CN101600924B - 使用供应有主要成分至少为氢和一氧化碳的混合物的蒸馏塔系统通过低温蒸馏生产一氧化碳的方法和设备 - Google Patents

使用供应有主要成分至少为氢和一氧化碳的混合物的蒸馏塔系统通过低温蒸馏生产一氧化碳的方法和设备 Download PDF

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CN101600924B
CN101600924B CN2008800039358A CN200880003935A CN101600924B CN 101600924 B CN101600924 B CN 101600924B CN 2008800039358 A CN2008800039358 A CN 2008800039358A CN 200880003935 A CN200880003935 A CN 200880003935A CN 101600924 B CN101600924 B CN 101600924B
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A·布里利亚
A·达德
N·艾克-贝劳德
M-K·戚
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

本发明涉及一种利用蒸馏塔系统(5、11)通过低温蒸馏生产一氧化碳的方法，该蒸馏塔系统供应有至少以氢和一氧化碳作为主要成分且至少有时有氮的混合物，其中将该混合物在塔系统中分离，该塔系统包括用于产生富氮流和贫氮流的脱氮塔(11)，且从该塔系统中提取富含一氧化碳的流以用作产品，其特征在于，当混合物中的氮含量降到给定阈值以下时，就将来自不同于所述混合物的源的外部源的氮(17)进给到脱氮塔的上游或脱氮塔中。

Description

使用供应有主要成分至少为氢和一氧化碳的混合物的蒸馏塔系统通过低温蒸馏生产一氧化碳的方法和设备
技术领域
本发明涉及一种用于通过低温蒸馏生产一氧化碳的方法和设备。在已知的通过低温蒸馏生产氢和/或一氧化碳的方法中，常常使用脱氮塔以便从被氮污染的待分离的混合物中获得含氮量低的产品。
背景技术
但是有时待分离的混合物的氮含量极少或甚至为零，而单元已设计成带有脱氮塔。由临时进给有石脑油的SMR产生的待分离的混合物便是这种情况。由于脱氮塔的压力调节是通过控制氮排出流(清除流，purge azote)而进行的，这将不再能够使此塔的压力保持不变。由于此压力控制通常位于脱氮塔上游的CO/CH4塔的压力，因此，可能的波动将导致单元运行的明显恶化。
发明内容
根据本发明，为了解决进给气体中缺少氮的问题，在脱氮塔的上游——优选在跟随有CO(来自合成气或来自循环)的回路中、优选在低压下——注入氮，通过这种方法使得脱氮塔能够运行。
根据本发明的一个目的，提供了一种利用蒸馏塔系统通过低温蒸馏生产一氧化碳的方法，该蒸馏塔系统进给有至少以氢和一氧化碳作为主要成分且至少有时有氮的混合物，其中将该混合物在塔系统中分离，该塔系统包括用于产生富氮流和贫氮流的脱氮塔，且从该塔系统中提取富含一氧化碳的流以用作产品，其特征在于，如果混合物中的氮含量降到给定阈值以下，就将来自不同于所述混合物的源的外部源的富氮流体传输到脱氮塔的上游或脱氮塔中。
根据其它可选的目的：
-将富氮流体喷射到进给脱氮塔的流中，或者将富氮流体直接喷射到脱氮塔中；
-将富氮流体以高于-170℃、可选地高于0℃的温度进行喷射；
-富氮流体是液态或气态的；
-如果富氮流减少到给定流率以下，就将来自不同于所述混合物的源的外部源的富氮流体传输到脱氮塔的上游；
-该塔系统能够在脱氮塔的上游实现部分冷凝或甲烷清洗。
根据本发明的另一目的，提供了一种通过低温蒸馏生产一氧化碳的设备，该设备包括蒸馏塔系统、用于将至少以氢和一氧化碳作为主要成分且至少有时有氮的混合物进给该塔系统的装置，该塔系统包括用于生产富氮流和贫氮流的脱氮塔和用于从该塔系统提取富含一氧化碳的流作为产品的装置、以及用于将来自不同于所述混合物的源的外部源的富氮流体输送到脱氮塔上游或脱氮塔的装置，其特征在于，它包括用于测量以下指标的装置：
i)混合物的、作为混合物的源的流体的、或进给脱氮塔的流体(9)的氮含量，或
ii)脱氮塔的冷凝器(23)的、或进给脱氮塔的流体的排出(流)流率，或
iii)脱氮塔的冷凝器的排出(流)的膨胀阀(31)的开度
和能够根据测得的含量或测得的流率或测得的开度将来自不同于所述混合物的源的外部源的富氮流体(17)传输到脱氮塔的上游和/或脱氮塔的控制装置。
根据本发明的又一目的，在该设备中：
-用于输送来自外部源的富氮流体的装置连接于脱氮塔的入口；
-该设备包括用于测量富氮(流)流率的装置和能够在测得的流率低于给定阈值时将来自不同于所述混合物的源的外部源的富氮流体传输到脱氮塔上游的控制装置；
-该塔系统包括用于在脱氮塔的上游执行部分冷凝或甲烷清洗的装置。
附图说明
将结合附图更加详细地描述本发明，该附图示出了根据本发明的用于生产一氧化碳的设备。
具体实施方式
该设备至少包括两个蒸馏塔，包括CO/CH4塔5和脱氮塔11。
该设备可形成在CO/CH4塔的上游具有甲烷清洗步骤或部分冷凝步骤的设备的一部分。脱氮塔也可布置在CO/CH4塔的上游。
CO/CH4塔在不同高度处进给有两股流1、3，并生产富含甲烷的液体7和富含一氧化碳、但至少有时包含氮的流体9。该流体9在脱氮塔11的上部传输到脱氮塔。储罐液体(liquide de cuve)13被传输到脱氮塔11的塔顶冷凝器23以便使氮25冷凝。净化流27被从冷凝器23中抽出且被传输到热交换器29，它在该热交换器处蒸发且在阀31中膨胀。通过排出流27保持脱氮塔11的压力。
如果流9的氮含量和/或流9自身和/或排出流27降到给定的阈值以下，就将一股液态或气态氮流17传输到脱氮塔的顶部，直到所述流9的氮含量可接受为止。
此外或可供选择地，可以测量混合物或作为混合物的源的流体(例如天然气)的氮含量，并在此含量低于给定阈值时触发氮的输送。
或者，可以测量进给脱氮塔11的流体9的流率，并在此含量低于给定的阈值时触发氮的输送。
另一可供选择的方案是在脱氮塔的冷凝器的排出(流)的膨胀阀31的开度降到给定阈值以下时触发氮的输送。

Claims (9)

1.一种利用蒸馏塔系统通过低温蒸馏生产一氧化碳的方法，该蒸馏塔系统进给有至少以氢和一氧化碳作为主要成分且至少有时有氮的混合物，其中将该混合物在塔系统中分离，该塔系统包括用于产生富氮流和贫氮流(13)的脱氮塔(11)，且从该塔系统中提取富含一氧化碳的流(13)以用作产品，其特征在于，如果所述混合物中的氮含量降到给定阈值以下，就将来自不同于所述混合物的源的外部源的富氮流体(17)传输到脱氮塔的上游和/或脱氮塔中。
2.根据权利要求1所述的方法，其特征在于，将所述富氮流体注入进给脱氮塔(11)的流中，或者将所述富氮流体直接喷射到脱氮塔中。
3.根据权利要求1所述的方法，其特征在于，将所述富氮流体(17)以高于-170℃的温度喷射到脱氮塔中。
4.根据权利要求3所述的方法，其特征在于，将所述富氮流体(17)以高于0℃的温度进行喷射。
5.根据权利要求1所述的方法，其特征在于，如果所述富氮流(27)减少到给定流率以下，就将来自不同于所述混合物的源的外部源的所述富氮流体传输到脱氮塔的上游。
6.根据前述权利要求中的任何一项所述的方法，其特征在于，该塔系统能够在脱氮塔的上游实现部分冷凝或甲烷清洗。
7.一种通过低温蒸馏生产一氧化碳的设备，该设备包括蒸馏塔系统、用于将至少包括氢和一氧化碳作为主要成分且至少有时有氮的混合物进给该塔系统的装置，该塔系统包括用于生产富氮流和贫氮流的脱氮塔(11)和用于从该塔系统提取富含一氧化碳的流作为产品的装置、以及用于将来自不同于所述混合物的源的外部源的富氮流体(17)输送到脱氮塔上游或脱氮塔的装置，其特征在于，该设备包括用于测量以下指标的装置：
i)混合物的、作为混合物的源的流体的、或进给脱氮塔的流体(9)的氮含量，或
ii)脱氮塔的塔顶冷凝器(23)的排出流流率或进给脱氮塔的流体的排出流流率，或
iii)脱氮塔的塔顶冷凝器的排出流的膨胀阀(31)的开度
和能够根据测得的含量或测得的流率或测得的开度将来自不同于所述混合物的源的外部源的所述富氮流体(17)传输到脱氮塔的上游和/或脱氮塔的控制装置。
8.根据权利要求7所述的设备，其特征在于，用于输送来自外部源的所述富氮流体(17)的装置连接于脱氮塔(11)的入口。
9.根据权利要求7或8所述的设备，其特征在于，该塔系统包括用于在脱氮塔的上游执行部分冷凝或甲烷清洗的装置。
CN2008800039358A 2007-02-01 2008-01-30 使用供应有主要成分至少为氢和一氧化碳的混合物的蒸馏塔系统通过低温蒸馏生产一氧化碳的方法和设备 Active CN101600924B (zh)

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FR0752999A FR2912206B1 (fr) 2007-02-01 2007-02-01 Procede et appareil de production de monoxyde de carbone par distillation cryogenique
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FR3011069B1 (fr) 2013-09-24 2015-09-11 Air Liquide Procede et appareil de separation cryogenique d'un melange contenant au moins du monoxyde de carbone, de l'hydrogene et de l'azote

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FR2895067A1 (fr) * 2007-01-09 2007-06-22 Air Liquide Procede integre de deux separations cryogeniques et appareil integre pour la mise en oeuvre du procede

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GB9800692D0 (en) * 1998-01-13 1998-03-11 Air Prod & Chem Separation of carbon monoxide from nitrogen-contaminated gaseous mixtures also containing hydrogen and methane
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DE2814660A1 (de) * 1978-04-05 1979-10-11 Linde Ag Verfahren zur gewinnung von kohlenmonoxid und wasserstoff
US4623370A (en) * 1984-09-11 1986-11-18 Aeci Limited Gas treatment process
DE3741906A1 (de) * 1987-12-10 1989-06-22 Linde Ag Verfahren zur gewinnung von h(pfeil abwaerts)2(pfeil abwaerts) und co
CN1221102A (zh) * 1997-10-14 1999-06-30 液体空气乔治洛德方法利用和研究有限公司 超高纯度氮气和氧化发生器装置
US6062042A (en) * 1998-01-13 2000-05-16 Air Products And Chemicals, Inc. Seperation of carbon monoxide from nitrogen-contaminated gaseous mixtures
FR2895067A1 (fr) * 2007-01-09 2007-06-22 Air Liquide Procede integre de deux separations cryogeniques et appareil integre pour la mise en oeuvre du procede

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JP2010517909A (ja) 2010-05-27
FR2912206A1 (fr) 2008-08-08
FR2912206B1 (fr) 2015-05-29
WO2008099124A2 (fr) 2008-08-21
CN101600924A (zh) 2009-12-09
US20100150813A1 (en) 2010-06-17
US9459043B2 (en) 2016-10-04
KR20090115182A (ko) 2009-11-04
EP2118599A2 (fr) 2009-11-18

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