CN102933927A - 用于通过低温蒸馏分离空气的方法和设备 - Google Patents

用于通过低温蒸馏分离空气的方法和设备 Download PDF

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CN102933927A
CN102933927A CN201080063941XA CN201080063941A CN102933927A CN 102933927 A CN102933927 A CN 102933927A CN 201080063941X A CN201080063941X A CN 201080063941XA CN 201080063941 A CN201080063941 A CN 201080063941A CN 102933927 A CN102933927 A CN 102933927A
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air
delivered
tower
gas separation
compressor
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CN102933927B (zh
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B·哈
J-R·布吕热罗勒
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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Abstract

在一种用于通过低温蒸馏分离空气而产生氮和富含氧的液体的方法中，将第一空气流送至交换器以形成第一冷却的空气流，将第一冷却的空气流送至塔的底部再沸器，将冷凝的空气从底部再沸器送至塔的顶部冷凝器，将气化的空气从顶部冷凝器送至第一压缩机，将空气从第一压缩机送至塔，将空气送至第二压缩机并从第二压缩机送至交换器以产生冷却的第二空气流，将冷却的第二空气流送至第一涡轮膨胀器并从涡轮膨胀器送至塔，从塔除去底部液体并从塔顶部除去气态氮。

Description

用于通过低温蒸馏分离空气的方法和设备
技术领域
本发明涉及一种用于通过低温蒸馏分离空气的方法/工艺和应用。
背景技术
在不久的将来可以建造大型的气体或煤气化站点。所有气化工艺需要大量高压氧气。
ASU设备尺寸在近四十年来稳步增长，且该趋势没有停止迹象。随着设备尺寸变得越来越大，液体储备问题对于持续数小时以上的设备中断变得不切实际或不可能。
当前技术将允许设备尺寸高达每天7000公吨氧。目前，最大基准设备尺寸介于每天4000到5000公吨之间。
例如，在不久的将来，煤气化可能需要高达50000T/D的非常大的氧气消耗量。气液转化设备是具有在20000-40000T/D的范围内的高氧气需求量的另一个示例。在这种大型设施中，显然需要改进的和合理的氧生产理念。
本发明提供了一种用于建造需要多个大型制氧设备群组（train）的大型设施的新方法。这种新方案中还结合了一种用于成本划算的生产储备的新概念。
附图说明
图1示出了如本发明的一个实施例中所示的用于低成本储备目的而增加产量的本发明的一种新方法。
图2示出了根据本发明的一个实施例的氮发生器的细节。
图3示出了根据本发明的一个实施例在独立模式下操作以向复合体（complex）供给公用氮气（公共事业氮气，nitrogen utility gas）的氮发生器的一个实施例。
图4示出了根据本发明的一个实施例的具有高压塔、中压塔、低压塔和辅助塔的系统。
发明内容
本发明涵盖了用于大型空气分离设施的低温工艺的三个主要方面：
1.制氧设备的工艺选择：本发明的目的是提供一种能够氧产量很高的空气分离工艺。所选的工艺的另一个特征是其有效地接纳更高的空气流量以增加氧产量的能力。
2.用于多个群组的经济储备：本发明的该方面的目的是提供一种用于通过使用诸如氮发生器的辅助单元来对设备生产进行储备的新方法。
为了达到很高的产量，需要一种用于空气分离设备的不同工艺方案。传统的双塔工艺在约6bar（巴）的低供料空气压力下操作，从而在制氧设备的低温部分前需要用于前端清洗以除去水分和CO2的大型吸附容器。
用于对包括以并联方式操作的若干个群组的生产设施进行储备的传统方法是安装全尺寸备用群组。该备用群组或单元可以在短时间内投入使用，以解决其它群组的构件之一的中断而造成的生产懈怠。由于同时发生两处中断的可能性低，所以常见的做法是仅使用一个备用群组来确保多个群组的可靠性。在一些情况下，如果备用单元必须在很短的时间内起动或瞬时起动，则包括备用单元的全部设备必须永久以降低的速率运行；当一个单元停机时，可以迅速提高剩余单元的生产速度以维持总产量。
根据本发明，提供了一种用于通过空气的低温蒸馏而产生氮和富含氧的液体的设备，该设备包括：具有顶部冷凝器和底部再沸器的塔；第一压缩机；第二压缩机；第一涡轮膨胀器；热交换器；用于将第一空气流送至交换器以形成第一冷却的空气流的导管装置；用于将第一冷却的空气流送至底部再沸器的导管装置；用于将冷凝的空气从底部再沸器送至顶部冷凝器的导管装置；用于将气化的空气从顶部冷凝器送至第一压缩机的导管装置；用于将空气从第一压缩机送至塔的导管装置；用于将空气送至第二压缩机并从第二压缩机送至交换器以产生冷却的第二空气流的导管装置；用于将冷却的第二空气流送至第一涡轮膨胀器并从涡轮膨胀器送至塔的导管装置；用于从塔除去底部液体的导管装置；以及用于从塔顶部除去气态氮的导管装置。
可选地，所述设备包括：
-用于将液氮送至塔顶部的导管装置。
-又一个冷凝器；用于将底部液体从塔送至所述又一个冷凝器的导管装置；用于将气态氮从塔顶部送至所述又一个冷凝器的导管装置；以及用于从所述又一个冷凝器除去气化的底部液体的导管装置。
根据本发明，可以提供一种用于制氧的设施，该设施包括：至少一个空气分离单元；至少一个如上所述的设备；用于将空气送至至少一个设备的压缩装置；用于将空气送至至少一个空气分离单元的压缩装置；用于从至少一个空气分离单元除去氧的导管装置；用于将富氧液体从所述设备送至至少一个空气分离单元的塔的导管装置。
该设施可包括：
-用于将富氮液体从至少一个空气分离单元的塔送至所述设备的导管装置。
-用于将空气送至至少一个设备的压缩装置和用于将空气送至至少一个空气分离单元的压缩装置包括连接到至少一个空气分离单元和至少一个设备的至少一个压缩机。
根据本发明的又一方面，提供了一种用于通过低温蒸馏分离空气而产生氮和富含氧的液体的方法，其中将第一空气流送至交换器以形成第一冷却的空气流，将第一冷却的空气流送至塔的底部再沸器，将冷凝的空气从底部再沸器送至塔的顶部冷凝器，将气化的空气从顶部冷凝器送至第一压缩机，将空气从第一压缩机送至塔，将空气送至第二压缩机并从第二压缩机送至交换器以产生冷却的第二空气流，将冷却的第二空气流送至第一涡轮膨胀器并从涡轮膨胀器送至塔，从塔除去底部液体并从塔顶部除去气态氮。
该方法可包括将液氮送至塔顶部。
一种用于在一设施中制氧的集成方法包括根据上述方法操作至少一个空气分离单元和至少一个设备，其中将空气送至所述设备并送至空气分离单元，将底部液体从所述设备送至空气分离单元的塔，并从空气分离单元提取氧。
该方法可至少包括第一和第二空气分离单元并且当第二空气分离单元不工作时将底部液体送至第一空气分离单元。
当第二空气分离单元工作时，可将空气从压缩机送至第二空气分离单元，而当第二空气分离单元不工作时，可将空气从压缩机送至所述设备。
具体实施方式
用于基于低成本储备目的而提高产量的本发明的新方法在图1中示出。与其中提供完整备用群组以保证产量的传统方法相比，提出了一种更简单和成本更低的氮发生器来替代备用冷箱。该氮发生器设计成在类似于制氧设备的压力（在本发明中为约11bar）下操作，以保证简单的压缩机设备储备。然而，可以使用其它压力。
这种使用氮发生器的储备概念一般可以适用于低温制氧设备的多群组装置。在以下详细描述中，氮发生器协同类似于在本发明的图4中描述的工艺的冷箱工艺布置。在图1中，氮发生器将空气分离成富氮流205和极富/极浓液流200。应注意，极富液流200的组分类似于图4的极富液体12的组分。
图2的实施例示出了氮发生器的细节：压力为11bar的经压缩、冷却和净化的供料空气1的一部分3由压缩机24进一步压缩而形成压力更高的流4。流4然后在交换器20中冷却并经由膨胀器21膨胀进蒸馏塔30。供料空气的另一部分2在交换器20中冷却并在交换器32中冷凝，以向塔提供沸腾。这样形成的冷凝后的空气10然后膨胀并被送至冷凝器31，以与塔30的顶部处的冷凝气体发生作用而在较低压力下气化。离开冷凝器31的气化后的空气11然后在冷压缩机22中被冷压缩而形成流12并进入塔以进行蒸馏。塔30将供料空气分离成顶部的富氮气体和底部的极富液体50。富氮气体在冷凝器31中冷凝，以产生用于蒸馏的液体回流。富氮气体41的一部分被回收并作为氮产品45在交换器20中被加温。富氮气体的一部分42可以可选地在膨胀器23中膨胀，以提供附加制冷。
当用作用于多个制氧群组的储备单元时，氮发生器从先前向目前停机的群组供给空气的压缩机接收空气1，该空气1被分离成氧含量为约65mol%的极富液体50和氮流41。极富液体流60经由流88被送至图4的制氧设备。为了维持制氧设备和氮发生器两者的制冷平衡，经由图4的流89从制氧设备萃取液氮流并将其送至氮发生器（图2的流40）。由于通向制氧设备的极富液体供料60包含的氮比空气少得多（约35mol%，而不是78%），由极富液体供给的氧产量的提高并未在塔顶部增加如在空气的情形中那么多的氮流量。因此，该系统能够产生形式为气态氧流72的更高氧流量。图1的图示示出了这种具有三个制氧群组的系统的效力：代替设置处理1000单位空气的完整备用群组，可以使用仅处理400单位空气（小60%）的小得多的氮气发生器作为备用生产单元。可以对这种氮气发生器使用如上所述经由第二低压塔用更高的空气流量进行空气加速（增强）的概念。最终结果是，通过将空气流量增加到约1300单位或者比设计高30%并且给制氧设备供给由氮气发生器提供的极富液体，各生产群组的氧产量输出可以增加约50%。使用仅2个制氧群组和氮气发生器，总氧输出与使用3个制氧设备的情况相同。该氮气发生器储备系统小得多并且成本更低。
在起动和计划停机时段，在这种大型生产设施中需要利用氮气（氮气层、仪表气等）。在这种时段，可以方便地使用氮气发生器来供给所需的氮气利用。图3示出了在独立模式下操作以向复合体供给公用氮气的氮气发生器的一个实施例。在该模式中，全部或一部分极富液体在位于塔顶部的另一个冷凝器33中在低压力下气化。气化后的流51然后在交换器20中被加温并作为流52离开。
图4的设备包括高压塔100、中压塔101和低压塔102。还使用了辅助塔103。
供给到该工艺的空气的压力为约11bar，这使得吸附器/吸附剂容器更紧凑且体积更小。吸附器可以用于更高的空气流量，因为空气密度更高并且对于水分和CO2的吸附而言高压更加有利。
通过使高压供料空气膨胀至辅助低压塔中而减少高压塔的顶部蒸气流量，所述辅助低压塔将空气蒸馏为顶部氮气流和底部富氧液体。该辅助低压塔在类似于低压塔的压力下操作，它由顶部的液态氮回流供给。该压力可以低于、高于或等于低压塔的压力。液态空气流可以可选地供给到该辅助塔，以提高其蒸馏性能。
压力为11bar的空气1在压缩、冷却和净化后被分为三股流。
所述流中的一股为流8，流8在热交换器90中冷却而形成流6，流6呈气态形式被送至高压塔100。流6在高压塔100中被分离成顶部的富氮流和底部的富氧液流10。富氮流在第一冷凝器91中冷凝而产生第一液体回流。一部分氮42可以作为产品流在高压塔的顶部被萃取并送至热交换器90进行加温。第一回流的一部分11作为回流14被送至低压塔102并作为回流15被送至辅助塔103。回流的一部分89可以用作液氮产品。全部或一部分底部富液10被送至中压塔101的底部以进行进一步蒸馏。中压塔在介于高压塔的压力与低压塔的压力之间的中间压力下操作。第一冷凝器91在高压塔的顶部与中压塔的底部之间传热。中压塔将富液分离成顶部的第二富氮气体和底部的极富液12。第二富氮气体的一部分在第二冷凝器92中冷凝而产生第二回流，并且其余部分40作为气态流被除去并在热交换器90中加温。极富液12作为供料被送至低压塔102。在冷凝器92中形成的第二回流的一部分16可以作为回流被送至低压塔。第二冷凝器92在中压塔101的顶部与低压塔102的底部之间传热。
代替仅使供料空气膨胀到低压塔，利用涡轮80使供料空气的一部分31膨胀至辅助塔103中。辅助塔在介于1.1bar（绝对压力，absolute）与1.8bar（绝对压力）之间的压力下工作，该压力与低压塔102的压力大约相同。在高压塔或中压塔中产生的液体回流的一部分15作为回流被供给到辅助塔顶部。该辅助塔103将膨胀后的空气32分离成顶部的富氮气体21和底部的富含氧的第二富液60。第二富液然后膨胀并作为供料输送到低压塔102。辅助塔103可以位于低压塔102上方，以使得第二富液60可以通过重力供料流入低压塔中，或者可以使用输送泵。低压塔102将其供料分离成底部的液氧70和顶部的低压氮气20。液氧被泵压到高压并在主热交换器90中气化而产生气态高压氧产品72。供料空气的一部分2在热增压器84中被进一步压缩，在热交换器90中冷却而形成流3，流3在冷压缩机82中被压缩而形成高压流4，并用于与主交换器90中的气化液氧产品发生作用而冷凝。来自交换器90的流体5液化并被送至高压塔100。
压力为11bar的供料空气30的一部分可以或者可以不在涡轮81中作为流33膨胀而形成被送至低压塔102的流34。
通过将中压塔中产生的极富液供给到低压塔，大幅提高了低压塔的蒸馏性能，从而能以良好的氧回收速率执行大量膨胀后的空气流向第二低压塔、以及在高压塔和/或中压塔中萃取大量氮。
在图1所示的实施例中，示出了用于O2气化的冷压缩方案：空气部分2由压缩机84增压，然后在交换器90中冷却而产生冷的加压空气流3，空气流3然后由压缩机82冷压缩而产生压力更高的流4。流4接下来在交换器90中冷却而产生液流5，液流5然后被供给到塔系统。供料空气的一部分33可以可选地膨胀至低压塔102中，以向系统提供额外的制冷。膨胀器80或81的出口处的一部分低压膨胀空气可以经由管线36被送至塔103和102，以按需向塔均匀地分配空气流。
确定辅助塔103中的蒸气流速，以使得低压塔102上部区段的直径不大于多蒸馏塔系统的任何其它区段的直径。这里，低压塔102始终具有与高压塔100相同的直径。
由塔100、101和102的三塔装置提供的蒸馏性能的增强允许在正常操作下在辅助塔103的顶部实现大于在低压塔上部区段的顶部的蒸气流速的约50%的蒸气流速。

Claims (11)

1.一种用于通过空气的低温蒸馏而产生氮和富氧液体的设备，所述设备包括：具有顶部冷凝器和底部再沸器的塔；第一压缩机；第二压缩机；第一涡轮膨胀器；热交换器；用于将第一空气流送至所述交换器以形成第一冷却的空气流的导管装置；用于将所述第一冷却的空气流送至所述底部再沸器的导管装置；用于将冷凝的空气从所述底部再沸器送至所述顶部冷凝器的导管装置；用于将气化的空气从所述顶部冷凝器送至所述第一压缩机的导管装置；用于将空气从所述第一压缩机送至所述塔的导管装置；用于将空气送至所述第二压缩机并从所述第二压缩机送至所述交换器以产生冷却的第二空气流的导管装置；用于将所述冷却的第二空气流送至所述第一涡轮膨胀器并从所述涡轮膨胀器送至所述塔的导管装置；用于从所述塔除去底部液体的导管装置；以及用于从所述塔顶部除去气态氮的导管装置。
2.根据权利要求1所述的设备，包括用于将液氮送至所述塔顶部的导管装置。
3.根据权利要求1所述的设备，包括：另外的冷凝器；用于将底部液体从所述塔送至所述另外的冷凝器的导管装置；用于将气态氮从所述塔顶部送至所述另外的冷凝器的导管装置；以及用于从所述另外的冷凝器除去气化的底部液体的导管装置。
4.一种用于制氧的设施，所述设施包括：至少一个空气分离单元；至少一个根据前述权利要求中任一项所述的设备；用于将空气送至至少一个设备的压缩装置；用于将空气送至至少一个空气分离单元的压缩装置；用于从至少一个空气分离单元除去氧的导管装置；用于将来自所述设备的富氧液体送至至少一个空气分离单元的塔的导管装置。
5.根据权利要求4所述的设施，包括用于将富氮液体从至少一个空气分离单元的塔送至所述设备的导管装置。
6.根据权利要求4所述的设施，其中，所述用于将空气送至至少一个设备的压缩装置和所述用于将空气送至至少一个空气分离单元的压缩装置包括连接到至少一个空气分离单元和至少一个设备的至少一个压缩机。
7.一种用于通过低温蒸馏分离空气而产生氮和富氧液体的方法，其中将第一空气流送至交换器以形成第一冷却的空气流，将所述第一冷却的空气流送至塔的底部再沸器，将冷凝的空气从所述底部再沸器送至所述塔的顶部冷凝器，将气化的空气从所述顶部冷凝器送至第一压缩机，将空气从所述第一压缩机送至所述塔，将空气送至第二压缩机并从所述第二压缩机送至所述交换器以产生冷却的第二空气流，将所述冷却的第二空气流送至第一涡轮膨胀器并从所述涡轮膨胀器送至所述塔，从所述塔除去底部液体并从所述塔顶部除去气态氮。
8.根据权利要求7所述的方法，包括将液氮送至所述塔的顶部。
9.一种用于在一设施中制氧的集成方法，所述设施包括根据权利要求7所述的方法操作的至少一个空气分离单元和至少一个设备，其中将空气送至所述设备并送至所述空气分离单元，将底部液体从所述设备送至所述空气分离单元的塔，并从所述空气分离单元提取氧。
10.根据权利要求9所述的方法，其中，所述方法至少包括第一和第二空气分离单元并且当所述第二空气分离单元不工作时将底部液体送至所述第一空气分离单元。
11.根据权利要求10所述的方法，其中，当所述第二空气分离单元工作时，将空气从一压缩机送至所述第二空气分离单元，而当所述第二空气分离单元不工作时，将空气从所述压缩机送至所述设备。
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