CN210688920U - 一种从天然气中浓缩氦气的系统 - Google Patents

一种从天然气中浓缩氦气的系统 Download PDF

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CN210688920U
CN210688920U CN201921074722.6U CN201921074722U CN210688920U CN 210688920 U CN210688920 U CN 210688920U CN 201921074722 U CN201921074722 U CN 201921074722U CN 210688920 U CN210688920 U CN 210688920U
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郝文炳
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Shanghai Lianfeng Energy Technology Co ltd
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Abstract

本实用新型公开了一种从天然气中浓缩氦气的系统，该系统包括：空气膨胀机、冷却器、冷箱、主换热器、空气再沸器、LNG再沸器、精馏塔、过冷器、冷凝蒸发器等。主要针对含有氦气的原料气中又富含氢气的特点，使用空气膨胀工艺，提供一种低温精馏环境下同时浓缩氦气与氢气的方法。本实用新型提供的从天然气中浓缩氦气的系统，流程设计合理，操作简单，氦气的提取率高，解决了含氢气原料的浓缩问题。

Description

一种从天然气中浓缩氦气的系统
技术领域
本实用新型涉及氦气浓缩技术领域，尤其涉及一种从天然气中浓缩氦气的系统。
背景技术
氦气是一种战略性物质，在航天、国防、医疗和检漏等领域具有非常重要的作用。氦气是惰性气体，其在空气中的含量仅为5.24×10-6。氦气在空分设备精馏塔内为不凝气，而以气态聚集在主冷凝器顶部和氮回流液中。不易被分离。氦气主要存在于天然气中，从天然气中提取氦气，是氦气生产的主要来源。但中国天然气中的氦含量极少，而液化天然气的闪蒸气(BOG)或其它以天然气为原料的化工尾气中富含氦，从中提取的经济价值更高。但部分BOG气体中会含有少量氢气，使用深冷法分离氦气与氢气的能耗较高，会使氦气的经济价值下降。
现有技术中，专利号CN207456020U《一种LNG闪蒸气的提氦、脱氮和再液化装置》中，流程组织中不涉及氢气，对于有氢气的原料气体，此装置不具备浓缩条件。以及现有技术中，专利号CN208042611U《从天然气中提氦并液化的装置》，使用双塔，操作复杂，并且也无法分离氦气中的氢气。因此，本领域的技术人员致力于开发一种可以浓缩原料中含有微量氢气的方法。
实用新型内容
本实用新型的目的是针对含有氦气的原料气中又富含氢气的特点，使用空气膨胀工艺，提供一种低温精馏环境下从天然气中浓缩氦气的系统。
为实现上述目的，本实用新型采用以下技术方案：
本实用新型提供一种从天然气中浓缩氦气的系统，包括空气膨胀机、主换热器、空气再沸器、LNG再沸器、精馏塔、过冷器和冷凝蒸发器，其中：
所述空气膨胀机通过管道经所述主换热器连接所述空气再沸器，所述LNG 再沸器设置于所述精馏塔的塔底，所述精馏塔的塔底通过管道连通所述空气再沸器的中上部，所述空气再沸器的顶部通过管道连通所述精馏塔的中下部；天然气原料通过管道经所述主换热器降温至部分带液后送入所述精馏塔塔底，被所述 LNG再沸器内的LNG液体进一步降温后通过管道经调压后送入所述精馏塔中部参与精馏；以及
所述精馏塔的顶部通过管道经所述冷凝蒸发器连接所述主换热器，用于将精馏后的轻组分送入所述冷凝蒸发器进行液化，含氦气的不凝气从所述冷凝蒸发器顶部依次通过管道经所述过冷器和所述主换热器复热后排出。
进一步地，所述的从天然气中浓缩氦气的系统，还包括：
冷箱，所述主换热器、空气再沸器、LNG再沸器、精馏塔、过冷器和冷凝蒸发器均设置于所述冷箱内。
进一步地，所述的从天然气中浓缩氦气的系统，还包括：
设置于所述空气膨胀机与所述主换热器之间管道上的冷却器，用于对所述空气膨胀机压缩后的空气进行预降温处理。
进一步地，所述的从天然气中浓缩氦气的系统，还包括：
设置于所述LNG再沸器与所述精馏塔中部之间管道上的LNG节流阀；和
设置于所述过冷器与所述冷凝蒸发器之间管道上的液空节流阀。
进一步地，所述精馏塔底部通过管道连接所述主换热器，用于将精馏后的重组分经所述主换热器复热后排出。
本实用新型采用上述技术方案，与现有技术相比，具有如下技术效果：
本实用新型提供的从天然气中浓缩氦气的系统，针对含有氦气的原料气中又富含氢气的特点，使用空气膨胀工艺，在低温精馏环境下同时浓缩氦气与氢气；且原料中的氦气大部分(>95％)都在提纯后的不凝气中，为下一步提纯创造条件；本实用新型提供的浓缩氦气的系统，流程设计合理，操作简单，氦气的提取率高，解决了含氢气原料的浓缩问题。
附图说明
图1为本实用新型一种天然气中浓缩氦气的系统的流程示意图；
1-空气膨胀机，2-冷却器，3-冷箱，E1-主换热器，K1-空气再沸器，K2-LNG 再沸器，C1-精馏塔，E2-过冷器，K3-冷凝蒸发器，V1-液空节流阀、V2-LNG节流阀。
具体实施方式
下面通过具体实施例对本实用新型进行详细和具体的介绍，以使更好的理解本实用新型，但是下述实施例并不限制本实用新型范围。
实施例1
如图1所示，本实施例提供一种从天然气中浓缩氦气的系统，包括空气膨胀机1、主换热器E1、空气再沸器K1、LNG再沸器K2、精馏塔C1、过冷器E2 和冷凝蒸发器K3。
所述空气膨胀机1通过管道经所述主换热器E1连接所述空气再沸器K1，用于对去除水和二氧化碳后的空气进行压缩处理，并将所述压缩后的空气经所述主换热器E1降温后，从所述主换热器E1中部抽出送入所述空气再沸器K1，以加热所述空气再沸器K1内的LNG液体。
所述空气再沸器K1通过管道连接所述主换热器E1，以将加热所述LNG液体后的降温的空气送入所述主换热器E1进行进一步降温，所述进一步降温的空气分为两部分，一部分降温后的空气在所述主换热器E1内被液化后通过管道送入所述过冷器E2进行过冷降温，另一部分所述进一步降温的空气从所述主换热器E1中下部抽出通过管道连通所述空气膨胀机1，以送入所述空气膨胀机1的膨胀端进行膨胀升温，膨胀升温后的空气再通过管道送入所述主换热器E1的冷端作为冷源，复热后排出。
所述过冷器E2通过管道连接所述冷凝蒸发器K3，用于将所述过冷降温后的液化空气送入所述冷凝蒸发器K3内进行蒸发处理，被汽化后的空气通过管道送入所述过冷器E2回收冷量，再通过管道送入所述主换热器E1经复热后排出。
所述LNG再沸器K2设置于所述精馏塔C1的塔底，所述精馏塔C1的塔底通过管道连通所述空气再沸器K1的中上部，所述空气再沸器K1的顶部通过管道连通所述精馏塔C1的中下部；天然气原料通过管道经所述主换热器E1降温至部分带液后送入所述精馏塔C1塔底，被所述LNG再沸器K2内的LNG液体进一步降温后通过管道经调压后送入所述精馏塔C1中部参与精馏。
所述精馏塔C1底部通过管道连接所述主换热器E1，用于将精馏后的重组分经所述主换热器E1复热后排出；所述精馏塔C1的顶部通过管道经所述冷凝蒸发器K3连接所述主换热器E1，用于将精馏后的轻组分送入所述冷凝蒸发器K3 进行液化，含氦气的不凝气从所述冷凝蒸发器K3顶部依次通过管道经所述过冷器E2和所述主换热器E1复热后排出。
如图1所示，在本实施例中，该从天然气中浓缩氦气的系统，还包括冷箱3，所述主换热器E1、空气再沸器K1、LNG再沸器K2、精馏塔C1、过冷器E2和冷凝蒸发器K3均设置于所述冷箱3内。
如图1所示，在本实施例中，该从天然气中浓缩氦气的系统还包括：设置于所述空气膨胀机1与所述主换热器E1之间管道上的冷却器2，用于对所述空气膨胀机1压缩后的空气进行预降温处理。以及还包括：设置于所述LNG再沸器 K2与所述精馏塔C1中部之间管道上的LNG节流阀V2；和设置于所述过冷器 E2与所述冷凝蒸发器K3之间管道上的液空节流阀V1。
在本实施例中，所述天然气原料为带压力的天然气原料，且组分为：He： 1.7％，H2:0.26％，N2:10.3％，CH4：余量；所述含氦气的不凝气的组分为：He:19.4％， H2:2.9％，N2余量。原料中的氦气大部分都在不凝气中，为下一步提纯创造条件。
实施例2
本实施例提供一种基于上述实施例1所示系统的从天然气中浓缩氦气的方法，具体包括如下步骤：
空气经过压缩、预冷纯化(空气的压缩、预冷纯化为现在空分中常规技术，本方法中不再叙述)，去除水和二氧化塔后，压力为～0.7MPaA(为绝压，下同)，流量为4800Nm3/h，温度为10～20℃，经由GA-101进入1空气膨胀机增压端的进口，被增压至0.9～1MPaA后，进入2冷却器冷却降温至40℃，经GA-103进入冷箱。空气首先进入E1主换热器降温，至-107～-109℃从主换热器中部抽出后，送入K1空气再沸器，利用空气的热量为加热K1空气再沸器中的LNG液体，空气被降温至-133～-135℃后，进入E1主换热器中部进一步降温。从E1主换热器中下部，抽出流量为～4100Nm3/h空气温度为-140℃～-145℃，送入1膨胀机膨胀端膨胀至压力0.13MPaA，空气本身温度降低至-189℃，被送回E1主换热器冷端，作为冷源，复热至～17℃出冷箱放空或循环利用。另流量为～700Nm3/h 的空气，从在E1主换热器冷端被液化后，由LA-106进入E2过冷器，进一步过冷降温至-173～-178℃，在LA107经过节流阀V1调节压力至0.2～0.3MpaA后由LA107送入K3冷凝蒸发器。液空在K3冷凝蒸发器中被蒸发汽化为空气，吸收热量。由GA-108汽化后的空气进入E2过冷器回收冷量，再送入E1主换热器复热出冷箱。通过GA-110放空或循环使用。
带压力的天然气原料(组分：He：1.7％，H2:0.26％，N2:10.3％，CH4：其余)进入冷箱，流量为2500Nm3/h，压力为1.2MPa首先进入E1主换热器被降温 -122～-124℃，部分带液后，由GNG-301抽出送入C1精馏塔底部的K2.LNG再沸器中对另一侧的LNG液体加热，本身被进一步液化后由LNG-302出K2.LNG 再沸器，温度降至-134～-135℃，由LNG-302通过节流阀V2调节压力至比塔压略高0.6MpaA后送入C1精馏塔中部参与精馏。在C1精馏塔内，有多块塔板或者填料，以供各组分在上面精馏，重组分(主要为CH4)在塔底积聚，塔底甲烷浓度可达>97％)。设置于塔底的K1空气再沸器和K2 LNG再沸器加热塔底液体，重组分以气体形式从塔底部通过GNG-303抽出，压力为0.56MpaA，经过 E1主换热器复热回收冷量后，送出3冷箱，送给用户。本实施例中精馏塔底部压力为0.56MPaA，塔底温度为：-135.6℃，与两个再沸器保持温差。塔顶压力为0.55MpaA，塔顶温度为～-181.6℃。
轻组分(主要为氮气、氦气、氢气)在C1精馏塔顶部聚集，由GN-404送入K301冷凝蒸发器中液化，部分不凝气从K3冷凝蒸发器顶部抽出。本案例中，不凝气的组分为：He:19.4％,H2:2.9％,N2：其余。流量为：218Nm3/h。被液化的液体流回C1精馏塔内，为精馏提供液体。不凝气由GN-402通过E2过冷器后，再送入E1主换热器回收冷量，被复热的常温后送出3冷箱。原料中的氦气大部分(>95％)都在不凝气中，为下一步提纯创造条件。
以上对本实用新型的具体实施例进行了详细描述，但其只是作为范例，本实用新型并不限制于以上描述的具体实施例。对于本领域技术人员而言，任何对本实用新型进行的等同修改和替代也都在本实用新型的范畴之中。因此，在不脱离本实用新型的精神和范围下所作的均等变换和修改，都应涵盖在本实用新型的范围内。

Claims (5)

1.一种从天然气中浓缩氦气的系统，其特征在于，包括空气膨胀机(1)、主换热器(E1)、空气再沸器(K1)、LNG再沸器(K2)、精馏塔(C1)、过冷器(E2)和冷凝蒸发器(K3)，其中：
所述空气膨胀机(1)通过管道经所述主换热器(E1)连接所述空气再沸器(K1)；
所述LNG再沸器(K2)设置于所述精馏塔(C1)的塔底，所述精馏塔(C1)的塔底通过管道连通所述空气再沸器(K1)的中上部，所述空气再沸器(K1)的顶部通过管道连通所述精馏塔(C1)的中下部；天然气原料通过管道经所述主换热器(E1)降温至部分带液后送入所述精馏塔(C1)塔底，被所述LNG再沸器(K2)内的LNG液体进一步降温后通过管道经调压后送入所述精馏塔(C1)中部参与精馏；以及
所述精馏塔(C1)的顶部通过管道经所述冷凝蒸发器(K3)连接所述主换热器(E1)，用于将精馏后的轻组分送入所述冷凝蒸发器(K3)进行液化，含氦气的不凝气从所述冷凝蒸发器(K3)顶部依次通过管道经所述过冷器(E2)和所述主换热器(E1)复热后排出。
2.根据权利要求1所述的从天然气中浓缩氦气的系统，其特征在于，还包括：
冷箱(3)，所述主换热器(E1)、空气再沸器(K1)、LNG再沸器(K2)、精馏塔(C1)、过冷器(E2)和冷凝蒸发器(K3)均设置于所述冷箱(3)内。
3.根据权利要求1所述的从天然气中浓缩氦气的系统，其特征在于，还包括：
设置于所述空气膨胀机(1)与所述主换热器(E1)之间管道上的冷却器(2)，用于对所述空气膨胀机(1)压缩后的空气进行预降温处理。
4.根据权利要求1所述的从天然气中浓缩氦气的系统，其特征在于，还包括：
设置于所述LNG再沸器(K2)与所述精馏塔(C1)中部之间管道上的LNG节流阀(V2)；和
设置于所述过冷器(E2)与所述冷凝蒸发器(K3)之间管道上的液空节流阀(V1)。
5.根据权利要求1所述的从天然气中浓缩氦气的系统，其特征在于，所述精馏塔(C1)底部通过管道连接所述主换热器(E1)，用于将精馏后的重组分经所述主换热器(E1)复热后排出。
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