CN103080677B - 用于蒸馏分离含有二氧化碳的混合物的设备和方法 - Google Patents

用于蒸馏分离含有二氧化碳的混合物的设备和方法 Download PDF

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CN103080677B
CN103080677B CN201180011702.4A CN201180011702A CN103080677B CN 103080677 B CN103080677 B CN 103080677B CN 201180011702 A CN201180011702 A CN 201180011702A CN 103080677 B CN103080677 B CN 103080677B
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condenser
mixture
destilling tower
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separated
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B·贝托梅
L·佩吕
F·里沃阿尔
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

本发明涉及一种用于蒸馏分离混合物的设备，所述混合物作为主要成分包括二氧化碳和选自包含氮、氧、氩、氢、甲烷及一氧化碳的组的至少一种其它流体，所述设备包括蒸馏塔（8）、冷凝器（9）、再沸器（7，11）、用于将要分离的混合物输送到塔或冷凝器的装置、用于将来自塔的顶部气体输送到冷凝器的装置、以及用于将在冷凝器中冷凝的液体输送到塔的顶部的装置。冷凝器由钎焊铝制成的板翅式交换器构成，每m3交换器的换热表面积大于400m2/m3，采用氨作为冷却剂。

Description

用于蒸馏分离含有二氧化碳的混合物的设备和方法
技术领域
本发明涉及用于通过蒸馏分离二氧化碳混合物的设备和方法。
背景技术
已知在低于环境温度的温度下通过蒸馏分离含有二氧化碳以及至少一种其它气体的混合物。塔顶部处的回流是通过来自塔的顶部气体的至少一部分冷凝而形成。目前，使用由不锈钢制成的壳管式冷凝器执行用于分离含有二氧化碳的混合物的塔顶部气体的液化，如US-A-3317278中所述。该热交换器（其具有下列显著优点：能够抵抗高压以及管和主体的自由膨胀，并且其接受所有类型的动力）具有一些缺点，比如体积和造价。
使用包括壳管式交换器的技术使来自塔的顶部气体液化需要使用占地面积约为30m2的重而且昂贵的支承件。冷凝器的长度超过10m，现场设备的组装和结合的优化很难施行，维修时需要租借吊车和特殊举升装置。
其次，蒸馏过程通常包括氨冷却线路。交换器越大，冷却剂的体积增加就越多，这和目前降低工业现场氨体积的策略相矛盾。
最后，利用壳管式技术，CO2和氨之间的热交换不是非常有效。
发明内容
本发明优选适用于其中二氧化碳构成总量的至少90%的混合物。混合物的至少一种其它组分可以从包括氮、甲烷、氧以及氩的组中选取。所有的百分比为摩尔百分比。
待分离的混合物可以是来自富氧燃烧、铁和钢制造工艺、生物乙醇（bioéthanol）生产或合成气处理的废气或者是发酵或水泥作业过程中产生的气体。
根据本发明的主题，提供了一种用于通过蒸馏分离混合物的设备，所述混合物作为主要成分包括二氧化碳和选自由氮、氧、氩、氢、甲烷和一氧化碳组成的组的至少一种其它流体，所述设备包括蒸馏塔、冷凝器、再沸器、用于将要分离的混合物输送到蒸馏塔或冷凝器的装置、用于将来自蒸馏塔的顶部气体输送到冷凝器的装置以及用于将在冷凝器中冷凝的液体输送到蒸馏塔的顶部的装置，冷凝器由钎焊铝制成的板翅式交换器组成，每m3交换器的交换表面积大于400m2/m3，并且冷凝器布置在液态冷却剂的浴中，所述冷却剂为氨。
根据其它可选的特征：
-冷凝器与用于供给液态或两相氨的装置相连接；
-在使用中，冷凝器布置在蒸馏塔的的上方；
-在使用中，构成冷凝器的交换器的最大尺寸沿大致垂直的轴线。
根据本发明的另一个主题，提供了一种用于在包括蒸馏塔、冷凝器和再沸器的组件中通过蒸馏分离混合物的方法，所述混合物作为主要成分包括二氧化碳和选自由氮、氧、氩、氢、甲烷和一氧化碳组成的组的至少一种其它流体，其中，待分离的混合物被输送到蒸馏塔或冷凝器，来自蒸馏塔的顶部气体加热冷凝器、被液化并返回蒸馏塔，冷凝器由钎焊铝制成的板翅式交换器组成，每m3交换器的交换表面积大于400m2/m3，并且通过将氨流输送至冷凝器来冷却该冷凝器。
可选地，在将待分离的混合物输送到蒸馏塔或冷凝器之前通过所述待分离的混合物加热蒸馏塔的贮槽。
冷凝器可处于氨的浴中。
液态或两相氨能在冷凝器中被再加热。
液态或两相氨能来自一罐，并且在冷凝器中蒸发的氨能返回该罐。
在冷凝器中未冷凝的气体能被排出。
蒸馏塔的贮槽液体的一部分能够被从蒸馏塔抽取出作为产品。
优选地，没有蒸馏塔的贮槽液体被输送到冷凝器。
混合物可包含至少90%的二氧化碳。
附图说明
下面参照附图更详细地描述本发明，图1至3示出根据本发明的分离设备。
具体实施方式
图1示出用于分离混合物的设备，该混合物作为主要成分包括二氧化碳、醇、氢气、氧气、氩气、氮气、一氧化碳和其他杂质。在2000Nm3/h到5000Nm3/h之间的来自生物乙醇或合成气制备类型工业源的混合物进入管道1并且在压缩机2中被压缩。混合物被再加热到大约80°C（未示出），随后在第一洗涤塔3中通过与受控的食品级水直接接触而被冷却及洗涤，所述食品级水通过与氨间接接触而冷却。在洗涤过程中，可溶的一部分杂质比如醇和挥发性的含氧成分被水吸收并排出。随后，源自第一级洗涤塔的混合物通过压缩机4被压缩到大约20bara（bar，绝对压力）并被引入第二洗涤塔5，在这里残余的杂质以及微量的含氧分子大部分被吸收。
在第二洗涤塔中洗涤后的混合物通过经过净化单元6而经历净化阶段，该净化单元由数个活性炭以及氧化铝床组成，这些床的作用是阻挡脂肪族、含氧及芳香碳氢化合物、硫和氮化合物、微量的油和极性颗粒，比如水。离开净化单元6时，混合物41是干燥的而且符合ISBT（InternationalSociety of Beverage Technologists，国际饮料技术协会）的质量标准，除了不可冷凝的产品，例如氢气、氧气、氩气、氮气和一氧化碳，这些成分将在蒸馏过程中被排出。
接下来，源自净化单元6的混合物41进入冷箱（未示出），在第一交换器7中冷却，并且被输送到蒸馏塔8的顶部。蒸馏塔是包括堆叠的填料或板的塔。混合物41含有至少90%的二氧化碳，其以气态形式进入蒸馏塔，然后大部分流入冷凝器9。冷凝器9由钎焊铝制成的板翅式交换器构成，其最大尺寸沿垂直方向取向，并被放置在蒸馏塔8上方。虽然混合物中的二氧化碳在冷凝器9中冷凝，但是较轻的气体（氧气、氮气、氩气、一氧化碳）保持不可冷凝并且大部分经由排气管道10从冷凝器9离开。存在于在冷凝器9中冷凝的液态CO2中的微量不可冷凝产品通过蒸馏去除，以便在蒸馏塔贮槽中获得需要的纯度。
混合物在冷凝器9中的冷凝通过氨在1.1bara和-31.8°C下的蒸发实现。液态氨23被输送到罐27，该罐通过管道29经由底部供给冷凝器。氨在冷凝器中通过与蒸馏塔的塔顶气体换热而蒸发，并且以气态形式通过管道31离开，管道31使气体返回罐27的顶部。罐内的气体通过管道25被传送到冷却线路。
富含二氧化碳的液体在蒸馏塔的贮槽内形成。该液体的一部分13在交换器12中利用液态氨21过冷却并且然后压力降低到16bara后用作产品。
富含二氧化碳的流的另一部分15在交换器11中与液态氨19相互作用而被加热，所生成的富含二氧化碳的气体返回蒸馏塔。
富含二氧化碳的流的另一部分17在交换器7中与来自净化单元6的原料混合物相互作用而被加热，所生成的富含二氧化碳的气体返回蒸馏塔的顶部，如前文描述的那样。
二氧化碳的纯度由用作再沸器的交换器7和11来调节。
图2和3描述了分离设备的两个可选的形式。图2中，冷凝器9是热虹吸管类型。冷凝器9安装在蒸馏塔的上方，气体通过蒸馏塔的延伸部朝冷凝器9上升，该延伸部允许气体上升以及液体下降。冷凝器通过针对图1已经描述的管道29和31与氨罐27连接。冷凝器9是由钎焊铝制成的板翅式交换器，该交换器每立方米的换热面积大于400m2/m3。
混合物41要么被输送到蒸馏塔8的顶部，要么输送到冷凝器9的入口。
对于图3，冷凝器9放置在制冷流体（在该情形中为氨）的浴33中。冷凝器9是由钎焊铝制成的板翅式交换器，该交换器每立方米的换热面积大于400m2/m3。
要分离的混合物41要么被输送到蒸馏塔8的顶部，要么经由管道39输送到冷凝器9的入口。
顶部气体经由连接冷凝器顶部和蒸馏塔8顶部的管道39被输送到冷凝器。在冷凝器中冷凝后的液体经由管道43返回蒸馏塔，而另一管道10用于排出不可冷凝的产物。入口35为浴33供给制冷流体，一出口排出在浴中蒸发的气体。
在图2和图3两种情形中，冷凝器9都定位在蒸馏塔8的上方，但是可以设想其它布置结构。为了简化附图，图2和3中没有示出贮槽再沸器。
对于图2和3给出的示例，蒸馏塔8在18bara到30bara之间的压力下操作，更高的压力是可以的但是需要更昂贵的设备。为了简化起见，这些图中没有示出再沸器。
使用由钎焊铝制成的板翅式交换器使得可以减轻设备的总重量，可以减少所使用的氨的体积并且将氨的使用主要限制在蒸馏塔所处的冷箱内，可以减小设备的占地面积，并且降低其成本。

Claims (7)

1.一种用于通过蒸馏分离混合物的设备，所述混合物作为主要成分包括二氧化碳和选自由氮、氧、氩、氢、甲烷和一氧化碳组成的组的至少一种其它流体，所述设备包括蒸馏塔(8)、冷凝器(9)、再沸器(7，11)、用于将要分离的所述混合物输送到所述冷凝器的装置、用于将来自所述蒸馏塔的顶部气体输送到所述冷凝器的装置以及用于将在所述冷凝器中冷凝的液体输送到所述蒸馏塔的顶部的装置，所述冷凝器由钎焊铝制成的板翅式交换器组成，每m3交换器的换热表面积大于400m2/m3，并且所述冷凝器(9)布置在液态冷却剂的浴中，所述冷却剂为氨，
其中，所述冷凝器(9)连接到用于供给液态或两相氨的装置，
其中，在使用中，所述冷凝器(9)布置在所述蒸馏塔(8)的上方，待分离的混合物和所述顶部气体二者经由一公共管道被输送到所述冷凝器(9)，
其中，所述设备包括用于排出在氨的浴(33)中蒸发的气体的出口，和用于通过排气去除在所述冷凝器(9)中未冷凝的气体的装置。
2.根据权利要求1所述的设备，其中，在使用中，构成所述冷凝器(9)的交换器的最大尺寸沿基本垂直的轴线。
3.一种用于在包括蒸馏塔(8)、冷凝器(9)和再沸器(7，11)的组件中通过蒸馏分离混合物的方法，所述混合物作为主要成分包括二氧化碳和选自由氮、氧、氩、氢、甲烷和一氧化碳组成的组的至少一种其它流体，其中，待分离的所述混合物被输送到所述冷凝器，来自所述蒸馏塔的顶部气体加热所述冷凝器、被液化并返回所述蒸馏塔，所述冷凝器由钎焊铝制成的板翅式交换器组成，每m3交换器的换热表面积大于400m2/m3，并且通过将氨流输送至所述冷凝器来冷却所述冷凝器，
其中，所述冷凝器处于氨的浴中，在所述冷凝器(9)中未冷凝的气体被排出，
其中，没有所述蒸馏塔(8)的贮槽液体被输送到所述冷凝器(9)，
其中，待分离的混合物和所述顶部气体经由一公共管道被输送到所述冷凝器(9)。
4.根据权利要求3所述的方法，其中，液态或两相氨在所述冷凝器中被再加热。
5.根据权利要求3或4所述的方法，其中，在将待分离的混合物输送到所述冷凝器(9)之前通过所述待分离的混合物加热所述蒸馏塔(8)的贮槽。
6.根据权利要求3或4所述的方法，其中，所述混合物包含至少90％的二氧化碳。
7.根据权利要求3或4所述的方法，其中，从所述蒸馏塔抽取所述蒸馏塔的贮槽液体的一部分作为产品。
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