CN1028746C - 生产富氧气体产物的方法 - Google Patents

生产富氧气体产物的方法 Download PDF

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CN1028746C
CN1028746C CN91102015A CN91102015A CN1028746C CN 1028746 C CN1028746 C CN 1028746C CN 91102015 A CN91102015 A CN 91102015A CN 91102015 A CN91102015 A CN 91102015A CN 1028746 C CN1028746 C CN 1028746C
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広岡永治
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Abstract

本发明提供一种两床压力变动吸附来生产富氧气体的方法，它具有高的回收率和产率。本法利用细的或通常尺寸的沸石分子筛料和较短的循环周期，借助在不同步骤中连续使用一台真空泵而达到节省能耗之效果。

Description

本发明涉及由含氧、氮成分的混合气如空气，借助压力变动吸附（PSA）而获得富氧气体的方法。
压力变动吸附系统及方法已被广泛使用于从混合气（包括空气）制备富氧气体，且此种系统和方法已被大量采用。
在如此系统中利用较短循环周期，在尽可能短的时间内很好地利用分子筛材料吸附某一成分之方法是有优点的。短的循环周期一般使用更细的分子筛材料颗粒尺寸以减少扩散阻力。具体的短循环周期实例请见美国专利4194891及4194892。采用上述专利方法可增加氧气产量，但回收率较低，仅为10-20%。
传统的真空PSA方法可得高的氧气回收率（50-60%），但产率稍低。传统的三床PSA方法产率不很高;举一例子，床尺寸系数为2000-2600kg沸石/吨氧气/天。
显然，人们都希望借助更快的循环周期和更细的分子筛颗料而获得高的产率及以传统的三床系统为代表的回收率，而在方法操作上仍然经济简单。
本发明的PSA方法获得富氧气体产物，具有高的氧气回收率及高的产率，解决了已有技术的缺点，且降低成本并保持简单操作。
本发明系统采用短循环周期而很好利用分子筛材料，仅需两个床，因而大大简化了已有技术中的高回收率的三床法。
正如后面所叙述，本发明的另一特征是节省能耗。借助一真空泵的连续运行于两塔系统，输送富氧气体至塔的出口进行压力平 衡，同时从同一塔的入口端进行解吸出富氮气体。在此情况下，在整个过程及其他过程中真空泵连续运行，由于真空泵在整个过程各步骤中不空转，故其功率是最理想的。
因此，具有高回收率和产率的二床PSA法借助较细沸石分子筛料颗粒、如20-35筛目，甚至较大颗粒如8-12目在少于30秒、最好在15-25秒内的短循环时间内得以完成。压力变动范围是使用小于40，000帕，最好26，660帕的真空用于解吸，使用小于135，800帕、最好小于122，000帕的最大产物压力。
为更好地理解本发明，以下结合附图对本发明的实施例进行说明。其中：
图1是本发明的流程示意图;
图2是本发明的塔循环周期图。
以下结合图1所示的流程示意图和图2所示的塔循环周期图对本发明进行详述。
图1、2共同表示从一含有氧气、氮气的气体如空气中连续制备富氧气流的方法。每一吸附塔A、B均含有选择性吸附氮气的吸附剂。
本方法借助较细的沸石颗粒、约8-35筛目、最好约12-20筛目。
具体的沸石筛料可从不同的沸石制造商处购置，呈球粒或丸粒状。各步骤的控制可借助常规方法，如用计时器控制的标准设计电磁阀。
步骤1中，阀门1A、2A处于关闭状态，从而隔绝第一塔A的下端即入口端。在塔A的顶端即出口端，阀4A、5A关闭，阀3A开启。对第二塔B而言，阀9B、10B关闭，因而来自塔B出口的气体通过阀3A进入塔A的出口，并由阀8B控制。此时在步骤1中，塔B的入口端的阀6B关闭而阀7B开启，因而气体从塔B的入口端被真 空泵16吸出。
此步骤期间，原先较塔A压力高的塔B之压力使两塔中的压力相等，就是说，在步骤1开始时塔B的压力可为约135，000帕，减少至步骤1结束时的约66，650帕，而塔A的压力从起始时的约34，700帕升至62，650帕。因此，步骤1结束时，塔间压力基本平衡。步骤1极快进行，一般用2-6秒，最好约4秒钟。
步骤2中，阀3A关闭，阀5A，2A开启，同时来自贮器18的富氧产物气体进入塔A的出口并由计量阀26控制回充塔A、进一步升高塔A之压力，具体而言，因为产物贮器中的压力约为106，600帕，塔A中的压力从62，650帕连续增加至约88，000帕。同时，气体仍借助真空泵16通过开启的阀门7B从塔B的入口抽出，塔B的压力继续减少。在步骤2中，该压力可从66，650帕减少至约60，000帕。此外，步骤2所用时间极短，一般为1-5秒，最好3秒。
步骤3中，阀1A开启，空气或其它主要含氧、氮的进气在一预设定进气压力下引入塔A的入口。入口压力可变化，但其应具有的最小预设定压力值，为122，000至149，600帕，该最小预设定压力值最好为约135，800帕。在塔A出口处，阀5A关闭，阀4A打开，因此进气流经塔A，在该处氮气被吸附，而后富氧产物气体从塔A的出口端流过阀4A。逆止阀11及管道20到达产物贮器18。在此制备富氧气体产物步骤期间，塔A中的压力可从88，000帕增加至约135，000帕。同时，在步骤3中，气体继续借助真空泵从塔B的入口端抽出从塔B解吸氮气及抽空氮浓缩气，同时随着塔B在其入口端的解吸，阀10B及24开启同时富氧产物气流被引至塔B的出口端以吹洗塔B。富氧产物气的流量用计量阀26控制。因而塔B即可借助富氧气体引至其出口端而吹洗，而同时富氮气体从其入口端抽出而解吸。因此，当真空泵不间断地连续抽吸时塔B的压力持续减少，从约60，000帕减至约34，700帕。步骤3也进行得相当快，其时间 一般为10-25秒，最好为18秒。
接着进行步骤4，将塔A的较高压力气输入塔B时，压力再次走向平衡。在关闭塔A出口端的阀4A及开启阀3A压力再次走向平衡。在塔B出口端，阀10B关闭，因此气体从塔A流至塔B，压力平衡由计量阀8B控制。同时，当然要关闭塔A进口端的阀1A以切断进气并开启阀2A，从而气体可从塔A的进口端经由真空泵16抽出。塔B的入口端因关闭阀7B而完全隔绝。
因此，在步骤4中，塔A、B中的压力近似平衡，塔A的压力从约135，000帕减至约66，650帕，而塔B的压力从约34，700帕增至约62，650帕。步骤4在约2-6秒内完成，最好4秒。
步骤5中，阀3A关闭，因而完全关闭塔A的出口端，而气体继续从塔A进口端抽出使压力下降，从66，650帕降至60，000帕。阀10B、28开启，富氧气体从产物贮器18进入塔B由计量阀30控制回充该塔便使塔B中的压力从约62，650帕增至约88，000帕。另外，如步骤2一样，回充步骤在1-5秒、最好在约3秒内完成。
最后是步骤6，此步骤中阀6B开启，从而将有压力的进气引入塔B入口。阀9B开启从而富氧产物气体从塔B经由逆止阀12、而后经管道20流至贮器18。
在步骤6中，由计量阀26控制，阀24、5A开启允许富氧气体进入塔A的出口而吹洗塔A。同时，随着塔A的吹洗，气体继续靠真空泵16从塔A的入口排出，以解吸即抽空富氮气体。具体而言，塔A的压力约60，000帕减少至34，700帕，而塔B的压力从约88，000帕增至约135，000帕。步骤6的进行时间可为10-25秒，最好18秒。
在步骤6完成后，在继续循环基础上重复以上全部步骤，在每一步骤期间经由阀32持续地从产物贮器18得到富氧产物（富氧气体）。
可以看到，真空泵16是连续交替地从两塔之一排除气体，因而能有效地用来减少本方法能耗。
实例
使用上述装置，步骤顺序和上述而进行本方法，获得富氧气体产物。而吸附塔A、B的直径为2英寸，高15英寸，内充以球粒状钙×沸石分子筛材料，其可从Laporte    Co.公司购置，（运行了三个周期）以及丸粒状沸石料，从Tosoh    Company公司购置，（运行了一个周期）。
回收率，产量如下表所示：
表1
分子筛材料（沸石）    Laporte公司    Tosoh    Zeolum    SA公司
分子筛尺寸    0.4-0.8mm（球粒）    1.5（丸粒）
压力变动范围    125，000～74，700帕
循环时间（秒）    25    20    17    25
氧纯度（%）    93    93    93    93
容积密度（kg/cm3） 681 620
氧回收率（%）    59    58    56    55
比产率（所获氧气的标    40    51    59    40
准升/小时/床体积
升）
床尺寸系数（kg沸石/    535    420    375    487
吨氧/天）
从以上试验可知借助两塔系统，在每一步骤期间持续对一塔或另一塔施以真空则可获得高的回收率、高的产率，真空泵被有效地利用，因此，降低了能耗。循环进行极快，能很好地利用分子筛料。显然此种两床系统的结构和效果比复杂而昂贵的三床系统有更多的优点。
尽管本发明的实施例已经给出，但可以理解本发明并不局限于此，人们还可进行不同的改进，但只要这些变化是在所附的权利要求书精神实质和范围之内，则可以认为本发明是包括这些改进的。

Claims (10)

1、一种制备富氧气体的方法，该方法以至少含有氧、氮的空气为原料气，采用装有选择性吸附氮的吸附剂的两个吸附塔和一个产物贮器，其特征在于该方法的步骤为：
(i)将气体从较高压力的第二吸附塔出口引至处于低压的第一吸附塔出口，使两个塔的压力大体平衡，这时从第二塔的入口端则进行排气，如附图2A的步骤1所示；
(ii)步骤1平衡后，将置于产物贮器中处于较高压力的产物气引至第一塔的出口，以便在气体继续从第二塔入口排气期间回充第一塔，如附图2B的步骤2所示；
(iii)在最低预设定压力下将进气引入第一塔并将氧浓缩产物气从第一塔的出口回收引入产物贮器，同时将部分产物气引至第二塔出口以吹洗第二塔并同时从第二塔入口排出气体，从而为第二塔解吸和抽空富氮气体，如附图2C的步骤3所示；
(iv)将气体从最初处于高压的第一塔出口引至第二塔的出口以平衡二塔间的压力，同时将气体从第一塔之入口排出，如附图2D的步骤4所示；
(v)步骤(iv)平衡完成后，将产物贮器中较高压力的氧浓缩气产物引至第二塔的出口，同时继续将气体从第一塔的入口排出，如附图2E的步骤5所示；
(vi)将预设定最小压力的进气引入第二塔之入口，并从第二塔的出口将富氧气体产物回收引入产物贮器，同时将部分产物气引至第一塔的出口以吹洗第一塔，与此同时将气体从第一塔入口排出，从而为第一塔解吸、抽空富氮气体，如附图2F的步骤6所示；
(vii)重复步骤(i)-(vi)，同时将富氧气体从产物贮器中取出使用。
2、如权利要求1所述的方法，其特征是所用吸附剂为8-35目的细沸石粒，而且在步骤（ⅲ）及（ⅵ）中引入的进气为压力122，000-149，600帕的空气。
3、如权利要求2所述的方法，其特征是所用细沸石粒呈球粒或丸粒状，尺寸为12-20目。
4、如权利要求1所述的方法，其特征是步骤（ⅰ）及（ⅳ）在约2-6秒内进行;所述步骤（ⅱ）及（ⅴ）在1-5秒内进行;所述（ⅲ）及（ⅵ）在10-25秒内进行。
5、如权利要求4所述的方法，其特征是步骤（ⅰ）及（ⅳ）在约4秒内进行;步骤（ⅱ）及（ⅴ）在3秒内进行;步骤（ⅲ）及（ⅵ）在18秒内进行。
6、如权利要求1所述的方法，其特征是所述步骤（ⅰ）及（ⅳ）包括使塔中的压力平衡到62，650至66，650帕;所述产物气在步骤（ⅱ）及（ⅴ）中以106，600帕的压力引入;所述进气在步骤（ⅲ）及（ⅵ）中以122，000-149，600帕的压力引入。
7、如权利要求6所述的方法，其特征是所述进气在步骤（ⅲ）及（ⅵ）中以小于135，800帕的压力引入。
8、一种用于制备权利要求1所述富氧气体的装置，其特征在于该装置包括两吸附塔（A、B）、重复在接纳所述空气进气和制备的所述富氧气体之间循环所述两吸附塔的装置以及一真空泵（16），如图1所示;所述真空泵与二吸附塔相连并可持续将气体在所述的重复循环周期期间从这一或另一吸附塔抽出气体。
9、如权利要求9所述的装置，其特征是所述进气具有123，000-149，600帕的压力，且所述吸附塔内装有8-35目大小的细沸石粒料。
10、如权利要求9所述的装置，其特征是所述细沸石粒料呈球粒或丸粒状，尺寸为10-20目。
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