CN202599013U - 一种返流膨胀制冷生产带压低纯氧和高纯氮的装置 - Google Patents

一种返流膨胀制冷生产带压低纯氧和高纯氮的装置 Download PDF

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CN202599013U
CN202599013U CN2012201818521U CN201220181852U CN202599013U CN 202599013 U CN202599013 U CN 202599013U CN 2012201818521 U CN2012201818521 U CN 2012201818521U CN 201220181852 U CN201220181852 U CN 201220181852U CN 202599013 U CN202599013 U CN 202599013U
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周大荣
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SHANGHAI QIYUAN AIR SEPARATION TECHNOLOGY DEVELOPMENT Co Ltd
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Abstract

本实用新型提供一种返流膨胀制冷生产带压低纯氧和高纯氮的装置，装置包括上塔、下塔、主换热器、过冷器、凝蒸发器、液氧蒸发器和透平膨胀机。采用双塔制氮制氧，低纯液氧通过液位差增压后在液氧蒸发器中汽化出冷箱，避免的氧气压缩机或液氧泵等动设备，节省了设备投资、降低了能耗、提高了产品附加值。

Description

一种返流膨胀制冷生产带压低纯氧和高纯氮的装置
技术领域
本实用新型涉及一种利用液化作用进行气体分离的装置，尤其涉及一种从空气中分离低纯氧和高纯氮的装置。 
背景技术
随着浮法玻璃、化工等行业的快速发展，对高纯氮气、带压低纯氧需求量急剧增大，通常浮法玻璃行业在使用的高纯氮气压力为0.2～0.5MPa，氮气纯度为99.999％（O2浓度≤3ppm）；由于玻璃原料的融化需要空气或氧气助燃，而且随着国家节能减排政策的实施及燃料成本的上升，氧气助燃有着更为广阔的应用前景。采用氧气助燃可以大大减少氧化亚氮、二氧化碳的排放，并可以节约燃料、提高玻璃产品等级，其中氧气助燃需要的氧气纯度大于90％，最好能够大于93％，同时压力应大于0.15MPa。 
空气中的主要气体成分为氮气和氧气，氮气和氧气体积分数分别为78.12％和20.98％，而空气作为廉价资源无处不在，因此通过分离空气来生产氮气和氧气是最为传统的方法。 
传统的低纯氧空分采用空气膨胀进上塔的双塔空分流程制取的93％O2低纯氧气的设备氧气提取可达99％以上，单因氧气、氮气压力低（一般氮气压力＜0.05MPa，氧气＜0.07MPa），其电耗一般为0.5～0.55KWh/m3，能耗较高，其副产品低压氮气不能直接输送，需增加氮气压缩机，氮气纯度也不能满足高端浮法玻璃的需求。同时生产的氧气压力小于0.1MPa，而浮法玻璃、化工行业需要大量的带压力的高纯氮气、低纯氧气，氮气及氧气压力要求大于0.15MPa。同时为了达到节能减排的要求，从空分过程中直接生产高提取率、带压力的高纯氮、低纯氧是非常具有价值的。 
全氧燃烧浮法玻璃生产线，氧气需求量远远大于氮气需求量，氧氮比一般为3∶1～4∶1，因此空分设备如何低成本地生产带压的低纯氧气及少量带压氮气成为关键。 
实用新型内容
本实用新型提供了一种以空气为原料生产带压低纯氧和高纯氮的装置，采用双塔制氮制氧，低纯液氧通过液位差增压后在液氧蒸发器中汽化出冷箱，避免的氧气压缩机或液氧泵等动设备，节省了设备投资、降低了能耗、提高了产品附加值。 
为了实现上述目的，本发明提供一种返流膨胀制冷生产带压低纯氧和高纯氮的装置，所述装置包括上塔、下塔、主换热器、过冷器、冷凝蒸发器、液氧蒸发器和透平膨胀机， 
装置入口管道分别与液氧蒸发器管程入口和下塔塔釜相连通，所述液氧蒸发器管程出口和下塔塔釜之间设有管路；所述上塔底部与下塔顶部、液氧蒸发器壳程入口之间分别设有管路，冷凝蒸发器设置在上塔内。所述上塔顶部或中上部设有排污氮气管道，排污氮气管道穿过主换热器和/或过冷器后与污氮气排除管相连通。 
所述冷凝蒸发器管程、壳程和液氧蒸发器的壳程之间设有管路，冷凝蒸发器比液氧蒸发器高；所述液氧蒸发器壳程出口设有排低纯氧管道，所述排低纯氧管道穿过主换热器和/或过冷器后和低纯氧供应管道相连通。 
所述上塔和/或下塔顶部设有排高纯氮管道，所述排高纯氮管道穿过主换热器和/或过冷器后与高纯氮供应管路相连通；所述装置入口管道、排污氮气管道和排低纯氧管道穿过换热器时进行换热。 
在本发明中的一个优选实施例中，所述上塔的操作压力大于0.08MPa。 
在本发明中的一个优选实施例中，气氧出所述主换热器后的压力大于0.15MPa。 
在本发明中的一个优选实施例中，所述污氮气经透平膨胀机膨胀至大气压后离开。 
在本发明中的一个优选实施例中，所述冷凝蒸发器与液氧蒸发器之间的高度差大于5m。 
在本发明中的一个优选实施例中，所述冷凝蒸发器、上塔和下塔为一体式结构，冷凝蒸发器设置在下塔顶部，冷凝蒸发器顶部设有上塔。 
在本发明中的一个优选实施例中，下塔的塔板数为50～100块，操作压力为 0.6～1.1MPa。上塔的塔板数为40～100块，操作压力为0.08～0.25MPa。 
本发明和传统技术相比具有以下优点： 
1）本实用新型提供的装置中采用提高上塔压力，低纯液氧依靠重力自增压生产带压氧气，并能够同时生产带压高纯氮，装置冷量由返流污氮膨胀提供，与传统的低纯液氧自增压流程采用空气膨胀进上塔比，所有空气均进入了下塔精馏后进入上塔精馏分离，提高了氧气提取率，同时达到生产带压氮气的目的。 
2）本实用新型提供的装置生产的氮气压力可达0.06～0.25MPa，纯度达99.999％（氧气含量小于5ppm），同时生产的氧气纯度可达到90％～98％，压力达0.1～0.25MPa。并可从下塔抽取氧气产量50％以下的高压压力氮气，而氧气提取率无明显降低，同时满足浮法玻璃全氧燃烧所需氧气、氮气，不需额外的氧气、氮气压缩机或液氧泵等设备。 
附图说明
图1为本发明实施例1的流程图。 
图2为本发明实施例2的流程图。 
其中，C1为下塔，C2为上塔，E1为主换热器，E2为过冷器，K1为上塔冷凝蒸发器，K2为液氧蒸发器，TP为透平膨胀机，V1、V2、V3、V4为节流阀。1、2、3为压缩空气，4为液态空气，5为液态空气，6为减压后的液态空气，7为液态氮气，8为高纯液氮产品，9为减压后的液态氮气，10为上塔顶带压氮气，11为带压氮气产品，12为污氮气，13为膨胀前的污氮，14为膨胀后的污氮，15为出冷箱的污氮，16为低纯液氧，17为蒸发的带压低纯氧，18为带压低纯氧，19为下塔顶带压氮气，20为出冷箱带压氮气产品。 
具体实施方式
本实用新型提供的返流膨胀制冷生产带压低纯氧和高纯氮装置的工艺步骤中，采用下塔、上塔双塔设计，根据所需氮和氧的纯度和压力的不同，塔内塔板数和操作压力可分别从以下范围中选择：下塔塔板数量为50～100块，操作压力在0.6MPa～1.1MPa；上塔塔板数量为40～100块，操作压力在0.08MPa～0.25MPa。 
以下通过实施例对本实用新型提供的生产带压低纯氧和高纯氮的装置，以便更好理解本发明创造的内容，但实施例的内容并不限制本发明创造的保护范围。 
实施方式1 
参照图1，上塔C2和下塔C1按照图1方式通过管道连接，其中，上塔C2内安装45块塔板，操作压力0.12MPa；下塔C1内安装50块塔板，操作压力0.65MPa。 
经分子筛吸附除去二氧化碳和水的空气1经过主换热器E1进行冷却成为饱和状态，部分空气2送入下塔C1中，部分空气3送入液氧蒸发器K2中被冷凝成液空4进入下塔底部以上3块塔板的位置，进入下塔的空气和液空与塔顶回流的液氮精馏，塔顶得到氮气和塔釜得到富氧液态空气5。 
下塔氮气在上塔内的冷凝蒸发器K1冷却成液氮大部分回流至下塔C1，将部分液氮7经过冷器E2过冷后通过节流阀V3送入上塔C2的顶端，进行精馏，液态空气5通过节流阀V2上塔上部第24块塔板处进入上塔进行精馏，得到带压力的氮气和低纯液氧，从塔顶抽出氮气10，经过冷器E2和主换热器E1复热，得到供用户使用的大于99.999％纯度、0.09MPa压力的高纯氮气。 
从上塔底部抽出纯度为93％、压力为0.13MPa的低纯液氧16，经低纯液氧管路进入液氧蒸发器。由于上塔冷凝蒸发器顶部比液氧蒸发器顶部高超过7m，利用上塔冷凝蒸发器与液氧蒸发器的高度差，增加液氧压力0.08MPa至0.21MPa，在液氧蒸发器中蒸发后经主换热器复热后出冷箱压力≥0.17MPa。 
从上塔顶部位置抽出氮气10，经过冷器E2、主换热器E1复热至常温作为带压氮气产品11输出。 
从上塔上部15块塔板位置抽出污氮气12，经过冷器E2、主换热器E1下段中复热至-140℃～-160℃进入透平膨胀机TP中膨胀至大气压或接近大气压制冷，以补充装置冷量。 
实施方式2 
参照图2，上塔C2和下塔C1按照图2方式通过管道连接，其中，上塔C2内安装40块塔板，操作压力0.11MPa；下塔C1内安装55块塔板，操作压力0.62MPa。 
经分子筛吸附除去二氧化碳和水的空气1经过主换热器E1进行冷却成为饱和状态，部分空气2送入下塔C1中，部分空气3送入液氧蒸发器K2中被冷凝成液空4进入下塔底部以上3块塔板的位置，进入下塔的空气和液空与塔顶回流的液氮精馏，塔顶得到氮气和塔釜得到富氧液态空气5。从下塔塔顶抽出压力氮气19，经主换热器E1复热出冷箱，得到供用户使用的大于99.999％纯度、0.6MPa的压力高纯氮气。 
下塔氮气在上塔内的冷凝蒸发器K1冷却成液氮大部分回流至下塔C1，将部分液氮7经过冷器E2过冷后通过节流阀V3送入上塔C2的顶端，进行精馏，液态空气5通过节流阀V2上塔上部第24块塔板处进入上塔进行精馏，得到带压力的氮气和低纯液氧。 
从上塔底部抽出纯度为93％、压力为0.11MPa的低纯液氧16，经低纯液氧管路进入液氧蒸发器。由于上塔冷凝蒸发器顶部比液氧蒸发器顶部高超过7m，利用上塔冷凝蒸发器与液氧蒸发器的高度差，增加液氧压力0.08MPa至0.19MPa，在液氧蒸发器中蒸发后经主换热器复热后出冷箱压力≥0.15MPa。 
从上塔顶部或中上部抽出污氮气12，经过冷器E2、主换热器E1下段中复热至-140℃～-160℃进入透平膨胀机TP中膨胀至大气压或接近大气压制冷，以补充装置冷量。 
在实施例1中，制得纯度大于99.999％、压力为0.09MPa的氮气，制得纯度为93％、压力为0.17MPa的氧气。在实施例2中，制得纯度大于99.999％、压力为0.6MPa的氮气，制得纯度为93％、压力为0.15MPa的氧气。 
以上对本实用新型的具体实施例进行了详细描述，但其只是作为范例，本发明并不限制于以上描述的具体实施例。对于本领域技术人员而言，任何对本发明创造进行的等同修改和替代也都在本发明的范畴之中，如实施方式1也可像实施方式2在下塔抽取压力氮气，进入主换热器复热作为产品输出。因此，在不脱离本发明的精神和范围下所作的均等变换和修改，都应涵盖在本实用新型的范围内。 

Claims (8)

1.一种返流膨胀制冷生产带压低纯氧和高纯氮的装置，所述装置包括上塔、下塔、主换热器、过冷器、冷凝蒸发器、液氧蒸发器和透平膨胀机，其特征在于，
装置入口管道分别与液氧蒸发器管程入口和下塔塔釜相连通，所述液氧蒸发器管程出口和下塔塔釜之间设有管路；所述上塔底部与下塔顶部、液氧蒸发器壳程入口之间分别设有管路，冷凝蒸发器设置在上塔内；
所述上塔顶部或中上部设有排污氮气管道，排污氮气管道穿过主换热器和/或过冷器后与污氮气排除管相连通；
所述冷凝蒸发器管程、壳程和液氧蒸发器的壳程之间设有管路，冷凝蒸发器比液氧蒸发器高；所述液氧蒸发器壳程出口设有排低纯氧管道，所述排低纯氧管道穿过主换热器和/或过冷器后和低纯氧供应管道相连通；
所述上塔和/或下塔顶部设有排高纯氮管道，所述排高纯氮管道穿过主换热器和/或过冷器后与高纯氮供应管路相连通；
所述装置入口管道、排污氮气管道和排低纯氧管道穿过换热器时进行换热。
2.根据权利要求1所述的装置，其特征在于，所述上塔的操作压力大于0.08MPa。
3.根据权利要求1所述的装置，其特征在于，气氧出所述主换热器后的压力大于0.15MPa。
4.根据权利要求1所述的装置，其特征在于，所述污氮气经透平膨胀机膨胀至大气压后离开。
5.根据权利要求1所述的装置，其特征在于，所述冷凝蒸发器与液氧蒸发器之间的高度差大于5m。
6.根据权利要求1所述的装置，其特征在于，所述冷凝蒸发器、上塔和下塔为一体式结构，冷凝蒸发器设置在下塔顶部，冷凝蒸发器顶部设有上塔。
7.根据权利要求1所述的装置，其特征在于，所述下塔的塔板数为50～100块，操作压力为0.6～1.1MPa。
8.根据权利要求1所述的装置，其特征在于，所述上塔的塔板数为40～100块，操作压力为0.08～0.25MPa。 
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