CN103038588A - 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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CN103038588A
CN103038588A CN2010800639180A CN201080063918A CN103038588A CN 103038588 A CN103038588 A CN 103038588A CN 2010800639180 A CN2010800639180 A CN 2010800639180A CN 201080063918 A CN201080063918 A CN 201080063918A CN 103038588 A CN103038588 A CN 103038588A
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tower
pressure column
column
nitrogen
lower pressure
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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
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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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    • 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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    • F25J2290/12—Particular process parameters like pressure, temperature, ratios
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/80—Retrofitting, revamping or debottlenecking of existing plant

Abstract

一种使用至少包括高压塔（“HP塔”）和低压塔（“LP塔”）的多塔蒸馏系统低温分离空气的方法，所述方法包括：将冷却的供料空气供给到高压塔，以分离成高压富氮塔顶蒸气和粗制液氧；将包含氮和氧的至少一股低压塔供料流供给到低压塔以分离成富氮塔顶蒸气和液氧；使来自或来源于高压塔的液体流回流到低压塔中；将膨胀后的空气供给到辅助分离塔以分离成辅助塔富氮塔顶蒸气和富氧液体并将富氮塔顶蒸气作为产品流除去；将来自辅助塔的底部液体供给到低压塔的中间位置；以及使来自或来源于HP塔的富氮液体流回流到辅助塔。

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/工艺和设备。
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。
空气分离单元（ASU）的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（GTL）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。
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增加空气流量或加速（增强，boosting）而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。
在大部分情况下，塔顶的氮流量决定塔尺寸或设备尺寸。瓶颈不仅出现在低压塔的顶部，而且出现在高压塔的顶部。因此，为了大幅增加产量输出，所选的工艺必须减少所有塔顶部的蒸气流量。
可以通过经由使一些供料空气膨胀至低压塔中产生设备制冷而减少高压塔的顶部流量。必须限制膨胀空气流，否则蒸馏效率将降低，因为膨胀空气流减少了低压塔的再沸和回流。
可以通过从高压塔顶部萃取氮使得较少的氮到达低压塔从而减少低压塔的顶部蒸气流量来使低压塔的顶部流量最小化。同样，由于蒸馏效率方面的考虑，必须限制氮气萃取流量。
就使膨胀空气流量或高压氮萃取最大化而言，双塔方案并非非常适合。实际上，对于约95-97%（摩尔百分比）的氧纯度，总供料空气的大约25-30%可膨胀至低压塔。在这种大量膨胀的空气的情况下，难以从高压塔有效地萃取氮。显然，空气膨胀可以减少高压塔的顶部蒸气流量，但不会减少低压塔的顶部流量，因为膨胀的空气中包含的氮必须在低压塔的顶部离开。如果没有膨胀的空气，则可以在高压塔的顶部将高达20-25%的总空气流量作为氮气除去。由于氧气流量代表供料空气的20%，所以这意味着代表总供料空气流量的约55-60%的流量必须在低压塔的顶部离开。如果从高压塔除去更多氮气，则蒸馏效率将受影响，导致氧气回收损失，并且需要更高的空气流量来生产给定量的氧气。因此，这种氮移除技术可以提高低压塔的顶部流量，但对高压塔的顶部流量不起作用。
根据本发明，提供了一种用于使用至少包括高压塔（“HP塔”）和低压塔（“LP塔”）的多塔蒸馏系统低温分离空气的方法，所述方法包括：将经冷却的供料空气供给到高压塔，以分离成高压富氮塔顶蒸气和粗制（crude）液氧；将包含氮气和氧气的至少一股低压塔供料流供给到低压塔以分离成富氮塔顶蒸气和液氧；使来自或来源于高压塔的液体流回流到低压塔；将膨胀空气供给到辅助分离塔以分离成辅助塔富氮塔顶蒸气和富氧液体并将富氮塔顶蒸气作为产品流除去；将来自辅助塔的底部液体供给到低压塔的中间位置；以及使来自或来源于HP塔的富氮液体流回流到辅助塔。
根据可选特征：
-确定辅助塔中的蒸气流速，以使得低压塔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。
-辅助分离塔中的蒸气流速大于LP塔上部区段中的蒸气流速的约50%。
-没有来自低压塔的液氧被送至混合塔。
-该方法包括中压塔，该中压塔从高压塔接收粗制液氧并产生供给低压塔的包含氮和氧的所述至少一股低压塔供料流。
-从低压塔提取液氧并使其在主热交换器中气化。
-从低压塔提取的液氧的量增加，送至辅助塔的膨胀空气的量增加x%，送至高压塔的气态空气的量增加y%，y小于x且辅助塔的操作压力增大。
-y大致为零。
-空气膨胀至低压塔中，并且如果所提取的液氧的量增加，则膨胀至低压塔的空气量增加z%，z小于x。
-该方法包括从高压塔顶部除去高压富氮塔顶蒸气；使其至少一部分在位于低压塔底部中的再沸器/冷凝器中冷凝；并且将冷凝的氮的至少一部分作为回流供给到HP塔。
-在再沸器/冷凝器中产生的冷凝氮回流到辅助塔。
-辅助分离塔中的液体未由再沸器/冷凝器煮沸。
根据本发明的又一方面，提供了一种用于低温分离空气的设备，该设备包括：用于将经冷却的供料空气分离成高压富氮塔顶蒸气和粗制液氧的高压塔；用于将包含氮和氧的至少一股低压塔供料流分离成低压富氮塔顶蒸气和液氧的低压塔；用于将来自或来源于高压塔的液体流作为回流供给到低压塔的导管装置；用于将空气分离成辅助塔富氮塔顶蒸气和富氧液体的辅助分离塔；用于将富氮塔顶蒸气作为产品除去的导管装置；用于将来自辅助塔的富氧液体膨胀并且供给到低压塔中的中间位置的导管装置；以及用于将来自或来源于HP塔的富氮液体流作为回流供给到辅助塔的导管装置。
-低压塔（30）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。
-该设备还包括空气膨胀涡轮和用于将来自所述涡轮的排出流的至少一部分作为膨胀空气供给到辅助分离塔的导管装置。
-该设备还包括：再沸器/冷凝器，其用于使所述高压富氮塔顶蒸气的至少一部分通过与低压塔的底部中的液氧进行间接热交换而冷凝；用于将来自高压塔顶部的高压富氮蒸气供给到再沸器/冷凝器的导管装置；以及用于将来自再沸器/冷凝器的冷凝氮的至少一部分作为回流供给到高压塔顶部的导管装置。
-用于将来自高压塔的冷凝氮作为回流供给到辅助分离塔的导管装置。
-该设备不包括混合塔。
-辅助分离塔不具有再沸器/冷凝器。
附图说明
针对大型制氧设备提出如图1所示的改型三塔工艺。
具体实施方式
该设备包括高压塔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，以改善其蒸馏性能。
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以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作为气态流被移除并在热交换器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。
由包括塔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实现在辅助分离塔103的顶部的蒸气流速大于在低压塔上部区段的顶部的蒸气流速的约50%。
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。
解决储备问题的另一个方案（也称为加速/增强）是加大各群组的尺寸（使尺寸带余量），以使得在一个群组中断的情况下可以提高或升高其生产速率，以维持总产量。
上述方案在图2中示出。
显然，上述用于储备的规定在资本支出方面是昂贵的，因为备用设备或额外的生产能力在大部分时间未得到充分利用。因此，需要改善备用设备的成本和效力，尤其是在由多个群组组成的大型设施的情况下。
本发明的图1的工艺也可以用于有效地适应更高的空气吞吐量以提高产量。实际上，经历设计条件之上的更高空气流量的低温系统的主要代价是背压的提高。在较高的空气流量下，工艺中的所有流量增加，导致所有管道回路中的压降更高。低压回路中背压的提高对系统效率不利，因为在双塔系统的情况下，例如由于较高压降而引起的100mbar（毫巴）的背压提高将引起高压塔的压力提高约300mbar。空气压缩机除了克服在更高流量下的压降提高外还必须克服这种背压的提高，同时必须传送更高的空气流量。在增加的空气流量下压力的增加还要求加大空气压缩机的尺寸以使排出压力更高，这会对压缩机的效率不利并且导致每单位产品的功耗更高。此外，流量的增加还增加了在高压塔与低压塔之间传热的主蒸发器的冷凝器负荷。负荷的增加引起温差更高，因此使空气压缩机的运转压力更高。
塔100中的空气被分离成粗制氧流10和富氮流。粗制氧流被送至低压塔底部。可以仅经由增加通向膨胀器80和塔103的流31的流量来执行总空气流量的增加。在这种情况下，如果在正常流量下塔103在比塔102的压力低或与塔102的压力相等的压力下操作，则塔103将在比塔102的压力高的压力下操作。可以保持供给其它塔100、101和102的空气流量恒定，以避免上面所述的背压提高。在塔103中以及膨胀器80的出口处，背压将增加。通过限制膨胀器80和第二低压塔103的专用回路中的背压的提高，并且仅限制在总体流的一小部分上，可以推动更多流量通过系统以提高产量。而且可以避免流量的增加和背压的提高导致的对整个系统的不利影响。在膨胀器80和塔103的回路上将存在更高的压降和更高的背压，但是对功耗的影响将最小并且在储备模式期间可以容易地进行调整。除专用回路外，在加速模式的较高流量下，工艺的主回路在基本与正常条件下相同的压力下操作。因此，可以在不必加大热交换器群组和相关的管道设备的尺寸的前提下实现加速。

Claims (19)

1.一种使用至少包括高压塔（“HP塔”）和低压塔（“LP塔”）的多塔蒸馏系统来低温分离空气的方法，所述方法包括：将冷却后的供料空气供给到所述高压塔，以分离成高压富氮塔顶蒸气和粗制液氧；将包含氮和氧的至少一股低压塔供料流供给到所述低压塔以分离成富氮塔顶蒸气和液氧；使来自或来源于所述高压塔的液体流回流到所述低压塔；将膨胀后的空气供给到辅助分离塔以分离成辅助塔富氮塔顶蒸气和富氧液体并将所述富氮塔顶蒸气作为产品流除去；将来自所述辅助塔的底部液体供给到所述低压塔的中间位置；以及使来自或来源于所述HP塔的富氮液体流回流到所述辅助塔。
2.根据权利要求1所述的方法，其中，确定所述辅助塔中的蒸气流速，以使得所述低压塔上部区段的直径不大于所述多蒸馏塔系统的任何其它区段的直径。
3.根据权利要求1所述的方法，其中，所述辅助分离塔中的蒸气流速大于所述LP塔上部区段中的蒸气流速的约50%。
4.根据权利要求1所述的方法，其中，来自所述低压塔的液氧未被送至混合塔。
5.根据权利要求1所述的方法，包括中压塔，所述中压塔从所述高压塔接收粗制液氧并产生供给所述低压塔的包含氮和氧的所述至少一股低压塔供料流。
6.根据权利要求1所述的方法，其中，从所述低压塔提取液氧并使其在主热交换器中气化。
7.根据权利要求1所述的方法，其中，从所述低压塔提取的液氧的量增加，送至所述辅助塔的膨胀空气的量增加x%，送至所述高压塔的气态空气的量增加y%，y小于x且所述辅助塔的操作压力增大。
8.根据权利要求7所述的方法，其中，y大致为零。
9.根据权利要求7所述的方法，其中，空气膨胀至所述低压塔中，并且如果所提取的液氧的量增加，则膨胀至所述低压塔的空气量增加z%，z小于x。
10.根据权利要求1所述的方法，还包括：从所述高压塔的顶部除去高压富氮塔顶蒸气；使所述高压富氮塔顶蒸气的至少一部分在位于所述低压塔底部中的再沸器/冷凝器中冷凝；并且将冷凝的氮的至少一部分作为回流供给到所述HP塔。
11.根据权利要求10所述的方法，其中，在所述再沸器/冷凝器中产生的冷凝的氮回流到所述辅助塔。
12.根据权利要求1所述的方法，其中，所述辅助分离塔中的液体未由再沸器/冷凝器煮沸。
13.一种用于低温分离空气的设备，包括：用于将冷却后的供料空气分离成高压富氮塔顶蒸气和粗制液氧的高压塔；用于将包含氮和氧的至少一股低压塔供料流分离成低压富氮塔顶蒸气和液氧的低压塔；用于将来自或来源于所述高压塔的液体流作为回流供给到所述低压塔的导管装置；用于将空气分离成辅助塔富氮塔顶蒸气和富氧液体的辅助分离塔；用于将所述富氮塔顶蒸气作为产品除去的导管装置；用于使来自所述辅助塔的富氧液体膨胀并且将其供给到所述低压塔中的中间位置的导管装置；以及用于将来自或来源于所述HP塔的富氮液体流作为回流供给到所述辅助塔的导管装置。
14.根据权利要求13所述的设备，其中，所述低压塔上部区段的直径不大于所述多蒸馏塔系统的任何其它区段的直径。
15.根据权利要求13所述的设备，还包括空气膨胀涡轮和用于将来自所述涡轮的排出流的至少一部分作为膨胀空气供给到所述辅助分离塔的导管装置。
16.根据权利要求13所述的设备，还包括：再沸器/冷凝器，其用于使所述高压富氮塔顶蒸气的至少一部分通过与所述低压塔的底部中的液氧进行间接热交换而冷凝；用于将来自所述高压塔顶部的高压富氮蒸气供给到所述再沸器/冷凝器的导管装置；以及用于将来自所述再沸器/冷凝器的冷凝氮的至少一部分作为回流供给到所述高压塔顶部的导管装置。
17.根据权利要求16所述的设备，还包括用于将来自所述高压塔的冷凝氮作为回流供给到所述辅助分离塔的导管装置。
18.根据权利要求13所述的设备，不包括混合塔。
19.根据权利要求13所述的设备，其中，所述辅助分离塔不具有再沸器/冷凝器。
CN2010800639180A 2009-12-17 2010-12-03 用于通过低温蒸馏分离空气的方法和设备 Pending CN103038588A (zh)

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