CN104990366A - 一种从空分装置液氮中提取粗氖氦产品的方法 - Google Patents
一种从空分装置液氮中提取粗氖氦产品的方法 Download PDFInfo
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Abstract
本发明公开了一种从空分装置液氮中提取粗氖氦产品的工艺方法,采用此种方法后可使空分装置生产粗氖氦产品。采用本发明的工艺,具有工艺简单易操作控制,氖氦组分提取率高的特点,其中重要的氖组分提取率不低于81%,适合工业生产的需求。
Description
技术领域
能源、化工、空气分离、低温设备领域。
背景技术
稀有气体是一般指氩、氖、氦、氪、氙五种气体。除了氦主要由天然气提取外,空气是这些稀有气体的主要来源。随着国民经济的发展,稀有气体的应有越来越广泛,需求也越来越大,从空气中回收稀有气体显露出极高的经济价值。
目前氖氦粗制气的提取主要通过大型空分中所带的氖氦粗制装置实现。这种制取方法必须在空分下塔顶部安装一段精馏塔板,如若建设初期没安装这段塔板则不能够通过这种方法制取粗氖氦气,而且在下塔加装的这段塔板上气液比和下塔其他部分相比有很大差别,稍有设计偏差和操作偏差容易造成整个空分工况的不稳定。因此,设计操作难度高,投资大,产量受空分规模的限制,难适应现代化企业对氖氦越来越大的需求。
本方法可在不增加空分下塔塔板的前提下提取粗氖氦气,既适用于新有空分的建设也适用于原有未带氖氦粗制装置的空分改造。
发明内容
本发明所要解决的技术问题是提供一种从空分装置液氮中提取粗氖氦产品的方法,该方法可用于新上空分装置也可用于原有空分装置改造。该方法具备投资及占用空间都比较小且适用性强的特点。
本发明提供的技术方案是:
从空分装置液氮中提取粗氖氦产品的方法,同时进行以下作业流程:
a、将粗氖氦塔冷凝器、粗氖氦塔、粗氖氦塔蒸发器自上而下依次固定布置,粗氖氦塔冷凝器吸收腔通过管路与粗氖氦塔他顶部连通,粗氖氦塔蒸发器与粗氖氦塔底部连通。然后同时进行后续作业流程;
b、空分主冷凝蒸发器吸收腔产生的液氮分为两路,一路进下塔顶部,另一路从的中部送入粗氖氦塔精馏;放出冷量的液氮(氖氦组分从液氮中蒸发)从粗氖氦塔蒸发器通过连接管路输入过冷器吸收冷量后分为两路,一路输入上塔中部精馏,另一路降压后输入粗氖氦塔冷凝器再次释放冷量,变成气相后输入上塔顶部低压氮气管路;
c、粗氖氦塔顶部气体输入粗氖氦塔冷凝器吸收腔吸收冷量后得到气液相混合物,其中液相部分输回粗氖氦塔顶部,气相部分作为产品粗氖氦气输出系统;
d、中压气液临界点的空气(或氮气)进入粗氖氦塔蒸发器吸收腔吸收冷量后转换为液态后输入上塔的液空(或液氮)管线;
粗氖氦塔冷凝器内液氮的蒸发温度低于吸收腔内氮气(富含氖氦组分)的液化温度,通过控制液氮的压力和氮气(富含氖氦组分)的压力实现,粗氖氦塔蒸发器内空气的液化温度高于液氮的蒸发温度,通过控制空气和液氮的压力实现。
本发明的工作原理是:
1、空气中的氖含量为18ppm,氦含量为5.2ppm。在空分下塔实现氧氮分离的过程中,空气中微量的氖氦都浓缩在液氮中(含氖50ppm左右)进入空分上塔,然后随氮气产品输出系统,加入粗氖氦塔后,使主冷凝蒸发器产生的液氮先经过粗氖氦塔精馏提取其中的氖氦成分,再将取出了氖氦组分的液氮送入上塔继续参加精馏。
2、通过控制输入粗氖氦塔内的液氮压力以及输入粗氖氦塔蒸发器的中压气液临界点的空气(或氮气)压力,保证两种物流存在温差(例如:液氮压力为0.557MPa(A)时,蒸发温度为-177.8℃;中压空气为0.562MPa(A)时,冷暖温度为-171.8℃,两者存在温差6℃)。这样,中压空气(或氮气)的冷凝和液氮的蒸发可同时进行。
3、由于输入粗氖氦塔冷凝器液氮的压力低,而粗氖氦塔内氮气(富含氖氦组分)压力高,所以可以控制两种物流的压力来保证温差(例如:液氮压力为0.131MPa(A)时,蒸发温度为-193.5℃;氮气(富含氖氦组分)压力为0.48MPa(A)时,冷凝温度为-188.3℃,两者存在温差5.2℃)。这样,液氮的蒸发和氮气(富含氖氦组分)冷凝可同时进行。
4、在粗氖氦塔中,上升蒸发气与下流冷凝液产生热交换,不断的热交换使顶部气体中的氖氦浓缩,从而得到氖氦总含量为45%~50%左右的粗氖氦气。
本发明的有益效果是:
首先,本方法能从空分下塔产生的液氮中提取粗氖氦气,无需对空分主流路进行更改,可用于新建空分项目也可应用于原有空分改造,应用范围广而且投资小,流程效率高,大大降低了粗氖氦气的生产门槛。其次,粗氖氦气产量高,整套空分中氖的提取率达81%左右,粗氖氦塔中氖提取率达95%左右。第三,具有低温精馏方法的一切优点,而无技术背景所述的原方法的局限。
附图说明
图1是《不提取粗氖氦的空分流程示意图》。其中:C1为下塔,C2为上塔,K1为主冷凝蒸发器,K2为过冷器。图2是《空分液氮中提取粗氖氦的流程图》。其中:C1为上塔,C2为下塔,C3为粗氖氦塔,K1为主冷凝蒸发器,K2为粗氖氦塔冷凝器,K3为粗氖氦塔蒸发器,G1为主冷凝蒸发器吸收腔,G2为粗氖氦塔冷凝器吸收腔,G3为粗氖氦塔蒸发器吸收腔,E1为过冷器。
具体实施方式
本发明具有以下特点:
1、从液氮中分离出产品粗氖氦气
氧氮分离中,氖氦为轻组分存在于氮产品中,本发明用主冷凝蒸发器产生的液氮作为原料,将原料中的氖氦与氮组分进行分离;
2、具有充足的热源冷源
如前所述,粗氖氦塔的热源及冷源都可采用来自原空分内的流路,分别被冷凝和蒸发后再次进入原空分参与精馏,其冷源和热源的量不受约束,能够充分满足粗氖氦塔的精馏需要,从而提高粗氖氦塔的粗氖氦提取率。
以下通过实施例进一步说明。
实施例:
a、从主冷凝蒸发器吸收腔G1引出的液氮流入1号管路后分为两股,一股通过2号管路进下塔,一股通过3号管路作为原料气进入粗氖氦塔C3中部精馏,在G2粗氖氦塔冷凝器吸收腔的中通过4号管路取出粗氖氦产品,K3粗氖氦塔蒸发器底部液氮通过5号管路进入过冷器E1中过冷后分成两股,一股通过6号管路降压后进入K2粗氖氦塔冷凝器释放冷量,一股通过7号管路降压后进入上塔参与精馏;
b、气液临界点的空气大部分通过10号管路进入下塔参与精馏,另外一小部分通过11号管路进入G3粗氖氦塔蒸发器吸收腔做吸收冷量,液化后的液空通过12号管路降压后并入上塔中部参与精馏;
c、K2粗氖氦塔冷凝器的顶端输出口还通过13号管路连接上塔顶部氮气输出管线。
粗氖氦塔冷凝器K2、粗氖氦塔C3、粗氖氦塔蒸发器K3从上到下依次布置,粗氖氦塔冷凝器内液氮的蒸发温度低于含氖氦组分的氮气的液化温度,通过控制液氮的压力和含氖氦组分的氮气的压力实现,粗氖氦塔蒸发器内空气的液化温度高于液氮的蒸发温度,通过控制空气和液氮的压力实现。
所述粗氖氦塔C3的结构与化工设备的精馏塔结构相同;精馏元件可采用填料+分布器,也可采用筛板结构,或填料、筛板的组合塔结构;上述设备以及元件、部件可全部外购或自制。
说述粗氖氦塔冷凝器K2和粗氖氦塔蒸发器K3可根据传热温差的需要,采用板翅式换热器或管式换热器结构;也可外购或自制。
以上所述的所有管路均分别安装有调节管路内介质压力的控制阀门(常规结构阀门,可外购获得)。
本实施例工作流程如下:
主冷凝蒸发器吸收腔G1中温度为-177.8℃的液氮中作为原料进入粗氖氦塔C3的中部参与精馏,在粗氖氦塔蒸发器吸收腔G3中,通过11号管路输入的临界温度为-171.8℃的空气将粗氖氦塔蒸发器K3中的液氮蒸发,在粗氖氦塔冷凝器K2中,通过6号管路输入过冷并节流降压的低温液氮,将粗氖氦塔冷凝器G2中的含氖氦组分的氮气液化,在粗氖氦塔C3中,上升蒸发气与下流冷凝液产生热交换,不断的热交换使顶部气体中的氖氦浓缩,从而得到氖氦总含量为45%~50%左右的粗氖氦气。
流程特点:
本流程从液氮中分离出粗氖氦产品。
Claims (1)
1.一种从空分装置液氮中提取粗氖氦产品的方法,其特征是:
a、将粗氖氦塔冷凝器、粗氖氦塔、粗氖氦塔蒸发器自上而下依次固定布置,粗氖氦塔冷凝器吸收腔通过管路与粗氖氦塔他顶部连通,粗氖氦塔蒸发器与粗氖氦塔底部连通,然后同时进行后续作业流程;
b、空分主冷凝蒸发器吸收腔产生的液氮分为两路,一路进下塔顶部,另一路从的中部送入粗氖氦塔精馏;放出冷量的液氮(氖氦组分从液氮中蒸发)从粗氖氦塔蒸发器通过连接管路输入过冷器吸收冷量后分为两路,一路输入上塔中部精馏,另一路降压后输入粗氖氦塔冷凝器再次释放冷量,变成气相后输入上塔顶部低压氮气管路;
c、粗氖氦塔顶部气体输入粗氖氦塔冷凝器吸收腔吸收冷量后得到气液相混合物,其中液相部分输回粗氖氦塔顶部,气相部分作为产品粗氖氦气输出系统;
d、中压气液临界点的空气(或氮气)进入粗氖氦塔蒸发器吸收腔吸收冷量后转换为液态后输入上塔的液空(或液氮)管线;
粗氖氦塔冷凝器内液氮的蒸发温度低于吸收腔内氮气(富含氖氦组分)的液化温度,通过控制液氮的压力和氮气(富含氖氦组分)的压力实现,粗氖氦塔蒸发器内空气的液化温度高于液氮的蒸发温度,通过控制空气和液氮的压力实现。
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