CN1106563C - 具有热透平循环系统的低温空气分离 - Google Patents

具有热透平循环系统的低温空气分离 Download PDF

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CN1106563C
CN1106563C CN98115108A CN98115108A CN1106563C CN 1106563 C CN1106563 C CN 1106563C CN 98115108 A CN98115108 A CN 98115108A CN 98115108 A CN98115108 A CN 98115108A CN 1106563 C CN1106563 C CN 1106563C
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air
low temp
fractionation system
compressor
heat exchanger
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CN1200476A (zh
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H·E·霍瓦德
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Praxair Technology Inc
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    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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Abstract

一种低温空气分离系统，其中进料空气在一台多级初级空气压缩机中压缩，使第一部分进行透平膨胀后送入低温空气分离设备，使第二部分进行透平膨胀后，将已透平膨胀后的第二部分中的至少一部分再循环回到该初级空气压缩机的级间位置。

Description

具有热透平循环系统的低温空气分离
本发明一般地涉及低温空气分离，更具体地说；它涉及低温空气分离系统，其中来自低温空气分离设备的液体在回收之前蒸发。
氧气是通过进料空气在一台低温空气分离设备内低温精馏而在商业上大量生产的。有时也需要生产较高压力的氧气。当气态氧可从低温空气分离设备抽出并压缩到所需压力时，为了节省投资，一般优选从低温空气分离设备抽出液体氧，增加液体氧的压力，接着蒸发已压缩的液氧，来生产所需的高压产品氧气。
氧作为液体从低温分离设备抽出从需要大量冷量回用的设备中消除了大量冷量。除了高压氧气外，甚至在需要从设备回收液体产物，如液氧和/或液氮的情况下更是这样。
向低温空气分离设备提供致冷的一种非常有效的方法是使一股已压缩的气流进行透平膨胀，并将那股气流，或将至少因此产生的冷量送入该设备。在从该设备抽出大量液体的情况下，常要使用一个以上的这样的透平膨胀机。但是，就低温空气分离设备和初级空气压缩机而言，由于涡轮流动和压力间的小差异会引起系统效率急剧下降，导致系统不经济，因此多个透平膨胀机的使用是很复杂的。
因此，本发明的一个目的就是提供一种使用一个以上透平膨胀机的用于进料空气低温精馏的改进系统。
通过阅读说明书，对本领域的技术人员来说，上述及其它目的会变得更明显，这些目的可以通过本发明实现，其一个方面是：
一种进行低温空气分离的方法，包括：
(A)在一台具有第一至第n多个压缩级的初级空气压缩机中压缩进料空气，以生产已压缩的进料空气；
(B)冷却所述已压缩进料空气的第一部分，使该已冷却的第一部分进行透平膨胀，且把该已透平膨胀的第一部分送入一台低温空气分离设备；
(C)进一步压缩该已压缩过的进料空气的第二部分，冷却该已进一步压缩后的第二部分，使该已冷却的第二部分中的至少一部分进行透平膨胀，并使该已透平膨胀的第二部分中的至少一部分再循环回到第一和第n压缩级之间的进料空气；
(D)在该低温空气分离设备中生产液氧，从该低温空气分离设备中抽出液氧，并通过与正在冷却的进料空气的第一部分和正在冷却的进料空气的第二部分间接换热，使该已抽出的液氧蒸发，生产出气态氧及；
(E)回收气态氧作为产品。
本发明的另一个方面是：
进行低温空气分离的装置，包括：
(A)一台具有第一至n多个压缩级的初级空气压缩机，一台主换热器，一台初级透平膨胀机，及一台低温空气分离设备；
(B)用于把进料空气送入该初级空气压缩机第一级的装置，及用于从该初级空气压缩机的第n级抽出进料空气的装置；
(C)用于把进料空气从该初级空气压缩机的第n级送到主换热器，从主换热器送到初级透平膨胀机，及从该初级透平膨胀机送到该低温空气分离设备的装置；
(D)一台辅助压缩机，一台第二级透平膨胀机，将进料空气从初级空气压缩机的第n级送到该辅助压缩机、从该辅助压缩机送到该主换热器、从该主换热器送到第二级透平膨胀机，及从该第二级透平膨胀机送到1至n压缩级之间的初级空气压缩机的装置；及
(E)将液体从低温空气分离设备送到该主换热器的装置，及从该主换热器回收蒸汽的装置。
此处所用术语“液氧”意指氧摩尔百分比浓度大于50。
此处所用的术语“塔”意指一种蒸馏或精馏塔或区，即一种接触塔或区，在其中液、汽两相逆流接触以实现液体混合物的分离，例如借助汽、液两相在一系列沿塔内纵向间隔安装的塔盘或塔板上，和/或在有规马放和/或无规堆放的填料元件上进行接触。关于蒸馏塔的进一步讨论，请参见“Chemical Engineer’sHandbook fifth edition”(《化学工程师手册·第五版》)，由R·H·perry和C·H·Chilton编，McGraw-Hill Book Company出版。NewYork，Section 13，“连续蒸馏过程”。术语双塔常指一种其上端与一低压塔的下端有热交换的较高压力的塔。关于双塔的进一步讨论，请参见Ruheman的“气体的分离”，牛津大学出版社，1949，第七章，商用空气分离。
汽、液接触分离过程取决于各组分的蒸汽压差。高蒸汽压(易挥发或低沸点)组分将浓集在气相中，而低蒸汽压(难挥发或高沸点)组分将浓集在液相中。部分冷凝是一种分离过程，其中冷却的蒸汽混合物将易挥发组分浓集在汽相中，从而将不易挥发的组分浓集在液相中。精馏或连续蒸馏是一种分离过程，如同在借助对汽液相施以逆流处理而达到的那样，该过程把连续的部分蒸发与冷凝结合一体。汽、液相的逆流接触是绝热的，且可包括相间的积分(分段)或微分(连续)接触。应用精馏原理分离混合物的分离过程的设备常常用几个可互换的术语表示：精馏塔、蒸馏塔或分馏塔。低温精馏是一种精馏过程，该精馏过程至少一部分在150°K或更低温度下进行。
此处所用的术语“间接换热”意指让两种液体流在没有任何物理接触或彼此间流体不相互混合时的换热关系。
此处所用的术语“进料空气”意指一种主要含有氮和氧的混合物，例如环境空气。
此处所用的术语塔的“上部”和“下部”分别指塔上比塔中点高和低的那些部分。
此处所用的术语“透平膨胀”和“透平膨胀机”分别指使高压气体通过涡轮机降低气体的压力和温度，而产生致冷作用的方法和设备。
此处所用的术语“压缩机”意指一种通过作功能增加气体压力的机器。
此处所用的术语“低温空气分离设备”意指用来分馏进料空气的设备，包括一个或多个塔及管道，阀门和附属的换热设备。
此处所用的术语“初级空气压缩机”指为使低温空气分离设备运行提供所需的绝大部分空气压缩的空气压缩机。
此处所用的术语“辅助压缩机”意指一台压缩机，该压缩机提供附加压缩，以便达到液氧蒸发和/或连同低温空气分离设备的分步涡轮膨胀所需要的较高空气压力。
此处所用的术语“压缩级”意指压缩机的单个部件，例如压缩机的压缩轮，通过该部件，气体的压力升高。一台压缩机必定由至少一个压缩级组成。
图1是本发明的一优选实施例的示意图；
图2是本发明的另一个优选实施例的示意图；
图中相同的附图标记表示相同的部件。
在本发明的应用中，一部分进料空气绕过使进料空气膨胀的初级透平膨胀机，进入低温空气分离设备，且代之以在一台第二级透平膨胀机中膨胀，并再循环回到初级空气压缩机的中间级位置。这就减少了初级空气压缩机的功率消耗，从而提高了低温空气分离系统的总体效率。
下面将参照附图更详细地描述本发明。参见图1，压力约为大气压的进料空气50通过过滤室1，被除去了杂质。所产生的进料空气51接着送入初级空气压缩机13，在图1所示的本发明的实施例中，初级空气压缩机具有5个压缩级，第5或最后一级是第n级。在本发明的应用中，初级空气压缩机一般具有至少3个压缩级，典型地具有4至6个压缩级。进料空气51送入初级空气压缩机13的第1压缩级2，在其中被压缩，所产生的进料空气52通过中间冷却器3而冷却。进料空气52接着通过初级空气压缩机13的第2压缩级4进一步压缩，所产生的进料空气53通过中间冷却器5冷却，进料空气53接着通过初级空气压缩机13的第3压缩级6再一次压缩，所产生的进料空气54通过中间冷却器7冷却。进料空气54接着送入预纯化器8，在其中除去高沸点杂质，如二氧化碳、水蒸汽和碳氢化合物。
纯化后的进料空气55接着送入初级压缩机13的第4压缩级9。如在图1中所示的本发明的实施例那样，优选使进料空气流55在汇合点56处并入加温涡轮再循环，所产生的合并的进料空气流57送入第4压缩级9，在其中压缩到一个较高压力。所产生的进料空气流58通过中间冷却器10冷却，接着送入初级空气压缩机13的第5压缩级11，在其中压缩到一个较高压力，并从第5压缩级中抽出，作为绝对压力范围为1379至5171kPa(200至750磅/平方英寸)的已压缩的进料空气流59。初级空气压缩机13由一台带有一个驱动主齿轮60的转子的外部电机(未示出)驱动。
已压缩的进料空气59通过后冷却器12冷却，并分为第一部分61和第二部分62。第一部分61约占已压缩进料空气59的50％至55％。将第一部分61送到主换热器17，在其中通过与返回流间接换热而冷却。在主换热器17的部分管程之后，已冷却的第一部分63送到初级透平膨胀机19，在其中被透平膨胀到448至586kPa(65至85磅/平方英寸)的透平压力。所产生的已透平膨胀的第一部分64送入低温空气分离设备。在图1所示的实施例中，该低温空气分离设备是一台包括第一或高压塔20和第二或低压塔22的双塔设备，且已透平膨胀的第一部分64送入高压塔20的下部。
第二部分62占已压缩料空气59的45％至50％。第二部分62送到辅助压缩机15，在其中进一步压缩到3447至9653kPa(500至1400磅/平方英寸)的压力。已进一步压缩的第二部分66通过冷却器16冷却，接着送入主换热器17，在其中通过与返回流间接换热而冷却。如图1中所示流67，该已冷却的第二部分中的至少有一部分在主换热器17的部分穿程之后抽出，并送到第二级透平膨胀机18，在其中被透平膨胀到517至1034kPa(75至150磅/平方英寸)的压力。所产生的已透平膨胀的第二部分68通过主换热器17的部分穿程而加热，接着再循环回到初级空气压缩机的第1和最后一级之间，也就是一个中间级位置。在图1所示的实施例中，为了再循环回到初级空气压缩机13的第3和第4压缩级之间，膨胀过的热循环气流69在再循环回到进料空气55合并点之前先通过压力控制装置14。例如，压力控制装置可以是一个阀、一台压缩机或一台送风机。
如果需要的话，可使第二部分66中的一部分完全穿过主换热器17，使它在其中液化。如图1实施例中70所示，这一部分通过阀23，进入高压塔20。部分70可以不通过阀23，而是通过一台密相(即超临界液体或液体)透平膨胀机来回收压力能。所回收的轴功一般将驱动一台发电机。
高压塔20通常在448至586kPa(65至85磅/平方英寸)的压力范围内运行。在高压塔20内进入塔20的进料空气通过低温精馏分离成富氮蒸汽和富氧液。富氧液从高压塔20下部抽出，作为流71，通过过冷器25过冷，并经过阀28进入低压塔22。富氮蒸汽从高压塔20抽出，作为流72，并送入主冷凝器21，在其中通过与低压塔22底部的沸腾液体间接换热而冷凝。所产生的富氮液73从主冷凝器21抽出，第一部分74作为返回流返回到高压塔20，第二部分75通过过冷器26过冷，并通过阀27，进入低压塔22。如果需要的话，该富氮液的一部分也可以回收，作为百分摩尔氮浓度至少为99.99的产品液氮。在图1所示的本发明的实施例中，富氮液75的一部分76通过阀30，并被回收为液氮产品77。
低压塔22在比高压塔20低的压力范围内运行，一般为103至172kPa(15至25磅/平方英寸)。在低压塔22内，不同的进料通过低温精馏分离成富氮蒸汽和富氧液。富氮蒸汽从低压塔22上部抽出，作为流78，通过换热器26、25及17加热，并被从系统中抽出，作为百分摩尔氮浓度至少为99.99的产品氮气79。为了控制产品纯度，一股含氮流80从低压塔22上的低于流78被抽出的高度处抽出。流80通过换热器26、25和17加热，并从该系统中抽出，作为流81。
富氧液，也即液氧，作为液氧流82从低压塔22下部抽出。如果需要的话，也可象图1所示的实施例中那样，回收该富氧液的一部分，作为产品液氧，图1中流83从流82中分出，通过阀29，并回收为液氧流84。
富氧液在蒸发前压力就提高了。在图1，所示的实施例中，流82的大部分85送到液体泵24，在其中被升压到1034至9653kPa(150至1400磅/平方英寸)。所产生的已压缩的液氧流86通过主换热器17，在其中通过与正在冷却的第一进料空气部分61和正在冷却的第二进料空气部分66间接换热而蒸发。所产生的气态氧从主换热器器17抽出，作为流87，并被回收为百分摩尔氧浓度至少为50的产品气态氧。该液氧通过主换热器17有效蒸发，而不是在单独的产品蒸发器中，因为这样能使流61的部分冷量传给流86，从而减少了辅助的进料空气流66所需的压力。此外，也可省去流86的蒸发所需的一台第二换热器装置。
图2表示本发明的另一个实施例。对图2的实施例中所示的那些与图2的实施例中所示的相同的部件将不再详细描述。
现参见图2；已进一步压缩的第二部分66，在通过冷却器16后分成流88和流89。流89通过压缩机31进一步压缩，并通过冷却器32除去压缩热，再通过主换热器17，在其中被液化。所产生的液体进料空气90通过阀23，进入高压塔20。进料空气90可以通过阀23，而是通过一台密相透平机来回收压力能，该已回收的轴功一般用来驱动一台发电机。第二部分66的流88通过主换热器17冷却，并通过第二级透平膨胀机18进行透平膨胀。所产生的已透平膨胀的流91分出流92，流92通过压力控制装置14，并再循环回到初级空气压缩机，并成为流93，该流93在主换热器17内冷却，通过阀33，并与初级透平膨胀机排出流64合并，以形成送入低温空气分离设备65的高压塔20的流94。图2所示的本发明的实施例在辅助压缩机15的排量不足以加热正在蒸发的氧流86时尤其有利。热透平膨胀流91分成流92和93可有效地用于再循环流92的流量大于所需的液体产品需求排放量的场合。通过增加流93，也就是再循环旁通流的流量，可以减少该过程的功率损耗，使得能够有效地生产液体产品。
在本发明的实施例中，至少一部分热透平轮排出量再循环回到初级空气压缩机的中间级位置，就可利用多个透平膨胀机有效地进行低温空气分离。尽管已参照某些最优选的实施例详细描述了本发明，但是本领域的技术人员可以认识到，在本发明权利要求书的精神和范围内还可以有其它实施例。例如，低温空气分离设备可以具有单个塔，或具有3个或3个以上的塔，比如低温空气分离设备可以是具有一个氩塔的双塔。可以用一台外部电机或利用透平膨胀机18和19产生的轴功驱动辅助压缩机15和31。

Claims (10)

1、一种进行低温空气分离的方法，包括：
(A)在一台具有第一至第n多个压缩级的初级空气压缩机中压缩进料空气，以生产已压缩的进料空气；
(B)冷却所述已压缩进料空气的第一部分，使该已冷却的第一部分进行透平膨胀，且把该已透平膨胀的第一部分送入一台低温空气分离设备；
(C)进一步压缩该已压缩过的进料空气的第二部分，冷却该已进一步压缩后的第二部分，使该已冷却的第二部分中的至少一部分进行透平膨胀，并使该已透平膨胀的第二部分中的至少一部分再循环回到第一和第n压缩级之间的进料空气；
(D)在该低温空气分离设备中生产液氧，从该低温空气分离设备中抽出液氧，并通过与正在冷却的进料空气的第一部分和正在冷却的进料空气的第二部分间接换热，蒸发该已抽出的液氧，生产气态氧及
(E)回收气态氧作为产品。
2、如权利要求1的方法，其中已透平膨胀的第二部分中的一部分与已透平膨胀的第一部分合并，并送入该低温空气分离设备。
3、如权利要求1的方法，进一步包括从该低温空气分离设备中回收液氧。
4、如权利要求1的方法，进一步包括在该低温空气分离设备中生产液氮，并从该低温空气分离设备中回收液氮。
5、进行低温空气分离的装置，包括：
(A)一台具有第一至n多个压缩级的初级空气压缩机，一台主换热器，一台初级透平膨胀机，及一台低温空气分离设备；
(B)用于把进料空气送入该初级空气压缩机第一级的装置，及用于从该初级空气压缩机的第n级抽出进料空气的装置；
(C)用于把进料空气从该初级空气压缩机的第n级送到主换热器、从主换热器送到该初级透平膨胀机，及从该初级透平膨胀机送到该低温空气分离设备的装置；
(D)一台辅助压缩机，一台第二级透平膨胀机，用于把进料空气从初级空气压缩机的第n级送到辅助压缩机、从辅助压缩机送到主换热器、从主换热器送到第二级透平膨胀机、及从第二级透平膨胀机送到初级空气压缩机的第一至第n压缩级之间的装置；及
(E)用于把液体从低温空气分离设备送到主换热器的装置，及用于从主换热器回收蒸汽的装置。
6、如权利要求5的装置，其中初级空气压缩机至少具有3个压缩级。
7、如权利要求5的装置，其中用于把液体从低温空气分离设备送到主换热器的设备包括一台液体泵。
8、如权利要求5的装置，其中低温空气分离设备包括一个具有一个高压塔和一个低压塔的双塔。
9、如权利要求8的装置，其中用于把进料空气从初级透平膨胀机送到低温空气分离设备的装置与高压塔相连。
10、如权利要求5的装置，进一步包括用于把进料空气从第二级透平膨胀机送入低温空气分离设备的装置。
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DE69801462T3 (de) 2008-03-20
CA2237044C (en) 2002-01-22
ES2159905T3 (es) 2001-10-16
EP0877217B1 (en) 2001-08-29
KR100343276B1 (ko) 2002-08-22
DE69801462D1 (de) 2001-10-04
CA2237044A1 (en) 1998-11-08
EP0877217B2 (en) 2007-10-17
EP0877217A1 (en) 1998-11-11
BR9801590A (pt) 1999-09-28
US5758515A (en) 1998-06-02
CN1200476A (zh) 1998-12-02
ES2159905T5 (es) 2008-04-01
DE69801462T2 (de) 2002-05-23
ID20671A (id) 1999-02-11

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