CN1104273C - 用吸附作用分离气体的设备和方法 - Google Patents
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Abstract
本发明公开了一种用称之为VSA或MPSA型的吸附分离气体的设备,它包括设置在用户管路(L)和待分离的气体混合物源(S)之间的至少一个模件(M),该模件包括串联设置的一个可反转的旋转机构R(通常为Roots机)、一个吸附器(A)和至少一个容器(C),可交替地驱动上述旋转机构(R),使之在增压和生产的第一阶段按一个方向旋转,而在减压和解吸的第二阶段按另一方向旋转。本发明尤其适用于以模件组装的小型和中型生产氧气的设备。
Description
本发明涉及用称之为VSA或MPSA型变压吸附作用分离气体的设备,更具体地说,涉及中型或小型分离设备,该设备包括至少一台以压缩方式或泵送方式作用于吸附器上的旋转机构。
如1983年的美国专利文献US-A4534346和更新一些的在1993年公布的美国专利文献US-A-5370728所描述的现有设备包括一台具有高压侧和低压侧的旋转机构,该机构被调整为以相同方向和同一速度恒定运转。由于使用了很多阀门,使旋转大大偏离最佳运行状况,一方面阀的数量多另一方面要保证对这些阀门进行同步调节,因此,明显地提高了设备的制造和运行费用。
本发明的目的是提供一种吸附设备,该设备能简化流程,大大减少阀门的数量,从而能够提供单独的吸附模件,这种模件使用起来非常方便,尤其能将它们并联成模件组,从而能扩大使用范围,控制设备的运行条件。
为此,本发明的设备至少包括一个模件,该模件包括:
一根始终与待分离的气体混合物源相通的进气管;
一根与至少一个贮气装置相连的排气管,上述贮气装置用于贮存至少已减少了气体混合物中某种组分的气体;
一台串联在进气管和排气管之间可反转的旋转机构和一台吸附器:以及
用于顺序调节旋转机构反向旋转的装置。
本发明的其它特征为:
一个与上述已减少了气体混合物中某种组分的气体的使用管路固定相连的第一贮存装置;
至少一个只与排气管道相连的第二贮存装置;
上述设备包括至少两个并联地设置在气体混合物源和用户管路之间的单独的模件。
本发明的另一目的是提供操作这种适于广泛使用和适于分离各种气体的设备的方法。
按照本发明的一部分内容,与一台吸附器相连的旋转机构交替地运行,在第一阶段或将气体送入吸附器的阶段,旋转机构按一个方向旋转,然后,在第二阶段或将气体排出吸附器阶段,旋转机构按另一方向旋转。
按照本发明的一个更独特的特征,在每个阶段结束的一定期间内旋转机构停止转动。
采用本发明的设备和方法,在旋转机构的两侧尤其在旋转机构和吸附器入口之间不必设置隔离阀,旋转机构的可逆转性能确保交替而顺序地将待分离的气体混合物压缩到吸附步骤所需的高循环压力和抽空到解吸步骤所需的低循环压力,通过利用由反向压差和施加在旋转机构的一些旋转部件的惯性力产生的最大自动旋转可以灵活而经济地实现这种反转。
下面将结合附图对本发明的完全起说明作用而非限制性的实施例进行描述,通过这些描述,将能更清楚地反映出本发明的其它特征和优点,其中:
图1为本发明吸附模件的实施例示意图;
图2为旋转机构的压力与相应的转动周期的关系的示意图;
图3的曲线反映出特定压力周期与图1所示的模件的阀相应的动作状况的关系;
图4是采用两个模件的设备示意图;
图5是与图3类似的曲线,它反映出图4所示设备的阀开/关周期;
图6为本发明模件的特定实施例的示意图。
在下面的描述和附图中,相同或相似的部件尽可能用相同的标号表示。
图1示出了本发明的吸附模件M,通常它包括一个典型的竖直构形的吸附器A,该吸附器有一个入口1和一个出口2,吸附器中装有至少一种能留存待分离的气体混合物的至少一种组分的吸附剂。入口1经一可反转的旋转机构R与入口管道1相连,通常上述旋转机构是一种Roots机或一种具有多叶片转子的机器,该机器由一台用控制箱B控制的电动机D驱动。出口2与排气管道O相连,再经过一个隔离阀V1和一个贮气罐C与用户管路L相连,同时进气管1可与待分离的气体混合物源S相连,上述混合物源S可以接收由本发明设备排出的残余气。根据本发明的一个具体应用,待分离的气体混合物是空气,气源S是大气,吸附器中装有至少一种吸附剂,上述吸附剂能通过吸附来滞留需要的产品组分(通常为氧有时为氮)中不希望有的各种组分。
有利的是,如图1所示,使排气管道0经隔离阀V1与至少一个贮气罐T相连,只将上述贮气罐与排气管0相连是为了如后面结合图3所描述的那样通过回收至少部分事先已存贮在贮气罐中的气体对吸附器A的均压和再增压阶段或对吸附器的均压和冲洗阶段起作用。
图2示出了与压力有关(在上部)和与旋转机构的旋转有关(在下部)的周期。压力周期包括增压和生产阶段T0-T1以及减压和解吸阶段T1-T2,在增压和生产阶段,此时,压力在低循环压力Pm和高循环压力PM之间,低循环压力Pm低于大气压力Pa,一般在0.2×105Pa和0.6×105Pa之间,最好在0.3×105Pa和0.5×105Pa之间,高循环压力PM略高于大气压力,一般在1.05×105和1.5×105Pa之间,而在减压和解吸阶段压力在PM和Pm之间。电机只在循环周期的中心部分j和j’期间驱动旋转机构。在压缩步骤j,电机驱动压气机,在两阶段之间的反向时刻T1之前的一段短时间内,停止向电机供电,在步骤k,由于动能的作用,旋转机构在自身的动量作用下继续转动,直到时刻T1自然停止转动为止,此时在气体反向流动的通路3和4之间的压力差的作用下,旋转机构按相反方向自然开始转动,在步骤i’结束时,由于电机驱动, 旋转机构在相反方向的转速加快,在步骤j’期间,旋转机构以泵送模式运转,在到达低压的时刻T2之前一段短时间内,机械驱动同样停止,在步骤k′期间转动机构由于其自身的动量继续转动,直到停止转动为止,在时刻T2,旋转机构开始转动,在步骤i,在通路3和4之间的压力差作用下,旋转机构以相反方向转动,接着,在步骤j,如前所述,在电机的驱动下,旋转机构的转速增加。本申请人进行的研究表明,依照上述运行状况,减速自旋转阶段k和k′的持续时间约1秒,加速自旋转阶段的持续时间约2至5秒,上述时间范围与大多数吸附循环的总持续时间(根据容量和应用从20至150秒)完全相适应。当然,如果需要,也可使旋转机构的惯性与VSA循环相匹配,例如,需要时可采用飞轮装置,使之与单向离心离合器相连。
图3再次示出了图2的压力周期,图3还示出了气体从吸附器入口和出口流入/流出贮气罐和贮气容器的情况。可从借助于旋转机构R将待分离的气体混合物送入吸附器A的入口1这一过程的加压/生产阶段T0-T1中分出一初始步骤a,在该步骤中,阀V1′开启,同时不被优先吸附的气体或气体混合物或产品气(如氧)经吸附器A的出口逆向流入。继上述第一加压步骤之后是仅由待分离的气体混合物引起的第二加压步骤b,此时阀门V1,V1′关闭。在第二加压步骤b结束时,压力超过大气压,在生产步骤C阀V1开启,压力略有增加或大体为恒压,其值为高循环压力PM。
如上所述,在T1时刻,在生产步骤结束时,在高循环压力下旋转机构R的旋转反向,在整个第二阶段T1-T2富含被吸附组分的气体混合物经入口1排出。在第二阶段的第一步骤d期间,阀V1′开启,使得吸附器能同时从顶部和底部减压,此后,在步骤e1期间,阀V1和V1′关闭,吸附器继续减压,在阶段T1-T2结束时,吸附器暴露于真空,压力降至低循环压力Pm。为了用贮气罐的产品气进行冲洗步骤e2,最好略在T2时刻之前开启V1阀。
由于运行的独立性,图1所示的单个吸附设备对T0-T1和T1-T2阶段各自的持续时间以及组成上述各阶段的步骤都没有特别的限制。电机D既可在正反两个旋转方向以相同的转速驱动压气机,也可以不同转速驱动压气机。最好使旋转机构R在泵送阶段T1-T2的步骤j′期间以最大转速旋转,而在T0-T1的空气压缩阶段的步骤j期间以较低转速旋转,一般约以最大转速的50%的转速旋转。
作为一种变型,可以在时刻T1或者甚至在时刻T1之后的一小段时间内停止给电机供电。在这种情况中,旋转机构自然停止,并在步骤d期间自然反转。同样在减压结束时,在T2时刻或者就在T2时刻之后的一小段时间内停止向电机供电。如果电机由一可变速的驱动单元供电,可对该单元编程,使旋转机构的自然停止和方向的自然转换同时进行和/或有利于上述转换。
图4示出的分离设备采用了两个如图1-图3所描绘过的模件M1和M2。在这种情况中,分别与阀V1,V2相连的排气管O1和O2与在生产线L上游段D的同一贮气罐C相连,上游段D上设有一个隔离阀Vp,该隔离阀的开启和关闭操作曲线示于图5曲线中阀1和阀2的开启和关闭操作曲线旁边,图5中还示出了两个模件M1和M2的压力周期。
在这种带两个模件的实施例中,一个吸附器处于加压/生产阶段的第一步骤a期间,气体逆向流入该吸附器时另一吸附器处于减压阶段的步骤d,开始进行均压或准均压运行,旋转机构R1和R2的压力和机械驱动周期与前面在图2和图3中所描述的情况相同。
在这种双模件设备中,如上所述,步骤a的持续时间与步骤d的持续时间相同,各模件的阶段T0-T1和T1-T2的持续时间也相同,一个吸附器的循环与另一吸附器的循环错开一个循环阶段。如前所述,每个旋转机构在泵送步骤j′旋转速度最大,在加压阶段j转速降低,一般为最大转速的一半。
应该懂得,按照本发明的用吸附作用分离气体的设备可以包括若干并联设置的模件M,各模件之间同步运行。例如一台三模件设备,若每个模件的步骤a和d的持续时间仍然相同,在这种情况下,加压/生产阶段T0-T1的持续时间等于减压/解吸阶段T1-T2的持续时间的一半,各模件之间其各自的周期在时间上偏移整个循环周期的三分之一。对高循环压力在1.1×105Pa和1.5×105Pa之间以及低循环压力在0.5×105Pa和0.3×105Pa之间的运行条件而言,驱动电机在两个方向的速度为相同速度是最好的能耗/费用兼顾方案。
对于从空气中生产氧气的设备,所使用的吸附剂至少包括一种沸石,尤其是一种LiX沸石,压力PM和Pm一般为前文所述的那些值,一个周期的总持续时间通常在30秒和120秒之间。
根据本发明模件的独立性,可将它们组成具有n个模件的模件组,可根据需要对它们进行全部或部分自动或手动操作。此外,即使一个模件出现故障或对其维修,该设备仍能方便地至少是临时地用n-1个模件运行。
图6示出了本发明模件的一个具体实施例。可以看出,通常具有水平的内部气体环流的竖直吸附器A有一个也设置在下部的出口2,吸附器A由一呈裙状的支座5支承,在该支座限定的内部空间装有旋转机构R及其驱动电机D,支座5衬有隔音内衬6。图6还示出了一个蓄热器7,该蓄热器处于进气管道I和旋转机构R之间,在冷却工况,它回收泵送阶段的部分热能,用以在压缩阶段加热送入吸附器的气体混合物。还可以在旋转机构的通道4和吸附器的入口1之间安装一台冷却器,例如安装一台空气冷却器型冷却器。
Claims (21)
1.用吸附作用分离气体的VSA型设备,它包括至少一个模件(M),该模件包括:
一根与待分离的气体混合物源(S)固定相通的进气管(I);
一根可以与至少一个贮气装置(C,R)相连的排气管(O),上述贮气装置用于贮存已减少了气体混合物中某种组分的气体;
一台串联在进气管(I)和排气管(0)之间具有多叶片转子的可反转的旋转机构(R)和一台吸附器(A),以及
用于连续调节上述旋转机构(R)反向旋转的装置(B、D)。
2.如权利要求1所述的设备,其特征在于将第一贮气装置(C)与上述已减少了气体混合物中某种组分的气体的一根用户管路(L)固定相连。
3.如权利要求2所述的设备,其特征在于至少一个第二贮气装置(R)只与排气管(0)相连。
4.如权利要求1或2所述的设备,其特征在于它包括至少两个并联地设置在气源(S)和用户管路(L)之间的上述模件(Mi)。
5.如上述任一项权利要求所述的设备,其特征在于它还包括一个连在第一通道(3)和气源(S)之间的蓄热器(7)。
6.如上述任一项权利要求所述的设备,其特征在于上述吸附器(A)被支承在一个装有旋转机构(R)并包括隔音构件(6)的支座(5)上。
7.如权利要求4所述的设备,其特征在于吸附器(A)的入口(1)和出口(2)位于该吸附器的基座上。
8.如上述任一项权利要求所述的设备,其特征在于上述旋转机构(R)由一台可变速电动机(D)驱动。
9.如上述任一项权利要求所述的设备,其特征在于上述旋转机构(R)是一台Roots机。
10.一种VSA型吸附式分离气体的设备的运行方法,该设备包括至少一个具有一个送入待分离的气体混合物的入口和一个出口的模件,上述出口与用于已减少了气体混合物中至少一种组分的气体的一根用户管路(L)相连,该模件包括串联设置的一个具有多叶片转子的可反转的旋转机构(R)和一台吸附器(A),所用循环包括下述顺序步骤:
在第一阶段按第一方向驱动旋转机构,以便能以高于大气压的高循环压力将气体混合物供入吸附器以输送已减少了某种组分的气体(L);
停止驱动上述旋转机构;
在第二阶段按第二方向驱动旋转机构,以便将吸附器的压力减至不超过0.6×105Pa的低循环压力;以及
停止驱动上述旋转机构。
11.如权利要求10所述的方法,其特征在于上述低循环压力在0.3×105Pa和0.5×105Pa之间。
12.如权利要求10所述的方法,其特征在于在每个阶段(T0-T1)、(T1-T2)的结束时刻前后的规定期间(k,k′)停止对旋转机构(R)进行机械驱动。
13.如权利要求10至12中任一项所述的方法,其特征在于旋转机构(R)的转速根据上述不同阶段而改变。
14.如权利要求10至13中任一项所述的方法,其特征在于在第一阶段(T0-T1)的第一部分(a)期间,同时将上述已减少了某种组分的气体的一部分经出口(2)送入吸附器(A)中。
15.如权利要求10至14中任一项所述的方法,其特征在于在第二阶段(T1-T2)的第一部分(d)期间,同时使上述已减少了某种组分的气体的一部分从吸附器(A)的出口(2)排出。
16.如权利要求14和15所述的采用了至少两个模件(Mi)的方法,其特征在于第一阶段(T0-T1)和第二阶段(T1-T2)的第一部分(a;d)的持续时间相等。
17.如权利要求10至16中任一项所述的采用了两个模件(Mi)的方法,其特征在于每个模件(Mi)的第一阶段(T0-T1)和第二阶段(T1-T2)的持续时间相等。
18.如权利要求10至16中任一项所述的采用了三个模件的方法,其特征在于每个模件(Mi)的第二阶段(T1-T2)的持续时间是第一阶段(T0-T1)的持续时间的两倍。
19.如权利要求18所述的方法,其特征在于在每个阶段大体以相同速度驱动旋转机构(R)。
20.如权利要求10至17中任一项所述的方法,其特征在于旋转机构(R)在第一阶段(T0-T1)的旋转速度低于在第二阶段(T1-T2)的转速。
21.如权利要求10至20中任一项所述的方法,其特征在于上述待分离的混合物是空气。
Applications Claiming Priority (2)
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FR9505956A FR2734172B1 (fr) | 1995-05-19 | 1995-05-19 | Dispositif et procede de separation de gaz par adsorption |
FR9505956 | 1995-05-19 |
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CN1104273C true CN1104273C (zh) | 2003-04-02 |
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EP (2) | EP0743087B1 (zh) |
JP (1) | JPH0999208A (zh) |
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CN (1) | CN1104273C (zh) |
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DE (2) | DE69626564T2 (zh) |
ES (2) | ES2194084T3 (zh) |
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ZA (1) | ZA963967B (zh) |
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1996
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- 1996-05-16 JP JP8122037A patent/JPH0999208A/ja not_active Withdrawn
- 1996-05-17 AU AU52334/96A patent/AU710281B2/en not_active Ceased
- 1996-05-17 CA CA002176916A patent/CA2176916A1/fr not_active Abandoned
- 1996-05-17 CN CN96110436A patent/CN1104273C/zh not_active Expired - Fee Related
- 1996-05-17 ZA ZA963967A patent/ZA963967B/xx unknown
- 1996-05-20 KR KR1019960016913A patent/KR960040428A/ko not_active Application Discontinuation
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2138663A1 (zh) * | 1971-05-25 | 1973-01-05 | Sulzer Ag | |
US5370728A (en) * | 1993-09-07 | 1994-12-06 | Praxair Technology, Inc. | Single bed pressure swing adsorption system and process |
Also Published As
Publication number | Publication date |
---|---|
ZA963967B (en) | 1996-11-25 |
EP1243306B1 (fr) | 2005-05-11 |
DE69626564T2 (de) | 2004-04-08 |
FR2734172B1 (fr) | 1997-06-20 |
DE69634741T2 (de) | 2006-01-12 |
KR960040428A (ko) | 1996-12-17 |
ES2194084T3 (es) | 2003-11-16 |
FR2734172A1 (fr) | 1996-11-22 |
JPH0999208A (ja) | 1997-04-15 |
AU5233496A (en) | 1996-11-28 |
EP0743087B1 (fr) | 2003-03-12 |
EP0743087A1 (fr) | 1996-11-20 |
CA2176916A1 (fr) | 1996-11-20 |
EP1243306A3 (fr) | 2003-03-12 |
AU710281B2 (en) | 1999-09-16 |
DE69634741D1 (de) | 2005-06-16 |
EP1243306A2 (fr) | 2002-09-25 |
CN1148517A (zh) | 1997-04-30 |
ES2241916T3 (es) | 2005-11-01 |
US5679134A (en) | 1997-10-21 |
DE69626564D1 (de) | 2003-04-17 |
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