CN115461584A - 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 - Google Patents

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 Download PDF

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CN115461584A
CN115461584A CN202080100033.7A CN202080100033A CN115461584A CN 115461584 A CN115461584 A CN 115461584A CN 202080100033 A CN202080100033 A CN 202080100033A CN 115461584 A CN115461584 A CN 115461584A
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stream
argon
column
nitrogen
oxygen
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B·R·克罗默
N·M·普罗塞
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Praxair Technology Inc
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Praxair Technology Inc
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    • 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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Abstract

提供了一种中压制氮和制氩低温空气分离单元，该中压制氮和制氩低温空气分离单元包括三个蒸馏塔系统和涡轮空气流旁通布置或回路。涡轮空气流旁通布置或回路被构造成通过任选地将涡轮空气流的一部分分流到从低温空气分离单元的低压塔抽取的氮废物流回路，使得涡轮空气流的分流部分绕过蒸馏塔系统，从而在所选的操作模式下改善氩和氮回收率。

Description

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
技术领域
本发明涉及从制氮低温空气分离单元中提高液氧回收率，并且更具体地，涉及从具有高氩和氮回收率的中压低温空气分离单元中提高液氧回收率。
背景技术
以制氮为目标并在中压(即，高于常规低温空气分离单元压力的压力)下操作的空气分离设备已存在一段时间。在常规空气分离单元中，如果中压下的氮是期望的，则可在高于常规空气分离单元的压力下操作低压塔。然而，这种操作通常会导致氩回收率的显著降低，因为很多氩会在富氧流或富氮流中损失而不是传递至氩塔。
为了在此类中压制氮空气分离单元中增加氩回收率，在20世纪80年代晚期和20世纪90年代早期开发了改进的空气分离循环。参见例如技术出版物Cheung，中压低温空气分离过程、气体分离和纯化(Moderate Pressure Cryogenic Air Separation Process,GasSeparation&Purification)，第5卷，1991年3月和美国专利号4,822,395(Cheung)。在这些现有技术文献中，公开了氩回收率略高的制氮和制氩空气分离设备。改进的空气分离循环涉及在优选地介于约80psia至150psia之间的标称压力下操作高压塔，而低压塔优选地在约20psia至45psia的标称压力下操作，并且氩塔也将优选地在约20psia至45psia的标称压力下操作。约20psia至45psia的中压下的高纯度氮(即，>99.98％纯度)的回收率大约为94％。97.3％纯度和介于约20psia至45psia之间的压力下的高氩回收率一般高于90％但上限为93％。
在上述现有技术中压空气分离循环中，来自低压塔的贮槽的高纯度液氧用作氩冷凝器中的制冷剂而不是釜液体。然而，当使用来自低压塔的贮槽的高纯度液氧时，氩塔需要在比常规氩塔更高的压力下操作以便实现氩冷凝器中的所需温度差。氩塔的压力增加需要低压塔和高压塔也在中压或高于常规低温空气分离单元的压力下操作。
氩冷凝器中使用高纯度液氧也意味着避免了通常进给低压塔的较大釜蒸气流，这使得回收率显著提高。因此，通过该中压空气分离循环可实现对氮、氩和氧的高回收率，尽管与常规空气分离循环相比，高压另外会对回收造成罚分。空气分离单元的中压操作一般有利于制氮，因为这意味着氮压缩不太耗能并且氮压缩机往往比常规系统的氮压缩机更便宜。
尽管Cheung公布和美国专利号4,822,395中的空气分离单元提供了离开氩冷凝器的高纯度氧蒸气，但该氧流不用作氧产物，因为该流在过低的压力(例如，18psia)下离开该工艺并且将通常需要氧压缩机以足够的压力将氧产物递送给顾客。在一些地区中，由于安全和成本考虑，氧压缩机的使用通常是不可接受的。当使用氧压缩机时，氧压缩机非常昂贵并且通常需要更复杂的工程安全系统，这两者都不利地影响了空气分离单元的资本成本和操作成本。
美国专利申请序列号15/962,205、15/962,245、和15/962,297公开了用于中压低温空气分离单元的新的空气分离循环，其提高氩回收率并提供有限的氧回收率而不需要氧压缩机。然而，这些新的低温空气分离循环在非设计操作模式下诸如启动、高液制备、低氩制备、高纯度氮制备等时在操作上受到限制，因为需要从低压塔抽取废氮流，这继而又对氮回收、氩回收或两者都产生不利影响。
需要进一步改进中压低温空气分离单元和中压低温空气分离循环，使其与在正常操作模式下的氮回收率和氩回收率相比，能够在非设计操作模式下操作而不会显著降低氮回收率和/或氩回收率。
发明内容
本发明可以表征为制氮和制氩低温空气分离单元，其包括：(i)主空气压缩系统，该主空气压缩系统被构造成接收进入的进料空气流并产生压缩空气流；(ii)基于吸附的预纯化单元，该基于吸附的预纯化单元被构造用于从压缩空气流移除水蒸气、二氧化碳、一氧化二氮和烃类并且产生经压缩并且纯化的空气流，其中经压缩并且纯化的空气流被分成至少经压缩并且纯化的空气流的第一部分和经压缩并且纯化的空气流的第二部分；(iii)主换热系统，该主换热系统被构造成冷却经压缩并且纯化的空气流的第一部分并且部分地冷却经压缩并且纯化的空气流的第二部分；和(iv)涡轮膨胀机布置，该涡轮膨胀机布置被构造为使经压缩并且纯化的空气流的经部分冷却的第二部分膨胀以形成排气流；(v)蒸馏塔系统，该蒸馏塔系统具有经由冷凝器-再沸器以热传递关系连接的高压塔和低压塔，并且被构造成分离经压缩并且纯化的空气流的经冷却的第一部分与排气流的第一部分，并且产生来自低压塔的基部的富氧流和来自低压塔的塔顶的氮产物流；和(vi)涡轮空气流塔旁通回路，该涡轮空气流塔旁通回路被构造成将排气流的第二部分引导到从低压塔抽取的废物流，使得排气流的第二部分绕过蒸馏塔系统。
蒸馏塔系统还包括与低压塔操作地联接的氩塔布置，该氩塔布置具有至少一个氩塔和氩冷凝器，并且其中氩塔布置被构造成从低压塔接收富氩氧流，并且产生返回或释放到低压塔中的富氧塔底馏出物流和被引导到氩冷凝器的富氩塔顶馏出物。氩冷凝器被构造成依靠来自低压塔的富氧流的全部或一部分来冷凝富氩塔顶馏出物，以产生粗氩流或产物氩流、氩回流流和富氧废物流。
另选地，本发明可以表征为在低温空气分离单元中分离空气以产生一种或多种氮产物和粗氩产物的方法，该方法包括以下步骤：(a)压缩进入的进料空气流以产生压缩空气流；(b)在基于吸附的预纯化单元中纯化压缩空气流，该基于吸附的预纯化单元被构造成从压缩空气流移除水蒸气、二氧化碳、一氧化二氮和烃类以产生经压缩并且纯化的空气流；(c)将经压缩并且纯化的空气流分成至少经压缩并且纯化的空气流的第一部分和经压缩并且纯化的空气流的第二部分；(d)在主换热器系统中冷却经压缩并且纯化的空气流的第一部分和经压缩并且纯化的空气流的第二部分；(e)在涡轮膨胀机布置中使经压缩并且纯化的空气流的经冷却的第二部分膨胀以形成排气流；(f)将排气流的第一部分和经压缩并且纯化的空气流的经冷却的第一部分引导到蒸馏塔系统；(g)在蒸馏塔系统中分离排气流的第一部分与经压缩并且纯化的空气流的经冷却的第一部分，以产生来自低压塔的基部的富氧流和来自低压塔的塔顶的氮产物流；(h)在氩塔布置中进一步分离从低压塔获取的富氩氧流，以产生富氧塔底馏出物流和富氩塔顶馏出物；(i)将富氧塔底馏出物流引导到低压塔中；(j)将富氩塔顶馏出物引导至氩冷凝器的冷凝侧；(k)将富氧流的全部或一部分从低压塔引导到氩冷凝器的沸腾侧；(l)依靠来自低压塔的富氧流来冷凝富氩塔顶馏出物以产生粗氩流和氩回流流，同时使富氧流的第一部分和液氮沸腾以产生富氧废物流；以及(m)将排气流的第二部分引导到从低压塔抽取的废物流，使得排气流的第二部分绕过蒸馏塔系统。
附图说明
虽然本发明总结了明确指出申请人认为是其发明内容的主题的权利要求，但相信本发明在结合附图考虑时将得到更好的理解，其中：
图1是现有技术制氮和制氩中压低温空气分离单元的示意性工艺流程图；
图2是根据本发明的一个实施方案的制氮和制氩中压低温空气分离单元的示意性工艺流程图；并且
图3是示出随低压塔中的氮废物抽取位置变化的以及当采用根据本发明的涡轮空气旁通布置时的制氮和制氩中压低温空气分离单元中的氮和氩回收率的曲线图。
具体实施方式
本发明所公开的系统和方法提供了在中压空气分离单元中的低温空气分离，其特征在于非常高的氮回收率、高氩回收率以及有限的高纯度氧制备。如下文更详细地讨论，取自低压塔的高纯度富氧流的一部分或取自低压塔的低纯度富氧流用作氩冷凝器中的冷凝介质以使富氩流冷凝，并且来自氩冷凝器的富氧沸腾溢出然后用作吹扫气体以使基于吸附的预纯化单元中的吸附剂床再生。在随后的段落中提供本发明系统和方法的细节。
在中压ASU的正常操作模式下回收N2、Ar和O2
转到图1，其示出了空气分离单元10的简化示意图。如在美国专利申请序列号15/962,205、15/962,245、和15/962,297中所述，所示的中压低温空气分离单元包括主进料空气压缩机组或系统20、涡轮空气回路30、任选的增压空气回路40、初级换热器系统50和蒸馏塔系统70。如本文所用，主进料空气压缩机组、涡轮空气回路和增压空气回路共同构成“热端”空气压缩回路。类似地，主换热器、基于涡轮的制冷回路的部分和蒸馏塔系统的部分被称为通常容纳绝缘冷箱中的“冷端”设备。
在图1中所示的主进料压缩机组中，进入的进料空气22通常被抽吸穿过空气吸滤器外壳(ASFH)并且在多级中间冷却的主空气压缩机布置24中被压缩至可介于约6.5巴(a)与约11巴(a)之间的压力。该主空气压缩机布置24可包括串联或并联布置的整体齿轮式压缩机级或直接驱动压缩机级。离开主空气压缩机布置24的压缩空气流26被进料至具有一体式除雾器的后冷却器，以移除进入的进料空气流中的游离水分。通过用冷却塔水冷却经压缩进料空气，在后冷却器中将来自主空气压缩机布置24的最后压缩级的压缩的压缩热移除。来自该后冷却器以及主空气压缩布置24中的一些中间冷却器的冷凝物优选地输送到冷凝物罐，并且用于向空气分离设备的其他部分供应水。
然后将冷却且干燥的经压缩空气流26在预纯化单元28中纯化，以从该冷却且干燥的经压缩空气进料中移除高沸点污染物。如本领域所熟知，预纯化单元28通常包含根据变温吸附循环操作的氧化铝和/或分子筛的两个床，在该变温吸附循环中水分及其他杂质(诸如二氧化碳、水蒸气和烃类)被吸附。这些床中的一个床用于预纯化该冷却且干燥的经压缩空气进料，而另一个床是优选地利用来自空气分离单元的废氮的一部分再生的。这两个床定期交换功用。在设置在预纯化单元28下游的粉尘过滤器中，从经压缩、预纯化的进料空气中移除颗粒以产生经压缩、纯化的空气流29。
经压缩并且纯化的空气流29在包括高压塔72、低压塔74和氩塔129的多个蒸馏塔中被分离为富氧馏分、富氮馏分和富氩馏分。然而，在此类蒸馏之前，通常将经压缩并且预纯化的空气流29分成多个进料空气流，该多个进料空气流可包括锅炉空气流和涡轮空气流32。可将锅炉空气流在增压压缩机布置中进一步压缩，并且随后在后冷却器中冷却以形成增压空气流360，然后在主换热器52中将该增压空气流进一步冷却。优选地通过与包括氧流197、386的加热流以及来自蒸馏塔系统70的氮流195的间接换热来在主换热器52中完成对空气流的冷却或部分冷却，以产生经冷却的进料空气流。
使经部分冷却的进料空气流38在涡轮35中膨胀，以产生被引导至低压塔74的排气流64。用于空气分离单元10的制冷的一部分通常也由涡轮35产生。完全冷却的空气流47以及高压空气流被引入高压塔72中。任选地，不在涡轮进料流38中抽出涡轮空气回路30中流动的小部分空气。在换热器52的冷端处抽出任选的增压流48，使该增压流完全或部分冷凝，在阀49中降低压力，并且在离塔底若干级处进料至高压塔72。仅在所泵送的氧流386的大小足够高时利用流48。
主换热器52优选地为钎焊铝制板翅式换热器。此类换热器是有利的，因为它们具有紧凑设计、高传热速率，而且它们能够处理多个流。它们被制造为完全钎焊和焊接的压力容器。对于小型空气分离单元而言，具有单个芯的换热器可能已足够。对于处理较高流量的较大空气分离单元而言，换热器可由必须并联或串联连接的若干芯构造而成。
基于涡轮的制冷回路通常被称为下塔涡轮(LCT)布置或上塔涡轮(UCT)布置，其用于向双塔或三塔低温空气蒸馏塔系统提供制冷。在图1所示的UCT布置中，经压缩且经冷却的涡轮空气流32优选地在介于约6巴(a)至约10.7巴(a)之间的压力下。将经压缩、冷却的涡轮空气流32引导至或引入主换热器或初级换热器52中，在其中将该经压缩、冷却的涡轮空气流部分冷却至约140开尔文至约220开尔文之间的范围内的温度以形成经部分冷却、压缩的涡轮空气流38，该经部分冷却、压缩的涡轮空气流被引入涡轮35中以产生冷排气流64，该冷排气流随后被引入蒸馏塔系统70的低压塔74中。由该流38的膨胀而产生的补充制冷由此被直接施加到低压塔72，从而减轻了主换热器52的一些冷却负荷。在一些实施方案中，涡轮35可与用于直接或通过适当的齿轮装置进一步压缩涡轮空气流32的增压压缩机34联接。
虽然图1中所示的基于涡轮的制冷回路被示出为上塔涡轮(UCT)回路(其中涡轮排气流被引导至低压塔)，但可设想到基于涡轮的制冷回路另选地可为下塔涡轮(LCT)回路或部分下塔涡轮(PLCT)(其中膨胀的排气流被进料至蒸馏塔系统70的高压塔72)。更进一步，基于涡轮的制冷回路可以是本领域技术人员通常已知的LCT布置、UCT布置和/或热再循环涡轮(WRT)布置的某种变型或组合。
在包括高压塔72、低压塔74、氩塔129、冷凝器-再沸器75和氩冷凝器78的蒸馏塔系统70内分离进入的进料空气流的上述组分(即，氧、氮和氩)。高压塔72通常在介于约6巴(a)至约10巴(a)之间的范围内操作，而低压塔74在介于约1.5巴(a)至约2.8巴(a)之间的压力下操作。高压塔72和低压塔74优选地以热传递关系相连，使得从接近高压塔72的顶部提取为流73的富氮蒸气塔顶馏出物的全部或一部分在位于低压塔74的基部的冷凝器-再沸器75内依靠驻留在低压塔74的底部中的富氧液体塔底馏出物77而冷凝。富氧液体塔底馏出物77的沸腾引发在低压塔74内形成上升汽相。该冷凝产生含液氮流81，该含液氮流被分成干净搁板回流流83和富氮流85，该干净搁板回流流可用于回流低压塔74以引发这种低压塔74中下降液相的形成，并且该富氮流回流高压塔72。
经冷却的进料空气流47优选地是略高于其露点的蒸气空气流，但其可处于或略低于其露点，该经冷却的进料空气流被进料至高压塔中，从而因多个传质接触元件(被示出为塔盘71)内发生上升汽相与回流流85所引发的下降液相之间的传质而实现精馏。这产生了粗液氧塔底馏出物86(也称为釜液体，其作为流88取出)和富氮塔顶馏出物89(作为干净搁板液体流83取出)。
在低压塔中，上升汽相包括来自冷凝器-再沸器的汽化气体以及来自涡轮35的排气流64，该排气流在过冷单元99B中过冷并且在低压塔72的中间位置处作为蒸气流引入。下降液体由氮回流流83引发，该氮回流流被送至过冷单元99A，其在此处过冷并且随后先在阀96中膨胀，再在接近低压塔的顶部的位置处引入至低压塔74。如果需要，可经由阀101取出过冷氮回流流83的小部分作为液氮产物98。
低压塔74还设置有多个传质接触元件，这些接触元件可以是塔盘或规整填料或低温空气分离领域中的其他已知元件。低压塔74中的这些接触元件被示出为规整填料79。在低压塔74内发生的分离产生了富氧液体塔底馏出物77，该富氧液体塔底馏出物被提取为具有大于99.5％的氧浓度的富氧液体流377。低压塔还产生作为气态氮产物流95提取的富氮蒸气塔顶馏出物。
富氧液体流377可被分离成在泵385中泵送的第一富氧液体流380，并且所得的泵送氧流386被引导至主换热器52，在该主换热器中它被加热以产生高纯度气态氧产物流390。富氧液体流377的第二部分被分流为第二富氧液体流90。第二富氧液体流90优选地经由泵180泵送，然后在过冷单元99B中经由与富氧废物流196进行间接换热而过冷，并且然后传递至氩冷凝器78，其中它用于冷凝取自氩塔129的塔顶123的富氩流126。如图1所示，过冷的第二富氧液体流90的一部分或第一液体氧流的一部分可作为液氧产物。然而，如图1所示的液氧产物185的提取对空气分离单元的运行效率和其中的氩和氮的回收产生不利影响。
从氩冷凝器78汽化的蒸发氧流是在过冷器99B内加热的富氧废物流196。将经加热的富氧废物流197引导至主换热器或初级换热器，然后用作吹扫气体以再生基于吸附的预纯化单元28。另外，可从低压塔提取废氮流93以控制气态氮产物流95的纯度。优选地将废氮流93与过冷器99B上游的富氧废物流196合并。另外，在一些情况下，在可供使用的氧多于操作氩冷凝器78所需的氧时，通常在氩产量减少时，可需要蒸气废物氧流97。
从氩冷凝器容器120抽出液体流130，使该液体流穿过凝胶阱370并且返回至低压塔74的基部或基部附近。凝胶阱370用于移除原本可能积聚在系统中的二氧化碳、一氧化二氮和某些重质烃。另选地，可经由流130来抽出小流量作为来自系统的排放流，使得凝胶阱140被消除(未示出)。
优选地，图中所示的氩冷凝器是降流氩冷凝器。降流构型使得冷凝流与沸腾流之间的有效温差(ΔT)更小。如上所指示，更小的ΔT可引起氩塔、低压塔和高压塔内的操作压力降低，这使得产生各种产物流所需的功率减少以及氩回收率提高。降流氩冷凝器的使用还实现了塔级数量的潜在减少，特别是对于氩塔而言。从资本的角度来看，氩降流冷凝器的使用也是有利的，部分原因是本发明公开的空气分离循环中已经要求泵180。另外，由于液体流130已经提供离开氩冷凝器壳体的连续液体流，该液体流还提供再沸表面的必要润湿以防止氩冷凝器‘蒸干’。
使氮产物流95穿过过冷单元99A以经由间接换热来使氮回流流83和釜液体流88过冷。如上所述，过冷氮回流流83在阀96中膨胀并被引入低压塔74的最高位置，而过冷釜液体流88在阀107中膨胀并被引入低压塔74的中间位置。在穿过过冷单元99A之后，经加热的氮流195在主换热器52内进一步加热以产生经加热的气态氮产物流295。
第一富氧液体流380的流量可为多达约20％的离开系统的总富氧流。该布置的氩回收率介于约75％与96％之间，这大于现有技术的中压空气分离系统。虽然未示出，但取自外部源(未示出)的液氮流可与第二富氧液体流90和用于在氩冷凝器78中冷凝富氩流126的组合流组合，以增强氩回收。
在非设计操作模式中回收氮、氩和氧
在美国专利申请序列号15/962,205、15/962,245、和15/962,297中公开的并且上文参考图1论述的空气分离循环非常适合在非常高的气体回收率下制氮和制氩。在正常操作模式中，不需要从低压塔抽取废氮，这可以产生达到或接近100％的有效氮回收率。然而，在一些非设计操作模式诸如低氩模式、高液制备模式、启动模式等中，图1的低温空气分离单元可能需要氮废物抽取以维持从低压塔顶部获取的氮纯度。另外，由于低温空气分离单元的性能不佳，或由于与氮产物纯度相关的产物要求发生变化或增加，可能时不时在低压塔中采用氮废物抽取。从低压塔中抽出废氮具有提高低压塔顶部或上段的液气流量比(L/V)的效果，从而提高从低压塔顶盖或顶部获取的氮的氮纯度，并确保氮产物的纯度在产物规格内。
图2示出了本发明制氮和制氩中压低温空气分离单元的实施方案。图2所示的空气分离设备中的许多部件与上文参考图1所述的那些部件类似或相同，并且为了简洁起见将不再重复。图2的实施方案与图1所示的实施方案之间的差异在于增加了塔旁通回路500。如其中所见，包括绕过图2中的低压塔的经冷却的涡轮空气流502的分流部分504的涡轮空气旁通布置是来自图1的低压塔74的常规废氮抽取管线93的功能替代方案。
从任何制氮和制氩中压低温空气分离单元中的低压塔中选择氮废物抽取的最佳位置需要在氮回收率与氩回收率之间进行折衷。例如，在一方面，如果氮废物抽取位置在竖直方向上位于低压塔的较高位置处，则氩回收率最高。然而，来自竖直方向上较高位置的氮废物流量可能需要较大，以确保满足顶盖氮纯度要求，这对氮回收率产生了负面影响。另一方面，如果氮废物抽取位置在竖直方向上位于低压塔的较低位置处，则废物抽取中的氩浓度将相对较高并且可能对氩回收率具有负面影响。在氮废物抽取在竖直方向上位于低压塔的较低位置处的塔构型中，氮回收率可能更高，因为与竖直方向上较高的废物抽取位置处所需的氮废物抽取流量相比，满足氮产物纯度要求所需的总氮废物抽取流量下降。
在美国专利申请序列号15/962,205、15/962,245、15/962,297和图1中公开的低温空气分离单元的模拟已经示出，最佳氮废物抽取位置位于或接近与涡轮空气流64进料到低压塔74和/或釜液体88进料到低压塔74的相同位置处。
已经认识到，由于氮废物抽取在这些制氮和制氩中压低温空气分离单元中的理想位置位于或接近与涡轮空气流64进料到低压塔74的相同位置处，因此抽出氮废物流量对L/V比的影响与将经冷却的涡轮空气流502的一部分，或更准确地说第二部分504，直接分流到废物回路并绕过蒸馏塔系统对L/V比的影响相同。该旁通流被称为涡轮空气塔旁通流504。涡轮空气流的其余部分，或更准确地，涡轮空气流506的第一部分被进料到蒸馏塔系统中，优选地在低压塔74的中间位置处进料。
图3示出了与采用本发明涡轮空气旁通布置的实施方案相比，随低压塔中的氮废物抽取位置变化的制氮和制氩中压低温空气分离单元中的氮和氩回收率的曲线图。如其中所见，与从低压塔提取类似体积的废物相比，当将涡轮空气流的一部分直接分流到废气回路并绕过低压塔时，氮和氩回收率略微改善。
涡轮空气塔旁通布置代表了对传统的从低压塔抽取氮废物的改进有两方面的原因。第一个原因是，如果不需要从低压塔中抽取氮废物，那么低压塔的设计就不那么复杂，而且可能资金成本较低。与现有技术塔中具有涡轮空气流蒸气进料、釜液体进料和低压塔中的氮废蒸气抽取不同，本发明系统和方法只需要涡轮空气流蒸气进料和釜液体进料。
第二个原因是气体回收率改善。涡轮空气塔旁通流具有大致21％的氧浓度和约0.9％的氩浓度。因此，与在相同位置处从低压塔抽取氮废物相比(通常为约15％的氧浓度和1.2％的氩浓度)，此涡轮空气塔旁通流通常具有较高的氧浓度和较低的氩浓度。与在相同位置处从低压塔抽取氮废物相比，涡轮空气塔旁通流的增加的氧浓度导致氧的回收率更高。此外，与在相同位置处从低压塔抽取氮废物相比，涡轮空气塔旁通流的减少的氩浓度导致氩的回收率更高。
虽然已参考一个或多个优选的实施方案描述了本发明，但是应当理解，在不脱离所附权利要求书所阐述的本发明的实质和范围的情况下，可进行多种添加、改变和省略。

Claims (19)

1.一种制氮和制氩低温空气分离单元，所述制氮和制氩低温空气分离单元包括：
主空气压缩系统，所述主空气压缩系统被构造成接收进入的进料空气流并且产生压缩空气流；
基于吸附的预纯化单元，所述基于吸附的预纯化单元被构造用于从所述压缩空气流移除水蒸气、二氧化碳、一氧化二氮和烃类并且产生经压缩并且纯化的空气流，其中所述经压缩并且纯化的空气流被分成至少所述经压缩并且纯化的空气流的第一部分和所述经压缩并且纯化的空气流的第二部分；
主换热系统，所述主换热系统被构造成冷却所述经压缩并且纯化的空气流的所述第一部分并且部分地冷却所述经压缩并且纯化的空气流的所述第二部分；和
涡轮膨胀机布置，所述涡轮膨胀机布置被构造成使所述经压缩并且纯化的空气流的所述经部分冷却的第二部分膨胀以形成排气流；
蒸馏塔系统，所述蒸馏塔系统具有经由冷凝器-再沸器以热传递关系连接的高压塔和低压塔，并且被构造成分离所述经压缩并且纯化的空气流的所述经冷却的第一部分与所述排气流的第一部分，并且产生来自所述低压塔的基部的富氧流和来自所述低压塔的塔顶的氮产物流；
所述蒸馏塔系统还包括与所述低压塔操作地联接的氩塔布置，所述氩塔布置具有至少一个氩塔和氩冷凝器，并且其中所述氩塔布置被构造成从所述低压塔接收富氩氧流，并且产生返回或释放到所述低压塔中的富氧塔底馏出物流和被引导到所述氩冷凝器的富氩塔顶馏出物；
其中所述氩冷凝器被构造成依靠来自所述低压塔的所述富氧流的全部或一部分来冷凝所述富氩塔顶馏出物，以产生粗氩流或产物氩流、氩回流流和富氧废物流；和
涡轮空气流塔旁通回路，所述涡轮空气流塔旁通回路被构造成将所述排气流的第二部分引导到从所述低压塔抽取的氮废物流，使得所述排气流的所述第二部分绕过所述蒸馏塔系统。
2.根据权利要求1所述的制氮和制氩低温空气分离单元，其中所述低温空气分离单元具有所述压缩空气流中所含的氮的95％或更高的氮回收率和所述压缩空气流中所含的氩的92％或更高的氩回收率。
3.根据权利要求1所述的制氮和制氩低温空气分离单元，其中所述氩冷凝器被构造成利用来自所述低压塔的所述富氧流的第一部分来冷凝所述富氩流，并且其中来自所述低压塔的所述富氧流的第二部分被视为氧产物流。
4.根据权利要求1所述的制氮和制氩低温空气分离单元，其中所述高压塔被构造成在介于约6.0巴(a)与10.0巴(a)之间的操作压力下操作，所述低压塔被构造成在介于约1.5巴(a)与2.8巴(a)之间的操作压力下操作，并且所述氩塔被构造成在介于约1.3巴(a)与2.8巴(a)之间的压力下操作。
5.根据权利要求4所述的制氮和制氩低温空气分离单元，其中所述氩塔布置中的所述氩塔是具有介于180个与260个之间的分离级的超级塔或具有介于185个与270个之间的分离级的超超级塔。
6.根据权利要求4所述的制氮和制氩低温空气分离单元，其中所述氩塔布置还包括被构造为超级氩塔的第一氩塔、被构造为高比率氩塔的第二氩塔。
7.根据权利要求1所述的制氮和制氩低温空气分离单元，其中所述基于吸附的预纯化单元是被构造用于纯化所述压缩空气流的多床变温吸附单元，所述多床变温吸附单元被进一步构造成使得每个床在在线操作阶段与离线操作阶段之间交替，在所述在线操作阶段中，从所述压缩空气流吸附水蒸气、二氧化碳、一氧化二氮和烃类，在所述离线操作阶段中，使用从所述富氧废物流获取的吹扫气体来再生所述床。
8.根据权利要求7所述的制氮和制氩低温空气分离单元，所述制氮和制氩低温空气分离单元还包括再生鼓风机，所述再生鼓风机被构造成将所述富氧废物流的压力升高约0.1巴(a)至0.3巴(a)。
9.根据权利要求1所述的制氮和制氩低温空气分离单元，其中所述低温空气分离单元在第一设计模式下操作，其中所述排气流的所述第一部分包括所述排气流中的全部，并且所述低温空气分离单元进一步在第二非设计模式下操作，其中所述排气流的所述第一部分小于所述排气流中的全部，并且所述排气流的所述第二部分具有小于约9000Nm3/hr的流量。
10.根据权利要求9所述的制氮和制氩低温空气分离单元，其中所述排气流的所述第二部分具有介于约5000Nm3/hr与约7000Nm3/hr之间的流量。
11.一种在低温空气分离单元中分离空气以产生粗氩产物和一种或多种氮产物的方法，所述方法包括以下步骤：
(a)压缩进入的进料空气流以产生压缩空气流；
(b)在基于吸附的预纯化单元中纯化所述压缩空气流，所述基于吸附的预纯化单元被构造成从所述压缩空气流移除水蒸气、二氧化碳、一氧化二氮和烃类以产生经压缩并且纯化的空气流；
(c)将所述经压缩并且纯化的空气流分成至少所述经压缩并且纯化的空气流的第一部分和所述经压缩并且纯化的空气流的第二部分；
(d)在主换热器系统中冷却所述经压缩并且纯化的空气流的所述第一部分和所述经压缩并且纯化的空气流的所述第二部分；
(e)在涡轮膨胀机布置中使所述经压缩并且纯化的空气流的所述经冷却的第二部分膨胀以形成排气流；
(f)将所述排气流的第一部分和所述经压缩并且纯化的空气流的所述经冷却的第一部分引导到蒸馏塔系统；以及
(g)在所述蒸馏塔系统中分离所述排气流的所述第一部分与所述经压缩并且纯化的空气流的所述经冷却的第一部分，以产生来自所述低压塔的基部的所述富氧流和来自所述低压塔的塔顶的所述氮产物流；
(h)在氩塔布置中进一步分离从所述低压塔获取的富氩氧流，以产生富氧塔底馏出物流和富氩塔顶馏出物；
(i)将所述富氧塔底馏出物流引导到所述低压塔中；
(j)将所述富氩塔顶馏出物引导至氩冷凝器的冷凝侧；
(k)将所述富氧流的全部或一部分从所述低压塔引导到所述氩冷凝器的沸腾侧；
(l)依靠来自所述低压塔的所述富氧流来冷凝所述富氩塔顶馏出物以产生粗氩流和氩回流流，同时使所述富氧流的第一部分和所述液氮沸腾以产生富氧废物流；以及
(m)将所述排气流的第二部分引导到从所述低压塔抽取的废物流，使得所述排气流的所述第二部分绕过所述蒸馏塔系统。
12.根据权利要求11所述的方法，其中所述低温空气分离单元具有所述压缩空气流中所含的氮的95％或更高的氮回收率和所述压缩空气流中所含的氩的92％或更高的氩回收率。
13.根据权利要求11所述的方法，其中所述氩冷凝器被构造成利用来自所述低压塔的所述富氧流的第一部分来冷凝所述富氩流，并且其中来自所述低压塔的所述富氧流的第二部分被视为氧产物流。
14.根据权利要求11所述的方法，其中所述高压塔被构造成在介于约6.0巴(a)与10.0巴(a)之间的操作压力下操作，所述低压塔被构造成在介于约1.5巴(a)与2.8巴(a)之间的操作压力下操作，并且所述氩塔被构造成在介于约1.3巴(a)与2.8巴(a)之间的压力下操作。
15.根据权利要求14所述的方法，其中所述氩塔布置中的所述氩塔是具有介于180个与260个之间的分离级的超级塔或具有介于185个与270个之间的分离级的超超级塔。
16.根据权利要求14所述的方法，其中所述氩塔布置还包括被构造为超级氩塔的第一氩塔、被构造为高比率氩塔的第二氩塔。
17.根据权利要求11所述的方法，其中所述基于吸附的预纯化单元是被构造用于纯化所述压缩空气流的多床变温吸附单元，所述多床变温吸附单元被进一步构造成使得每个床在在线操作阶段与离线操作阶段之间交替，在所述在线操作阶段中，从所述压缩空气流吸附水蒸气、二氧化碳、一氧化二氮和烃类，在所述离线操作阶段中，使用从所述富氧废物流获取的吹扫气体来再生所述床。
18.根据权利要求11所述的方法，其中所述低温空气分离单元在第一设计模式下操作，其中所述排气流的所述第一部分包括所述排气流中的全部，并且所述低温空气分离单元进一步在第二非设计模式下操作，其中所述排气流的所述第一部分包括小于所述排气流中的全部，并且所述排气流的所述第二部分具有小于约9000Nm3/hr的流量。
19.根据权利要求18所述的方法，其中所述排气流的所述第二部分具有介于约5000Nm3/hr与约7000Nm3/hr之间的流量。
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