CN87106299A - 分离并回收挥发性溶剂的方法及装置 - Google Patents
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Abstract
从含有水蒸汽的排放空气中分离并回收挥发性溶剂的方法与装置,据此,排放空气首先通过只吸收水蒸汽的分子筛填料,接着再通过只吸收溶剂蒸汽的分子筛填料。靠加热来再生分子筛填料,用此方式可回收到不含水的溶剂。
Description
本发明涉及从含有水蒸气的排放空气中分离并回收挥发性溶剂的方法与装置,排放空气来自干洗机、金属表面去油设备、电子线路板清洗设备、溶剂浴以及类似设备。在此方法与装置中,排放空气通过可再生分子筛,然后再排放到大气中去。
已经有人提出过此类方法和相应的装置。然而事实表明,溶剂回收有一定困难,至少是代价太高,因为排放空气中所含的水蒸气会和溶剂蒸气一起凝结出来,所以还需使冷凝物脱去其中的水蒸汽。
因此,本发明的任务就是改进所引用的方法和装置,使该装置在实施此方法时是经济的,并且不仅能将水蒸气和溶剂蒸气有效地分离,回收到的溶剂还不含水。
根据本发明的解决方案,其特征在权利要求1中加以说明。为此,在所有情况下都采用了吸收水蒸气的分子筛填料和吸收溶剂蒸气的分子筛填料,这两种填料装填在分开的解吸回路中。
本方法的最大优点是依此能回收实际上不含水分的溶剂。实施本方法的装置其特征在权利要求5中加以叙述。
在附图中以单张图表示的流程示意图说明了根据本发明进行连续操作的装置的实施例。
在图示的装置中,既含有剩余溶剂(溶剂蒸气)又含有湿气(水蒸气)的排放气体用管道10加以输送。管道10分为两路,一个支路11通过阀门12接在吸收器13上,在吸收器13内装有已知的水蒸汽吸收型的分子筛填料14。水蒸气由下至上穿过分子筛填料14,由此空气湿度被滤除到露点最大为-80℃,含在排放气体中的溶剂蒸气不被明显吸收。去除了湿气的排放气体经阀门15和管道16进入热交换器17,在这里释放掉它的吸收热,被冷却到约+5至+20℃。
从所述排放气体管道10分开部位分出的第二条管道18通过阀门19接在第二个吸收器20上,其中装有分子筛填料21。吸收器20和分子筛填料21与吸收器13及分子筛填料14相同。从吸收器20通过阀门22经管道23通向热交换器17,这类似于上面所述管道16的情形。当吸收器13在吸收时(阀门12和15打开),先前已吸收过的吸收器20在再生,它的阀门19和22是关闭的。为此,用送风机24将空气、惰性气体或纯化气体从大气、惰性气体源或排气管道46经过管道25及过滤器26抽送到加热器27。
空气或惰性气体或纯化气体在加热器被直接加热(电加热)或间接加热(蒸气或热油)到100至200℃的温度。然后热气流经管道28及一打开的阀门29进入吸收器20,从上至下通过分子筛填料。用这种方式将吸收在填料21中的水排除,水蒸气经过阀门30及管道31进入排放管32,排入大气。在分子筛填料21再生之后,关闭加热器27,引入纯化气体将分子筛填料21吹冷,例如可以从管道46引入冷却空气到送风机24。
在完成了对分子筛填料21的再生和冷却之后,吸收器13和20进行切换,亦即将分子筛填料14进行再生,而使分子筛填料21进行吸收。为了再生过程,类似于吸收器20,有管道33和阀门34从加热器27通向吸收器13,同样有管道35和阀门36通向排放管32。
排放气体在经过两个分子筛填料层之一吸收湿气并经热交换器17冷却之后,通过管道37由送风机38通过管道39送至第二对吸收器。排放气体可以通过支管40和阀门41进入一个吸收器42,其中装有分子筛填料43。分子筛填料43是已知类型的,应选择能吸收排放气体中所含溶剂蒸气的。排放气体从下至上穿过分子筛填料,其中溶剂蒸气被脱除,再通过阀门44及管道45进入排放管46,由此将既无湿气又无溶剂蒸气的排放气体排入大气。
当然,取决于阀门的开闭状态,也可能将排放气体用送风机38经由管道39通过分管47及阀门48进入吸收器59,其中装有分子筛填料60。吸收器59及填料60与吸收器42及填料43相同。通过阀门61及管道62,排放气体亦可从吸收器59到达提到的排放管46。
当吸收器42进行吸收时,吸收器59被再生。为此送风机63将空气或惰性气体送到闭合回路中的加热器64。在这个加热器64内将空气或惰性气体直接(电加热)或间接(蒸气或热油)加热到温度在40℃与250℃之间。加热过的气体通过管路65和阀门66进入吸收器59,由上至下通过分子筛填料60,将前一吸收过程吸收的溶剂排除。然后溶剂蒸气沿阀门67和管道68送入冷凝器69,在这里溶剂蒸气被冷却到绝大部分的溶剂蒸汽被液化。根据溶剂或溶剂混合物的露点不同,冷凝器69用冷水(约20℃)、盐水(约-20℃至+5℃)或冷却剂(约-40℃至-20℃)进行冷却。在液滴分离器70内液态溶剂从循环气体中分离出来,流入溶剂槽71。由此将其用泵72送回溶剂罐(图中未画出)。基本不含溶剂蒸气的循环空气再通过管道73进入送风机63的吸入端,返回进入回路中。
在经过1到50小时的期间后,关闭送风机63和加热器64,终止加热状态。在接着的冷却状态过程中,送风机38将冷排放气体通过管道39和47以及阀门48吹入吸收器59,再由下至上通过分子筛填料60(在这步操作中阀67关闭)。冷的排放气体冷却了分子筛,然后通过阀门66从吸收器排走(在此操作期间阀门61关闭)。被加热的排放气体经过管道65流经关停的加热器64和关停的送风机63,并经过管道73和液滴分离器70进入冷凝热交换器69。这里排放气体被冷却并通过管道73a及管道74,还有阀门75进入吸收器42。在这个过程中阀门41被关闭。排放气体向上穿过分子筛43,在冷却分子筛60的过程中,分子筛43仍然工作在吸收状态。在吸收器42的顶部,排放气体通过阀门44进入管道45和46并逸入大气中。吸收器顶部另一阀门76在这段时间内被关闭,此阀安装在管线77上,该管线则与管道65以及加热器排出口相连。
经过1至3小时后,吸收器的冷却状态结束,因此可以将吸收操作从吸收器42切换到吸收器59。在吸收器59进行吸收期间,吸收器42被相应地进行再生处理。
替代沸石的还可以采用硅胶、氧化铝或分子筛焦碳做为分子筛填料。
为此,将一些作用相同的工作物料,如分子筛焦碳以及用来与水蒸气结合的硅胶当做分子筛来使用,就可以被理解了。
分子筛填料(14、21、43、60)是由1-10毫米的球形或园柱形颗粒构成。
Claims (9)
1、从含有水蒸气的排放空气中分离并回收挥发性溶剂的方法,排放空气来自干洗机、金属表面去油装置、电子线路板清洗设备、溶剂浴以及类似设备,在此方法中,排放空气通过可以再生的分子筛,然后再排放到大气中去,其中,排放空气先通过只吸收水蒸气的分子筛填料,接着通过只吸收溶剂蒸气的分子筛填料,并且两种分子筛填料相互独立地用空气或惰性气体加以再生,专门吸收水蒸气的分子筛填料在大气下再生,专门吸收溶剂的分子筛填料在密闭回路中再生,密闭回路中的溶剂蒸气在冷凝热交换器中被冷凝,然后收集再返回复用。
2、按照权利要求1的方法,进行连续操作,其中排放空气交替通过两个并联切换的分子筛填料,其中一个分子筛填料在某一时刻处于吸收状态,另一个则处于解吸状态。
3、按照权利要求1或2中的一项方法,其中处于解吸状态的分子筛填料被热空气或热惰性气体加热,加热时气体通过的方向与加料时排放空气流入的方向相反。
4、按照权利要求1至3中一项方法,其中在解吸状态之后,将冷却空气或冷却惰性气体通过分子筛填料,通过方向与排放空气在加料状态下的流动方向相同。
5、实施按照权利要求1至4的方法并带有可再生分子筛清洗步骤的装置,其中,至少有一个容器(13,20)装有吸收水蒸气的分子筛填料(14,21),至少有另一个容器(42,59)装有吸收溶剂的分子筛填料(43,60),一个热交换器(17)及一台送风机(38),热交换器(17)与送风机(38)相连,一方面,对吸收水蒸气的分子筛容器(13,20)是通过阀门(15,22)与排放管(16,23)相连,另一方面通过管道(39,40,47)及可关闭阀(41,48)与吸收溶剂的分子筛容器(42,59)相连。
6、按照权利要求5的装置,其中,吸收溶剂的分子筛容器(42,59)由管道(68,73a,74)所连接,这些管道可用阀(67,75)与冷凝热交换器(69)的联结点隔离开,冷凝热交换器则依次与液滴分离器(70)相连,后者再与溶剂罐(71)连接。
7、按照权利要求5或6的装置,其中,分子筛填料(14,21,43,60)是由1至10毫米的球形或圆柱形颗粒构成。
8、按照权利要求5至7中一项的装置,其中,每一个吸收水蒸气的分子筛容器(13,20)都具有两支带有关闭阀(15,36;22,30)的排放管道(16,35;23,31),在各种工况下,一支管道(16,23)通往吸收溶剂的分子筛容器(42,59),另一支管道(35,31)则通往大气,并且每一个吸收溶剂蒸气的分子筛容器(42,59)都具有两支带有关闭阀(44,75;61,67)的排放管道(45,74;62,68),在各种工况下,一支管道(45,62)通往大气;另一支管道(74,68)通往冷凝热交换器(69)。
9、按照权利要求5至8中一项的装置,其中有一台送风机(24)被接在连有吸收水蒸气的分子筛吸收器(13,20)和加热器(27)的管道上,另有一台送风机(63)则接在循环回路管线上,该回路管线上接有吸收溶剂的分子筛容器(42,59),一个加热器(64),冷凝热交换器(69)以及液滴分离器(70)。
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EP86112786A EP0215472B1 (de) | 1985-09-18 | 1986-09-16 | Verfahren und Vorrichtung zum Abscheiden und Rückgewinnen von flüchtigen Lösungsmitteln |
EP86112786.8 | 1986-09-16 | ||
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CN87106299A true CN87106299A (zh) | 1988-04-13 |
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CN87106299A Expired CN1010554B (zh) | 1986-09-16 | 1987-09-15 | 分离并回收挥发性溶剂的方法及装置 |
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US (1) | US4846852A (zh) |
EP (1) | EP0260481B1 (zh) |
JP (1) | JPS63147517A (zh) |
CN (1) | CN1010554B (zh) |
AU (1) | AU587145B2 (zh) |
GR (1) | GR3001990T3 (zh) |
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-
1987
- 1987-08-24 EP EP87112265A patent/EP0260481B1/de not_active Expired - Lifetime
- 1987-08-26 ZA ZA876348A patent/ZA876348B/xx unknown
- 1987-09-11 AU AU78321/87A patent/AU587145B2/en not_active Ceased
- 1987-09-14 US US07/096,675 patent/US4846852A/en not_active Expired - Fee Related
- 1987-09-15 CN CN87106299A patent/CN1010554B/zh not_active Expired
- 1987-09-16 JP JP62229944A patent/JPS63147517A/ja active Pending
-
1991
- 1991-05-22 GR GR91400667T patent/GR3001990T3/el unknown
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---|---|---|---|---|
CN102649499A (zh) * | 2012-05-14 | 2012-08-29 | 高鼎精细化工(昆山)有限公司 | 溶剂储罐 |
Also Published As
Publication number | Publication date |
---|---|
EP0260481A3 (en) | 1988-07-27 |
EP0260481B1 (de) | 1991-04-17 |
ZA876348B (en) | 1988-07-27 |
CN1010554B (zh) | 1990-11-28 |
GR3001990T3 (en) | 1992-11-23 |
EP0260481A2 (de) | 1988-03-23 |
US4846852A (en) | 1989-07-11 |
AU7832187A (en) | 1988-03-24 |
AU587145B2 (en) | 1989-08-03 |
JPS63147517A (ja) | 1988-06-20 |
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