出口1603连通、高纯氮气输出管道出口与氮气使用管道连通将高纯氮输出；所述污氮气管道入口通过串接有第二主换热器13和过冷器15的管道与所述透平膨胀机10连通、污氮气管道出口与分子筛纯化系统2通过管路连通。 
采用上述设备制取氮气时，首先变频螺杆式空气压缩机按照用户所需氮气量将适当量的过滤过的原料空气压缩，经过空气压缩机末端的冷却器冷却之后，通过管路输送到冷气机组6进行冷却并将其输送到分子筛纯化系统3中。原料空气进入分子筛纯化系统3后，被分子筛吸附器8将其中的H2O、CO2及C2H2等碳氢化合物清除掉，经过进一步净化后的原料空气通过管道输送到分馏塔系统4中。 
原料空气通过原料空气管道首先进入第一主换热器12中并与第一主换热器中的污氮气管道和高纯氮气输出管道中流过的污氮气和高纯氮气进行热交换，冷却后的原料空气经过第二主换热器13继续换热后从填料式精馏塔16的原料空气入口1605进入填料式精馏塔的底部，富氧液空积存在填料式精馏塔16的底部，氮气上升并在填料层中与回流液进行传质不断分离出氮气，最后到达塔顶处的氮气纯度可到99.9999%，一部分高纯氮气作为产品氮气直接从高纯氮出口1603输出，经过高纯氮气输出管道进入第一主换热器12中与流经此处的原料空气进行热交换，将原料空气冷却而使自身复热到常温后输出；另一部分高纯氮气通过管道从冷凝蒸发器17的氮气进口1701进入冷凝蒸发器，被通过富氧液空进口1703进入冷凝蒸发器的富氧液空冷凝成为液氮，液氮作为回流液从冷凝蒸发器的液氮出口1705流出，在自身重力作用下通过管道从填料式精馏塔16的塔体液氮进口1604进入填料式精馏塔内设置的液体分布器的接入口，通过液体分布器将液氮均匀喷洒在填料层上，并逐级向下流动将各层填料层润湿，使液体与上升至该层的氮气进行传质逐级分馏；另一部分液氮经液氮回流管抽出进入液体量筒14并向液氮贮槽输送。冷凝蒸发器中的不凝气体通过其上的不凝气体出口1704排出。 
填料式精馏塔底部积存的富氧液空一部分通过连接富氧液空接口1601和富氧液空进口1703的、串接有过冷器的管道被抽送到冷凝蒸发器17中，将冷凝蒸发器17中的部分高纯氮气冷凝成为液氮，换热后的富氧液空通过其上开设的富氧液空排放口1706排放；另一部分通过填料式精馏塔底部的排放口1606排出。 
冷凝蒸发器17中产生的污氮气从其顶端开设的污氮气排出口1702排出，通过管道上设置的过冷器15后进入第二主换热器13回收部分冷量，然后进入透平膨胀机10，在透平膨胀机10中进行膨胀制冷，膨胀后的污氮气从透平膨胀机输出，经过过冷器15冷却后进入第二主换热器13、第一主换热器12，在第二主换热器和第一主换热器中与原料空气热交换，将原料空气冷却，然后一部分通过管道从分子筛吸附器的再生器入口进入分子筛吸附器中作为再生气体，另一部分通过第二消音器11排放到空气中；透平膨胀机中多余的污氮气用做风机制动气。 
当氮气使用量小于额定用量时，变频螺杆式空气压缩机可降低原料空气的用量，节约能源，继而改变进入填料式精馏塔的空气量，改变氮气产量，填料式精馏塔具有大范围变负荷的能力，氮气产量可根据实际用量在30%～120%之间变化。 
在本实施例中变频空气压缩机采用变频螺杆式空气压缩机，在本实用新型的其他实施例中也可采用变频活塞式空气压缩机等其他常用的变频空气压缩机。 
在本实施例中原料空气经过变频螺杆式空气压缩机后依次通过预冷系统对其进行冷却、分子筛纯化系统去除原料空气中的H2O、CO2及C2H2等碳氢化合物后进入分馏塔系统，在本实用新型的其他实施例中除空气压缩机和填料式精馏塔外的其他结构也可采用背景技术中的结构。 
在本实施例中污氮气从冷凝蒸发器顶部的污氮气排放口排出，最后从分子筛吸附器的再生气入口进入分子筛吸附器中作为再生气体，在污氮气排放口与分子筛吸附器的连接管道上依次设置有过冷器、第二主换热器、透平膨胀机和第一主换热器，在本实用新型的其他实施例中也可只设置一个主换热器或不设置过冷器、第二主换热器、透平膨胀机和第一主换热器，若需要对原料空气进行冷却时，在管道附近设置制冷箱等外置冷源。 
在本实施例中在污氮气管路以及富氧液空接口与富氧液空进口的连接管道上均串接有过冷器，在本实用新型的其他实施例中也可不设置过冷器。 

Claims (8)

1.高纯氮制取设备，包括空气压缩机和分馏塔系统，所述分馏塔系统包括精馏塔和冷凝蒸发器，其特征在于：所述空气压缩机为用于调节原料空气使用量的变频空气压缩机，所述精馏塔包括塔高沿上下方向延伸的塔体，所述塔体内沿塔高方向间隔设置有至少一层填料层，所述填料层上方设置有对用于润湿填料层的液体进行均匀分布的液体分布器，所述塔体于所述填料层下方设置有用于使变频空气压缩机压缩后的原料空气进入塔体内的原料空气入口、用于将塔体底部的富氧液空抽送进所述冷凝蒸发器的富氧液空接口、与所述液体分布器连通用于将作为回流液的液氮输送进塔体内部的塔体液氮进口和用于将分馏出的高纯氮气输出的高纯氮出口。
2.根据权利要求1所述的高纯氮制取设备，其特征在于：所述变频空气压缩机为变频螺杆式空气压缩机。
3.根据权利要求1或2所述的高纯氮制取设备，其特征在于：还包括分子筛吸附器，所述冷凝蒸发器顶部开设有将污氮气排出冷凝蒸发器的污氮气排出口，周壁上开设有通过管道与所述富氧液空接口连接而使富氧液空进入冷凝蒸发器的富氧液空进口、与所述高纯氮出口管道连接用于使部分氮气进入冷凝蒸发器的氮气进口和用于与所述塔体液氮进口通过管道连通以将氮气与流经冷凝蒸发器的富氧液空进行热交换而形成的液氮输出冷凝蒸发器的液氮出口，所述污氮气排出口通过管道与所述分子筛吸附器的再生气入口连通。
4.根据权利要求3所述的高纯氮制取设备，其特征在于：所述冷凝蒸发器一体设置于所述精馏塔上方。
5.根据权利要求3所述的高纯氮制取设备，其特征在于：还包括主换热器，所述主换热器中设有原料空气管道和用于与原料空气管道中的原料空气热交换而对原料空气进行冷却的污氮气管道，所述污氮气管道具有与所述分子筛吸附器的再生气入口通过管道连通的出口端和与污氮气排出口通过管道连通的入口端。
6.根据权利要求5所述的高纯氮制取设备，其特征在于：所述主换热器与污氮气排出口连接的管道上设置有对污氮气进行膨胀冷却的透平膨胀机，透平膨胀机的入口通过管道与污氮气排出口连通，透平膨胀机的出口通过管道与主换热器的污氮气管道的入口端连通。
7.根据权利要求3所述的高纯氮制取设备，其特征在于：所述富氧液空接口与所述富氧液空进口的连接管道上串接有过冷器。
8.根据权利要求3所述的高纯氮制取设备，其特征在于：所述冷凝蒸发器的液氮出口的管路分为两个分支，其中一个支路与所述塔体液氮进口连通，另一个支路上连接有液体量筒。
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Cited By (3)

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CN103759499A (zh) * 2014-01-13 2014-04-30 浙江海天气体有限公司 一种超低能耗制氮装置
CN111550675A (zh) * 2020-05-09 2020-08-18 开封黄河空分集团有限公司 一种自动增压的低温液体送出方法及装置
CN114307220A (zh) * 2021-12-06 2022-04-12 杭州制氧机集团股份有限公司 一种纯氮设备用节能型双腔双层冷凝蒸发器

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103759499A (zh) * 2014-01-13 2014-04-30 浙江海天气体有限公司 一种超低能耗制氮装置
CN103759499B (zh) * 2014-01-13 2016-05-25 浙江海天气体有限公司 一种超低能耗制氮装置
CN111550675A (zh) * 2020-05-09 2020-08-18 开封黄河空分集团有限公司 一种自动增压的低温液体送出方法及装置
CN114307220A (zh) * 2021-12-06 2022-04-12 杭州制氧机集团股份有限公司 一种纯氮设备用节能型双腔双层冷凝蒸发器

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