CN210892360U - 一种从天然气中提取氦气的装置 - Google Patents

一种从天然气中提取氦气的装置 Download PDF

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CN210892360U
CN210892360U CN201921299770.5U CN201921299770U CN210892360U CN 210892360 U CN210892360 U CN 210892360U CN 201921299770 U CN201921299770 U CN 201921299770U CN 210892360 U CN210892360 U CN 210892360U
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heat exchanger
natural gas
nitrogen
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helium
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任小坤
孙立佳
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Beijing Hengtai Jieneng Technology Co ltd
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Abstract

本实用新型涉及一种从天然气中提取氦气的装置，包括PSA单元、压缩机及位于冷箱内的深冷分离单元和制冷单元；所述PSA单元具有与外部管网连接的天然气入口和输出提浓后天然气的天然气送出口，所述PSA单元与下级压缩机联通，所述压缩机进入冷箱后依次联通初级换热器、精馏塔的塔底，塔底再依次联通初级换热器、节流阀和精馏塔；精馏后液相依次流经塔底的冷凝液出口、初级换热器、天然气送出口后并入天然气管网；精馏后气相依次流经深冷换热器、分离器进行分离，分离器底部的液氮通过节流阀节流降温至‑200℃后给内纯化器降温，后经富氮气出口排出；具有能耗低、氦气回收率高、投资省、操作灵活、变工况适应能力强等特征。

Description

一种从天然气中提取氦气的装置
技术领域
本实用新型涉及气体分离装置领域，具体是一种从天然气中提取氦气的装置。
背景技术
氦气的特殊性质之一是其沸点约为－269℃，是已知的沸点最低的物质。此外氦气还具有比热大、导热率高的特点，可用于冷却用途。比如，在光纤制造工序中，可用于冷却熔融成型的玻璃，在半导体制造的溅射工序中，可用于冷却高温的硅晶圆。而且，在利用超导线圈的MRI(核磁共振成像)设备及MEG(脑磁仪)等医疗设备中，氦气也不可或缺。另外，氦气的分子量较小，而且与氢气不同，具有惰性，十分稳定，因此填充到气球中也很安全。此外其分子直径也很小，因此还广泛用于气密性检查方面的用途。
如果仅以冷却为目的，可用氮气替代氦气，如果仅作为惰性气体利用，可用氩气代替。不过，在利用氦气多种特性的光纤及半导体制造等用途中，却很难有其他替代原料。
氦气通常是从含量比例较高的天然气中提取。虽然天然气田为数众多，但能开采出氦气的气田没有大幅增加的倾向。原因是，能够以合算的成本提取氦的气田有限。最近大力开采的页岩气田也无法提取氦气。
我国主要含油气盆地的含氦天然气资料显示，氦气分布广泛，层位众多，但研究程度低。目前，已知渭河、四川、塔里木、柴达木、松辽、渤海湾、苏北、海拉尔等8 个盆地发现有含氦天然气显示。总体而言，西部大型叠合盆地、东部郯庐断裂带具有氦 气资源前景。四川盆地威远气田是我国首个实现氦气商业化利用的气田，也是目前我国 唯一进行工业开采的氦气田。
天然气提氦工艺有深冷法与非深冷工艺之分，深冷工艺仍是工业化的主要选择方法。非低温法主要采用膜分离和变压吸附。我国研究的膜分离技术采用国产聚砜/硅橡 胶中空纤维膜，常温下经一级膜分离可使氦浓缩5～5.5倍,氦收率达到63～75％。但该 工艺技术还没工业化，同时膜的可靠性和稳定还需进一步研究证明。
低温法中，现有的外部制冷工艺虽可联产LNG，但能耗高，而前膨胀制冷工艺， 提氦塔操作压力较低，操作温度低(最低-192C°)，对塔体材质要求高，在到达相同氦气 浓度的情况下，冷量需求大，能耗高。
实用新型内容
本实用新型所要解决的技术问题是提供一种从天然气中提取氦气的装置，以解决现有技术中存在的缺陷。
本实用新型解决上述技术问题的技术方案如下：
一种从天然气中提取氦气的装置，包括PSA单元、压缩机及位于冷箱内的深冷分离单元和制冷单元；所述PSA单元具有与外部管网连接的天然气入口和输出提浓后天然气的天然气送出口，所述PSA单元与下级压缩机联通，所述压缩机进入冷箱后依次联通初级换热器、精馏塔的塔底，所述精馏塔的塔底再依次联通初级换热器、节流阀和精馏塔；精馏后液相依次流经塔底的冷凝液出口、初级换热器、天然气送出口后并入天然气管网；精馏后气相依次流经深冷换热器、分离器进行分离，分离器底部的液氮通过节流阀节流降温至-200℃后给内纯化器降温，后经富氮气出口排出；分离器顶部的氦气依次流经内纯化器、深冷换热器、初级换热器后通过高纯氦出口排出；
进一步的，所述压缩机选用膜压机、活塞压缩机和螺杆压缩机中的一种；
进一步的，所述冷箱包括提供深冷分离所需冷量的制冷单元，所述制冷单元采用氮膨胀剂冷循环；
进一步的，所述制冷单元包括与初级换热器连接的氮气压缩机，氮气经压缩升压至2.6所述初级换热器的MPa后进入初级换热器降温至-70到 -55℃，一部分氮气进入高温膨胀机膨胀至0.2到0.4MPa，降温至-120到 -110℃进入初级换热器；另一部分氮气进入深冷换热器进一步降温后至-130 到120℃，进入低温膨胀机胀至0.2到0.4MPa，降温至-200到-190℃进入深冷换热器量，提供冷量后的低压氮气经过初级换热器复温至常温后回到氮气压缩机入口；
本实用新型的有益效果是：含有少量氦气的天然气先经过PSA装置预提浓，提浓后的天然气再回到管网送出，提浓后的富氦气压缩后进入冷箱深冷分离及低温纯化获得高纯氦，分离出的高压LNG经复温回收冷量后并入管网。低温冷凝下的富氮液体节流后给内纯化器提供冷量。该工艺具有能耗低、氦气回收率高、投资省、操作灵活、变工况适应能力强等特征。
附图说明
图1为本实用新型结构示意图；
附图标记说明如下：
1、PSA单元，2、压缩机，3、冷箱，5、天然气入口，6、天然气送出口， 7、初级换热器，8、精馏塔，9、节流阀，10、深冷换热器，11、分离器， 12、内纯化器，13、富氮气出口，14、高纯氦出口，15、氮气压缩机，16、高温膨胀机，17、低温膨胀机；
具体实施方式
以下结合附图对本实用新型的原理和特征进行描述，所举实例只用于解释本实用新型，并非用于限定本实用新型的范围。
如图1所示，一种从天然气中提取氦气的装置，包括PSA单元1、压缩机2及位于冷箱3内的深冷分离单元和制冷单元；所述PSA单元1具有与外部管网连接的天然气入口5和输出提浓后天然气的天然气送出口6，所述PSA 单元1与下级压缩机2联通，所述压缩机2进入冷箱3后依次联通初级换热器7、精馏塔8的塔底，所述精馏塔8的塔底再依次联通初级换热器、节流阀9和精馏塔8；精馏后液相依次流经塔底的冷凝液出口、初级换热器7、天然气送出口6后并入天然气管网；精馏后气相依次流经深冷换热器10、分离器11进行分离，分离器11底部的液氮通过节流阀节流降温至-200℃后给内纯化器12降温，后经富氮气出口13排出；分离器11顶部的氦气依次流经内纯化器、深冷换热器、初级换热器后通过高纯氦出口14排出；
具体实施时，含有少量氦气的天然气压力5.0MPa，温度常温，先经过 PSA装置将氦气预提浓至10-15％，压力为5.0MPa的提浓后天然气再回到管网送出，提浓后的富氦气压力为0.2MPa,温度40℃，氦气含量10-15％，经过压缩机压缩至6.0MPa后进入冷箱。
在一个具体实施例中，所述压缩机2选用膜压机、活塞压缩机和螺杆压缩机中的一种；
预提浓的含氦天然气经过初级换热器降温至-60℃后进入精馏塔塔底再沸器进一步冷却至-85到-95℃后回到初级换热器降温至-105到-100℃后，经过节流阀减压至5.2到5.4MPa进入精馏塔精馏。其中液相向下流向塔底，通过再沸器加热蒸发出携带的少量氮气、氦气后从冷凝液出口流出，得到压力为5.1到5.2MPa，温度为-145℃左右，甲烷浓度≥96％的LNG，该LNG通过换热器复温至常温并入天然气管网。
精馏塔顶部压力为4.9到5.0MPa，温度为-160到-155℃的粗氦，进入深冷换热器进行进一步冷却降温至-200到-195℃的，粗氦中的氮气及少量氢气冷凝成液体通过分离器进一步分离，分离器底部的液氮通过节流阀节流降温至-200℃后给内纯化器降温，保持内纯化器的低温运行。
分离器底部的氦气进入内纯化器，通过活性炭吸附其中少量的氮气、氢气等杂质，制得纯度>99.999％的高纯氦；高纯氦再回到换热器复温后送出。
在一个具体实施例中，所述冷箱3包括提供深冷分离所需冷量的制冷单元，所述制冷单元采用氮膨胀剂冷循环；
更具体的，所述制冷单元包括与初级换热器连接的氮气压缩15机，氮气经压缩升压至2.6MPa后进入初级换热器降温至-70到-55℃，一部分氮气进入高温膨胀机16膨胀至0.2到0.4MPa，降温至-120到-110℃进入初级换热器；另一部分氮气进入深冷换热器进一步降温后至-130到120℃，进入低温膨胀机17胀至0.2到0.4MPa，降温至-200到-190℃进入深冷换热器量，提供冷量后的低压氮气经过初级换热器复温至常温后回到氮气压缩机入口；
以上所述仅为本实用新型的较佳实施例，并不用以限制本实用新型，凡在本实用新型的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本实用新型的保护范围之内。

Claims (4)

1.一种从天然气中提取氦气的装置，其特征在于：包括PSA单元、压缩机及位于冷箱内的深冷分离单元和制冷单元；所述PSA单元具有与外部管网连接的天然气入口和输出提浓后天然气的天然气送出口，所述PSA单元与下级压缩机联通，所述压缩机进入冷箱后依次联通初级换热器、精馏塔的塔底，所述精馏塔的塔底再依次联通初级换热器、节流阀和精馏塔；精馏后液相依次流经塔底的冷凝液出口、初级换热器、天然气送出口后并入天然气管网；精馏后气相依次流经深冷换热器、分离器进行分离，分离器底部的液氮通过节流阀节流降温至-200℃后给内纯化器降温，后经富氮气出口排出；分离器顶部的氦气依次流经内纯化器、深冷换热器、初级换热器后通过高纯氦出口排出。
2.根据权利要求1所述的一种从天然气中提取氦气的装置，其特征在于：所述压缩机选用膜压机、活塞压缩机和螺杆压缩机中的一种。
3.根据权利要求2所述的一种从天然气中提取氦气的装置，其特征在于：所述冷箱包括提供深冷分离所需冷量的制冷单元，所述制冷单元采用氮膨胀剂冷循环。
4.根据权利要求3所述的一种从天然气中提取氦气的装置，其特征在于：所述制冷单元包括与初级换热器连接的氮气压缩机，氮气经压缩升压至2.6MPa后进入初级换热器降温至-70到-55℃，一部分氮气进入高温膨胀机膨胀至0.2到0.4MPa，降温至-120到-110℃进入初级换热器；另一部分氮气进入深冷换热器进一步降温后至-130到120℃，进入低温膨胀机胀至0.2到0.4MPa，降温至-200到-190℃进入深冷换热器量，提供冷量后的低压氮气经过初级换热器复温至常温后回到氮气压缩机入口。
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111928574A (zh) * 2020-07-27 2020-11-13 合肥万豪能源设备有限责任公司 一种氦气回收系统及方法
CN111981767A (zh) * 2020-08-20 2020-11-24 中国石油工程建设有限公司 一种天然气单塔深冷提氦装置和方法

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111928574A (zh) * 2020-07-27 2020-11-13 合肥万豪能源设备有限责任公司 一种氦气回收系统及方法
CN111981767A (zh) * 2020-08-20 2020-11-24 中国石油工程建设有限公司 一种天然气单塔深冷提氦装置和方法
CN111981767B (zh) * 2020-08-20 2024-03-08 中国石油工程建设有限公司 一种天然气单塔深冷提氦装置和方法

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