CN1074748A - 生产增压产品的低温精馏*** - Google Patents
生产增压产品的低温精馏*** Download PDFInfo
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Abstract
一种生产较高压力的低温精馏***,其中双塔系
统中的较低压塔在增压下操作,从较低压塔的上部取
出的含氮流体被用于产生设备冷冻及用于再生物料
的吸附净化床,因而可避免任何物料膨胀的需要。
Description
本发明涉及包含氧气和氮气,例如空气,的混合物的低温精馏***,更具体地涉及从低温精馏中增压产品的生产。
空气之类的混合物经低温分离制氧和/或氮是成熟的工业过程。液体和蒸气经一个或多个塔进行对流接触,氧氮间的蒸气压差造成氮在蒸气中浓缩,而氧在液体中浓缩。在分离塔中压力越低,由于蒸气差之故使氧氮分离越容易。因此,最后分离成氧和/或氮产品的过程一般是在较低的压力下进行的,通常只有大气压之上每平方英寸几磅的压力。
常常需要较高压力的氧和/或氮产品。在一些情况下,用压缩机将产品压缩到所需压力。除了产品压缩机的投资值外,这种压缩从能量费用方面的观点来看是浪费的。
因此,本发明的目的之一在于为生产氧和/或氮提供一种改进的低温精馏***。
本发明的另一目的是为生产氧和/或氮提供一种改进的低温精馏***,在该***中可以生产出较高压力的氧和/或氮,因而可以消除或减少产品气体压缩的需要。
对于本领域的技术人员而言,当他阅读了本申请文件后,本发明的上述目的和其它目的就显得非常明显,这些目的可由本发明实现。
本发明的一方面是:
产生较高压力产品用的低温精馏方法,包括:
(A)将含氧和氮的物料通入一个吸附净化床,将进入床中物料中的可吸附污物除去得到清洁物料;
(B)将该清洁物料冷却,将冷却的清洁物料通入一高压塔,由低温精馏将物料分离成富氮和富氧流体;
(C)将富氮和富氧流体从高压塔通入操作压力比高压塔低但至少20磅/平方英寸的增压塔中,由增压塔内低温精馏生产出富氮和富氧流体;
(D)从增压塔上部除去含氮流体,使该含氮流体经过涡轮膨胀,产生冷冻,将所得含氮流体以间接换热方式与物料接触使之冷却;
(E)将从增压塔的含氮流体通入吸附净化床,使该床再生;及
(F)从增压塔回收富氮和富氧流体的至少一种作为增压产品。
本发明的另一方面包括:
一种低温精馏装置,包括:
(A)一吸附净化床,一主换热器和将物料从吸附净化床通入主换热器的装置;
(B)一塔***,包括第一塔和第二塔,将物料从主换热器通入第一塔的装置和将流体从第一塔通入第二塔的装置;
(C)从第二塔上部排放流体的装置;
(D)一涡轮膨胀机,将从第二塔上部排出的流体通入该涡轮膨胀机的装置和将膨胀后的流体从该涡轮膨胀机通入主换热器的装置;
(E)将从第二塔上部排出的流体通入吸附净化床的装置;及
(F)从第二塔回收产品流体的装置。
这里所用的术语“塔”意指一种蒸馏塔或蒸馏区,或者精馏塔或精馏区,即液体和蒸气相连续对流接触以进行流体混合物分离的接触塔或区,例如液体和蒸气相在蒸气一液体接触元件上,如塔内安装的一系列垂直相间的塔板上和/或在结构填充元件上和/或在自由填充元件上进行的接触。对于蒸馏塔的进一步讨轮,请参见R.H.Perry和C.H.chil-ton编辑的“化学工程师手册”,第5版,McGraw-Hill Book Company,纽约,第13节,“蒸馏”,B.D.Smith等人,第13-3页,“The Continu-ous Distillation Process”。术语双塔的意思是一个较高压力塔和一个较低压力塔,较高压塔的上端与较低压塔的下端有换热关系。对于双塔的进一步讨轮,请参见Ruheman的“The Separation of Gases”,牛津大学出版社,1949,第Ⅶ章,Commercial Air Separation。
蒸气和液体接触分离过程取决于多组分的蒸气压之差。高蒸气压(或较挥发的或低沸的)组分趋于在蒸气相内浓缩,而低蒸气压(或较不挥发的或高沸的)组分趋于在液相内浓缩。蒸馏是这样一种分离过程,液体混合物加热可用于在蒸气相内浓缩挥发性组分,而较不挥发组分留在液相中。部分冷凝是这样一种分离过程,蒸气混合物的冷却可用于蒸气相内浓缩挥发性组分,而较不挥发性组分留在液相中。精馏,或连续蒸馏是这样一种分离过程,它将由蒸气相和液相的对流处理获得的连续部分蒸发和部分冷凝相结合起来。使用精馏原理分离混合物的分离过程装置常常被通用地称为精馏塔、蒸馏塔或分馏塔。低温精馏是一种至少部分在低温下,如在150°K或低于此温度下进行的精馏过程。
这里所用的术语“间接换热”意指使两种流体流以互不进行接触或相混的形式发生的换热关系。
这里所用的术语“氩塔”意指一个包括一个塔和一个上方冷凝器的***,该***处理含有氩气的物料,产生氩浓度超过物料内氩浓度的产品。
这里所用的术语,增压塔或第二塔的“上部”意指塔的上半部,并且尤指富氧流体通入该塔之点以上的塔部分。
这里所用的术语“填充”意指具有预定构型、大小和形状的用作塔间隔的任何实心或空心体,以在两相逆流流动时,在液体一蒸气界面给液体提供表面积。
这里所用的术语“结构填充”意指各个元件相互之间和相对塔的轴而言,具有特定的指向。
这里所用的术语“涡轮膨胀”意指高压气体流经一涡轮,而使气体压力和温度降低,因而产生冷冻。如发电机、功率计或压缩机等设备是典型用于回收能量的负载设备。
这里所用的术语“吸附净化床”意指用吸附手段从物料流中除去二氧化碳、水气及微量烃类物质的介质。这种介质被放在两个或多个平行的床中。
图1 是本发明的一个优选实施方案的流程图。
图2 是本发明应用一对涡轮膨胀机一压缩机装置的实施方案的流程图。
图3 是本发明应用一对涡轮膨胀机一压缩机装置的另一实施方案的流程图。
图4 是本发明的低温精馏***的一个优选实施方案可达到的优点的图示说明。
本发明涉及一个低温精馏***,其中从一个增压塔中生产出压力较高的产品。从塔的上部排出的增压物流经涡轮膨胀,使得装置冷冻。因此,所有物料可被保持在高压下,并就这样通入高压塔中以进行第一次分离。从该塔流出的流体,凭其较高压力,也被用于再生吸附床的净化器。
下面参考附图更详细地描述本发明。
参考图1,含有氧和氮的物料1,例如空气,由通过型压缩机50压缩,经冷却器2冷却除去压缩热,然后流过吸附净化床51,该净化床除去物料中的水蒸气、二氧化碳和微量烃并使之吸附在吸附剂床颗粒上。为清楚起见,图1仅示出一单个吸附床,实际中会使用2个或多个吸附床,其中一个应用于进行物料净化,而另一个在进行再生。此后进入床的流体被合适的阀改变流向,致使再生过的床用于净化物料,而吸附了杂质的床被再生。一般而言,所用的吸附剂是分子筛,如沸石13X或13X与氧化铝等的结合。
无杂质的高压物料3由导管装置从吸附床51送入主换热器53,其中无杂质物料由间接换热被返回气流,包括一种规定的涡轮膨胀的气流所冷却,这在下面还要详细叙述。无杂质冷却的高压物料4被送入第一塔或高压塔54,该塔是双塔***中的较高压力塔,操作压力一般在95-250磅/平方英寸绝对压力(psia)。在高压塔54内,物料由低温精馏分离成富氮蒸气和富氧液体。
富氧液体从高压塔54流出,通入第二塔或增压塔55,该塔是双塔***中压力较低的塔。在图1所示的实施方案中,还包括一氩塔57,富氧液体被用于驱动氩塔塔顶冷凝器,再通入增压塔55。富氧液体从塔54排出物流5,通入换热器61被冷却,然后作为物流8通过阀59,进入氩塔塔顶冷凝器62,在冷凝器62中,它被部分蒸发而冷凝氩塔塔顶蒸气。得到的富氧蒸气和其余的富氧液体,作为气流9和液流10,被分别通入塔55。
富氮蒸气40从塔54排出,被通入双塔主冷凝器56,在冷凝器56中,它被冷凝而使塔55的塔底组分再沸腾。富氮蒸气40的一部分7可以作为产品高压氮回收,如图1所示,其中部分7由流经主换热器53而被加温,如果需要,再由压缩机66压缩再作为气流32被回收。富氮液体41从主冷凝器56中排出,一部分液体42作为回流液返回塔54,另一部分液体6由流经换热器61被冷却,并通过阀60流入增压塔55使该塔回流。一部分液体13可作为液氮产品而回收。
增压塔55在压力低于塔54的操作压力下操作,但在至少20psia的压力下操作,一般在25至90psia的范围内。这样,由塔55生产的产品是具有较高压力的,因而减少或免去了产品压缩的需要。塔55可在较高压力下以高产品回收率操作,因为没有经压缩的物料需要膨胀以产生冷冻或其它目的,因而液体回流可以达到最大。在增压塔55内,送入该塔的流体由精馏分成富氧流体和富氮流体。富氮蒸气可从塔55的上部作为气流22而排出,受流经的换热器61而加温,受经过的主换热器53再加温,并以增压产品氮气29回收。在图1所示的实施方案中,增压氮产品29被压缩机66进一步压缩,并以部分高压氮产品32回收。该氮产品的纯度一般达99%。
富氧蒸气可从塔55的下部作为气流20排出,由通过主换热器53加温,并以增压氧产品气28回收。在图1所示的实施方案中,增压氧产品28被压缩机65进一步压缩,并以高压氧产品31回收。如果需要,也可以回收得到液氧产品,这可由从塔55排出一股富氧液体流,以液流14所示。该氧产品一般纯度达95%。
较高压含氮流体是从增压塔55上部排出的,最好是从一中间位置排出。此“中间位置”的意思是指在塔顶以下处。通常含氮流体的氮浓度在90-99.99%的范围内,可以是废气也可以是氮产品。以物流或导管21所示的排出的含氮流体,由通过换热器61加温,然后引入主换热器53。较高压氮气的第一部分33完全通过主换热器53。该物流流经吸附净化床以再生该吸附剂,带是所吸的杂质,并从床的流出气流37中除去。氮的较高压力给此以足够的驱动力,以有效通过该床和再生该吸附净化床。
较高压的废氮气的第二部分25是在部分通过后从换热器53排出,并经涡轮膨胀机63进行涡轮膨胀,因而产生冷冻。经涡轮膨胀的物流26然后过换热器53,因而用作冷却物料和使塔***冷冻以进行低温精馏。得到的加温的氮30以物流38排出该***。物流38的部分或全部,以物流35所示,除物流33外,它可通过吸附净化床以再生吸附剂,或者也可用于代替物流33。即使在经涡轮膨胀后,由于物流从增压塔取得的压力较高,因而在物流35中仍有足够的残余压力以通过该净化器并有效地再生吸剂。如果需要,就不要以物流33流动,从塔55上部来的全部较高压物流,可流经物流25至涡轮膨胀机63。
吸附净化床可由少量流体有效地再生。例如,含较高压氮气的气流的流速不需超过物料流速的约20%。因此,第二塔可在较高压力下操作,而不需要为了再生目的将大量废气排放,因而可从第二塔生产出更多的氮产品。
涡轮膨胀机63最好与一负载设备相连接,如示于图1的再生器64,以收集由涡轮膨胀机63产生的能量。
前已述及,图1所示的本发明的实施方案中也包括一氩塔。当物料包括氩,例如物料是空气时,可使用氩塔。在该实施方案中,含氧和氩的物流15从第二塔55排出而进入氩塔57,在此塔57中氩塔的物料被低温精馏分离成富氩流体和富氧流体。富氧流体从氩塔57流出并作为物流16返回较高压塔55。富氩流体作为物流17通入塔顶冷凝器62,在其中它如前面已讨论过的,相对于富氧流体而言被部分冷凝。得到的富氩流体通入相分离器43,从43富氩液体作为回流物流18返回塔57,从43排出气流19并作为粗氩被回收。一般粗氩浓度至少为96.5%。
当使用氩塔时,本发明优选的实施方案是应用填充,优选结构填充,如在增压塔55中的蒸气一流体接触元件那种,也优选塔板,如筛板,如氩塔57中蒸气一液体接触元件那种。在此种场合,优选增压塔全塔使用填充,氩塔则全塔使用塔板。该种安排示于图1的代表性方式中。
增压塔中采用结构填充允许氩以较高比率回收。因此,增压塔可以较高压力操作,当增压塔内使用结构填充时,仍能达到可接受的氩回收率。与使用筛板相比,由于结构填充的压降小,与此有关的是可以实现使用较小功率的物料压缩机的优点。然而,氩塔可以是,并且最好完全是塔板填充的。氩塔的较高压力水平操作意味着,即使使用塔板填充的塔,产品粗氩气流的压力也可达足够高。当塔中塔板填充时,氩塔塔顶的冷凝器内通常存在着满意的温差。氩塔中使用筛板而不用结构填充时,可以实现氩回收的改进。这是由于带塔板的塔的平均操作压力降低,因而改进与氧相比氩的挥发性。这一改进的氩回收图示于图4,其中,以物料中氩的百分数表示的氩回收示于纵坐标上,增压塔在塔顶之下在氮排出点处的压力示于横坐标上。曲线A是当增压塔充满塔板时可达到的氩回收,而曲线B是增压塔充满结构填充时可达到的氩回收,而氩塔在增压塔的压力范围之内是全部被塔板填充的。由图4可知,在一给定压力下,全填充增压塔和全塔板填充氩塔的配置可达到的氩回收可以大大超过常规配置时达到的氩回收。
图2和图3演示了本发明的其它实施例,其中,涡轮膨胀与提高氮压力的压缩机相连。对于一给定的氮产品率和液体产品率,增压塔的压力水平将降低。这在氩生产率方面具有优点,因而在保持可接受的氩回收率之下,允许增加产品氮产率和增加液体产率。图2和图3中与图1中相同的部件的标号也相应,相同的部件这里就不作详细讨论。
现参考图2,含氮部分25经涡轮膨胀机63膨胀至很低压水平,一般低于大气压。这涡轮膨胀产生冷冻。生成的涡轮膨胀气流70由通入主换热器53冷却物料而受加温,然后由压缩机71压缩,该压缩机与涡轮膨胀机63相连并受其驱动。经压缩气流72因此能达到可以流出该过程或驱动经吸附净化床用于再生。
现参考图3示出的实施方案,整个含氮气流21全部通入主换热器53。其后,一部气气流73被压缩机74压缩,该压缩机与涡轮膨胀机63相连并受其驱动。生成的压缩气流75然后在后冷却器76中被冷却,再在主换热器53中被冷却。然后,气流75经涡轮膨胀机63进行涡轮膨胀产生冷冻,生成的气流77经通入主换热器53而加温并冷却物料。气流77然后可放入大气或全部或部分用于再生吸附净化床。
使用本发明,人们可生产较高压的产品氧和/或氮,同时减少或省去产品压缩的需要。本发明应用从双塔***中较低压塔来的较少量但较高压的氮气流的涡轮膨胀,以产生装置冷冻,因而避免了对所有物料进行膨胀的需要。而且,该较高压氮气即使在涡轮膨胀以后,也能有效再生物料的吸附净化床。虽然再生气流可以来自增压塔上部但不经涡轮膨胀的气流,但是最好使用经涡轮膨胀的物流去再生该床。在优选的实施方案中,含氩物料被处理,氩回收可通过使用包含结构填充的增压塔和包含塔板的氩塔得到改进。通过将氮涡轮膨胀机与升高氮气压力的压缩机相连,可以实现增加氮的生产和增加液体的生产,同时保持可接受的氩回收。
虽然本发明参考一些优选实施方案进行了详细描述,但是对于本领域的技术人员而言,也认识到本发明还有其它实施方案,这包括于本申请权利要求的范围和精神之内。
Claims (14)
1、一种产生较高压力产品的低温精馏方法,包括:
(A)将含氧和氮的物料通入一个吸附净化床,将进入床中物料中的可吸附污物除去得到清洁物料;
(B)将该清洁物料冷却,将冷却的清洁物料通入一高压塔,由低温精馏将物料分离成富氮和富氧流体;
(C)将富氮和富氧流体从高压塔通入操作压力比高压塔低但至少20磅/平方英寸的增压塔中,由增压塔内低温精馏生产出富氮和富氧流体;
(D)从增压塔上部除去含氮流体,使该含氮流体经过涡轮膨胀,产生冷冻,将所得含氮流体以间接换热方式与物料接触使之冷却;
(E)将从增压塔的含氮流体通入吸附净化床,使该床再生;及
(F)从增压塔回收富氮和富氧流体的至少一种作为增压产品。
2、权利要求1的方法,其中的物料是空气。
3、权利要求1的方法,其中步骤(E)中用于再生吸附净化床的含氮流体是在步骤(D)中经涡轮膨胀的流体。
4、权利要求1的方法,其中步骤(E)中用于再生吸附净化床的含氮流体在用于再生前未经过涡轮膨胀。
5、权利要求1的方法,其中含氮流体在涡轮膨胀前被压缩。
6、权利要求1的方法,其中含氮流体在涡轮膨胀后被压缩。
7、权利要求1的方法,其中物料含有氩,方法还包括使增压塔流出的含氩流体通入氩塔,并由低温精馏在氩塔内产生一富氩流体。
8、权利要求7的方法,其中在增压塔内的低温精馏是在含有结构填充的蒸气一流体接触元件上进行的,在氩塔内的低温精馏是在含有塔板的蒸气一液体接触元件上进行的。
9、一种低温精馏装置,包括:
(A)一吸附净化床,一主换热器和将物料从吸附净化床通入主换热器的装置;
(B)一塔***,包括第一塔的第二塔,将物料从主换热器通入第一塔的装置和将流体从第一塔通入第二塔的装置;
(C)从第二塔上部排放流体的装置;
(D)一涡轮膨胀机,将从第二塔上部排出的流体通入该涡轮膨胀机的装置和将膨胀后的流体从该涡轮膨胀机通入主换热器的装置;
(E)将从第二塔上部排出的流体通入吸附净化床的装置;及
(F)从第二塔回收产品流体的装置。
10、权利要求9的装置,其中将从第二塔上部排出的流体通入吸附净化床的装置包括涡轮膨胀机。
11、权利要求9的装置,其中将从第二塔上部排出的流体通入吸附净化床的装置不包括涡轮膨胀机。
12、权利要求9的装置,其中的涡轮膨胀机是与一压缩机相连。
13、权利要求9的装置,还包括一氩塔,将流体从第二塔通入氩塔的装置和从氩塔回收流体的装置。
14、权利要求13的装置,其中第二塔装有包含结构填充的蒸气一液体元件,氩塔装有包含塔板的蒸气一液体接触元件。
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US07/823,685 US5197296A (en) | 1992-01-21 | 1992-01-21 | Cryogenic rectification system for producing elevated pressure product |
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- 1993-01-20 JP JP5023428A patent/JPH05256569A/ja active Pending
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- 1993-01-20 CN CN93101149A patent/CN1074528C/zh not_active Expired - Fee Related
- 1993-01-20 EP EP93100824A patent/EP0552747B2/en not_active Expired - Lifetime
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---|---|---|---|---|
CN106232197A (zh) * | 2014-05-23 | 2016-12-14 | 株式会社神户制钢所 | 蒸馏装置 |
CN106232197B (zh) * | 2014-05-23 | 2018-09-25 | 株式会社神户制钢所 | 蒸馏装置 |
Also Published As
Publication number | Publication date |
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MX9300286A (es) | 1993-07-01 |
CN1074528C (zh) | 2001-11-07 |
DE69301033T3 (de) | 1999-06-10 |
BR9300227A (pt) | 1993-07-27 |
CA2083562A1 (en) | 1993-07-22 |
KR0144128B1 (ko) | 1998-07-15 |
EP0552747B1 (en) | 1995-12-20 |
ES2081143T5 (es) | 1999-04-01 |
EP0552747A1 (en) | 1993-07-28 |
DE69301033T2 (de) | 1996-09-05 |
KR930016748A (ko) | 1993-08-26 |
DE69301033D1 (de) | 1996-02-01 |
ES2081143T3 (es) | 1996-02-16 |
JPH05256569A (ja) | 1993-10-05 |
US5197296A (en) | 1993-03-30 |
CA2083562C (en) | 1996-04-23 |
EP0552747B2 (en) | 1999-01-20 |
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