CN2811892Y - 一种返流膨胀空气分离的装置 - Google Patents

一种返流膨胀空气分离的装置 Download PDF

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CN2811892Y
CN2811892Y CN 200520071105 CN200520071105U CN2811892Y CN 2811892 Y CN2811892 Y CN 2811892Y CN 200520071105 CN200520071105 CN 200520071105 CN 200520071105 U CN200520071105 U CN 200520071105U CN 2811892 Y CN2811892 Y CN 2811892Y
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江楚标
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SUZHOU XINGLU AIR SEPARATION PLANT SCIENCE AND TECHNOLOGY DEVELOPMENT Co Ltd
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Abstract

一种返流膨胀空气分离的装置，涉及到在低温下利用精馏及返流膨胀来分离空气的装置。在空气分离的过程中，使用了产品氮气和污氮这两种不同工质的膨胀机。产品氮气和污氮各自在不同的温度下进行膨胀，为空气分离过程提供冷量。分离过程采用双级精馏塔，精馏塔由下塔，上塔和两塔之间的冷凝蒸发器组成。下塔的操作压力是0.65MPa(表压)以上，上塔的操作压力是0.08MPa(表压)以上。采用这样的装置来分离空气，可使装置造价大幅下降，单位产品的电耗较同类流程有明显的下降，可优化性能价格比，使用和维修也更方便和经济。

Description

一种返流膨胀空气分离的装置
技术领域
本实用新型涉及到一种空气分离的装置，特别涉及到在低温下利用精馏及返流膨胀来分离空气的装置。
背景技术
在本实用新型提出之前，在低温下利用精馏来分离空气是一种公知的工业生产技术。整个装置包括以下设备：依次为压缩机，预冷设备，净化设备，增压透平膨胀机，换热器，精馏塔等。精馏塔则由下塔，上塔和冷凝蒸发器组成。物料以下述方式流过各个设备：经过压缩机压缩的空气在预冷设备中冷却，在净化设备中除去水蒸汽，二氧化碳等有害杂质后分为两股气流。一股气流为膨胀制冷用空气流，它经过增压机增压及水冷器冷却后进入换热器，降低温度后进入膨胀机，空气对外做功，降压降温后，或去精馏塔的上塔参与精馏，或返回换热器复热后回到压缩机的进口或去水冷塔。另一股气流为分离用空气流，它经过换热器降温到飽和温度或部份带液后进入精馏塔的下塔的底部。空气在下塔中得到初步分离，在底部获得含氧较多的富氧液空，富氧液空被引出下塔后经过过冷和节流膨胀进入上塔，作为上塔的回流液。下塔的顶部获得氮气，少部分可作为产品经复热后外供。其余氮气在冷凝蒸发器内与液氧换热而冷凝成为液氮。该液氮的一部分成为下塔的回流液，另一部分液氮被引出下塔后经过过冷大部分经节流膨胀进入上塔，作为上塔的回流液。少部分也可作为产品外供。在上塔的底部获得液氧，一部份液氧可作为产品引出，大部分液氧在冷凝蒸发器内被氮气所加热成为气氧，一部份气氧也可作为产品经复热后外供。大部份气氧则作为上升气流参与精馏。上塔的顶部可获得氮气及污氮气。在上塔的适当部位还可以抽提出含氩较高的馏份，在制氩系统通过精馏可获得产品氩。采用这样的装置来分离空气获得不同形态的氧，氮和氩，特别是液态氧，氮产品及压力氧、氮产品。单位产品电耗较高。
实用新型内容
本实用新型的目的是提出一种新的低温下空气分离的装置，使单位产品的电耗有较大的下降，装置的性能价格比更优良。使用维护更简便。
本实用新型是通过以下的技术措施来实现的。本实用新型的主要特征在于：装置内依次由压缩机，预冷设备，净化设备，膨胀机增压机，水冷器，换热器，精馏塔等组成。还有将返流污氮和产品氮进行降压降温的返流污氮和产品氮两种膨胀机。精馏塔由操作压力为0.65MPa(表压，下同)以上的下塔，操作压力为0.08MPa以上的上塔和两塔之间的冷凝蒸发器组成。返流污氮膨胀机和产品氮膨胀机中的一种是增压透平膨胀机，另一种可以带也可以不带增压机。
物料的流路如下：经过压缩机压缩的空气在预冷设备中冷却，在净化设备中除去水蒸汽，二氧化碳等有害杂质后进入膨胀机增压机增压及水冷器冷却后进入主换热器，经与返流气体换热降温到飽和温度或部分带液后，进入精馏塔的下塔的底部，成为下塔的上升气流，在塔板上与下降液流充分接触进行热量和质量的交换。在下塔的底部获得含氧较多的富氧液空。该富氧液空被引出下塔后，先经过液空过冷器被由上塔顶部来的返流污氮和产品氮过冷，再经过节流膨胀进入上塔成为上塔的回流液之一。在下塔的顶部获得的氮气，少部分可作为产品经复热后外供。大部分氮气在两塔之间的冷凝蒸发器内与液氧换热而冷凝成液氮。该液氮的一部分成为下塔的回流液，其余的液氮从冷凝蒸发器引出后，经过液氮过冷器被由上塔顶部来的返流污氮和产品氮过冷，少部分作为产品外供；大部分经过节流膨胀进入上塔的顶部成为上塔的另一支回流液。上述两股回流液成为上塔的下降液流。在塔板上下降液流与上升气流充分接触进行热量和质量的交换。在上塔的底部获得液氧，一部分可作为产品外供，一部分经低温液体泵升压后再在换热器中复热后去使用点，大部分液氧在两塔之间的冷凝蒸发器内被氮气加热成气氧，少部分气氧可作为产品经复热后外供，其余气氧则作为上升气流。上塔的顶部获得的返流污氮及产品氮进入返流污氮及产品氮膨胀机，气体对外做功，降压降温后再返回换热器复热后进入工艺预定位置。
在本实用新型中，在上塔获得的返流污氮及产品氮的温度较低，可以在液氮过冷器，液空过冷器，和主换热器的冷段复热。因此返流污氮膨胀机和产品氮膨胀机中的一台可位于液氮过冷器之前；或位于液氮过冷器之后；或位于液空过冷器之后。另一台则位于主换热器冷段。
在本实用新型中，返流污氮膨胀机和产品氮膨胀机是同时开动运行的。
在本实用新型中，可设置高压换热器及低温泵，生产内压缩气体产品。
在本实用新型中，可在上塔的适当位置抽出含氩较高的氩餾份去制氩系统制得氩产品。
本实用新型实施上述技术措施之后，可使装置造价大幅下降，单位产品的电耗较同类流程有明显的下降，可优化性能价格比。使用和维修也更方便和经济。
附图说明
附图是返流膨胀空气分离的装置示意图。内中设备序号如下：1为膨胀机增压机，2为水冷器，3为主换热器，4为返流污氮膨胀机，5为精馏塔，6为下塔，7为上塔，8为冷凝蒸发器，9为液空过冷器，10为液氮过冷器，11为产品氮膨胀机，12为低温液体泵。此外相关的物料流也作如下编号：101为原料空气，104为富氧液空，105为产品氮，106为液氧，107为液氮，108为液氮产品，109为氩馏分，110为返流污氮，111为液氧产品，112为内压缩氧气产品。
具体实施方式    下面结合附图和实施例对本实用新型作进一步说明。
经过压缩机压缩的在预冷系统中冷却并在净化系统中除去水蒸汽，二氧化碳等有害杂质后的原料空气101经过膨胀机4的增压机1增压及水冷器2冷却后进入主换热器3，经过主换热器3降温到飽和温度或部份带液后，进入精馏塔5的下塔6，精馏塔5由下塔6，上塔7和两塔之间的冷凝蒸发器8组成。下塔6的操作压力是0.65Mpa，上塔7的操作压力是0.08MPa。分离用原料空气流101进入下塔6的底部，成为下塔6的上升气流，在塔板上与下降液流充分接触进行热量和质量的交换。在下塔6的底部获得含氧较多的富氧液空104。该富氧液空104被引出下塔6后，先经过液空过冷器9被由上塔7顶部来的产品氮105和返流污氮110过冷，再经过节流膨胀进入上塔7成为上塔7的回流液之一。在下塔6的顶部获得的氮气，少部分可作为产品经复热后外供，大部分氮气在两塔之间的冷凝蒸发器8内与液氧换热而冷凝成液氮。该液氮的一部分成为下塔6的回流液。其余的液氮107经过液氮过冷器10被由上塔7顶部来的产品氮105和返流污氮110过冷，少部分作为产品108外供；大部分经过节流膨胀进入上塔7的顶部成为上塔7的另一支回流液。上述两股回流液成为上塔7的下降液流。在塔板上下降液流与上升气流充分接触进行热量和质量的交换。在上塔7的底部获得液氧，一部分液氧可作为产品111外供，一部分液氧经低温液体泵12升压到所需压力后经主换热器复热后成为内压缩氧气产品112去使用点，其余液氧在两塔之间的冷凝蒸发器8内被氮气加热成气氧，少部分气氧可作为产品经复热后外供，其余气氧成为上塔7的上升气流。在上塔7的顶部获得的产品氮105在液氮过冷器10和液空过冷器9中复热后进入产品氮膨胀机11，气体对外做功，降压降温后再进入液空过冷器9和主换热器3复热，之后引出冷箱作为产品。在上塔7的上部获得的返流污氮110在液氮过冷器10、液空过冷器9及主换热器3冷段复热后去返流污氮膨胀机4，降压降温后进入主换热器3与原料空气换热，之后去工艺预定位置。两台膨胀机4和11在流程中的位置可以互换。返流污氮膨胀机4和产品氮膨胀机11是同时开动运行的。
在上塔的适当位置抽出含氩较高的氩餾份109去制氩系统制得氩产品。
本实用新型不局限于上述实施方式，不论在装置上作任何变化，凡具有产品氮气和返流污氮这两种不同工质的膨胀机，且下塔的操作压力是0.65MPa(表压)以上，上塔的操作压力是0.08MPa(表压)以上的双级精馏空气分离装置均落在本实用新型的保护范围之内。

Claims (6)

1.一种返流膨胀空气分离的装置，依次由
(1)对空气进行加压，冷却和除去有害杂质使之成为原料空气的压缩机，预冷设备，和净化设备，
(2)对原料空气进行增压和冷却的膨胀机增压机(1)，水冷器(2)，
(3)对各种不同的流体进行冷热交换的主换热器(3)，过冷器(9)，(10)，
(4)将分离用原料空气进行分离获得产品的精馏塔(5)组成，
其特征在于：
(1)还有设置在液氮过冷器(10)和液空过冷器(9)之后的产品氮膨胀机(11)，
(2)还有设置在主换热器(3)冷段之后的返流污氮膨胀机(4)，
(3)精馏塔(5)是双级精馏塔，由操作压力为表压0.65MPa以上的下塔(6)，操作压力为表压0.08MPa以上的上塔(7)和两塔之间的冷凝蒸发器(8)组成。
2.根据权利要求1所述的一种返流膨胀空气分离装置，其特征是：产品氮膨胀机(11)设置在从精馏塔(5)的上塔(7)获得的产品氮(105)进入液氮过冷器(10)之前。
3.根据权利要求1所述的一种返流膨胀空气分离的装置，其特征是：产品氮膨胀机(11)设置在从精馏塔(5)的上塔(7)获得的产品氮(105)经过液氮过冷器(10)之后。
4.根据权利要求1所述的一种返流膨胀空气分离装置，其特征是：产品氮膨胀机(11)和返流污氮膨胀机(4)在流程中的位置是可以互换的。
5.根据权利要求1所述的一种返流膨胀空气分离装置，其特征是：返流污氮膨胀机(4)是增压透平膨胀机，产品氮膨胀机(11)带增压机，或不带增压机。
6.根据权利要求1所述的一种返流膨胀空气分离装置，其特征是：产品氮膨胀机(11)是增压透平膨胀机，返流污氮膨胀机(4)带增压机，或不带增压机。
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Cited By (8)

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CN102003867A (zh) * 2010-11-09 2011-04-06 上海启元科技发展有限公司 一种生产高纯氮和低纯氧的方法
CN102032755A (zh) * 2010-08-03 2011-04-27 苏州制氧机有限责任公司 空气分离装置
CN102032756A (zh) * 2011-01-07 2011-04-27 苏州市兴鲁空分设备科技发展有限公司 空气分离方法
CN102052821A (zh) * 2011-01-07 2011-05-11 苏州市兴鲁空分设备科技发展有限公司 一种空气分离方法
CN102141337A (zh) * 2011-03-30 2011-08-03 苏州市兴鲁空分设备科技发展有限公司 一种空气分离的方法
CN102230716A (zh) * 2011-06-08 2011-11-02 杭州优埃基空分设备有限公司 空气增压返流膨胀内压缩空气分离的方法及其装置
CN102445054A (zh) * 2011-12-22 2012-05-09 开封黄河空分集团有限公司 一种由空气分离制取氧气和氮气的工艺
CN103712417A (zh) * 2013-12-30 2014-04-09 上海启元空分技术发展股份有限公司 一种空气增压返流膨胀内压缩空气分离的方法和装置

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Publication number Priority date Publication date Assignee Title
CN102032755A (zh) * 2010-08-03 2011-04-27 苏州制氧机有限责任公司 空气分离装置
CN102003867A (zh) * 2010-11-09 2011-04-06 上海启元科技发展有限公司 一种生产高纯氮和低纯氧的方法
CN102032756A (zh) * 2011-01-07 2011-04-27 苏州市兴鲁空分设备科技发展有限公司 空气分离方法
CN102052821A (zh) * 2011-01-07 2011-05-11 苏州市兴鲁空分设备科技发展有限公司 一种空气分离方法
CN102141337A (zh) * 2011-03-30 2011-08-03 苏州市兴鲁空分设备科技发展有限公司 一种空气分离的方法
CN102141337B (zh) * 2011-03-30 2013-05-01 苏州市兴鲁空分设备科技发展有限公司 一种空气分离的方法
CN102230716A (zh) * 2011-06-08 2011-11-02 杭州优埃基空分设备有限公司 空气增压返流膨胀内压缩空气分离的方法及其装置
CN102445054A (zh) * 2011-12-22 2012-05-09 开封黄河空分集团有限公司 一种由空气分离制取氧气和氮气的工艺
CN103712417A (zh) * 2013-12-30 2014-04-09 上海启元空分技术发展股份有限公司 一种空气增压返流膨胀内压缩空气分离的方法和装置
CN103712417B (zh) * 2013-12-30 2016-09-28 上海启元空分技术发展股份有限公司 一种空气增压返流膨胀内压缩空气分离的方法和装置

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