CN100554838C - 用于生产高压氮的深冷*** - Google Patents
用于生产高压氮的深冷*** Download PDFInfo
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Abstract
用于生产高压氮的深冷空气分离***,其中将进料到主换热器(101)的下游的产品压缩机(110)的氮产品的一部分作为制冷剂氮从产品压缩机(110)中取出,优选从产品压缩机(110)的中间点取出,并且进行涡轮膨胀,以为所述***产生制冷作用。
Description
技术领域
本发明一般地涉及深冷空气分离,更具体地涉及用于生产高压氮的深冷空气分离。
背景技术
一些工艺,例如提高油回收的工艺,需要大量的高压氮,这些氮是通过空气的深冷分离生产的。对于这样的空气分离***,有效地产生制冷作用是特别重要的,特别是还需要生产某些液体产品时更是如此。此外,对液体产品的波动需求增加了对有效地产生制冷作用的设备的需要。
在使用进料空气膨胀的***中,提高的液体需求显著地降低了产品回收率,必需大大提高动力消耗,并且要求进料压缩机具有过大的可调范围。对于双塔氮装置,氮回收率的大幅度降低还导致大的塔压力变化。这还导致装置具有差的可操作性。在使用无用的膨胀的***中,提高的液体需求要求显著地提高塔压力,这将降低产品回收率,并且极大地提高装置的动力消耗。改变塔压力将不利地影响装置的可操作性。使用产品氮膨胀的常规模式的***在以下两个方面之一中存在不足:(1)提高的液体需要量要求产品压缩机的较低的级具有过大的可调范围,或者(2)如果被设计成能适当地适应变化的液体需要量,现有的产品膨胀方法将需要多个涡轮机,并且在高压下操作,这将严重地限制热交换器芯的选择。
因此,本发明的目的是提供改进的通过空气的深冷分离生产高压氮的***。
发明内容
本领域技术人员在阅读本发明时将清楚的上述及其他目的通过本发明而达到。本发明的一个方面是:
用于生产高压氮的深冷空气分离装置,其包括:
(A)主换热器,深冷空气分离装置,和用于将进料空气送到主换热器和从主换热器送到深冷空气分离装置的设备;
(B)具有多个级的产品压缩机,涡轮膨胀机,用于将氮从深冷空气分离装置送到主换热器和从主换热器送到产品压缩机的设备,和用于将氮从产品压缩机送到主换热器和从主换热器送到涡轮膨胀机的设备;
(C)增压压缩机,用于将氮从涡轮膨胀机送到主换热器和从主换热器送到增压压缩机的设备,和用于将氮从增压压缩机送到产品压缩机的设备;和
(D)用于从产品压缩机回收高压氮的设备。
本发明的另一个方面是:
用于生产高压氮的方法,其包括:
(A)将进料空气在主换热器中冷却,将冷却的进料空气送到深冷空气分离装置中,和通过在深冷空气分离装置内进行深冷精馏生产氮;
(B)将从深冷空气分离装置抽出的氮在主换热器中加热,将加热的氮在产品压缩机中压缩,将一部分压缩的氮作为制冷剂氮送到主换热器,将制冷剂氮冷却,并且使制冷剂氮进行涡轮膨胀以产生制冷作用;
(C)将涡轮膨胀的制冷剂氮在主换热器中加热,将涡轮膨胀的制冷剂氮在增压压缩机中压缩,和将得到的制冷剂氮送到产品压缩机;和
(D)从产品压缩机回收高压氮。
正如在此使用的,术语“塔”指蒸馏或者分馏塔或者区,即接触塔或者区,其中液相和蒸气相被逆流地接触,以进行流体混合物的分离,例如在塔内安装的一系列垂直间隔的塔盘或者塔板上和/或在结构化的或者随机填装的填料元件上使蒸气相与液相接触。关于蒸馏塔的进一步讨论,参考R.H.Perry和C.H.Chilton编著的“化学工程师手册”,第五版,McGraw-Hill Book Company,纽约,第13部分,连续蒸馏工艺。术语“双塔”用来指较高压力的塔和较低压力的塔,该较高压力的塔的上端与较低压力的塔的下端处于热交换关系。双塔的进一步讨论见于Ruheman“气体的分离”,牛津大学出版社,1949,第VII章,工业空气分离。
蒸气和液体接触分离工艺依赖于组分的蒸气压的差异。高蒸气压(或者更具挥发性的或者沸点低的)组分倾向于在气相中浓缩,而低蒸气压(或者较小挥发性的或者高沸点的)组分倾向于在液相中浓缩。部分冷凝是这样一种分离工艺,借助于该分离工艺,蒸气混合物的冷却可用于将挥发性组分在气相中浓缩,并且因此将较低挥发性组分在液相中浓缩。精馏,或者连续蒸馏,是这样一种分离工艺,其通过蒸气相与液相的逆流处理实现了连续的局部汽化和冷凝。蒸气相与液相的逆流接触一般是绝热的,并且可以包括所述相之间的积分(分级的)或者微分(连续的)接触。利用精馏原理分离混合物的分离工艺设备经常可互换地称为精馏塔、蒸馏塔或者分馏塔。深冷精馏是这样一种精馏工艺,其至少部分地在等于或低于150开氏度(K)的温度下进行。
正如在此使用的,术语“间接热交换”是指使两种流体处于热交换关系,但是不存在任何物理接触或者所述流体互相之间的混合。
正如在此使用的,术语“进料空气”指主要地包含氧和氮的混合物,例如环境空气。
正如在此使用的,术语塔的“上部”和“下部”指分别高于和低于塔的中点的塔的部分。
正如在此使用的,术语“涡轮膨胀”和“涡轮膨胀机”分别指方法和设备,它们用于使高压气体流动通过涡轮机,以降低气体的压力和温度,因此产生制冷作用。
正如在此使用的,术语“深冷空气分离装置”指塔或者多个塔,在其中进料空气借助于深冷精馏被分离以生产氮,以及视需要的氧和/或氩,以及互联管道、阀、换热器等等。
正如在此使用的,术语“压缩机”指通过作功来提高气体压力的机器。
正如在此使用的,术语“氮”指氮浓度为至少98摩尔百分数的流体。
正如在此使用的,术语“增压压缩机”指通过施加由涡轮膨胀机产生的功提高离开涡轮膨胀机的氮的压力的机器。
正如在此使用的,术语“压缩级”指压缩机的单一元件,例如压缩轮,气体通过它时压力增大。压缩机必须由至少一个压缩级组成。
正如在此使用的,术语“顶部冷凝器”指热交换设备,其由塔的蒸气产生塔的向下流动的液体。
正如在此使用的,术语“过冷却器”指一种热交换器,其中通过与一种或多种加热物流进行间接热交换将液体冷却到低于在存在的压力下该液体的饱和温度的温度。
附图说明
唯一的附图是本发明优选实施方案的略图,其中深冷空气分离装置是双塔***,包括较高压力塔和较低压力塔。
详细说明
本发明包括新颖的用于将深冷空气分离装置制冷的***,其中产品氮压缩机被用于提高制冷剂氮在涡轮膨胀之前的压力。本发明可以用于将装置制冷,该装置可以仅仅生产高压氮,或者除高压氮之外还生产氧和/或氩。
现在参考附图更详细地讨论本发明。现在参考附图,进料空气1,其已经被净化,除去了高沸点杂质例如水蒸汽、二氧化碳和烃,通过与返回物流在主换热器101中进行间接热交换被冷却。主换热器101可以是单件的,虽然主换热器可以并且优选包含多个模块。然后,净化和冷却的进料空气2从主换热器101被送到深冷空气分离装置,在附图中举例说明的实施方案中,该深冷空气分离装置包括较高压力的塔102和较低压力的塔104。在该实施方案中,进料空气2被送到较高压力的塔102。
较高压力的塔102在通常90到150每平方英寸绝对磅数(psia)范围内的压力下操作。在较高压力的塔102内,进料空气通过深冷精馏被分离成富氧液体和较高压力的氮蒸气。在物流3中,从较高压力的塔102的较低的部分抽出富氧液体,并且送到过冷却器106,在其中将其过冷。然后将过冷的富氧液体在物流4中送到阀113,然后作为物流5进入较低压力的塔104,其在低于较高压力的塔102并且通常在50到75psia范围内的压力下操作。
被送到较低压力的塔104的进料通过深冷精馏被分离成较低压力的氮蒸气和氧液体。较高压力的氮蒸气在管线6中从较高压力的塔被送到主冷凝器或者重沸器103,在其中通过与沸腾的氧液体间接热交换而被冷凝,以为塔104提供向上流动的蒸气。得到的冷凝的较高压力的氮在管线9中被返回到塔102,作为回流。在管线11中从塔104的较低的部分抽出氧液体,并且通过过冷却器106被过冷。物流12中的过冷的氧液体通过阀114并且作为物流13被送到顶部冷凝器105。
在管线16中,较低压力的氮蒸气从较低压力的塔104的上部被送到顶部冷凝器105,在其中其通过与在物流13中提供到顶部冷凝器105的沸腾的过冷的氧间接热交换被冷凝。得到的冷凝的较低压力的氮在管线19中被返回到塔104,作为回流。根据需要,冷凝的较低压力氮的部分20可以作为产品液体氮被回收。在物流14中从顶部冷凝器105抽出蒸发的氧,通过从过冷却器106和主换热器101中通过而被加热,并且在物流25中从***中除去。
氮从深冷空气分离装置被送到主换热器,然后被送到产品压缩机。在附图中举例说明的实施方案中,来自较高压力的塔和较低压力的塔两者的氮被送到产品压缩机。再参考附图,氮从较高压力塔102的上部被送到主换热器101,然后被送到产品压缩机110。在附图中举例说明的本发明的实施方案中,物流6的一部分作为氮物流7被送到过冷却器106,在其中其被加热,然后在物流10中从过冷卸器106送到主换热器101,在其中其被进一步加热。得到的氮在物流31中从主换热器101中抽出,并且送到产品压缩机110。
物流16的一部分作为氮物流17被送到过冷却器106,在其中其被加热,然后在物流22中从过冷却器106送到主换热器101,在其中其被进一步加热。得到的氮在物流23中从主换热器101中抽出,并且送到产品压缩机110。
产品压缩机110包括2到6个级。将一部分压缩的氮取出,优选从产品压缩机110的中间点,即在第一级之后,但是在最后一级之前的点取出,并且作为制冷剂氮物流26送到主换热器101,在其中其被冷却,然后在物流34中从主换热器101送到涡轮膨胀机109,在其中其进行涡轮膨胀以产生制冷作用。在物流28中将得到的具有制冷作用的制冷剂氮从涡轮膨胀机109送到主换热器101,在其中其被加热以为进料空气提供冷却。然后在物流29中将得到的制冷剂氮从主换热器101送到增压压缩机108。
附图举例说明了本发明操作的两种不同的模式。在第一种模式中,该模式在回收很少的或不回收液体氮产品时使用,例如当物流20不被使用时,在产品压缩机110的较低的或者上游的级之后,例如在第一个压缩级之后,在物流43中将制冷剂氮抽出,通过阀120,并且作为物流45用于形成上述的物流26。在第二种模式中,该模式在回收液体氮产品时使用,即在使用物流20时,将制冷剂氮在物流42中从产品压缩机110的较高的或者下游的级抽出,通过阀119并且作为物流44用于形成上述的物流26。在该第二种模式中,物流42可以从压缩机110的最后压缩级之后取出。通常,在第一种模式中,物流26将处于50到340psia的压力下,而在第二种模式中,物流26将处于90到700psia的压力下。
优选,正如附图中所示,增压压缩机108与涡轮膨胀机109机械地偶联,并且涡轮膨胀机109用来驱动增压压缩机108。在增压压缩机108中,物流29中的氮被压缩到通常为20到390psia的压力。得到的增压的氮35在后冷却器111中被冷却,除去压缩热,形成增压的氮物流30,其被送到主产品压缩机110。在如上所述的第一种模式中,此时回收很少的或者不回收液体氮产品,增压的氮在管线47中通过阀122,并且作为物流49与物流23合并,被送到产品压缩机110的上游的级,例如进口,其压力在20到220psia范围内。在如上所述的第二种模式中,此时回收液体氮产品,增压的氮在管线46中通过阀121,并且作为物流48与物流31合并,以50到390psia的压力送到产品压缩机110。正如可以从附图中看到的,物流31在这样的级被送到产品压缩机110,该级位于物流23被送到产品压缩机110的压缩级的下游。氮在物流32中从主产品压缩机110的最后一级抽出,并且作为产品高压氮回收,其压力通常在150到5000psia范围内。
本发明利用了这样的事实,即在从主换热器出来之后需要对氮产品进行进一步压缩。通过从主产品压缩机取出仅仅一部分、通常大约3到25%的氮蒸气流用于制冷,提供给主产品压缩机的主产品压缩机流的主要部分保持不变,与制冷需求无关。此外,因为氮蒸气进行涡轮膨胀产生制冷作用,然后被送到增压压缩机,而不是用相反的方式进行,因此制冷剂操作压力保持在合理的范围,与液体需求无关。
附图中举例说明的设备的变化方案包括使用平行的涡轮机-增压压缩机***,如果宽的制液范围能力是重要的。
虽然已经参考某些优选的实施方案详细描述了本发明,本领域技术人员将理解,在权利要求的精神和范围内存在本发明的其他实施方案。
Claims (10)
1.用于生产高压氮的深冷空气分离装置,其包括:
(A)主换热器,深冷空气分离装置,和用于将进料空气送到主换热器和从主换热器送到深冷空气分离装置的设备;
(B)具有多个级的产品压缩机,涡轮膨胀机,用于将氮从深冷空气分离装置送到主换热器和从主换热器送到产品压缩机的设备,和用于将氮从产品压缩机送到主换热器和从主换热器送到涡轮膨胀机的设备;
(C)增压压缩机,用于将氮从涡轮膨胀机送到主换热器和从主换热器送到增压压缩机的设备,和用于将氮从增压压缩机送到产品压缩机的设备;和
(D)用于从产品压缩机回收高压氮的设备。
2.权利要求1的装置,其中所述深冷空气分离装置包括较高压力的塔和较低压力的塔,其中来自较高压力的塔和较低压力的塔两者的氮被送到产品压缩机。
3.权利要求1的装置,其还包括过冷却器,其中用于将氮从深冷空气分离装置送到主换热器的设备包括该过冷却器。
4.权利要求1的装置,其中用于将氮从产品压缩机送到主换热器的设备从产品压缩机的中间点取出氮。
5.权利要求1的装置,其中用于将氮从产品压缩机送到主换热器的设备包括第一管道,其具有阀门并且与产品压缩机在第一位置连通,和第二管道,其具有阀门并且与产品压缩机在第二位置连通,该第二位置位于所述第一位置的下游。
6.权利要求1的装置,其中用于将氮从增压压缩机送到产品压缩机的设备包括:用于将氮送到产品压缩机的上游级的管道设备,和用于将氮在产品压缩机的所述上游级的下游送到产品压缩机的管道设备。
7.用于生产高压氮的方法,其包括:
(A)将进料空气在主换热器中冷却,将冷却的进料空气送到深冷空气分离装置中,和通过在深冷空气分离装置内进行深冷精馏生产氮;
(B)将从深冷空气分离装置抽出的氮在主换热器中加热,将加热的氮在产品压缩机中压缩,将一部分压缩的氮作为制冷剂氮送到主换热器,将制冷剂氮冷却,并且使制冷剂氮进行涡轮膨胀以产生制冷作用;
(C)将涡轮膨胀的制冷剂氮在主换热器中加热,将涡轮膨胀的制冷剂氮在增压压缩机中压缩,和将得到的制冷剂氮送到产品压缩机;和
(D)从产品压缩机回收高压氮。
8.权利要求7的方法,其以两种操作模式实施,其中在第一种模式中,被送到主换热器的制冷剂氮具有50到340psia的压力,并且所得到的被送到产品压缩机的制冷剂氮具有20到220psia的压力,并且在第二种模式中,被送到主换热器的制冷剂氮具有90到700psia的压力,并且所得到的被送到产品压缩机的制冷剂氨具有50到390psia的压力。
9.权利要求7的方法,其以两种模式操作,其中在第一种模式中,制冷剂氮从产品压缩机的上游级被送到主换热器,并且在第二种模式中,制冷剂氮从所述上游级的下游的级被送到主换热器。
10.权利要求7的方法,其以两种模式操作,其中在第一种模式中,得到的制冷剂氨被送到产品压缩机的上游级,并且在第二种模式中,得到的制冷剂氮被送到产品压缩机的位于所述上游级的下游的级。
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US10/743,797 US7114352B2 (en) | 2003-12-24 | 2003-12-24 | Cryogenic air separation system for producing elevated pressure nitrogen |
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US7514056B2 (en) * | 2005-02-07 | 2009-04-07 | Co2 Solution Inc. | Process and installation for the fractionation of air into specific gases |
EP2789958A1 (de) * | 2013-04-10 | 2014-10-15 | Linde Aktiengesellschaft | Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage |
CN104514986A (zh) * | 2013-09-30 | 2015-04-15 | 宝山钢铁股份有限公司 | 一种中压氮气制取装置及方法 |
EP3059536A1 (de) * | 2015-02-19 | 2016-08-24 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung eines Druckstickstoffprodukts |
FR3059087A3 (fr) * | 2016-11-18 | 2018-05-25 | Air Liquide | Appareil de separation a temperature subambiante |
US10663224B2 (en) * | 2018-04-25 | 2020-05-26 | Praxair Technology, Inc. | System and method for enhanced recovery of argon and oxygen from a nitrogen producing cryogenic air separation unit |
US10663223B2 (en) * | 2018-04-25 | 2020-05-26 | Praxair Technology, Inc. | System and method for enhanced recovery of argon and oxygen from a nitrogen producing cryogenic air separation unit |
KR20230008178A (ko) * | 2020-05-11 | 2023-01-13 | 프랙스에어 테크놀로지, 인코포레이티드 | 중압 극저온 공기 분리 유닛에서 질소, 아르곤, 및 산소의 회수를 위한 시스템 및 방법 |
CN115485519A (zh) * | 2020-05-15 | 2022-12-16 | 普莱克斯技术有限公司 | 用于产生氮和氩的低温空气分离单元的集成式氮液化器 |
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US4453957A (en) * | 1982-12-02 | 1984-06-12 | Union Carbide Corporation | Double column multiple condenser-reboiler high pressure nitrogen process |
US4783209A (en) * | 1986-07-02 | 1988-11-08 | Erickson Donald C | Cryogenic air distillation with companded nitrogen refrigeration |
FR2651035A1 (fr) * | 1989-08-18 | 1991-02-22 | Air Liquide | Procede de production d'azote par distillation |
US5114452A (en) * | 1990-06-27 | 1992-05-19 | Union Carbide Industrial Gases Technology Corporation | Cryogenic air separation system for producing elevated pressure product gas |
US5108476A (en) * | 1990-06-27 | 1992-04-28 | Union Carbide Industrial Gases Technology Corporation | Cryogenic air separation system with dual temperature feed turboexpansion |
GB9124242D0 (en) * | 1991-11-14 | 1992-01-08 | Boc Group Plc | Air separation |
US5197296A (en) * | 1992-01-21 | 1993-03-30 | Praxair Technology, Inc. | Cryogenic rectification system for producing elevated pressure product |
FR2703140B1 (fr) * | 1993-03-23 | 1995-05-19 | Air Liquide | Procédé et installation de production d'oxygène gazeux et/ou d'azote gazeux sous pression par distillation de l'air. |
US5675977A (en) * | 1996-11-07 | 1997-10-14 | Praxair Technology, Inc. | Cryogenic rectification system with kettle liquid column |
US5758515A (en) * | 1997-05-08 | 1998-06-02 | Praxair Technology, Inc. | Cryogenic air separation with warm turbine recycle |
US6286336B1 (en) * | 2000-05-03 | 2001-09-11 | Praxair Technology, Inc. | Cryogenic air separation system for elevated pressure product |
US6543253B1 (en) * | 2002-05-24 | 2003-04-08 | Praxair Technology, Inc. | Method for providing refrigeration to a cryogenic rectification plant |
DE10238282A1 (de) * | 2002-08-21 | 2003-05-28 | Linde Ag | Verfahren zur Tieftemperatur-Zerlegung von Luft |
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