CN1286387A - 生产甚高纯氧的低温精馏系统 - Google Patents

生产甚高纯氧的低温精馏系统 Download PDF

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CN1286387A
CN1286387A CN00126404A CN00126404A CN1286387A CN 1286387 A CN1286387 A CN 1286387A CN 00126404 A CN00126404 A CN 00126404A CN 00126404 A CN00126404 A CN 00126404A CN 1286387 A CN1286387 A CN 1286387A
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lower pressure
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D·P·博纳奎斯特
J·F·比林哈姆
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Abstract

本发明涉及一种用于生产甚高纯氧的低温空分系统,该系统采用有以隔板隔开的下部空间的低压塔,和以一种相对于隔板的确定方式与低压塔相联的浓集器。

Description

生产甚高纯氧的低温精馏系统
本发明一般说来涉及空气进料的低温精馏，更具体而言涉及空气进料生产氧的低温精馏。
在空气进料生产氮和氧产品的低温精馏中，产生的氧的典型纯度约为99.5％(摩尔)。由于空气组分的相对挥发性，进料空气中的氩倾向于随氧富集，而不是随氮富集。因此，常规低温空分过程的典型氧产品物流中的残留物主要是氩。
对于大多数用途而言，在氧物流中存在少量氩不是问题。但是，在某些情况下，例如在用氧制备化学物质，例如环氧乙烷的情况下，由于氩的惰性，它会在化学反应器中积累，从而需要供反应器定期通风，以避免制备反应变慢。这种周期性通风会引起价值产品的损失。
氩积累引起的制备反应负担的问题可用增加反应器的氧进料的纯度加以说明，生产纯度高于常规氧的系统亦是已知的。但是，这类系统一般只能生产较少量的高纯氧。此外，这类系统一般不易适应现有的为生产常规纯度氧而设计的低温精馏系统。
因此，本发明的目的在于提供一咱生产甚高纯氧的改进型低温精馏系统。
本发明的另一目的在于提供一种生产甚高纯氧的改进型低温精馏系统，该系统易于适应现有的为生产常规纯度氧而设计的系统。
专业技术人员在阅读本发明说明时会理解本发明的上述及其它目标，本发明的一个方面在于：
一种用于空气进料生产甚高纯氧的低温精馏方法，它包括：
(A)将进料空气送入高压塔，在此高压塔中以低温精馏将进料空气分离成富氮流体和富氧流体；
(B)将富氮流体和富氧流体从高压塔送入低压塔，该低压塔的下部有一隔板，并在低压塔中以低温精馏生产富氧液体；
(C)将富氧液体从低压塔的隔板上部送入浓集塔，在这浓集塔中以低温精馏生产更富氧的液体；
(D)将富氧的液体从浓集塔的下部送入该低压塔的隔板下部，至少部分蒸发该更富氧的液体以生产更富氧的流体；和
(E)将更富氧的流体从低压塔中回收，作为甚高纯氧产品。
本发明的另一方面在于：
用进料空气生产甚高纯氧的低温精馏的设备，它包括：
(A)高压塔和将进料空气送入高压塔的装置；
(B)低压塔、将流体从高压塔送入低压塔的装置、和置于低压塔下部的隔板；
(C)浓集塔、将液体从隔板上部的低压塔送至浓集塔上部的装置、和将蒸汽从隔板下部的低压塔送至浓集塔下部的装置；
(D)将蒸汽从浓集塔上部送至隔板上部的低压塔的装置、和将流体从浓集塔下部送至隔板下部的低压塔的装置；
(E)从低压塔隔板下部回收甚高纯氧的装置。
本文所用的术语“进料空气”系指主要含氧、氮和氩的混合物，例如环境空气。
本文所用的术语“塔”系指蒸馏或精馏塔或区段，即接触塔或区段，其中液相和汽相逆流接触实现流体混合物的分离，例如，使汽相和液相在安装在塔内的一系列垂直隔开的塔板和/或填料元件，例如结构填料或无规则填料上接触。为进一步讨论蒸馏塔，可参阅化学工程师手册，第五版，R.H.Perry和C.H.Chilton编，McGraw-Hill BookCompany,New York，第13章，连续蒸馏过程。
术语“双塔”系指高压力塔，其上部与低压力塔的下部具有热交换关系。有关双塔的进一步讨论可见Ruheman的“气体的分离”，牛津大学出版社，1949，第八章，工业空分。
蒸汽和液体接触分离过程取决于各组分的蒸汽压差。高蒸汽压(或更易挥发的或低沸点的)组分倾向于在汽相浓集，而低蒸汽压(或难挥发的或高沸点的)组倾向于在液相浓集。部分冷凝是一种分离过程，其中蒸汽混合物的冷却可用于将挥发的组分浓集在汽相中，同时使较难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，该过程组合了汽相和液相以逆流处理得到的接续部分蒸发和冷凝。汽相和液相的逆流接触通常是绝热的并可包括积分(逐级的)或微分(连续的)相间接触。利用精馏原理分离混合物的分离过程设备经常可通用地称为精馏塔，蒸馏塔或分馏塔。低温精馏是一种至少部分在150°K或150°K以下的温度下进行的精馏过程。
本文所用之术语“间接热交换”系指在流体之相无任何实体接触或相互混合的条件下两种流体发生的热交换关系。
本文所用术语“涡轮膨胀”和“涡轮膨胀器”系指用于高压气体流经涡轮以降低气体的压力和温度从而产生冷冻的相应的方法和设备。
本文所用术语“上部”和“下部”系指分别高于和低于塔中点的塔段。
本文所用的术语“塔板”系指接触级，该级不一定是平衡级，它可意指其它接触设备，诸如具有相当于一块塔板的分离能力的填料。
本文所用的术语“平衡级”系指离开该级的蒸汽和液体是呈传质平衡的汽-液接触级，即具有100％效率的塔板或相当于一个理论板(HETP)的填料元件高度。
本文所用的术语“甚高纯氧”系指氧浓度高于99.9％(摩尔)的流体。
本文所用的术语“隔板”系指防止或基本上防止物流穿过的部件。
唯一的附图是本发明低温精馏系统一个优选实施方案的简化流程图。
本发明将参照附图作较详细的叙述。
现参看图，将已除去诸如水蒸汽、二氧化碳和烃类并已冷却到近其露点的进料空气送入高压塔1，塔1是双塔的一部分，双塔还包括低压塔2。附图所示的本发明的实施方案中，进料以蒸汽物流10送入高压塔1，也可以液相或混合相物流11送入，物流11在物流10进入塔1处上面的1-10平衡级的部位进入塔1。还可使部分进料空气经涡轮膨胀产生冷冻再以物流16进入低压塔2。
高压塔1的操作压力通常在75-125磅/英寸2(绝对)(psia)。在高压塔1中，进料空气以低温精馏分离成富氮流体和富氧流体。富氮流体从高压塔1的上部以蒸汽物流20流出并进入主冷凝器4，其中它与更富氧的液体发生间接热交换而冷凝，这将在下面详细叙述。所得富氮液体从主冷凝器以物流70流出。物流70的第一部分22返回高压塔1作回流液，第二部分21经过冷(未示)，然后以物流24进入低压塔2的上部作回流液。
富氧流体从高压塔1的下部流出并进入低压塔。附图所示的本发明的实施方案是一个优选的实施方案，该方案采用有顶冷凝器的氩侧臂塔。根据这个实施方案，富氧流体从高压塔1以液体物流12流出，部分经过冷(未示)，然后以物流13进入氩塔顶冷凝器5。这里富氧液体经部分汽化，所得富氧蒸汽以物流14进入低压塔2，其余的富氧液体以物流15进入低压塔2。富氧液体12的其余部分同样以物流17进入低压塔2，或者单独地，或者如图所示与物流15汇合进入。
低压塔2的操作压力低于高压塔1，通常在15-25 psia范围内。在低压塔2中，各种进入流塔的进料以低温精馏分离成富氮蒸汽和富氧液体。富氮蒸汽以物流25从低压塔2上部流出，并从系统去除。富氮蒸汽物流25可以全部或部分作为氮产品回收，其氮浓度至少为99.9％(摩尔)。为了控制产品纯度，废物物流23从低压塔2上部低于物流25流出的部位流出该系统。
低压塔2在其下部但在主冷凝器4之上装有隔板9，富氧液体收集在隔板9的上表面。隔板可直接装在主冷凝器上面，或者在主冷凝器和隔板之间可有一个或多个平衡级。富氧液体从隔板9上面，或者如图所示从收集在隔板9上的液体，或者从隔板9上面的塔板或填料床从低压塔2流入浓集塔7的上部。在附图所示的实施方案中，以物流31表示富氧液体的流径。蒸汽隔板9下面的低压塔2空间的蒸汽以物流35流入浓集塔7的下部。
浓集塔7的操作压力通常在16-26 psia范围内。在浓集塔7内，流入该塔的流体以低温精馏分离成更富氮的蒸汽和更富氧的液体。更富氮的蒸汽从浓集器7的上部以物流32流出并在隔板9上面流入低压塔2。更富氧的液体从浓集塔7的下部以物流33流出，经过泵8，以物流34在隔板9的下面泵入低压塔2。更富氧的液体与上述在主冷凝器4中的冷凝富氮蒸汽发生间接热交换而至少部分汽化，所得更富氧的蒸汽的一部分经管线35按上面所述送入浓集塔7的下部。更富氧的蒸汽的另一部分从低压塔2的隔板9下面以物流30流出，并作为甚高纯氧产品回收。如果希望，一些更富氧的液体，可以液态甚高氧液体直接从浓集塔7或从低压塔2的隔板9下面回收。
如上所述，附图所示的本发明实施方案是一个优选实施方案，其中采用氩侧臂塔生产氩产品。现在再参照附图，含氩和氧的物流从低压塔2的隔板9上面以物流44直接从隔板9上面，即在物流44流出部位和隔板9之间无平衡级处流出，或者从在物流44流出部位和隔板9之间存在一个或数个平衡级处流出。物流44流入氩塔3，并在其中以低温精馏分离成更富氩的蒸汽和其余的含氧液体。其余的含氧液体以物流45从氩塔3下部送入隔板9的上面处的低压塔2，通常在隔板9上面20-50平衡级处，氩塔3的操作压力通常在15-25 psia范围内。
更富氩的蒸汽经管线40从氩塔3送入顶冷凝器5，其中与上述的部分汽化的富氧液体发生间接热交换而发生部分冷凝。所得更富氩的两相流体以物流41送入相分离器6，其中以重力分离成更富氩的蒸汽和更富氩液体，前者作为氩产品物流42回收，春氩浓度为90-100％(摩尔)，后者以物流43返回氩塔作回流液。如果需要，物流43的一部分46可作为液体氩产品回收。
本发明的一个特殊优点在于，它容易适应现有的常规低温空分，以生产甚高纯氧。例如，浓集塔7、泵8和大部分管线31、32、33、34和35可提前装配，并可以成套部件的方式在现有工厂仍处于运行的情况下安装到包括有低压塔2的现有工厂的一侧。一旦新的部件到位，现有工厂即可停车。然后将隔板9安装到现有的低压塔2之中，同时将管线31、32、33、34和35与现有低压塔进行联接。
虽然本发明是参照具体的实施方案予以详细叙述的，但专业技术人员将理解，在权利要求的实质和范围内，本发明还有其它实施方案。例如，氩塔和浓集塔可组合在一起或用其它方式一体化。在这种情况下，附图中以物流45表示的其余含氧液体将会流入浓集塔的上部。来自浓集塔上部的一些蒸汽也可流入氩塔的下部。

Claims (10)

1．一种用空气进料低温精馏生产甚高纯氧的方法，包括：
(A)将进料空气送入高压塔，在此高压塔中以低温精馏将进料空气分离成富氮流体和富氧流体；
(B)将富氮流体和富氧流体从高压塔送入低压塔，该低压塔的下部有一隔板，并在低压塔中以低温精馏生产富氧液体；
(C)将富氧液体从低压塔的隔板上部送入浓集塔，在这浓集塔中以低温精馏生产更富氧的液体；
(D)将富氧的液体从浓集塔的下部送入该低压塔的隔板下部，至少部分蒸发该更富氧的液体以生产更富氧的流体；和
(E)将更富氧的流体从低压塔中回收，作为甚高纯氧产品。
2．权利要求1的方法，还包括将更富氧的流体作为蒸汽从低压塔的隔板下面送入浓集塔的下部。
3．权利要求1的方法，还包括在浓集塔生产更富氮的蒸汽，并将更富氮的蒸汽从浓集塔上部送入隔板上面的低压塔。
4．权利要求1的方法，还包括将含氩流体从隔板上面的低压塔送入氩塔，并以低温精馏分离含氩流体，以生成更富氩的流体作为氩产品回收。
5．权利要求4的方法，还包括将来自氩塔下部的流体送入隔板上面的低压塔。
6．一种用空气进料低温精馏生产甚高纯氧的设备，包括：
(A)高压塔和将进料空气送入高压塔的装置；
(B)低压塔、将流体从高压塔送入低压塔的装置、和置于低压塔下部的隔板；
(C)浓集塔、将液体从隔板上部的低压塔送至浓集塔上部的装置、和将蒸汽从隔板下部的低压塔送至浓集塔下部的装置；
(D)将蒸汽从浓集塔上部送至隔板上部的低压塔的装置、和将流体从浓集塔下部送至隔板下部的低压塔的装置；
(E)从低压塔隔板下部回收甚高纯氧的装置。
7．权利要求6的设备，还包括氩塔和顶冷凝器、将流体从隔板上部的低压塔送入氩塔的装置、和从氩塔上部回收氩产品装置。
8．权利要求7的设备，还包括将流体从氩塔下部送入隔板上部的低压塔的装置。
9．权利要求6的设备，其中低压塔包括位于隔板下面的主冷凝器，而且在主冷凝器和隔板之间无平衡级。
10．权利要求6的设备，其中低压塔包括位于隔板下面的主冷凝器，而且在主冷凝器和隔板之间有一个或多个平衡级。
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100436989C (zh) * 2004-01-29 2008-11-26 宝山钢铁股份有限公司 一种用全低压空分装置制取高纯氧的方法
CN102721260A (zh) * 2012-07-04 2012-10-10 开封空分集团有限公司 高纯氧提取装置及利用该装置提取高纯氧的方法
CN103148675A (zh) * 2011-10-20 2013-06-12 林德股份公司 用于低温空气分离装置的双塔

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012177907A1 (en) 2011-06-22 2012-12-27 Praxair Technology, Inc. System and method for oxygen supply for wastewater treatment plant having biological treatment system and supercritical water oxidation treatment of sludge
JP6368118B2 (ja) 2014-03-31 2018-08-01 株式会社日本触媒 エチレンオキシドの製造方法
US10663222B2 (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
US10981103B2 (en) * 2018-04-25 2021-04-20 Praxair Technology, Inc. System and method for enhanced recovery of liquid oxygen from a nitrogen and argon producing cryogenic air separation unit
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
US10816263B2 (en) * 2018-04-25 2020-10-27 Praxair Technology, Inc. System and method for high recovery of nitrogen and argon from a moderate pressure cryogenic air separation unit
CN115461584A (zh) 2020-05-11 2022-12-09 普莱克斯技术有限公司 用于从中压低温空气分离单元回收氮、氩和氧的系统和方法
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
US11619442B2 (en) 2021-04-19 2023-04-04 Praxair Technology, Inc. Method for regenerating a pre-purification vessel

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2535489C3 (de) * 1975-08-08 1978-05-24 Linde Ag, 6200 Wiesbaden Verfahren und Vorrichtung zur Zerlegung eines tiefsiedenden Gasgemisches
US4615716A (en) 1985-08-27 1986-10-07 Air Products And Chemicals, Inc. Process for producing ultra high purity oxygen
US4838913A (en) 1988-02-10 1989-06-13 Union Carbide Corporation Double column air separation process with hybrid upper column
JPH0672740B2 (ja) * 1989-01-20 1994-09-14 ル・エール・リクイツド・ソシエテ・アノニム・プール・ル・エチユド・エ・ル・エクスプルワテション・デ・プロセデ・ジエオルジエ・クロード 空気分離及び超高純度酸素製造方法並びに装置
US5049173A (en) 1990-03-06 1991-09-17 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
US5339648A (en) 1993-08-05 1994-08-23 Praxair Technology, Inc. Distillation system with partitioned column
GB9513765D0 (en) * 1995-07-06 1995-09-06 Boc Group Plc Production of argon
US5590543A (en) 1995-08-29 1997-01-07 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
DE19605500C1 (de) * 1996-02-14 1997-04-17 Linde Ag Vorrichtung und Verfahren zum Verdampfen einer Flüssigkeit
US5611219A (en) * 1996-03-19 1997-03-18 Praxair Technology, Inc. Air boiling cryogenic rectification system with staged feed air condensation
US5765396A (en) * 1997-03-19 1998-06-16 Praxair Technology, Inc. Cryogenic rectification system for producing high pressure nitrogen and high pressure oxygen
US5956972A (en) * 1997-12-23 1999-09-28 The Boc Group, Inc. Method of operating a lower pressure column of a double column distillation unit
US5918482A (en) 1998-02-17 1999-07-06 Praxair Technology, Inc. Cryogenic rectification system for producing ultra-high purity nitrogen and ultra-high purity oxygen
US5881570A (en) 1998-04-06 1999-03-16 Praxair Technology, Inc. Cryogenic rectification apparatus for producing high purity oxygen or low purity oxygen

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100436989C (zh) * 2004-01-29 2008-11-26 宝山钢铁股份有限公司 一种用全低压空分装置制取高纯氧的方法
CN103148675A (zh) * 2011-10-20 2013-06-12 林德股份公司 用于低温空气分离装置的双塔
CN102721260A (zh) * 2012-07-04 2012-10-10 开封空分集团有限公司 高纯氧提取装置及利用该装置提取高纯氧的方法

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