CN106123488A - 一种带泵双塔的制氮方法 - Google Patents

一种带泵双塔的制氮方法 Download PDF

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CN106123488A
CN106123488A CN201610494554.0A CN201610494554A CN106123488A CN 106123488 A CN106123488 A CN 106123488A CN 201610494554 A CN201610494554 A CN 201610494554A CN 106123488 A CN106123488 A CN 106123488A
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蒋彬
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SUZHOU OXYGEN PLANT CO Ltd
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Abstract

本发明公开了一种带泵双塔的制氮方法，步骤如下：1：将原料空气压缩冷却后进入纯化系统；2、在纯化系统中吸附掉原料空气中的水分、二氧化碳及碳氢化合物后进入分馏塔；3、在分馏塔的主换热器中进行换热，降温至接近空气液化点进入精馏塔精馏得到高纯度氮气；4、从精馏塔的塔底抽取富氧液空，经过冷器过冷在主冷中蒸发；5、富氧液空在主冷内蒸发后，一部分进入主换热器复热后进入膨胀机制冷，膨胀后的富氧气经主换热器复热后进入去纯化系统作为再生气和冷吹气;另一部分进入辅塔精馏，精馏的液氮经低温泵进入精馏塔，液空节流后进入辅冷蒸发，蒸汽经过冷与主换热器复热后放空。通过上述方式，本发明既可直接生产压力氮，提取率高。

Description

一种带泵双塔的制氮方法
技术领域
本发明涉及一种制氮方法，特别是一种结合双塔废气膨胀精馏制氮流程和单塔返流精馏制氮流程优点，既可直接生产压力氮，又有较高提取率的带泵双塔的制氮方法。
背景技术
随着经济发展，科技研发民用工业，都离不开气体工业与低温技术，全球特别是中国的经济增长，使空分市场前景看好、形势乐观。石化、电子、化纤、多晶硅等工业的发展需要高纯氮气走越来越多。制氮设备属于国家鼓励发展的节能环保范畴。项目符合国家节约资源、坚持可持续发展的要求。国家发布实施的《促进产业结构调整暂行规定》和与之相配的《产业结构调整指导目录》，“能耗”是划分“目录”的一个很重要的标准。采用高新技术来降低能耗的项目列入“鼓励类”，凡是资源和能源消耗高、严重污染环境和破坏环境的项目则被列入“淘汰类”，一批落后产品将被限期淘汰。
过去双塔废气膨胀精馏制氮流程只能生产压力比较低的氮气：单塔返流精馏制氮流程生产压力比较高的压力氮，但是提取率比较低。
发明内容
本发明主要解决的技术问题是提供一种结合双塔废气膨胀精馏制氮流程和单塔返流精馏制氮流程优点，既可直接生产压力氮，又有较高提取率的带泵双塔的制氮方法。
为解决上述技术问题，本发明采用的一个技术方案是一种带泵双塔的制氮方法，具体步骤如下：
步骤1：将原料空气由在自洁式过滤器吸附灰尘后经空气压缩机压缩至0.9MPa，然后通过预冷机组冷却到10℃后进入纯化系统；
步骤2：在纯化系统中吸附掉原料空气中的水分、二氧化碳及碳氢化合物后进入分馏塔；
步骤3：在分馏塔的主换热器中，空气作为热流体与返流冷流体的富氧气和氮气进行换热，温度降至接近空气液化点进入精馏塔进行精馏，在精馏塔的顶部得到高纯度氮气；
步骤4：将高纯度氮气分为二部分；第一部份作为产品氮气，经主换热器复热后出分馏塔，送至用户；第二部份经主冷冷凝液化成为液氮，所得液氮的一部份作为产品输出，另一部份重新进入精馏塔作为回流液；
步骤5：从精馏塔的塔底抽取精馏出氮后剩下的富氧液空，通过过冷器的过冷后节流在主冷中蒸发；
步骤6：富氧液空在主冷内蒸发后，一部分进入主换热器复热后进入膨胀机制冷，膨胀后的富氧气经主换热器复热后出分馏塔，进入去纯化系统作为纯化系统的再生气和冷吹气;另一部分进入辅塔精馏，精馏的液氮经低温泵进入精馏塔，液空节流后进入辅冷与主冷未蒸发液空汇合蒸发，蒸发后蒸汽经过冷与主换热器复热后放空。
优选的，所述步骤4中获得的氮气产品可通过膨胀机增压端增压，提高出塔压力。
优选的，主冷与辅冷器之间的冷量分配，可以调节进入膨胀机的流量，从而调节产品液氮量。
优选的，所述分馏塔由主塔、辅塔，主冷，辅冷，主换热器，低温液体泵等组成。
本发明的有益效果是：本发明所述的一种带泵双塔的制氮方法，结合双塔废气膨胀精馏制氮流程和单塔返流精馏制氮流程优点，既可直接生产压力氮，又有较高提取率；产出的产品压力高，提取率高，节能效果明显；由于加工空气减少，可节省设备和土建投资。
附图说明
下面结合附图对本发明技术方案作进一步说明：
附图1为本发明所述的一种带泵双塔的制氮方法的流程图。
具体实施方式
下面对本发明的较佳实施例进行详细阐述，以使本发明的优点和特征能更易于被本领域技术人员理解，从而对本发明的保护范围做出更为清楚明确的界定。
本发明实施例包括：一种带泵双塔的制氮方法，具体步骤如下：
步骤1：将原料空气由在自洁式过滤器吸附灰尘后经空气压缩机（AC101）压缩至0.9MPa，然后通过预冷机组（Ru201）冷却到10℃，再进入纯化系统（MS301）；
步骤2：在纯化系统（MS301）中吸附掉原料空气中的水分、二氧化碳及碳氢化合物后进入分馏塔；
步骤3：在分馏塔的主换热器（E501/E502）中，空气作为热流体与返流冷流体的富氧气和氮气进行换热，温度降至接近空气液化点进入精馏塔（C501）进行精馏，在精馏塔的顶部得到高纯度氮气；
步骤4：将步骤3中的高纯度氮气分为二部分；第一部份作为产品氮气，经主换热器复热后出分馏塔，送至用户；第二部份经主冷（K501）冷凝液化成为液氮，所得液氮的一部份作为产品输出，另一部份重新进入精馏塔作为回流液；
步骤5：从塔底抽取的富氧液空，通过过冷器（E503）的过冷后节流在主冷中蒸发；
步骤6：富氧液空在主冷（K501）内蒸发后，一部分进入主换热器（E501/E502）复热后进入膨胀机（ET501/ET502）制冷，膨胀后的富氧气经主换热器（E501/E502）复热后出分馏塔，进入去纯化系统（MS301）作为纯化系统（MS301）的再生气和冷吹气;另一部分进入辅塔（C502）精馏，精馏的液氮经低温泵（P501）进入精馏塔（C501），液空节流后进入辅冷（K502）与主冷（K501）未蒸发液空汇合蒸发，蒸发后蒸汽经过冷（E503）与主换热器（E501/E502）复热后放空。
所述分馏塔由主塔、辅塔，主冷，辅冷，主换热器，低温液体泵等组成。
通过增加一台辅塔以及辅冷和增加一台液体泵将精馏塔与辅塔联系起来；并且可将出塔氮气产品通过膨胀机增压端增压，提高出塔压力；通过双塔流程，增加主塔的回流比，提高精馏塔的精馏效率，能够提高氮气的提取率，节约能耗；通过主冷与辅冷之间的冷量分配，可以调节进入膨胀机的流量，从而调节产品液氮量；通过低温泵的运行，可以保证抽取不同压力的液氮。
本发明的有益效果是：本发明所述的一种带泵双塔的制氮方法，结合双塔废气膨胀精馏制氮流程和单塔返流精馏制氮流程优点，既可直接生产压力氮，又有较高提取率；产出的产品压力高，提取率高，节能效果明显；由于加工空气减少，可节省设备和土建投资。
以上仅是本发明的具体应用范例，对本发明的保护范围不构成任何限制。凡采用等同变换或者等效替换而形成的技术方案，均落在本发明权利保护范围之内。

Claims (4)

1.一种带泵双塔的制氮方法，其特征在于：具体步骤如下：
步骤1：将原料空气由在自洁式过滤器吸附灰尘后经空气压缩机压缩至0.9MPa，然后通过预冷机组冷却到10℃后进入纯化系统；
步骤2：在纯化系统中吸附掉原料空气中的水分、二氧化碳及碳氢化合物后进入分馏塔；
步骤3：在分馏塔的主换热器中，空气作为热流体与返流冷流体的富氧气和氮气进行换热，温度降至接近空气液化点进入精馏塔进行精馏，在精馏塔的顶部得到高纯度氮气；
步骤4：将高纯度氮气分为二部分；第一部份作为产品氮气，经主换热器复热后出分馏塔，送至用户；第二部份经主冷冷凝液化成为液氮，所得液氮的一部份作为产品输出，另一部份重新进入精馏塔作为回流液；
步骤5：从精馏塔的塔底抽取精馏出氮后剩下的富氧液空，通过过冷器的过冷后节流在主冷中蒸发；
步骤6：富氧液空在主冷内蒸发后，一部分进入主换热器复热后进入膨胀机制冷，膨胀后的富氧气经主换热器复热后出分馏塔，进入去纯化系统作为纯化系统的再生气和冷吹气;另一部分进入辅塔精馏，精馏的液氮经低温泵进入精馏塔，液空节流后进入辅冷与主冷未蒸发液空汇合蒸发，蒸发后蒸汽经过冷与主换热器复热后放空。
2.根据权利要求1所述的带泵双塔的制氮方法，其特征在于：所述步骤4中获得的氮气产品可通过膨胀机增压端增压，提高出塔压力。
3.根据权利要求1所述的带泵双塔的制氮方法，其特征在于：主冷与辅冷器之间的冷量分配，可以调节进入膨胀机的流量，从而调节产品液氮量。
4.根据权利要求1所述的带泵双塔的制氮方法，其特征在于：所述分馏塔由主塔、辅塔，主冷，辅冷，主换热器，低温液体泵等组成。
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