CN1289404A - 蒸发液态氧的方法与装置 - Google Patents

蒸发液态氧的方法与装置 Download PDF

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CN1289404A
CN1289404A CN99802519A CN99802519A CN1289404A CN 1289404 A CN1289404 A CN 1289404A CN 99802519 A CN99802519 A CN 99802519A CN 99802519 A CN99802519 A CN 99802519A CN 1289404 A CN1289404 A CN 1289404A
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evaporator
pressure column
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弗朗茨·哈比希特
格哈德·蓬普尔
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Abstract

一种用于蒸发液态氧的方法与装置。在正常的运行条件下:将液态氧输入到主蒸发器3中并进行部分蒸发;第一次溢流5以液态从主蒸发器3中排出;第一次溢流5在辅助蒸发器6中被部分蒸发;第二次溢流7以液态从辅助蒸发器6中排出。加热操作会中断正常的运行,在加热过程中:从主蒸发器3中没有液体5输送到辅助蒸发器6中且辅助蒸发器的温度升高了,明显地高于正常运行条件下其的温度。

Description

蒸发液态氧的方法与装置
本发明涉及到一种蒸发液态氧的方法及其在通过低温分馏空气来制备氧气的工艺过程中的应用。
在现有的应用中，氧是指一些氧含量高于空气中氧含量的混合物，例如其中氧含量至少为70％，优选至少为98％。(在此应用中，除非另外有特殊说明，所有百分比均为摩尔百分比)其具体包括非纯净氧，工业级纯氧和纯度达到99.9％或更高的高纯氧。对许多应用而言，都需要在使用前通过蒸发将液态氧转化为气态，这个过程是在一个与热载体进行间接热交换的主蒸发器中实现的。
此种类型的蒸发特别易发生在通过低温精馏制备气态氧的过程中，因为氧较之氮与氩更不易挥发，所以氧以液态形式存在于精馏塔的底部。为了得到气态产物并产生用于精馏塔的上升蒸气，必须在主蒸发器中蒸发液态氧。现今最为普遍的方法是传统的林德双塔法，其主蒸发器置于低压塔的底部并通过对来自于压力塔顶部的氮气进行冷凝而实现运行。(见HAUSEN/LINDE，低温工程，第二版，4.1.2部分，第284页)在这种情况中，主蒸发器起到了冷凝与蒸发的双重作用，故常称其为主冷凝器。同时，它也可由起到循环蒸发器或降膜式蒸发器作用的一个或多个热交换元件进行实施。
本发明还涉及到其他的双塔方法，例如其中的主蒸发器用于蒸发空气，以及用于氮氧分离的三塔或多塔方法。精馏塔的下游，氮氧分离塔以及用于制备其它空气组分、特别是制备稀有气体(制备氩)的装置都可以相互连通。
假如完全地或基本上完全地蒸发液态氧，一些难挥发的杂质如CO2和N2O虽然只是以极低的浓度存在于待蒸发的氧气中，却很容易集聚在主蒸发器中(或待分馏的空气中)。(然而，曾经是令人忧虑的乙炔在具有通过吸附进行初步提纯功能的空气分馏装置中已不再是一个难题)。例如CO2和N2O等一些难挥发的杂质可能会沉积为固体，这就需要不时地将其移出装置外，从而避免了阻塞主蒸发器中的热交换通道。为了移出这些已分离出的固体物质，整个装置必须停工。例如对于一个大型的空气分馏装置，则意味着两天到五天的停工时间。
为了减少难挥发组分在主蒸发器中的聚集，通常需要持续不断地或经常性地将以溢流(flushing stream)形式存在的液体导出主蒸发器并且排出此液流。与上述溢流一起，集聚于仍处于液态的氧中的难挥发物质也都随之排出，由此其在主蒸发器中的浓度受到限制。在具有通过吸附进行初步提纯的空气分馏装置中，溢流量通常限制为在输入至主蒸发器的液态氧总量的0.02-0.04％。在进行空气蒸馏的精馏塔的上游，自从用分子筛吸附器替代了过去使用的可逆热交换器或交流热交换器，由易燃的难挥发组分集聚在这种类型的氧蒸发器中(主蒸发器)所带来的问题就有了很大程度的改善，以至于不需要采取其它措施，单独的溢流就足以阻止有害的碳氢化合物的蒸浓(见HAUSEN/LINDE，低温工程，第二版，4.5.1.5部分，第312-313页)。
本发明的目的是提高蒸发液态氧的主蒸发器的利用率，特别是尽可能防止操作的中断。
此目的通过如权利要求1中的特征部分而实现。在这个过程中，从主蒸发器导出的第一次溢流输送到与主蒸发器隔开放置的辅助蒸发器中。在辅助蒸发器中，第一次溢流的大部分得到蒸发，并可由此得到气态氧以及氧的半成品。接着，第二次溢流也从辅助蒸发器中导出。(在从液态氧制备氪和氙的特定情况下，需要进一步的操作)在第一次溢流持续不断地从主蒸发器输送到辅助蒸发器的同时，第二次溢流也不断地、间歇地导出辅助蒸发器。
在本发明中，较大量的液体可从主蒸发器中以第一次溢流的形式导出，从而有利于喷出所有的难挥发组分，使其在主蒸发器中的浓度较低。特别是使得主蒸发器中也没有固体物质沉积。但是，如此大量的溢流并不是完全都损失掉，因为部分的第一次溢流还会在辅助蒸发器中蒸发并以气态形式导出。从辅助蒸发器中导出的第二次溢流量就很一般了，例如只是输入主蒸发器的液态氧总量的0.02-0.5％，优选0.02-0.2％。(在间歇地导出第二次溢流的情况下，百分含量指的是时间平均值)第一次溢流的残留物又在辅助蒸发器中得到蒸发并可用作气态氧产物。
利用本发明可以使得那些易导致固态沉积的难挥发组分充分地从主蒸发器中溢出，从而保证其在主蒸发器中的含量极低。这些难挥发组分完全地输送到辅助蒸发器中并通过第二次溢流和间歇地加热操作将其排出。
因此，固态沉积只是发生在辅助蒸发器中而不发生在主蒸发器中。然而，辅助蒸发器比主蒸发器明显更易于通过加热除去固体。为此，偶尔会有加热步骤中断正常的运行，在此过程中，辅助蒸发器与主蒸发器隔离而没有液体从主蒸发器中输入其中。同时，辅助蒸发器的温度升至明显地高于正常的操作条件下的温度，例如至少提高20K，优选提高20K到50K。在此过程中，主蒸发器与它所属的整套装置的运行是不需要中断的。由于加强了主蒸发器中溢流冲洗，所以不再需要通过加热去除固体物质。
有利的情况是，从主蒸发器导出的第一次溢流量至少为输入主蒸发器的液氧液态氧总量的1％，和/或优选至少为1％，和/或至多为10％，优选至多为5％。
本发明进一步涉及如权利要求1和2所述方法的使用，它主要用于在如权利要求6所述的相应装置中进行如权利要求3所述的低温空气分馏工艺，特别用于通过吸附(例如在分子筛上)对空气进行预提纯的空气分馏工艺与装置中。这类方法与装置多用做制备氧气、氮气以及大气中存在的其它气体。
另外，本发明还涉及如权利要求4和5所述的用于蒸发液态氧的装置。
本发明及它的其它细节，在下面依照附图中所示的实施方案进行了更为详尽的解释。在附图之中：
图1表示包括由一个单元组成的主蒸发器的第一个实施方案。
图2表示包括由多个单元组成的主蒸发器的第二个实施方案。
图1所示为低温空气分馏双塔装置的一部分，即压力塔1的上部和低压塔2的底层部分。主蒸发器3用于蒸发从低压塔2的最底层的传质部流出的液态氧。(最底层的传质部在图中以塔板4表示，但也可能是装备的填充料)气态的氧气通过输送管9从低压塔中输出。
如图1所示，主蒸发器可以安装在双塔中，特别是在低压塔的底层。或者，它可以作为一个单独的部件独立于双塔之外，或者将其装入另外一个独立于双塔之外的部件中，例如在DE332870A1或DE2055099A中所示，将其并入到甲烷喷射塔中。第一次溢流通过置于主蒸发器3下部的输送管道5持续不断地从主蒸发器输出并输入到辅助蒸发器中。当第二次溢流7从辅助蒸发器6的下部持续不断地或间歇地导出时，而蒸发的氧气8又返回到低压塔中。此外，蒸气8可以从低压塔输入到氧气输送管9或进入另一装置例如进入如DE332870A1或DE2055099A中所示的甲烷喷射塔的底部。
用于对主蒸发器进行间接加热的热载体是来自于压力塔1顶部的氮气。在主蒸发器中冷凝的氮气11用于对两塔进行加热回流。在正常的运行条件下，辅助蒸发器也同样通过来自于压力塔顶部的氮气或作为热载体12的空气对其进行加热。冷凝后的热载体是通过输送管道13输出并随之输入一个或多个精馏塔中。
在一定的时间间隔内，例如从三个月到十二个月，优选约六个月，就需要关闭第一次溢流的输送管道5中的阀门14进行一次正常操作与加热操作的切换。同时要切断热载体12的输送。取而代之，大约300K的热空气就通过输送管15输入到辅助蒸发器6的液化室中，而后再从输送管16输出。加热阶段包括以下步骤：切断、排空、加热、再冷却、启动和保持，一般需要10到24小时，优选为20小时。
假如第一次溢流5在输入到辅助蒸发器6之前，先进入装置19，例如通过吸附作用去除难挥发物质，这是非常有益的，但在本发明中却不是绝对必要的。
图2中的实施方案与图1的区别主要在于图2的主蒸发器是由多个单元3A,3B组成的，单元3A、3B集中配置了一个中央管道用作来自于压力塔1的气态氮的输送管。显而易见，此实施方案也可以安装一个去除难挥发组分的装置(图1中的19)。

Claims (7)

1、一种用于蒸发液态氧的方法，其中在正常的操作条件下，
将液态氧输入到主蒸发器3中并在此进行部分蒸发，
第一次溢流5以液态从主蒸发器3中排出，
第一次溢流5在辅助蒸发器6中被部分蒸发，以及
第二次溢流7以液态从辅助蒸发器6中排出，其中在此过程中，正常的操作会被一个加热操作中断，在该加热过程中从主蒸发器3中没有液体5输送到辅助蒸发器6中，且辅助蒸发器的温度升至明显地高于在正常操作条件下其的温度。
2、如权利要求1所述的方法，在正常的运行条件下，从主蒸发器3输出的第一次溢流量5至少为输入主蒸发器的液氧液态氧总量的1％，和/或优选至少为1％，和/或至多为10％，优选至多为5％。
3、如权利要求1或2所述的方法在一精馏系统中低温分馏空气来制备氧气的工艺过程中的应用，所述精馏系统具有用于从低压塔中蒸发液态氧的一个压力塔1和一个低压塔2，其中在主蒸发器3和辅助蒸发器6中产生的蒸气8的一部分输入低压塔2或作为气态氧产物9从低压塔输出。
4、一种蒸发液态氧的装置，其包括：一主蒸发器3，一辅助蒸发器6，一用于将液态氧至输入主蒸发器的装置，从主蒸发器3中输出第一次溢流并将其输入至辅助蒸发器6的第一溢流输送管5，从辅助蒸发器6中输出第二次溢流的第二溢流输送管7，从辅助蒸发器6中输出蒸气的气体产物输送管8以及可与辅助蒸发器6相连的加热装置(15、16)。
5、如权利要求4所述的装置还包括一台用于调整溢流量的仪器，以保证主蒸发器输出的第一次溢流量至少为输入主蒸发器的液氧液态氧总量的1％，和/或优选至少为1％，和/或至多为10％，优选至多为5％。
6、如权利要求1或2所述的方法在一精馏系统中低温分馏空气来制备氧气的工艺过程中的应用，所述精馏系统具有：用于从低压塔中蒸发液态氧的一个压力塔1和一个低压塔2，用于将液态氧输入到与低压塔2相连的主蒸发器3中的装置以及具有一条从主蒸发器和辅助蒸发器中输出气态氧产物的输送管的装置。
7、如权利要求6所述的装置，其包括一条从辅助蒸发器6中输出蒸气的气体产物输送管8，此输送管与低压塔2相连或与一条同低压塔相通的产物输送管9相连。
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