CN113310282A - 一种带泵双塔精馏及低温正流膨胀制氮系统及制氮方法 - Google Patents

一种带泵双塔精馏及低温正流膨胀制氮系统及制氮方法 Download PDF

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CN113310282A
CN113310282A CN202110577154.7A CN202110577154A CN113310282A CN 113310282 A CN113310282 A CN 113310282A CN 202110577154 A CN202110577154 A CN 202110577154A CN 113310282 A CN113310282 A CN 113310282A
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rectifying tower
subcooler
pressure rectifying
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张行东
俞瑾
王丹
许峰杰
周凤华
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China National Air Separation Engineering Co ltd
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Abstract

本发明提供一种带泵双塔精馏及低温正流膨胀制氮系统及制氮方法，提取率高、能耗低且流程简单、易于操作、运行稳定。原料空气依次经过空气过滤器、空气压缩机、空冷塔、分子筛后进入主换热器，一部分空气被冷却后进入高压精馏塔，一部分空气被冷却后进入膨胀机后返回主换热器；在高压精馏塔获得的产品氮气一部分经主换热器复热后送至用户管网，一部分与低压精馏塔的富氧液空进行换热；在低压精馏塔获得的纯液氮经液氮泵、二号过冷器后送入高压精馏塔；冷凝蒸发器的富氧液空经过二号过冷器、三号过冷器后送入低压精馏塔的冷凝器，气化后生成的富氧气返回三号过冷器、一号过冷器、主换热器回收冷量，未被气化的富氧液空送至主换热器回收冷量。

Description

一种带泵双塔精馏及低温正流膨胀制氮系统及制氮方法
技术领域
本发明涉及一种带泵双塔精馏及低温正流膨胀制氮系统及制氮方法。
背景技术
随着我国的经济快速增长，空气分离市场前景看好，形式极为乐观。氮气作为一种保护气体，在玻璃、冶金、电子、化纤、多晶硅等行业中的需求急速增长，为确保高效低能耗以满足国家鼓励节能环保的要求，响应国家低碳发展，将降低能耗作为首要目标，对于制氮装置能耗及提取率要求随之提高，目前亟需一种提取率高、能耗低且流程简单、易于操作、运行稳定的制氮工艺。
发明内容
本发明的目的在于克服现有技术中存在的上述不足，而提供一种结构设计合理、提取率高、能耗低且流程简单、易于操作、运行稳定的带泵双塔精馏及低温正流膨胀制氮系统及制氮方法。
本发明解决上述问题所采用的技术方案是：一种带泵双塔精馏及低温正流膨胀制氮系统，其特征在于：包括空气过滤器、空气压缩机、空冷塔、分子筛、主换热器、高压精馏塔、冷凝蒸发器、低压精馏塔、一号过冷器、二号过冷器、三号过冷器、液氮泵和膨胀机；空气过滤器的出口与空气压缩机的进口连接，空气压缩机的出口与空冷塔的空气进口连接，空冷塔的空气出口与分子筛的进口连接，分子筛的出口与主换热器的热流体入口连接，主换热器的热流体出口分别与高压精馏塔的空气入口和膨胀机的进口连接，膨胀机的出口与主换热器的冷流体进口连接，主换热器的冷流体出口与分子筛的再生气入口连接；高压精馏塔的氮气出口分别与主换热器的冷流体入口和冷凝蒸发器的热流体入口连接，主换热器的冷流体出口与用户管网连接，冷凝蒸发器的热流体出口与高压精馏塔的回流液入口连接；高压精馏塔的富氧液空出口与一号过冷器的热流体进口连接，一号过冷器的热流体出口与低压精馏塔的富氧液空进口连接；低压精馏塔的液氮出口与液氮泵的进口连接，液氮泵的出口与二号过冷器的冷流体进口连接，二号过冷器的冷流体出口与高压精馏塔的液氮进口连接；低压精馏塔的富氧液空出口与冷凝蒸发器的冷流体入口连接，冷凝蒸发器的冷流体出口与二号过冷器的热流体进口连接，二号过冷器的热流体出口与三号过冷器的热流体入口连接，三号过冷器的热流体出口与低压精馏塔的冷凝器连接；低压精馏塔的富氧气出口与三号过冷器的冷流体入口连接，三号过冷器的冷流体出口与一号过冷器的冷流体入口连接，一号过冷器的冷流体出口与主换热器的冷流体入口连接；低压精馏塔的富氧液空出口与主换热器的冷流体入口连接。
本发明还包括补水泵，补水泵与空冷塔的冷却水进口连接。
本发明还包括电加热器，电加热器的入口与主换热器的冷流体出口连接，电加热器的出口与分子筛的再生气入口连接。
本发明所述的高压精馏塔和低压精馏塔均采用规整填料塔。
一种带泵双塔精馏及低温正流膨胀制氮方法，采用上述的带泵双塔精馏及低温正流膨胀制氮系统进行制氮，流程为：
S1、原料空气从空气过滤器的进口进入，依次经过空气过滤器过滤、空气压缩机压缩、空冷塔冷却、分子筛纯化后，进入主换热器，一部分空气被冷却到饱和温度后，进入高压精馏塔底部参与精馏，一部分空气被冷却后进入膨胀机膨胀后返回主换热器提供冷量，这部分复热后的空气进入分子筛作为再生气；
S2、经过精馏，在高压精馏塔顶部获得产品氮气，一部分经主换热器复热至常温后送至用户管网，一部分进入冷凝蒸发器，与低压精馏塔获得的富氧液空进行换热，冷凝得到的液氮作为高压精馏塔的回流液参与精馏；在高压精馏塔得到富氧液空，富氧液空经一号过冷器过冷后进入低压精馏塔再次精馏；
S3、在低压精馏塔获得纯液氮，纯液氮经液氮泵增压、二号过冷器换热后送入高压精馏塔参与精馏；低压精馏塔的富氧液空进入冷凝蒸发器作为冷源；冷凝蒸发器的富氧液空依次经过二号过冷器、三号过冷器过冷后送入低压精馏塔的冷凝器作为冷源冷凝低压精馏塔的塔顶氮气，而这股富氧液空本身被气化，气化后生成的富氧气依次返回三号过冷器、一号过冷器、主换热器回收冷量复热成常温的富氧气，未被气化的富氧液空送至主换热器回收冷量复热成常温的富氧气，这两股富氧气进入分子筛作为再生气。
本发明与现有技术相比，具有以下优点和效果：
1、本发明产品氮气出塔压力高，可以达到至少8.5bara，氮气产品出主换热器后直接供用户使用。
2、本发明采用双塔制氮，高压精馏塔顶部氮气与低压精馏塔底部富氧经冷凝蒸发器进行换热、低压精馏塔顶部液氮通过泵增压送入高压精馏塔，大大提高氮提取率，节能效果明显。
3、本发明一部分低温空气经膨胀机膨胀后返回主换热器提供冷量，膨胀后压力低，膨胀大，膨胀效率大大增加且发明简单。
4、本发明可根据用户需求，适当增加高压精馏塔工作压力即提高产品压力。
5、本发明不需要氮气压缩机就可以生产出至少8bara纯氮气，膨胀机正流膨胀，发明简洁、操作简单、运行稳定、能耗低、所需控制的阀门少，较易实现自动化控制。
附图说明
图1为本发明实施例的结构示意图。
具体实施方式
下面结合附图并通过实施例对本发明作进一步的详细说明，以下实施例是对本发明的解释而本发明并不局限于以下实施例。
本发明实施例包括空气过滤器1、空气压缩机2、补水泵3、空冷塔4、分子筛5、电加热器6、主换热器7、高压精馏塔8、冷凝蒸发器9、低压精馏塔10、一号过冷器11、二号过冷器12、三号过冷器13、液氮泵14和膨胀机15。
空气过滤器1的出口与空气压缩机2的进口连接，空气压缩机2的出口与空冷塔4的空气进口连接，空冷塔4的空气出口与分子筛5的进口连接，分子筛5的出口与主换热器7的热流体入口连接，主换热器7的热流体出口分别与高压精馏塔8的底部空气入口和膨胀机15的进口连接，膨胀机15的出口与主换热器7的冷流体进口连接，主换热器7的冷流体出口与分子筛5的再生气入口连接。分子筛5再生后的废气放空。
高压精馏塔8顶部的氮气出口与主换热器7的冷流体入口和冷凝蒸发器9的热流体入口连接，主换热器7的冷流体出口与用户管网连接，冷凝蒸发器9的热流体出口与高压精馏塔8的回流液入口连接；高压精馏塔8底部的富氧液空出口与一号过冷器11的热流体进口连接，一号过冷器11的热流体出口与低压精馏塔10中部的富氧液空进口连接。
低压精馏塔10顶部的液氮出口与液氮泵14的进口连接，液氮泵14的出口与二号过冷器12的冷流体进口连接，二号过冷器12的冷流体出口与高压精馏塔8顶部的液氮进口连接；低压精馏塔10底部的富氧液空出口与冷凝蒸发器9的冷流体入口连接，冷凝蒸发器9的冷流体出口与二号过冷器12的热流体进口连接，二号过冷器12的热流体出口与三号过冷器13的热流体入口连接，三号过冷器13的热流体出口与低压精馏塔10顶部的冷凝器连接；低压精馏塔10顶部的富氧气出口与三号过冷器13的冷流体入口连接，三号过冷器13的冷流体出口与一号过冷器11的冷流体入口连接，一号过冷器11的冷流体出口与主换热器7的冷流体入口连接；低压精馏塔10顶部的富氧液空出口与主换热器7的冷流体入口连接。
补水泵3与空冷塔4的冷却水进口连接。
高压精馏塔8和低压精馏塔10均采用规整填料塔，阻力小，氮提取率高，变负荷能力强。
电加热器6入口与主换热器7的冷流体出口连接，电加热器6出口与分子筛5的再生气入口连接。电加热器6加热主换热器7出来的空气，加热后的空气进入分子筛5作为再生气。
一种带泵双塔精馏及低温正流膨胀制氮方法，流程为：
S1、原料空气从从空气过滤器1的进口进入，依次经过空气过滤器1过滤、空气压缩机2压缩、空冷塔4冷却、分子筛5纯化被除去水分及二氧化碳等杂质后，压力变为8.85bara、温度变为25℃、流量变为5600Nm3/h，然后进入主换热器7，与返流的产品氮气和废气进行换热；一部分空气被冷却到饱和温度-167.3℃后，进入高压精馏塔8底部参与精馏；一部分空气被冷却至-110℃后进入膨胀机15膨胀至120kPa.A后返回主换热器7提供冷量，复热后的空气进入分子筛5作为再生气。
S2、经过精馏，在高压精馏塔8顶部获得产品氮气，压力为8.60 bara、温度为-171.6℃、流量为3000Nm³/h，一部分经主换热器7复热至常温后送至用户管网，一部分进入冷凝蒸发器9，与低压精馏塔10底部获得的富氧液空进行换热，冷凝得到的液氮作为高压精馏塔8的回流液参与精馏；在高压精馏塔8塔底得到富氧液空，压力为870kPa.a、温度为-167.7℃、流量为2900Nm³/h，富氧液空经一号过冷器11过冷后节流进入低压精馏塔10中下部再次精馏。
S3、在低压精馏塔10顶部获得纯液氮，压力为4.90 bara、温度为-180℃、流量为970Nm³，纯液氮经液氮泵14增压至9 bara、二号过冷器12换热后送入高压精馏塔8顶部参与精馏，可显著提高提取率。低压精馏塔10底部的富氧液空进入冷凝蒸发器9作为冷源。冷凝蒸发器9底部的富氧液空压力为5 bara、温度为-174℃、流量为2000Nm³/h，依次经过二号过冷器12、三号过冷器13过冷至-179℃后节流送入低压精馏塔10顶部冷凝器作为冷源冷凝低压精馏塔10的塔顶氮气，而这股富氧液空本身被气化，气化后生成的富氧气依次返回三号过冷器13、一号过冷器11、主换热器7回收冷量复热成常温的富氧气，未被气化的富氧液空直接送至主换热器7回收冷量复热成常温的富氧气，这两股富氧气进入分子筛5作为再生气。
此外，需要说明的是，本说明书中所描述的具体实施例，其零、部件的形状、所取名称等可以不同，本说明书中所描述的以上内容仅仅是对本发明结构所作的举例说明。凡依据本发明专利构思所述的构造、特征及原理所做的等效变化或者简单变化，均包括于本发明专利的保护范围内。本发明所属技术领域的技术人员可以对所描述的具体实施例做各种各样的修改或补充或采用类似的方式替代，只要不偏离本发明的结构或者超越本权利要求书所定义的范围，均应属于本发明的保护范围。

Claims (5)

1.一种带泵双塔精馏及低温正流膨胀制氮系统，其特征在于：包括空气过滤器、空气压缩机、空冷塔、分子筛、主换热器、高压精馏塔、冷凝蒸发器、低压精馏塔、一号过冷器、二号过冷器、三号过冷器、液氮泵和膨胀机；空气过滤器的出口与空气压缩机的进口连接，空气压缩机的出口与空冷塔的空气进口连接，空冷塔的空气出口与分子筛的进口连接，分子筛的出口与主换热器的热流体入口连接，主换热器的热流体出口分别与高压精馏塔的空气入口和膨胀机的进口连接，膨胀机的出口与主换热器的冷流体进口连接，主换热器的冷流体出口与分子筛的再生气入口连接；高压精馏塔的氮气出口分别与主换热器的冷流体入口和冷凝蒸发器的热流体入口连接，主换热器的冷流体出口与用户管网连接，冷凝蒸发器的热流体出口与高压精馏塔的回流液入口连接；高压精馏塔的富氧液空出口与一号过冷器的热流体进口连接，一号过冷器的热流体出口与低压精馏塔的富氧液空进口连接；低压精馏塔的液氮出口与液氮泵的进口连接，液氮泵的出口与二号过冷器的冷流体进口连接，二号过冷器的冷流体出口与高压精馏塔的液氮进口连接；低压精馏塔的富氧液空出口与冷凝蒸发器的冷流体入口连接，冷凝蒸发器的冷流体出口与二号过冷器的热流体进口连接，二号过冷器的热流体出口与三号过冷器的热流体入口连接，三号过冷器的热流体出口与低压精馏塔的冷凝器连接；低压精馏塔的富氧气出口与三号过冷器的冷流体入口连接，三号过冷器的冷流体出口与一号过冷器的冷流体入口连接，一号过冷器的冷流体出口与主换热器的冷流体入口连接；低压精馏塔的富氧液空出口与主换热器的冷流体入口连接。
2.根据权利要求1所述的带泵双塔精馏及低温正流膨胀制氮系统，其特征在于：还包括补水泵，补水泵与空冷塔的冷却水进口连接。
3.根据权利要求1所述的带泵双塔精馏及低温正流膨胀制氮系统，其特征在于：还包括电加热器，电加热器的入口与主换热器的冷流体出口连接，电加热器的出口与分子筛的再生气入口连接。
4.根据权利要求1所述的带泵双塔精馏及低温正流膨胀制氮系统，其特征在于：所述的高压精馏塔和低压精馏塔均采用规整填料塔。
5.一种带泵双塔精馏及低温正流膨胀制氮方法，其特征在于：采用权利要求1-4任一权利要求所述的带泵双塔精馏及低温正流膨胀制氮系统进行制氮，流程为：
S1、原料空气从空气过滤器的进口进入，依次经过空气过滤器过滤、空气压缩机压缩、空冷塔冷却、分子筛纯化后，进入主换热器，一部分空气被冷却到饱和温度后，进入高压精馏塔底部参与精馏，一部分空气被冷却后进入膨胀机膨胀后返回主换热器提供冷量，这部分复热后的空气进入分子筛作为再生气；
S2、经过精馏，在高压精馏塔顶部获得产品氮气，一部分经主换热器复热至常温后送至用户管网，一部分进入冷凝蒸发器，与低压精馏塔获得的富氧液空进行换热，冷凝得到的液氮作为高压精馏塔的回流液参与精馏；在高压精馏塔得到富氧液空，富氧液空经一号过冷器过冷后进入低压精馏塔再次精馏；
S3、在低压精馏塔获得纯液氮，纯液氮经液氮泵增压、二号过冷器换热后送入高压精馏塔参与精馏；低压精馏塔的富氧液空进入冷凝蒸发器作为冷源；冷凝蒸发器的富氧液空依次经过二号过冷器、三号过冷器过冷后送入低压精馏塔的冷凝器作为冷源冷凝低压精馏塔的塔顶氮气，而这股富氧液空本身被气化，气化后生成的富氧气依次返回三号过冷器、一号过冷器、主换热器回收冷量复热成常温的富氧气，未被气化的富氧液空送至主换热器回收冷量复热成常温的富氧气，这两股富氧气进入分子筛作为再生气。
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