CN109442867B - 一种外增压内液化纯氮制取装置及方法 - Google Patents
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Abstract
本发明公开一种外增压内液化纯氮制取装置，包括过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器、电加热器、主换热器、增压膨胀机、精馏塔I、精馏塔II、冷凝蒸发器I、冷凝蒸发器II、过冷器、液化器、增压机。本发明还公开一种外增压内液化纯氮制取方法。本发明采用污氮返流膨胀制冷，压力利用效率高，装置能耗低；采用双塔并联制氮，上塔压力可高于或低于下塔压力，可同时制取两种同压力等级或不同压力等级的氮气产品，并可制取部分液氮产品；设置内液化器和外部增压机，外增压机设在冷箱外部，便于维护和检修，内液化器设在冷箱内部，冷损失小，同时因外增压机在选型上不受限制，因此可极大增加本发明的应用范围。
Description
技术领域
本发明涉及空气分离技术领域，具体涉及一种外增压内液化纯氮制取装置及方法。
背景技术
随着化工、电子、新材料、瓷钢业、玻璃等行业技术发展和革新，对氮气需求量急速增加，同时对氮气纯度也提出了更高的要求。
目前市场上的常用的纯氮设备分为两种：单塔制氮和双塔制氮。单塔制氮流畅可制取一定压力的产品氮气直接供用户使用，该种流程形式虽然结构简单，但装置提取率较低，产品单耗高，不适合大规模用氮气量的需求；双塔制氮又分为常压氮气和带压氮气流程，常压氮气流程可以制取常压氮气或压力为0.1-0.2MpaG的低压氮气，装置提取率高，能耗较单塔制氮低，但是由于产品压力较低，产品氮气需要经氮气压缩机压缩后才能满足用户对氮气压力的要求，带压氮气流程一般为带液氮泵流程，对于氮气量＜4500Nm3/h的空分装置，液氮泵选择比较困难，同时因为液氮泵一般放置在冷箱内部，一旦液氮泵故障，必须对冷箱扒砂，因此液氮泵的配置上一般选择进口液体泵，且一用一备。
发明内容
本发明的目的是提供一种外增压内液化纯氮制取装置及方法，以解决现有技术的不足。
本发明采用以下技术方案：
一种外增压内液化纯氮制取装置，包括过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器、电加热器、主换热器、增压膨胀机、精馏塔I、精馏塔II、冷凝蒸发器I、冷凝蒸发器II、过冷器、液化器、增压机，
过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器、电加热器、增压机设于冷箱外，主换热器、增压膨胀机、精馏塔I、精馏塔II、冷凝蒸发器I、冷凝蒸发器II、过冷器、液化器设于冷箱内，冷凝蒸发器I设于精馏塔I上方，冷凝蒸发器II设于精馏塔II上方；
过滤器、透平空气压缩机、空气预冷机组、交替使用的分子筛吸附器依次连接，交替使用的分子筛吸附器和主换热器连接，主换热器和精馏塔I底部的原料空气进口连接；
精馏塔I顶部的压力氮气出口分别和主换热器、冷凝蒸发器I连接，主换热器连接外部管道以提供压力氮气产品；冷凝蒸发器I的液氮出口分别和精馏塔I顶部、冷箱外液氮存储罐连接，其中，冷凝蒸发器I的液氮出口和精馏塔I顶部的连接管路上设有角式冷阀；
精馏塔I底部的液空出口和过冷器连接，过冷器分别和冷凝蒸发器I、精馏塔II连接，过冷器和冷凝蒸发器I的连接管路上设有节流阀，过冷器和精馏塔II的连接管路上设有节流阀；冷凝蒸发器I的污氮气出口和液化器连接，液化器和增压机连接，增压机再和液化器连接，液化器和精馏塔II底部连接，液化器和精馏塔II底部连接管路上设有节流阀；
精馏塔II顶部的压力氮气出口分别和主换热器、冷凝蒸发器II连接，主换热器连接外部管道以提供压力氮气产品，冷凝蒸发器II的液氮出口和精馏塔II顶部连接；
精馏塔II底部的富氧液空出口和冷凝蒸发器II连接，精馏塔II底部的富氧液空出口和冷凝蒸发器II连接管路上设有节流阀，冷凝蒸发器II的污氮气出口和过冷器连接，过冷器和主换热器连接，主换热器部分复热出口和增压膨胀机连接，增压膨胀机和主换热器连接，主换热器分别和电加热器、外部放空管道连接，电加热器和交替使用的分子筛吸附器连接。
一种外增压内液化纯氮制取方法，包括如下步骤：
步骤一、将原料空气经过滤器过滤掉灰尘和机械杂质后，进入透平空气压缩机将空气压缩到设定压力；之后经空气预冷机组预冷后进入交替使用的分子筛吸附器中纯化；
步骤二、将纯化后的原料空气部分用于仪表空气，其余进入主换热器冷却至饱和并带有一定含湿后进入精馏塔I底部参与精馏；
步骤三、空气经精馏塔I精馏后分离为压力氮气和液空；压力氮气分成两股，一股直接引出经过主换热器复热后出冷箱作为产品供用户，另一股引入冷凝蒸发器I和液空换热，压力氮气被冷凝为液氮，引出部分液氮作为产品供用户，其余引入精馏塔I作为回流液；液空经过冷器过冷后分成两股，一股节流后引入精馏塔II参与精馏，另一股节流后进入冷凝蒸发器I作为冷源和压力氮气换热，液空汽化为污氮气，污氮气经液化器复热后出冷箱，经增压机增压后返回液化器，增压后污氮气和污氮气进行热交换，增压后污氮气被部分液化，节流后引入精馏塔II参与精馏；
步骤四、部分液化的污氮气和精馏塔I引入的液空经精馏塔II精馏后分离为富氧液空和压力氮气，压力氮气分成两股，一股直接引出经过主换热器复热后出冷箱作为产品供用户，另一股引入冷凝蒸发器II和富氧液空换热，压力氮气被冷凝为液氮，液氮引入精馏塔II作为回流液；富氧液空经节流后引入冷凝蒸发器II作为冷源和压力氮气换热，富氧液空被压力氮气汽化为污氮气，污氮气经过冷器复热、主换热器部分复热后引入增压膨胀机膨胀制取冷箱所需冷量，膨胀后污氮气经主换热器复合后出冷箱，部分作为再生气由电加热器加热后引入交替使用的分子筛吸附器，其余放空。
本发明的有益效果：
本发明采用污氮返流膨胀制冷，压力利用效率高，装置能耗低。
本发明采用双塔并联制氮，上塔压力可高于或低于下塔压力，可同时制取两种同压力等级或不同压力等级的氮气产品，并可制取部分液氮产品。
本发明设置了内液化器和外部增压机，外增压机设置在冷箱外部，便于维护和检修，内液化器设置在冷箱内部，冷损失小，同时因外增压机在选型上不受限制，因此可极大增加本发明的应用范围。
附图说明
图1为本发明装置结构示意图。
具体实施方式
下面结合实施例和附图对本发明做更进一步地解释。下列实施例仅用于说明本发明，但并不用来限定本发明的实施范围。
一种外增压内液化纯氮制取装置，包括过滤器1、透平空气压缩机2、空气预冷机组3、交替使用的分子筛吸附器4、电加热器5、主换热器6、增压膨胀机7、精馏塔I8、精馏塔II9、冷凝蒸发器I10、冷凝蒸发器II11、过冷器12、液化器13、增压机14，
过滤器1、透平空气压缩机2、空气预冷机组3、交替使用的分子筛吸附器4、电加热器5、增压机14设于冷箱外，主换热器6、增压膨胀机7、精馏塔I8、精馏塔II9、冷凝蒸发器I10、冷凝蒸发器II11、过冷器12、液化器13设于冷箱内，冷凝蒸发器I10设于精馏塔I8上方，冷凝蒸发器II11设于精馏塔II9上方；
过滤器1、透平空气压缩机2、空气预冷机组3、交替使用的分子筛吸附器4依次连接，交替使用的分子筛吸附器4和主换热器6连接，主换热器6和精馏塔I8底部的原料空气进口连接；
精馏塔I8顶部的压力氮气出口分别和主换热器6、冷凝蒸发器I10连接，主换热器6连接外部管道以提供压力氮气产品；冷凝蒸发器I10的液氮出口分别和精馏塔I8顶部、冷箱外液氮存储罐连接，其中，冷凝蒸发器I10的液氮出口和精馏塔I8顶部的连接管路上设有角式冷阀；
精馏塔I8底部的液空出口和过冷器12连接，过冷器12分别和冷凝蒸发器I10、精馏塔II9连接，过冷器12和冷凝蒸发器I8的连接管路上设有节流阀，过冷器12和精馏塔II9的连接管路上设有节流阀；冷凝蒸发器I10的污氮气出口和液化器13连接，液化器13和增压机14连接，增压机14再和液化器13连接，液化器13和精馏塔II9底部连接，液化器13和精馏塔II9底部连接管路上设有节流阀；
精馏塔II9顶部的压力氮气出口分别和主换热器6、冷凝蒸发器II11连接，主换热器6连接外部管道以提供压力氮气产品，冷凝蒸发器II11的液氮出口和精馏塔II9顶部连接；
精馏塔II9底部的富氧液空出口和冷凝蒸发器II11连接，精馏塔II9底部的富氧液空出口和冷凝蒸发器II11连接管路上设有节流阀，冷凝蒸发器II11的污氮气出口和过冷器12连接，过冷器12和主换热器6连接，主换热器6部分复热出口和增压膨胀机7连接，增压膨胀机7和主换热器6连接，主换热器6分别和电加热器5、外部放空管道连接，电加热器5和交替使用的分子筛吸附器4连接。
上述各部件的功能如下：
过滤器1，用于过滤原料空气中的灰尘和机械杂质；
透平空气压缩机2，用于将过滤后的原料空气压缩到设定压力；
空气预冷机组3，用于将过滤、压缩后的原料空气预冷；
交替使用的分子筛吸附器4，用于将过滤、压缩、预冷后的原料空气纯化，去除水分、CO2、C2H2等物质；
电加热器5，用于加热污氮气以再生分子筛吸附器；
主换热器6，用于将过滤、压缩、预冷、纯化后的原料空气冷却，将精馏塔I8的压力氮气、精馏塔II9的压力氮气、膨胀后污氮气复热，将经过冷器12复热后的污氮气部分复热；
增压膨胀机7，用于将主换热器6部分复热后的污氮气膨胀制取冷箱必需冷量；
精馏塔I8，用于将经过滤、压缩、预冷、纯化、冷却后的原料空气低温精馏而分离为压力氮气和液空；
精馏塔II9，用于将部分液化的污氮气和精馏塔I8引入的液空精馏而分离为富氧液空和压力氮气；
冷凝蒸发器I10，用于将精馏塔I8的压力氮气和液空换热，压力氮气被冷凝为液氮，液空汽化为污氮气；
冷凝蒸发器II11，用于将精馏塔II9的压力氮气和富氧液空换热，压力氮气被冷凝为液氮，富氧液空汽化为污氮气；
过冷器12，用于将液空过冷，将冷凝蒸发器II11的污氮气复热；
液化器13，用于将冷凝蒸发器I10的污氮气复热，增压后污氮气部分液化；
增压机14，用于将经液化器13复热后的污氮气增压。
一种外增压内液化纯氮制取方法，包括如下步骤：
步骤一、将原料空气经过滤器1过滤掉灰尘和机械杂质后，进入透平空气压缩机2将空气压缩到设定压力0.4-1.5MpaA；之后经空气预冷机组3预冷至5-8℃后进入交替使用的分子筛吸附器4中纯化，去除水分、CO2、C2H2等物质；
步骤二、将纯化后的原料空气部分用于仪表空气(图中未标示)，其余进入主换热器6冷却至饱和并带有一定含湿后进入精馏塔I8底部参与精馏；
步骤三、空气经精馏塔I8精馏后分离为压力氮气和液空；压力氮气分成两股，一股直接引出经过主换热器6复热后出冷箱作为产品供用户，另一股引入冷凝蒸发器I10和液空换热，压力氮气被冷凝为液氮，引出部分液氮作为产品供用户，其余引入精馏塔I8作为回流液；液空经过冷器12过冷后分成两股，一股节流后引入精馏塔II9参与精馏，另一股节流后进入冷凝蒸发器I10作为冷源和压力氮气换热，液空汽化为污氮气，污氮气经液化器13复热后出冷箱，经增压机14增压后返回液化器13，增压后污氮气和污氮气进行热交换，增压后污氮气被部分液化，节流后引入精馏塔II9参与精馏；
步骤四、部分液化的污氮气和精馏塔I8引入的液空经精馏塔II9精馏后分离为富氧液空和压力氮气，压力氮气分成两股，一股直接引出经过主换热器6复热后出冷箱作为产品供用户，另一股引入冷凝蒸发器II11和富氧液空换热，压力氮气被冷凝为液氮，液氮引入精馏塔II9作为回流液；富氧液空经节流后引入冷凝蒸发器II11作为冷源和压力氮气换热，富氧液空被压力氮气汽化为污氮气，污氮气经过冷器12复热、主换热器6部分复热后引入增压膨胀机7膨胀制取冷箱所需冷量，膨胀后污氮气经主换热器6复合后出冷箱，部分作为再生气由电加热器5加热后引入交替使用的分子筛吸附器4，其余放空。
Claims (1)
1.一种外增压内液化纯氮制取方法，其特征在于，包括如下步骤：
步骤一、将原料空气经过滤器过滤掉灰尘和机械杂质后，进入透平空气压缩机将空气压缩到设定压力；之后经空气预冷机组预冷后进入交替使用的分子筛吸附器中纯化；
步骤二、将纯化后的原料空气部分用于仪表空气，其余进入主换热器冷却至饱和并带有一定含湿后进入精馏塔I底部参与精馏；
步骤三、空气经精馏塔I精馏后分离为压力氮气和液空；压力氮气分成两股，一股直接引出经过主换热器复热后出冷箱作为产品供用户，另一股引入冷凝蒸发器I和液空换热，压力氮气被冷凝为液氮，引出部分液氮作为产品供用户，其余引入精馏塔I作为回流液；液空经过冷器过冷后分成两股，一股节流后引入精馏塔II参与精馏，另一股节流后进入冷凝蒸发器I作为冷源和压力氮气换热，液空汽化为污氮气，污氮气经液化器复热后出冷箱，经增压机增压后返回液化器，增压后污氮气和污氮气进行热交换，增压后污氮气被部分液化，节流后引入精馏塔II参与精馏；
步骤四、部分液化的污氮气和精馏塔I引入的液空经精馏塔II精馏后分离为富氧液空和压力氮气，压力氮气分成两股，一股直接引出经过主换热器复热后出冷箱作为产品供用户，另一股引入冷凝蒸发器II和富氧液空换热，压力氮气被冷凝为液氮，液氮引入精馏塔II作为回流液；富氧液空经节流后引入冷凝蒸发器II作为冷源和压力氮气换热，富氧液空被压力氮气汽化为污氮气，污氮气经过冷器复热、主换热器部分复热后引入增压膨胀机膨胀制取冷箱所需冷量，膨胀后污氮气经主换热器复合后出冷箱，部分作为再生气由电加热器加热后引入交替使用的分子筛吸附器，其余放空。
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