CN105716369B - 整体式预冷却混合制冷系统和方法 - Google Patents

整体式预冷却混合制冷系统和方法 Download PDF

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CN105716369B
CN105716369B CN201510736135.9A CN201510736135A CN105716369B CN 105716369 B CN105716369 B CN 105716369B CN 201510736135 A CN201510736135 A CN 201510736135A CN 105716369 B CN105716369 B CN 105716369B
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heat exchanger
steam
refrigeration
entrance
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CN105716369A (zh
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T.古斯哈纳斯
小道格.D.杜科特
J.波多尔斯基
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Chart Industries Inc
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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
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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    • F25J1/0217—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as at least a three level refrigeration cascade with at least one MCR cycle
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Abstract

一种在热交换器中用于冷却和液化气体的系统和方法，包括使用第一和最后压缩和冷却循环来压缩和冷却混合制冷剂，使得形成高压液体和蒸汽物流。高压液体和蒸汽物流在热交换器中被冷却，然后膨胀，使得在热交换器中提供主制冷物流。混合制冷剂在第一和最后压缩和冷却循环之间进行冷却和平衡，使得在该热交换器中形成预冷却液体蒸汽并过冷。然后物流膨胀并作为预冷却制冷物流穿过热交换器。使气体物流以与主制冷物流和预冷却制冷物流进行逆流热交换的方式穿过热交换器，使得气体被冷却。

Description

整体式预冷却混合制冷系统和方法
本申请是申请日为2011年3月4日、申请号为201180023625.4、发明名称为“整体式预冷却混合制冷系统和方法”的专利申请的分案申请。
技术领域
本发明大体上涉及用于冷却或液化气体的工艺和系统，更具体而言，涉及用于冷却或液化气体的改进的混合制冷系统和方法。
背景技术
天然气(其主要是甲烷)及其它气体在压力下液化以存储和运输。因液化导致的体积减小使得可以使用更实用和经济的设计的容器。液化典型地通过由一个或多个制冷循环进行的间接热交换对气体进行冷却来实现。由于所需设备的复杂性和所需的制冷剂性能的效率，这样的制冷循环在设备成本和操作两方面的代价较高。因此，目前需要一种具有改进的制冷效率并且操作成本降低、复杂性降低的用于气体冷却和液化的系统。
将天然气液化需要将天然气物流冷却至大致-160℃至-170℃，然后使压力降低至接近环境温度。图1显示了甲烷在60巴(bar)压力下、甲烷在35巴压力下以及甲烷和乙烷的混合物在35巴压力下的典型温度-焓曲线。该S形曲线有三个区，在约-75℃以上时气体是非过热的(de-superheating)，并且在大约-90℃以下液体过冷(subcooling)。在这两个区之间的相对平坦的区域中，气体被冷凝成液体。由于60巴曲线在临界压力之上，因此只存在一种相态(phase)；但是其比热大，接近临界温度，并且冷却曲线与压力较低的曲线近似。包含5％乙烷的曲线显示了杂质的影响，其改变了露点和起泡点。
制冷工艺对于为使天然气液化提供冷却来说是必要的，最高效的工艺将具有在其整个范围内均与图1所示冷却曲线接近到几度之内的加热曲线。然而，由于冷却曲线的S形形式和大温度范围，很难设计这样的制冷工艺。纯组分制冷剂工艺因其平坦的蒸发曲线在两相的区域中效果最好，而多组分制冷剂工艺因其倾斜的蒸发曲线更适于非过热区和过冷区。这两种类型的工艺以及二者的混合已被开发用于使天然气液化。
级联式、多级、纯组分循环最初使用了诸如丙烯、乙烯、甲烷和氮的制冷剂。通过足够多的级，这样的循环可生成接近图1所示冷却曲线的净热(net heating)曲线。然而，由于随着级数增加需要额外的压缩机组，机械复杂性变得非常高。这样的工艺在热力学上是低效的，因为纯组分制冷剂恒温蒸发而不是遵循天然气冷却曲线，并且制冷阀将液体不可逆地闪蒸为蒸汽。由于这些原因，已在寻求改进的工艺以降低资金成本，减少能量消耗，并且改善操作性能。
Manley的第5,746,066号美国专利描述了一种用于乙烯回收的类似制冷需求的级联式、多级、混合制冷剂工艺，其消除了级联式多级纯组分工艺的热力学效率低的问题。这是因为制冷剂遵循气体冷却曲线在温度升高时蒸发，并且液体制冷剂在闪蒸之前被过冷，因此降低了热力学不可逆性。此外，机械复杂性稍微低些，因为仅需要两个不同的制冷剂循环，而不是纯制冷剂工艺所需的三个或者四个。Newton的第4,525,185号、Liu等人的第4,545,795号、Paradowski等人的第4,689,063号和Fischer等人的第6,041,619号美国专利都显示了对如Stone等人的第2007/0227185号和Hulsey等人的第2007/0283718号美国专利申请公开中所做的这种应用于天然气液化的方案的变体。
这种级联式、多级、混合制冷剂工艺是已知最有效的，然而，对于大多数工厂来说，期望一种能够更易操作的、更简单的、有效的工艺。
Swenson的第4,0633,735号美国专利描述了一种单混合制冷剂工艺，其仅需要一个压缩机用于制冷工艺，并且其进一步降低了机械复杂性。然而，主要由于两个原因，这种处理消耗了比级联式、多级、混合制冷剂工艺稍多一些的功率。
首先，很难(如果并非不可能)找到将生成接近符合图1所示的典型天然气冷却曲线的净热曲线的单混合制冷剂组合物。这样的制冷剂必须由一系列相对高沸点和相对低分店的组分组成，并且其沸点温度在热力学上受相平衡的约束。此外，沸点较高的组分是受限的，这是因为它们必须在最低温度时不会凝固。由于这些原因，在冷却过程中的若干时间点上必然会发生相对大的温度差异。图2显示了在Swenson的'735专利的工艺中的典型复合物加热和冷却曲线。
第二，对于单混合制冷剂工艺，制冷剂中的所有组分均被携带至最低温度水平，即使较高沸点的组分仅在工艺中的制冷部分的较热端提供制冷。这需要能量来冷却和再加热这些在较低温度时为“惰性(inert)”的组分。这既不是级联式多级纯组分制冷工艺，也不是级联式多级混合制冷剂工艺。
为减轻这第二点的低效问题并且也解决第一点，已开发了许多方案，其将较重馏分从单混合制冷剂中分离出来，在较高温度水平的制冷中使用该较重馏分，然后将其与较轻馏分重新合并，用于后续压缩。Podbielniak的第2,041,725号美国专利说明了描述了一种实现上述内容的方法，其在低于环境温度时将若干个相分离级结合起来。Perret的第3,364,685号、Sarsten的第4,274,849号、Garrier等人的第4,274,849号、Fan等人的第4,901,533号、Ueno等人的第5,813,250号、Arman等人的第6,065,305号、Robers等人的第6,347,531号美国专利和Scmidt的第2009/0205366号美国专利申请公开内容也显示了该方案的变体。当认真地设计时，即使物流不在平衡时重新合并是热力学低效的，其也可改进能量效率。这是因为较轻和较重的馏分在高压下被分离，然后在低压下重新合并，因此它们可在单个压缩机中一起被压缩。无论何时物流在平衡状态下被分离，被分别处理，然后在非平衡条件下被重新合并，都会出现热力学损失，其在根本上提高了功率消耗。因此，这种分离的次数应该被最小化。所有这些工艺均在制冷工艺的不同地方使用了简单的蒸汽/液体平衡，以从较轻的一方中分离出较重馏分。
然而，简单的一级蒸汽/液体平衡分离并不能像使用具有回流的多平衡级完成的那样浓缩这些馏分。较大的浓度允许在分离在特定温度范围上提供制冷的组合物时具有较大的精度。这提高了加工能力以符合图1中的S型冷却曲线。Gauthier的第4,586,942号和Stochmann等人的第6,334,334号美国专利说明了在上述环境压缩机组中如何采用分馏以在不同温度区域中进一步浓缩用于制冷的分离馏分，并由此改进总的工艺热力学效率。浓缩馏分和降低其蒸发温度范围的第二个原因是要确保在它们离开工艺的制冷部分时其被完全蒸发。这完全利用了制冷的潜热，并排除了液体到下游压缩机的夹带。出于相同的原因，重馏分液体通常作为工艺的一部分被重新注入制冷剂的较轻馏分中。将重馏分分馏降低了重新注入时的闪蒸，并且改进了两相流体的机械分布。
正如Stone等人的第2007/0227185号美国专利申请公开内容所说明的，已知从该工艺的制冷部分中移除部分蒸汽化的制冷物流。Stone等人这样做是由于机械的(而非热力学的)原因，并且是在需要两种单独制冷剂的级联式、多级、混合制冷工艺的背景下。此外，在压缩之前，部分蒸汽化的制冷物流在与它们先前所分离出的蒸汽馏分重新合并之时，立即被完全蒸汽化。
附图说明
图1是甲烷在35巴和60巴压力下和甲烷与乙烷的混合物在35巴压力下的温度—焓曲线的图示；
图2是现有技术工艺和系统的复合物加热和冷却曲线的图示；
图3是说明本发明的工艺和系统的实施方式的工艺流程图和示意性说明；
图4是图3中工艺和系统的复合物加热和冷却曲线的图示；
图5是说明本发明的工艺和系统的第二实施方式的工艺流程图和示意性说明；
图6是说明本发明的工艺和系统的第三实施方式的工艺流程图和示意性说明；
图7是说明本发明的工艺和系统的第四实施方式的工艺流程图和示意性说明；
图8是提供了图2和图4中的复合物加热和冷却曲线的热端馏分的放大图的图示。
具体实施方式
依据本发明，并且如下文中所详述的，如果在重馏分离开工艺的主热交换器时重馏分没有完全蒸发，则重馏分的简单平衡分离足以改善混合制冷剂工艺效率。这表示在压缩机的抽吸处将存在一些液体制冷剂，并且这些液体制冷剂必须预先被分离并且被泵压至更高压力。当液体制冷剂与制冷剂中蒸发的较轻馏分混合时，压缩机抽吸气体被大大冷却并且所需要的压缩机功率进一步减少。中间级过程中重馏分的平衡分离还减少了第二级或更高级的压缩机上的负载，得到改进的工艺效率。制冷剂的重组分也被阻挡在工艺的冷端以外，降低了制冷剂结冰的可能性。
而且，在独立的预冷却制冷环路中使用重馏分导致加热/冷却曲线在热交换器的热端接近终止，带来了对制冷的更高效的使用。这在图8中进行了最佳的解释，在这里在被限定至+40℃到-40℃的相同轴上描绘了来自图2(开放曲线)和图4(闭合曲线)的曲线。
在图3中提供了说明本发明的系统和方法的实施方式的工艺流程图和示意性说明。现在将参考图3描述该实施方式的操作。
正如在图3中所说明的，该系统包括多物流热交换器(multi-stream heatexchanger)，大体上以6表示，其具有热端7和冷端8。该热交换器接收较高压力的天然气进料物流9，其在冷却通路5中通过与交换器中的制冷剂物流热交换来移除热量而被液化。结果，产生液体天然气产品的物流10。热交换器的多物流的设计能够将若干物流方便且能量高效地合并到单个交换器中。适合的热交换器可购自Chart Energy&Chemicals,Inc.ofWoodlands Texas。可得自Chart Energy&Chemicals,Inc.的平面式和鱼鳍式交换器提供了在物理上紧凑的进一步的优点。
包括热交换器6在内的图3的系统可被配置成执行在虚线框13表示的现有技术中已知的其它气体处理选项。这些处理选项可能要求气体物流离开并一次性或多次重新进入热交换器，并且可以包括，例如，天然气液体回收或氮排斥。此外，虽然本发明的系统和方法在下文中是按照对天然气的液化来描述的，但是它们可被用于冷却、液化和/或处理除天然气以外的气体，包括但不限于空气或氮。
对热量的去除是在图3中所说明的使用单混合制冷剂的热交换器中以及该系统的剩余部分中完成的。在表1中说明了这种制冷剂组合物、使用条件和该系统的制冷剂部分物流的流动，正如在下面所描述的。
参考图3的右上部分，第一级压缩机11接收低压蒸汽制冷剂物流12，并将其压缩至中间压力。物流14然后前行至第一级后冷却器16，并在此处被冷却。后冷却器16可以是例如热交换器，得到中间压力混合相制冷剂物流18前行至级间鼓(interstage drum)22，虽然所说明的是级间鼓22，但可使用替代方案的分离装置，包括但不限于另一种容器、旋风分离器、蒸馏单元、聚结分离器(coalescing separator)或者网式或叶片式除雾器。级间鼓22同时接收由泵26提供的中间压力液体制冷剂物流24，正如将要在下面更详细地解释的。在替代方案的实施方式中，物流24可改为在后冷却器16的上游与物流14合并，或者在后冷却器16的下游与物流18合并。
物流18和24在级间鼓22中合并并平衡，这使得所分离的中间压力蒸汽物流28离开鼓22的蒸汽出口，并且中间压力液体物流32离开鼓的液体出口。中间压力液体物流32(其是热的重馏分)离开鼓22的液体侧，并进入热交换器6的预冷却液体通路33，并且通过与下面所述的也经过热交换器的不同冷却物流进行热交换来过冷。所得物流34离开热交换器，并且通过膨胀阀36被闪蒸。作为膨胀阀36的替代方案，也可使用另一类膨胀装置，包括但不限于涡轮或者漏孔。所得物流38重新进入热交换器6以经由预冷却制冷通路39提供额外的制冷剂。物流42作为具有大量液体馏分的两相混合物离开热交换器的热端7。
中间压力蒸汽物流28从鼓22的蒸汽出口前行至第二级或末级压缩机44，在这里其被压缩至高压。物流46离开压缩机44并前行穿过第二级或末级后冷却器48，在这里被冷却。所得物流52包含蒸汽和液体相，其在累积鼓(accumulator drum)54中被分离。虽然说明了累积鼓54，但是也可以使用替代方案的分离装置，包括但不限于另一种容器、旋风分离器、蒸馏单元、聚结分离器或者网式或叶片式除雾器。高压蒸汽制冷剂物流56离开鼓54的蒸汽出口，并前行至热交换器6的热侧。高压液体制冷剂蒸汽58离开鼓54的液体出口，并同时前行到热交换器6的热端。应该注意的是，第一级压缩机11和第一级后冷却器16实现了第一压缩和冷却循环，同时末级压缩机44以及末级后冷却器48实现了最后压缩和冷却循环。然而，同时还应该注意，每一个冷却循环级是以多个压缩机和/或后冷却器为特征的。
当其穿过热交换器6的高压蒸汽通路59时，热的高压蒸汽制冷剂物流56被冷却、浓缩和过冷。结果，物流62离开热交换器6的冷端。物流62通过膨胀阀64被闪蒸，并且作为物流66重新进入热交换器，以在物流67前行通过主制冷通路65时提供制冷。作为对膨胀阀64的替代方案，也可以使用另一种膨胀阀，包括但不限于涡轮或漏孔。
热的高压液体制冷剂物流58进入热交换器6并且在高压液体通路69中被过冷。所得物流68离开热交换器并且通过膨胀阀72被闪蒸。作为膨胀阀72的替代方案，也可以使用另一种膨胀阀，包括但不限于涡轮或漏孔。所得物流74重新进入热交换器6，在此处其加入并在主制冷剂通道65中与物流67合并，以提供作为物流76的附加制冷剂，并作为过热蒸汽物流78离开热交换器6的冷端。
过热蒸汽物流78和如上所述的作为具有大量液体馏分的两相混合物的物流42通过蒸汽和混合相态入口分别进入低压抽吸鼓82，并且在低压抽吸鼓中合并和平衡。虽然所说明的是抽吸鼓82，但是也可以使用其它分离装置，包括但不限于另一种容器、旋风分离器、蒸馏单元、聚结分离器或者网式或叶片式除雾器。结果，低压蒸汽制冷剂物流12离开鼓82的蒸汽出口。如上所述，物流12前行到第一级压缩机11的入口。混合相物流42与包含组成非常不同的蒸汽的物流78在抽吸鼓82中在第一级压缩机11的抽吸入口处掺和产生了部分闪蒸冷却的效果，这降低了移动到压缩机中的蒸汽物流的温度，并且由此降低了压缩机自身的温度，从而减少了操作其所需的能量。
低压液体制冷剂物流84的温度也通过混合的闪蒸冷却效果而被降低，其离开鼓82的液体出口并通过泵26被泵至中间压力。正如以上所描述的，来自泵的出口物流24前行至级间鼓22.
结果，依据本发明，包括物流32、34、38和42的预冷却制冷回路进入热交换器6的热端并与大量液体馏分一起离开。部分液体物流42与来自物流78的已用制冷剂蒸汽合并，以用于抽吸鼓82中的平衡和分离，压缩机11中所得蒸汽的压缩和用泵对所得液体的抽取。抽吸鼓82中的平衡通过热传递和物质传递降低了进入压缩机11的物流的温度，因此降低了压缩机的功率用量。
在图4中显示了图3中的工艺的复合物加热和冷却曲线。与图2中类似于Swenson的第4,033,735号美国专利中所述的优化的单混合制冷剂工艺的曲线进行比较，显示了该复合物加热和冷却曲线已经变得更加靠近，因此使压缩机的功率降低约5％。这有助于减少设备的资本费用，并降低与环境排放有关的能量消耗。这些益处能够为小到中型液体天然气设备一年节省几百万美元。
图4还说明了图3中的设备和方法导致了冷却曲线的热交换器热端近乎终止(也见图8)。这是由于中等压力重馏分液体在比剩余制冷剂更高的温度下沸腾所产生的，并由此良好地适用于热端热交换制冷。在热交换器中使中等压力重馏分液体与较轻馏分的制冷剂独立沸腾允许甚至更高的沸腾温度，这导致了曲线的热端甚至更“接近”(并且因此更高效)。而且，保持将重馏分阻挡在热交换器的冷端以外有助于防止发生冻结。
应注意的是，以上描述的实施方式是用于在超临界压力下具有代表性的天然气进料的。在不同压力下对纯度较低的其它天然气液化时，优选的制冷剂组合物和操作条件将改变。但是由于其热力学的高效性，仍保持了这种工艺的优点。
在图5中提供了本发明的系统和方法的第二实施方式的工艺流程图和示意性说明。在图5的实施方式中，过热蒸汽物流78和两相混合物流42在102所示的混合装置中合并，而不是图3中的抽吸鼓82。混合装置102可以是例如静态混合器、物流78和42所流入的单管段(pipe segment)、热交换器6的外壳(packing)或头部。在离开混合装置102之后，经合并和混合的物流78和42作为物流106前行至低压抽吸鼓104的单个入口。虽然所说明的是抽吸鼓104，但是也可使用替代方案的分离装置，包括但不限于另一种容器、旋风分离器、蒸馏单元、聚结分离器或者网式或叶片式除雾器。在物流106进入抽吸鼓104时，蒸汽和液体相分离，使得低压液体制冷剂物流84离开鼓104的液体出口，同时低压蒸汽物流12离开鼓104的蒸汽出口，正如以上图3的实施方式所描述的。图5的实施方式中的剩余部分以相同组分为特征，并且如图3中的实施方式所描述的进行操作，但是表1中的数据可能不同。
在图6中提供了本发明的系统和方法的工艺流程图和示意性说明。两相混合蒸汽42从热交换器6前行回到鼓120。所得蒸汽相随返回蒸汽物流122前行到低压抽吸鼓124的第一蒸汽入口。过热蒸汽物流78从热交换器6前行到低压抽吸鼓124的第二蒸汽入口。合并的物流126离开用作返回分离器鼓和抽吸鼓的单个鼓或容器。而且，可以用其它类型的分离装置来替换鼓120和124，包括但不限于另一种容器、旋风分离器、蒸馏单元、聚结分离器或者网式或叶片式除雾器。
第一级压缩机131接收低压蒸汽制冷剂物流126并且将其压缩至中等压力。压缩的物流132然后前行至第一级后冷却器134，在此处其被冷却。器件，液体作为返回液体物流136从返回分离器鼓120的液体出口前行至泵138，然后所得物流142从第一级后冷却器134逆流而上加入物流132。
离开第一级后冷却器134的中等压力混合相制冷剂物流144前行至级间鼓146。虽然所说明的是级间鼓146，但是也可以使用替代方案的分离装置，包括但不限于另一种容器、旋风分离器、蒸馏单元、聚结分离器或者网式或叶片式除雾器。分离的中间压力蒸汽物流28离开级间鼓146的蒸汽出口，并且中等压力的液体物流32离开鼓的液体出口。中间压力蒸汽物流28前行至第二级压缩机44，同时中间压力液体物流32(其是热的重馏分)，前行至热交换器6，正如以上参考图2中的实施方式所描述的。图6中实施方式的剩余部分以与图3中的实施方式所描述的相同的组分和操作为特征，但是表1的数据可能是不同的。图6中的实施方式在鼓124处未提供任何冷却，并由此对第一级压缩机抽水机物流126未进行冷却。然而，在改善效率的方面，对冷却压缩机抽吸物流进行交换以降低到达压缩抽吸的蒸汽摩尔流动率。降低的到达压缩机抽吸的蒸汽流提供了降低的压缩机功率需求，其大致相当于在图3的实施方式中经冷却的压缩抽吸物流所提供的减少量。虽然对泵138的功率需求上具有相应的增长，但是与在图3的实施方式中的泵26相比，泵功率与在压缩机功率上的节省相比增长非常小(接近1/100)。
在图7中所说明的本发明的系统和方法的第四实施方式中，图3的系统任选地配备了一个或多个预冷却系统，其被表示成位于202、204和/或206处。当然，图5或图6中的实施方式或者本发明的系统的任意其它实施方式也可配备图7中的预冷却系统。预冷却系统202用于在热交换器6之前预冷却天然气物流9。预冷却系统204用于在混合相物流18从第一级后冷却器16前行至级间鼓22时对其进行级间预冷却。预冷却系统206用于在混合相物流52从第二级后冷却器48前行至累积鼓54时释放对其的预冷却。图7中实施方式的剩余部分以与图3中的实施方式所描述的相同的组分和操作为特征，但是表1中的数据可能是不同的。
预冷却系统202、204或206中的每一个可被结合到或依赖于热交换器6用于操作，或者可包括致冷器(其可以是例如第二个多物流热交换器)。此外，预冷却系统202、204和/或206中的两个或所有三个可被结合到单个多物流热交换器中。虽然在本领域中已知的任意预冷却系统都可被使用，但是图7的预冷却系统各自优选包括如下致冷器：其使用单组份制冷剂(如丙烷)或者第二种混合制冷剂作为预冷却系统制冷剂。更具体地，公知的丙烷C3-MR预冷却工艺或二元混合制冷剂工艺可与在单压力或多压力下蒸发的预冷却制冷剂一起使用。其它可适用的单组份制冷剂的例子包括但不限于正丁烷、异丁烷、丙烯、乙烷、乙烯、氨、氟利昂或水。
除了配备预冷却系统202之外，图7中的系统(或任何其它系统的实施方式)可用作下游工艺的预冷却系统，诸如液化作用系统或第二混合制冷剂系统。在热交换器的冷却通路中被冷却的气体也可以是第二混合制冷剂或单组分混合制冷剂。
虽然已经显示了并说明了本发明的优选实施方式，对于那些本领域技术人员将显而易见的是，在其中可造成改变和修改而不背离本发明的精神。其范围是通过随附的权利要求书限定的。
表1：物流表
摩尔百分比
氮 1.00 1.00 9.19 9.19 9.19 11.15 11.15 11.15 2.12
甲烷 99.00 99.00 24.20 24.20 24.20 29.03 29.03 29.03 11.37
乙烷 0.00 0.00 35.41 35.41 35.41 40.08 40.08 40.08 39.05
丙烷 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
正丁烷 0.00 0.00 21.45 21.45 21.45 15.20 15.20 15.20 35.14
异丁烷 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
异戊烷 0.00 0.00 9.75 9.75 9.75 9.75 4.53 4.53 12.31
摩尔百分比
氮 2.12 2.12 0.04 0.04 0.32 0.32 0.32 0.32 14.94
甲烷 11.37 11.37 0.43 0.43 2.35 2.35 2.35 2.35 36.43
乙烷 39.05 39.05 4.14 4.14 14.24 14.24 14.24 14.24 40.51
丙烷 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
正丁烷 35.14 35.14 42.13 42.13 49.63 49.63 49.63 49.63 6.84
异丁烷 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00
异戊烷 12.31 12.31 53.25 53.25 33.47 33.46 33.46 33.46 1.28
摩尔百分比
氮 14.94 14.94 14.94 11.16 11.16
甲烷 36.43 36.43 36.43 29.04 29.04
乙烷 40.51 40.51 40.51 40.08 40.08
丙烷 0.00 0.00 0.00 0.00 0.00
正丁烷 6.84 6.84 6.84 15.19 15.19
异丁烷 0.00 0.00 0.00 0.00 0.00
异戊烷 1.28 1.28 1.28 4.53 4.53

Claims (17)

1.一种使用混合制冷剂冷却气体的系统，包括：
a)热交换器，其包括热端和冷端，所述热端具有适于接收气体进料的进料气体入口，并且所述冷端具有产品通过其离开所述热交换器的产品出口，所述热交换器还包括在所述进料气体入口和所述产品出口之间延伸的冷却通路、预冷却液体通路、预冷却制冷通路、高压蒸汽通路、高压液体通路和主制冷通路；
b)抽吸分离装置，其具有蒸汽出口；
c)第一级压缩机，其具有抽吸入口和出口，所述抽吸入口与所述抽吸分离装置的蒸汽出口流体连通；
d)第一级后冷却器，其具有入口和出口，所述入口与所述第一级压缩机的出口流体连通；
e)级间分离装置，其具有与所述第一级后冷却器的出口流体连通的入口，所述级间分离装置还具有蒸汽出口和液体出口，所述液体出口与所述热交换器的预冷却液体通路流体连通；
f)第一膨胀装置，其具有入口和出口，所述入口与所述热交换器的预冷却液体通路流体连通，且所述出口与所述热交换器的预冷却制冷通路流体连通；
g)末级压缩机，其具有抽吸入口和出口，所述抽吸入口与所述级间分离装置的蒸汽出口流体连通；
h)末级后冷却器，其具有入口和出口，所述入口与所述末级压缩机的出口流体连通；
i)累积分离装置，其具有入口以及蒸汽出口和液体出口，所述入口与所述末级后冷却器的出口流体连通，所述蒸汽出口与所述热交换器的高压蒸汽通路流体连通，并且所述液体出口与所述热交换器的高压液体通路流体连通；
j)第二膨胀装置，其具有与所述热交换器的高压蒸汽通路流体连通的入口和与所述热交换器的主制冷通路流体连通的出口；
k)第三膨胀装置，其具有与所述热交换器的高压液体通路流体连通的入口和与所述热交换器的主制冷通路流体连通的出口；
l)所述预冷却制冷通路适于产生混合相物流，并且所述主制冷通路适于产生蒸汽物流；以及
m)所述抽吸分离装置还与所述热交换器的主制冷通路流体连通。
2.如权利要求1所述的系统，其中所述预冷却制冷通路经过所述热交换器的热端，但不经过所述冷端，所述主制冷通路经过所述热交换器的热端和冷端，并且所述级间分离装置适于产生包含所述制冷剂的重馏分的液体物流，使得所述气体的冷却曲线的热端和所述制冷剂的冷却曲线的热端通过产生混合相物流的所述预冷却制冷通路和产生蒸汽物流的主制冷通路而变得更靠近。
3.如权利要求1所述的系统，其中所述抽吸分离装置包括与所述热交换器的主制冷通路连通的蒸汽入口和与所述热交换器的预冷却制冷通路连通的混合相入口，使得来自所述主制冷通路的蒸汽物流和来自所述预冷却制冷通路的混合相物流在所述抽吸分离装置中合并并平衡，以将经冷却的蒸汽物流提供给所述第一级压缩机，由此降低所述第一级压缩机的功率损耗。
4.如权利要求1所述的系统，其中所述预冷却制冷通路和所述主制冷通路在所述热交换器中是独立通路。
5.如权利要求1所述的系统，其中所述抽吸分离装置包括液体出口，并且所述系统进一步包括具有入口和出口的泵，所述入口与所述抽吸分离装置的液体出口连通，且所述出口与所述级间分离装置流体连通。
6.如权利要求1所述的系统，其中所述抽吸分离装置也与所述热交换器的预冷却制冷通路流体连通。
7.如权利要求1所述的系统，还包括第一预冷却系统，所述第一预冷却系统适于接收和冷却所述气体进料，并将经冷却的气体导引至所述热交换器的气体进料入口。
8.如权利要求1所述的系统，还包括在所述第一级压缩机的出口与所述级间分离装置的入口之间的回路中的第一级预冷却系统和在所述末级后冷却器的出口与所述累积分离装置的入口之间的回路中的末级预冷却系统。
9.如权利要求1所述的系统，其中所述抽吸分离装置包括入口，并且所述系统进一步包括混合装置，所述混合装置具有与热交换器的主制冷通路流体连通的蒸汽入口和与所述热交换器的预冷却制冷通路流体连通的混合相入口，使得来自所述主制冷通路的蒸汽物流和来自预冷却制冷通路的混合相物流在所述混合装置中合并并混合，所述混合装置还具有与所述抽吸分离装置的入口连通的出口，使得所述合并并混合的物流被提供给所述抽吸分离装置。
10.如权利要求9所述的系统，其中所述混合装置包括所述热交换器的头部。
11.一种在具有热端和冷端的热交换器中冷却气体的方法，包括以下步骤：
a)使用第一和最后压缩和冷却循环来压缩和冷却混合制冷剂；
b)在所述第一和最后压缩和冷却循环之后平衡和分离所述混合制冷剂，使得形成高压液体和蒸汽物流；
c)使所述高压液体和蒸汽物流冷却和膨胀，使得在所述热交换器中提供主制冷物流；
d)在所述第一和最后压缩和冷却循环之间平衡和分离所述混合制冷剂，使得形成预冷却液体物流；
e)使所述预冷却液体物流以与所述主制冷物流进行逆流热交换的形式经过所述热交换器，使得所述预冷却液体物流被冷却；
f)使经冷却的预冷却液体物流膨胀，使得形成预冷却制冷物流；
g)使所述预冷却制冷物流经过所述热交换器；
h)使所述气体物流以与所述主制冷物流和所述预冷却制冷物流进行逆流热交换的形式经过所述热交换器，使得所述气体被冷却，并且由所述预冷却制冷物流产生混合相物流，并且由所述主制冷物流产生蒸汽物流。
12.如权利要求11所述的方法，其中步骤h)使得所述主制冷物流提供蒸汽物流，并且使所述预冷却制冷物流提供混合相物流，并且所述方法进一步包括以下步骤：
i)在所述第一压缩和冷却循环之前将所述蒸汽物流和所述混合相物流混合，使得降低温度的蒸汽物流被提供给第一压缩和冷却循环压缩机，由此使得所述压缩机的温度更低。
13.如权利要求12所述的方法，进一步包括以下步骤：
j)平衡和分离所述蒸汽物流和所述混合相物流，使得产生所述降低温度的蒸汽物流和经冷却的液体物流；以及
k)抽取所述经冷却的液体物流，使得其在所述最后压缩和冷却循环之前重新加入所述混合制冷剂。
14.如权利要求11所述的方法，其中步骤c)包括将所述高压蒸汽和高压液体物流以与所述主制冷物流和所述预冷却制冷物流进行逆流热交换的形式经过所述热交换器，使得所述高压蒸汽和高压液体物流被冷却。
15.如权利要求11所述的方法，其中所述气体也在步骤h)中被液化。
16.如权利要求11所述的方法，进一步包括以下步骤：预冷却所述气体然后使经预冷却的气体的物流经过所述热交换器。
17.如权利要求11所述的方法，进一步包括以下步骤：在第一压缩和冷却循环之后预冷却所述混合制冷剂和在最后压缩和冷却循环之后预冷却所述混合制冷剂。
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