CN210463761U - 带预冷节流氢液化装置 - Google Patents

带预冷节流氢液化装置 Download PDF

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CN210463761U
CN210463761U CN201921590604.0U CN201921590604U CN210463761U CN 210463761 U CN210463761 U CN 210463761U CN 201921590604 U CN201921590604 U CN 201921590604U CN 210463761 U CN210463761 U CN 210463761U
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hydrogen
heat exchanger
liquid nitrogen
precooling
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林定标
陈崇文
陈辉
卓涛涛
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Zhejiang Haichang Gas Co ltd
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Abstract

本实用新型属于制氢设备技术领域，具体涉及一种带预冷节流氢液化装置，包括输送原料氢气的氢液化路线和输送循环氢气的氢循环路线，两条路线分别依次经过一级预冷段、二级预冷段和液化段；一级预冷段设置有换热器一、常压液氮预冷器，二级预冷段设置有换热器二和负压液氮预冷器；氢液化路线经过换热器一、常压液氮预冷器被预冷后，进入换热器二和负压液氮预冷器继续冷却。本实用新型提供的带预冷节流氢液化装置，采用常压液氮预冷器和负压液氮预冷器的二级预冷结构，液化效果更好。

Description

带预冷节流氢液化装置
技术领域
本实用新型属于制氢设备技术领域，具体涉及一种带预冷节流氢液化装置。
背景技术
现有的氢液化设备预冷通常采用单个液氮预冷装置，如公布号CN108469150A的发明专利申请。单个预冷的液化系统原料氢气的液化效果较差，影响制氢效率。
实用新型内容
本实用新型的目的是提供一种带预冷节流氢液化装置，采用常压液氮预冷器和负压液氮预冷器的二级预冷结构，液化效果更好。
本实用新型的目的是这样实现的：一种带预冷节流氢液化装置，包括输送原料氢气的氢液化路线和输送循环氢气的氢循环路线，两条路线分别依次经过一级预冷段、二级预冷段和液化段；一级预冷段设置有换热器一、常压液氮预冷器，二级预冷段设置有换热器二和负压液氮预冷器，液化段设置换热器三和液氢过冷器；氢液化路线经过换热器一、常压液氮预冷器被预冷后，进入换热器二和负压液氮预冷器继续冷却，然后经过换热器三，进入液氢过冷器过冷，最终经节流阀三节流后进入气液分离罐；氢循环路线经过换热器一、常压液氮预冷器被预冷后，进入换热器二和负压液氮预冷器继续冷却；经过二级预冷后的氢循环路线分成两股，第一股分支经节流阀一节流后作为返流氢气再次经过换热器二和换热器一，最后汇合回氢循环路线；第二股分支经过换热器三继续冷却后，经节流阀二后汇入液氢过冷器，用于原料氢气的过冷。
进一步的，所述一级预冷段还设置有吸附器一、吸附器二、正仲氢转换一，氢液化路线经过换热器一、常压液氮预冷器被预冷后，经过吸附器一吸附杂质，再经过正仲氢转换一催化转化，回到常压液氮预冷器再次热交换后进入换热器二；氢循环路线预冷后经过吸附器二吸附杂质后再进入换热器二。
进一步的，所述液化段还包括正仲氢转换二，氢液化路线经过换热器三，进入液氢过冷器过冷后，再经过正仲氢转换二催化转化，回到液氢过冷器过冷后，最终经节流阀三节流后进入气液分离罐。
进一步的，所述气液分离罐、液氢过冷器内气化的氢气经换热器三、换热器二、换热器一后汇入氢循环路线。
进一步的，所述吸附器一和吸附器二为分子筛吸附器。
进一步的，所述常压液氮预冷器的常压管道经过换热器一后连通大气；所述负压液氮预冷器的负压管道经过换热器二和换热器一后连接真空泵。
进一步的，所示吸附器一和吸附器二分别成对运行，一个用于净化，另一个进行再生或处于备用状态。
进一步的，所述氢循环路线上依次经过压缩机一和压缩机二加压，压缩机一连接循环氢气补充口，所述第一股分支经过压缩机二加压后汇入氢循环路线，所述气液分离罐、液氢过冷器内气化的氢气最终经过压缩机一和压缩机二加压后汇入氢循环路线。
本实用新型相比现有技术突出且有益的技术效果是：液化装置先进行两级预冷，然后再进行液化，保证氢液化效果。并在预冷阶段通过分子筛吸附器实现冷却净化步骤，来去除杂质(一氧化碳，二氧化碳，甲烷，惰性气体等)；在预冷段和液化段进行两次催化转化，将正氢转化为仲氢，从而降低流程的不可逆性，增强热效率。
附图说明
图1是本实用新型实施例中带预冷节流氢液化装置的整体原理图。
图2是本实用新型实施例中氢液化路线图。
图3是本实用新型实施例中氢循环路线图。
附图标记：E1、换热器一；E2、换热器二；E3、换热器三；E4、常压液氮预冷器；E5、负压液氮预冷器；E6、液氢过冷器；A1、吸附器一；A2、吸附器二；K1、正仲氢转换一；K2、正仲氢转换二；V1、气液分离罐；V2、液氢储罐；J1、节流阀一；J2、节流阀二；J3、节流阀三；Y1、压缩机一；Y2、压缩机二。
具体实施方式
下面结合附图对本实用新型的具体实施方式作进一步详细说明。
一种带预冷节流氢液化装置，如图1所示，包括输送原料氢气的氢液化路线和输送循环氢气的氢循环路线，两条路线分别依次经过一级预冷段、二级预冷段和液化段。
一级预冷段设置有换热器一E1、常压液氮预冷器E4，以及吸附氢气中杂质的吸附器一A1和吸附器二A2，内装填催化剂的正仲氢转换一K1，常压液氮预冷器E4通过常压管道连通大气，常压管道经过换热器一E1。其中，为了能够提高以及确保正氢变为仲氢的转换效率，正仲氢转换一K1可串联有两个以上。
二级预冷段设置有换热器二E2和负压液氮预冷器E5，负压液氮预冷器E5通过负压管道连接真空泵，使得负压液氮预冷器E5内部保持真空或负压，负压管道经过换热器二E2和换热器一E1。
液化段设置换热器三E3和液氢过冷器E6，以及对原料氢气进行二次催化转化的正仲氢转换二K2，进行气液分离的气液分离罐V1。其中，为了能够提高以及确保正氢变为仲氢的转换效率，正仲氢转换二K2可串联有两个以上。
结合图1和图2，氢液化路线的管线布局具体为：原料氢气→换热器一E1→常压液氮预冷器E4→吸附器一A1→正仲氢转换一K1→常压液氮预冷器E4→换热器二E2→负压液氮预冷器E5→换热器三E3→液氢过冷器E6→正仲氢转换二K2→液氢过冷器E6→节流阀三J3→气液分离罐V1→液氢储罐V2
结合图1和图3，氢循环路线的管线布局具体为：循环氢气→压缩机一Y1→压缩机二Y2→换热器一E1→常压液氮预冷器E4→吸附器二A2→换热器二E2→负压液氮预冷器E5→两股分支
其中，第一股分支→节流阀一J1→换热器二E2→换热器一E1→压缩机二Y2
其中：第二股分支→换热器三E3→液氢过冷器E6
液氢过冷器E6内气化的氢气→换热器三E3→换热器二E2→换热器一E1→压缩机一Y1→压缩机二Y2
气液分离罐V1内的气化氢气→换热器E5→换热器E3→换热器E1→循环氢气
综上，本实施例中液化装置主要包括两大冷却步骤：先经过两级预冷，然后进行液化。在预冷阶段有一个冷却净化步骤来去除杂质(一氧化碳，二氧化碳，甲烷，惰性气体等)，否则杂质可能在氢气液化器的温度下冻结并堵塞换热器，一氧化碳和氮气必须在进入液化段之前去除掉。我们通过安装在一级预冷区的吸附器进行吸附来实现一氧化碳和氮气的脱除。
为了达到满意的净化水平，我们使用分子筛作为吸附剂。吸附器一A1和吸附器二A2均采用两个容器并排运行：其中一个处理要净化的氢气，而另一个进行再生或处于备用状态。设计切换周期大约为吸附8天，再生1.5天。根据设定好的顺序，通过一组阀门来实现吸附器切换，并保持氢气液化稳定运行。
一级预冷阶段：原料氢气和循环氢气首先在换热器一E1中，与返流的氮气和氢气冷却后进入常压液氮预冷器E4内，被预冷至约80K。
二级预冷阶段：经过一级预冷的氢气进入处于真空或负压状态的负压液氮预冷器E5，被液氮继续冷却至约65K-75K。二级预冷后的循环氢气分成2股，一股经过节流阀一J1节流后作为返流氢气对正流氢气进行冷却；另一股和原料氢气进入低温液化段的换热器继续冷却。
液化段：将65K-75K的氢气经过液化段冷却至接近20K-25K进行液化。循环氢气被冷却后经过节流阀二J2节流至常压进入液氢过冷器E6，将原料氢气液化并过冷。液化后的原料氢气节流至常压进入气液分离罐V1，通过气液分离罐V1向用户提供液氢产品；气液分离罐V1气化的氢气与液氢过冷器E6返流的常压循环氢气汇合，与正流氢气通过换热器进行热交换复热至常温，再次进入压缩机一Y1入口。
正仲氢催化转化：为了进行氢气液化，将正氢转化为仲氢很重要。这两种形式的氢气共存，并通过它们的电子自旋方向区分。在各种温度下，这两种氢气的比例都有对应的平衡值。在常温下，正仲氢气的平衡比例大约为75/25，而在低温情况下，大约为2/98。低温情况下，正氢处于不稳定的状态，并逐渐变为更加稳定的仲氢，释放热量并导致氢气在储存容器内蒸发。由于正氢占常温氢气中的75％，它的吸热汽化会大大增加液体氢气的储存难度和成本。这个转化的过程相当缓慢，因此需要催化剂来加速，并需要一些额外的冷量来补偿放热反应释放的热量。工艺管线上，在一级预冷段和液化段换热器或者专门容器内装填催化剂进行两次催化转化。由此在整个流程中分散转化的热量，从而降低流程的不可逆性，并由此增强热效率。
以上所述仅是本实用新型的优选实施方式，应当指出，对于本技术领域的普通技术人员来说，在不脱离本实用新型技术原理的前提下，还可以做出若干改进和替换，这些改进和替换也应视为本实用新型的保护范围。

Claims (8)

1.一种带预冷节流氢液化装置，其特征在于：
包括输送原料氢气的氢液化路线和输送循环氢气的氢循环路线，两条路线分别依次经过一级预冷段、二级预冷段和液化段；
一级预冷段设置有换热器一(E1)、常压液氮预冷器(E4)，二级预冷段设置有换热器二(E2)和负压液氮预冷器(E5)，液化段设置换热器三(E3)和液氢过冷器(E6)；
氢液化路线经过换热器一(E1)、常压液氮预冷器(E4)被预冷后，进入换热器二(E2)和负压液氮预冷器(E5)继续冷却，然后经过换热器三(E3)，进入液氢过冷器(E6)过冷，最终经节流阀三(J3)节流后进入气液分离罐(V1)；
氢循环路线经过换热器一(E1)、常压液氮预冷器(E4)被预冷后，进入换热器二(E2)和负压液氮预冷器(E5)继续冷却；经过二级预冷后的氢循环路线分成两股，第一股分支经节流阀一(J1)节流后作为返流氢气再次经过换热器二(E2)和换热器一(E1)，最后汇合回氢循环路线；第二股分支经过换热器三(E3)继续冷却后，经节流阀二(J2)后汇入液氢过冷器(E6)，用于原料氢气的过冷。
2.根据权利要求1所述的带预冷节流氢液化装置，其特征在于：所述一级预冷段还设置有吸附器一(A1)、吸附器二(A2)、正仲氢转换一(K1)，氢液化路线经过换热器一(E1)、常压液氮预冷器(E4)被预冷后，经过吸附器一(A1)吸附杂质，再经过正仲氢转换一(K1)催化转化，回到常压液氮预冷器(E4)再次热交换后进入换热器二(E2)；氢循环路线预冷后经过吸附器二(A2)吸附杂质后再进入换热器二(E2)。
3.根据权利要求1或2所述的带预冷节流氢液化装置，其特征在于：所述液化段还包括正仲氢转换二(K2)，氢液化路线经过换热器三(E3)，进入液氢过冷器(E6)过冷后，再经过正仲氢转换二(K2)催化转化，回到液氢过冷器(E6)过冷后，最终经节流阀三(J3)节流后进入气液分离罐(V1)。
4.根据权利要求1所述的带预冷节流氢液化装置，其特征在于：所述气液分离罐(V1)、液氢过冷器(E6)内气化的氢气经换热器三(E3)、换热器二(E2)、换热器一(E1)后汇入氢循环路线。
5.根据权利要求2所述的带预冷节流氢液化装置，其特征在于：所述吸附器一(A1)和吸附器二(A2)为分子筛吸附器。
6.根据权利要求1所述的带预冷节流氢液化装置，其特征在于：所述常压液氮预冷器(E4)的常压管道经过换热器一(E1)后连通大气；所述负压液氮预冷器(E5)的负压管道经过换热器二(E2)和换热器一(E1)后连接真空泵。
7.根据权利要求2所述的带预冷节流氢液化装置，其特征在于：所示吸附器一(A1)和吸附器二(A2)分别成对运行，一个用于净化，另一个进行再生或处于备用状态。
8.根据权利要求4所述的带预冷节流氢液化装置，其特征在于：所述氢循环路线上依次经过压缩机一(Y1)和压缩机二(Y2)加压，压缩机一(Y1)连接循环氢气补充口，所述第一股分支经过压缩机二(Y2)加压后汇入氢循环路线，所述气液分离罐(V1)、液氢过冷器(E6)内气化的氢气最终经过压缩机一(Y1)和压缩机二(Y2)加压后汇入氢循环路线。
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CN112212610A (zh) * 2020-09-16 2021-01-12 中国海洋石油集团有限公司 一种lng制备液氢的方法
CN112503852A (zh) * 2020-09-16 2021-03-16 中国海洋石油集团有限公司 一种lng制备氢气和氢气液化的方法

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112212610A (zh) * 2020-09-16 2021-01-12 中国海洋石油集团有限公司 一种lng制备液氢的方法
CN112503852A (zh) * 2020-09-16 2021-03-16 中国海洋石油集团有限公司 一种lng制备氢气和氢气液化的方法
CN112212610B (zh) * 2020-09-16 2022-04-19 中国海洋石油集团有限公司 一种lng制备液氢的方法

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