CN1443295A - 用于液化高压天然气的系统和方法 - Google Patents

用于液化高压天然气的系统和方法 Download PDF

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CN1443295A
CN1443295A CN01812854.8A CN01812854A CN1443295A CN 1443295 A CN1443295 A CN 1443295A CN 01812854 A CN01812854 A CN 01812854A CN 1443295 A CN1443295 A CN 1443295A
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B·C·普里斯
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Black and Veatch Pritchard Inc
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Abstract

一种系统和方法用于在利用涡轮膨胀器(86)和压缩机(90)产生的高压下从天然气流(26)中有效地排除天然气液体并且在高压下液化天然气流。

Description

用于液化高压天然气的系统和方法
技术领域
本发明涉及用于在高压下液化天然气流时从高压的天然气流中有效地排除天然气液体的方法。
背景技术
近几年来增长了对天然气的需求，在发现没有天然气储备或天然气储备不多的地区尤其如此。由于许多地区具有丰富的天然气供应，最好是能够将天然气从这些地区输送到需要地区。输送天然气的一种方法是通过将天然气液化。液化的天然气(LNG)的利用和液化天然气的方法是众所周知的。天然气可以在产地液化或者可以在一年的部分时期，即在热量需要不多的夏季几个月的时期可获量过剩时的利用地点液化。然后易于将天然气作为液化的天然气贮藏起来以满足冬季对超过通过一现有管线等的可获量的天然气的高峰需求。
天然气广泛地用作燃料并广泛地作为液化的天然气产品输送。天然气可以通过各种方法加以液化，其中之一通常称之为混合的致冷方法。这些方法说明于例如，1977年7月5日授予Leonard K.Swenson的U.S专利号4033735和1997年8月9日授予BrianC.Price的U.S.专利5657643中。这些文件全部在此引入作为参考。
在这些方法中一混合的致冷剂用于一单个的热交换区域以达到要求的冷却而液化天然气。
已采用的其他系统通常称之为级联系统。一种这样的系统说明于1974年12月24日授予Simon等人的U.S.专利3855810中。该文件全部也在此引入作为参考。这种方法利用多个致冷区域，其中降低沸点的致冷剂被汽化以产生一冷却剂。在这样的系统中，一般，最高沸点的致冷剂单独或与其他致冷剂一起被压缩、冷凝和分离用以在第一致冷区域内的冷却。然后将压缩的冷却的最高沸点的致冷剂闪蒸(flash)以形成一冷致冷剂流，其用于冷却在第一致冷区域内的压缩的最高沸点的致冷剂。在第一致冷区域内也可以使一些较低沸点的致冷剂冷却并继之冷凝和经过汽化，以便在第二或随后的致冷区域等内起一冷却剂的作用。因此，最高沸点的致冷剂首要的是压缩。
天然气液体的组分从一天然气源至另一气源可能广泛地变化。在所述两种型式的方法中，有必要从天然气中排除较重的天然气液体(C5+)以便防止堵塞天然气用的热交换通道。同样常常最好是在某些情况下回收较轻的碳氢化合物，例如C2、C3和C4。常常最好是与较重的碳氢化合物一起回收C2、C3和C4碳氢化合物，因为它们作为单独产品或作为天然气液体的一部分比作为LNG的一部分可以更有价值。然而，在所有的情况下，如果在进入天然气液化区域内的天然气中存在大量的较重的天然气液体，则它们在致冷区域内在液化温度下凝固于热交换通道内并堵塞通道。
在很多情况下，可在较高的压力下，即高达和也许超过约1500psig下得到天然气。在高压下比在较低压力下液化天然气要更有效得多。可惜，天然气液体和剩余的天然气流的组分的分离要求将天然气流的压力降到约650psig的压力以下以使甲烷从剩余的天然气组分中有效地分离。这导致天然气在脱甲烷后在较低压力下返回通过致冷区域的热交换通道，从而导致在较低压力下的液化。如上所述，在高压下液化天然气是更为有效的。
因此，已找到更有效的方法用来从高压天然气流中排除天然气液体而不降低压力，从而天然气可以在高压下加以液化。
发明内容
按照本发明，提供一种改进的方法，用于在一混合的致冷方法中有效地液化具有高于约500psig的压力的天然气流以生产液化的天然气流。该方法包括：在混合的致冷方法中在一热交换器内将天然气流冷却到低于约-40°F的第一温度以产生冷却的天然气流；使冷却的天然气流进入一液体分离区域以产生第一气体流和第一液体流；使第一液体流在低于约-40°F的温度和低于约650psig的压力下进入一甲烷分离塔，以产生包含至少50％甲烷的第二气体流和包含天然气液体的第二液体流；使第一气体流进入一涡轮膨胀器以将第一气体流的压力降到低于约650psig的压力，以便产生减压的气体流并使该减压的气体流进入甲烷分离塔；由该涡轮膨胀器驱动一压缩机；使第二气体流进入压缩机并将第二气体流压缩到至少约500psig的压力以产生压缩的气体流；以及使该压缩的气体流进入热交换器以便在至少约500psig的压力下液化。本发明还包括一种方法，用于在天然气液化方法中液化压力高于约500psig的天然气流以生产液化的天然气流。该方法包括：在一热交换器内将天然气流冷却到低于约-40°F的第一温度以产生冷却的天然气流；使该冷却的天然气流进入一液体分离区域以产生第一气体流和第一液体流；使第一液体流在低于约-40°F的温度和低于约650psig的压力下进入一甲烷分离塔，以产生包含至少50％甲烷的第二气体流和包含天然气液体的第二液体流；使第一气体流进入一涡轮膨胀器以将第一气体流的压力降到低于约650psig的压力，以便产生减压的气体流并使该减压的气体流进入甲烷分离塔；由涡轮膨胀器驱动一压缩机；使第二气体流进入压缩机并将第二气体流压缩到至少约500psig的压力以产生压缩的气体流；以及使该压缩的气体流进入热交换器以便在至少约500psig的压力下液化，从而生产液化的天然气。
本发明还包括一种系统，用于液化具有高于约500psig的压力的天然气流，该系统包括：一致冷单元，其适合于将天然气冷却到足以液化至少大部分的天然气的温度，该致冷单元具有一中间的气体出口、一中间的气体入口和一液化的天然气产品出口；一分离器，该分离器与所述中间的气体出口流体连通并且具有一气体出口和一液体出口；一甲烷分离器，该甲烷分离器与所述液体出口流体连通，并且具有一顶部的气体出口、一底部的液体出口和一气体入口；一涡轮膨胀器，其与来自所述分离器的气体出口和进入甲烷分离器的气体入口流体连通；以及一压缩机，该压缩机由涡轮膨胀器驱动，并且流体连通于所述顶部的气体出口，以及具有一与所述中间的气体入口流体连通的压缩气体出口。
本发明还包括一种方法，用于在高于约500psig的压力下从天然气流中有效地分离天然气液体以产生高压气体流和天然气液体流，其通过下列步骤实现：将天然气流冷却到低于约-40°F的第一温度以产生冷却的天然气流；使该冷却的天然气流进入一液体分离区域内以产生第一气体流和第一液体流；使该第一液体流在低于约650psig的压力下进入一甲烷分离塔，以产生包含至少50％甲烷的第二气体流和包含天然气液体的第二液体流；使第一气体流进入一涡轮膨胀器以将第一气体流的压力降到低于约650psig的压力，以便产生减压的气体流并使该减压的气体流进入甲烷分离塔；由涡轮膨胀器驱动一压缩机；以及使第二气体流进入压缩机并压缩该第二气体流以产生高压压缩的气体流。
附图说明
图1为用于液化天然气的现有技术的方法的示意图；
图2为用于液化天然气的现有技术的另一方法的示意图；
图3为本发明的方法的一个实施方案的示意图；以及
图4为在本发明中实用的涡轮膨胀器和压缩机的一个实施方案的示意图。
具体实施方式
在诸图的讨论中，同样的标号将始终用来指同样的或类似的部件。并且，为简明起见没有示出为达到要求的流程所需要的全部的泵、阀等。
图1中示出一现有技术的天然气液化方法10。该所示方法为一混合的致冷方法，例如在以上引入作为参考的U.S.专利4033735和5657643中所说明的。一混合的致冷剂在约80至约100°F，并且一般在约100°F的温度，和在约500至约600psig，并且一般在约550psig的压力下，经由一管线12进入一主热交换器16中，其中其通过一热交换通道14以冷却该混合的致冷剂。冷却过的混合致冷剂一般在约-260°F的温度和从约500至约600psig的压力下通过一管线18回收，其由管线18通过一膨胀阀20进一步降低混合的致冷剂的温度，该致冷剂在管线18中基本上完全是液体，从而该混合的致冷剂在其向上通过一热交换通道22时在管线21中开始汽化。当混合的致冷剂离开热交换通道22时，它已基本上汽化了并且处于从约50至约80°F的温度和从约40至约50psig的压力下。
天然气经由一管线26进入主热交换器16内，通过一热交换通道28。热交换通道28具有一中间的天然气出口30a通过一管线30。天然气经由管线30排出并经由阀32和管线33进入一甲烷馏除塔34。甲烷馏除塔34表明为一柱体，其包括许多浮阀塔盘或阀填料用以从天然气流的液体组分中有效地分离甲烷。通过管线30排出的天然气流一般处于从约-40至约-120°F的温度下并且可以处于从约200至约1500psig的压力下。该压力合乎要求地被降到低于约650psig以便在甲烷馏除塔中排除甲烷。
由于临界压力的条件，甲烷的排除必须在低于约650psig的压力下进行。从甲烷馏除塔34回收于管线36中的气体流包含至少50％的甲烷并且经由管线36返回主热交换器16中的一热交换通道72。然后甲烷气体在热交换通道72中被液化并产生作为液体天然气产品通过管线74。如本领域的那些技术人员众所周知的，通过管线74产生的LNG可以经过闪蒸等以便在贮藏以前进一步降低温度。一般管线74中液体流处于从约-230至约-275°F的温度和约1个大气压下。在天然气液化方法的操作的范围内广泛的改变是可能的。
甲烷馏除塔34通过利用一重沸器38来操作以便产生要求的分离所需要的热。甲烷馏除塔34合乎要求地在从约-100至约-150°F的塔顶温度和低于约650psig的压力下操作。液体流经由管线40作为底部流从甲烷馏除塔34中产生并且经由阀42和管线43进入一分馏塔44。分馏塔44一般在从约-10至约125°F的塔顶温度和从约250至约450psig的压力下操作。分馏塔44还包括一重沸器回路46并将管线40中的流分成底部流，其为一天然气液体流，一般作为具有要求的规格的产品流生产。
通过管线50回收的塔顶流为轻气体，其适当地与管线36中的气体重新混合。为了实现这种混合，管线50中的气体在冷却器52中冷却并经由管线53进入一液体分离器54。基本上管线50中的全部气体最后被液化并且或者经由管线60和泵62返回，通过管线64进入分馏塔44，或者经由管线56和泵58进入回收管线66，通过管线66其与管线36中的流相混合。该泵将液体的压力提高到一合适的压力以便使其很容易地与管线36中的气体流相混合。
一般在从约200至约1500psig或更高的压力下的这些方法可以得到天然气。由于在高压下液化天然气要更有效得多，极不希望排除天然气液体的方法导致使压力降到低于约500psig的压力。然而一般采用了这些方法，因为有必要排除较重的天然气液体(C5+)以防其凝固和堵塞主热交换器16中的热交换通道，并且因为天然气液体比经液化的天然气具有每单位容积或重量更高的价值。
图2中示出另一现有技术的实施方案，其中一液体气体分离器68用来从经由管线30进入分离器68的部分液化过的天然气中分离甲烷和其他类似气体组分。管线70中的顶部气体流与来自管线66的液体一起在基本上入口天然气流的压力下返回热交换通道76。从分离器68出来的液体经由管线29、阀32和管线33进入甲烷馏除塔34。在甲烷馏除塔34中发生以上讨论的同样的分离，其中气体流经由管线36回收并返回一热交换通道72。在热交换通道72中产生的液化的天然气是在较低压力下被液化的并且经由管线78在基本上如通过管线74回收的液化的天然气同样的温度下回收并且经过闪蒸、生产等等。
在该两实施方案中，有必要将天然气流的压力降到低于650psig的压力以便从天然气液体中分离天然气中的甲烷和较轻的碳氢化合物组分。因此，需要更大的功率用于附加的热交换要求以便在减压下液化天然气。最好是如果能保持天然气的压力的条件，便使液化方法可以在较高压力下更有效地进行。
在图1、2和3中，甲烷馏除塔34和分馏塔44表明是浮阀塔盘的塔。可以采用有效分离包含不同沸点的材料的任何合适的塔，例如一皱褶式塔(pucket tower)。这些塔的操作不予详细描述，因为这种用于分离不同沸点的材料重沸器和塔的应用对本领域的那些技术人员来说是众所周知的。
图3中示出本发明的一个实施方案。在该实施方案中，从热交换通道28的中间的天然气出口30a排出的流通过管线30并进入一分离器68。在分离器68中排出气体流80并使其进入一涡轮膨胀器86。在涡轮膨胀器86中，管线80中的天然气流的压力被降到低于约650psig的压力。然后该气体流经由管线35和阀35进入甲烷馏除塔34。从分离器68中回收的液体也经由管线82、阀32和管线33进入甲烷馏除塔34。
或者，管线35中的气体流通过关闭阀35’转向管线37并经由管线37和阀37’进入一分离器39。在分离器39中分离轻的碳氢化合物并使其进入管线84以便在一压缩机90进行压缩。在分离器39中排出的液体经由管线41和阀41’进入甲烷馏除塔34。该替代方案可以用来降低甲烷馏除塔34的上部的分离负荷。该负荷是由于经由管线35使大量气体进入甲烷馏除塔34的上部引起的。
在任一情况下，在甲烷馏除塔34中按以上所述进行分离，其塔顶气体流通过管线84回收并进入压缩机90，压缩机90至少部分地由涡轮膨胀器86驱动。这些单元合乎要求地用轴连接以便涡轮膨胀器86可以驱动压缩机90。压缩的气体离开压缩机90通过管线36返回天然气入口36a，进入热交换通道72。然后液化的天然气通过管线74按以下讨论产生。管线36中的较高压力使得可以在一较高压力下进行天然气的液化，一般压力高于约500psig。天然气在高压下的液化使LNG的生产可以在一较高温度下进行并降低LNG方法的功率要求。图4中示出涡轮膨胀器86由轴92轴连接于压缩机90以压缩来自甲烷馏除塔34的管线84中的天然气。压缩的气体如图中所示经由管线36排走。压缩机90可以只由涡轮膨胀器86驱动，并且在该实施方案中由于甲烷馏除塔34所需要的压力的降低，能够回收消耗在天然气流中的大部分的压缩能量。该压缩能量回收在压缩机90中，其中作为甲烷馏除塔34中的塔顶气体流产生的气体流由压缩机90压缩。在最后得到的返回热交换通道72的天然气流中的压力与在利用涡轮膨胀器86作为压缩机90的唯一能源时的入口气体流的压力相比较有些损失。不过，该气体仍可在一显著较高的压力下被液化，该压力显著高于在产品流从甲烷馏除塔34直接进入热交换通道72时能够达到的压力。
如果要求将所述压力提高到高于在只利用涡轮膨胀器86作为能源时可能的压力水平，则为了补充作为一能源的涡轮膨胀器86而将一马达96经由轴94等轴连接于压缩机90以提高管线36中的气体流的压力。这使天然气的液化可以合乎要求地在较高压力下进行。由马达96供给的能量可以广泛地予以改变并且取决于多种图素例如致冷剂压缩所需要的功率、要求的液化压力等。所用马达为一通用的马达，其合乎要求地为一电机，并且涡轮膨胀器86和马达96均通过通用的连接装置连接于压缩机90。这样的装置对本领域的那些技术人员来说是众所周知的并对其将不作进一步地讨论。
合乎要求地通过管线48生产符合天然气液体流规格的天然气液体。可使管线50中的塔顶流按需要改变以便在管线48中生产要求的规格的产品流。或者，可以经由管线40回收一产品流，其不仅包含天然气液体，而且也包含一些较轻的碳氢化合物。在某些情况下可能符合需要的是将该流用作为一产品流。
该方法易于按要求加以改变以便按天然气液体的各个组分或按一混合的天然气液体流等生产天然气液体。这些改变取决于适用于特定设备的经济状况。在任何情况下，本发明的方法涉及在一压力下将天然气流的轻气体组分返回热交换器16中的致冷通道，该压力高于通常从甲烷馏除塔34中回收的压力。这导致在主热交换器中提高的效率和改进的总方法的效率。
虽然以上参照混合的致冷方法讨论了本发明，但其同样可用于级联方法或其他的方法，因为这些方法在冷却到其液化温度以前也需要从天然气中排除较重的天然气液体。适用同样的考虑，即天然气液体作为单独的产品比作为LNG的一部分可以更有价值并且天然气流的重(C5+)组分如果不排除就倾向于凝固在致冷通道中。两种方法均提供在排除天然气液体以前将天然气冷却到一中等温度的灵活性，并且这种灵活性在排除天然气液体以后可进一步将剩余的天然气组分冷却到一液化温度。
许多天然气源在从200至约1500psig或更高的压力下生产天然气。该天然气合乎要求地在高压，即在高于约500psig的压力下被液化。如上所述，在现有技术的方法中，需要将天然气流的压力降到低于约650psig的压力以便从天然气中排除天然气液体。这种压力降低主要是由于甲烷馏除塔中的临界压力条件所需要的。因此，基本上在所有的脱甲烷方法中都是需要的。
按照本发明，气体压力能被回收并用来再压缩甲烷馏除塔的产品气体以便返回致冷区域。这导致在用于从天然气流中排除天然气液体的方法中大大降低了压力的损失。
至此参照本发明的优选的实施方案的某一些描述了本发明，应该指出所描述的实施方案在本质上是说明性的而非限制性的并且在本发明的范围内许多改变和改进是可能的。

Claims (23)

1.一种方法，用于在一混合的致冷方法中液化具有高于约500psig的压力的天然气流以生产液化的天然气产品，该方法包括：
a)在混合的致冷方法中在一热交换器内将天然气流冷却到低于约-40°F的第一温度以产生冷却的天然气流；
b)使冷却的天然气流进入一液体分离区域以产生第一气体流和第一液体流；
c)使第一液体流在低于约-40°F的温度和低于约650psig的压力下进入一甲烷分离塔，以产生包含甲烷的第二气体流和包含天然气液体的第二液体流；
d)使第一气体流进入一涡轮膨胀器以将第一气体流的压力降到低于约650psig的压力，以便产生减压的气体流并使该减压的气体流进入甲烷分离容器；
e)由该涡轮膨胀器驱动一压缩机；
f)使第二气体流进入压缩机并将第二气体流压缩到至少约500psig的压力以产生压缩的气体流；以及
g)使该压缩的气体流进入热交换器以便在至少约500psig的压力下液化，从而生产液化的天然气。
2.根据权利要求1所述的方法，其特征在于，所述第一温度为约-40至约-120°F。
3.根据权利要求1所述的方法，其特征在于，所述第一液体流在约-40至约-120°F的温度下进入甲烷分离塔。
4.根据权利要求1所述的方法，其特征在于，所述甲烷分离塔具有约-100至约-150°F的塔顶温度并在低于约650psig的压力下操作。
5.根据权利要求1所述的方法，其特征在于，所述第二液体流进入一分馏塔以产生第三气体流和包含天然气液体的流。
6.根据权利要求5所述的方法，其特征在于，所述第三气体流经冷却、液化并被泵送以与压缩的气体流组合。
7.根据权利要求1所述的方法，其特征在于，所述压缩机还由一马达驱动。
8.根据权利要求1所述的方法，其特征在于，所述减压气体流进入第二分离区域以产生第三气体流和第三液体流，使第三气体流进入压缩机并使第三液体流进入甲烷分离塔。
9.一种方法，用于在一天然气液化方法中液化具有高于约500psig的压力的天然气流以生产液化的天然气产品，该方法包括：
a)在天然气液化过程中在一热交换器内将天然气流冷却到低于约-40°F的第一温度以产生冷却的天然气流；
b)使冷却的天然气流进入一液体分离区域以产生第一气体流和第一液体流；
c)使第一液体流在低于约-40°F的温度和低于约650psig的压力下进入一甲烷分离塔，以产生包含甲烷的第二气体流和包含天然气液体的第二液体流；
d)使第一气体流进入一涡轮膨胀器以将第一气体流的压力降到低于约650psig的压力，以便产生减压的气体流并使该减压的气体流进入甲烷分离塔；
e)由所述涡轮膨胀器驱动一压缩机；
f)使第二气体流进入压缩机并将第二气体流压缩到至少约500psig的压力以产生压缩的气体流；以及
g)使该压缩的气体流进入热交换器以便在至少约500psig的压力下液化，从而生产液化的天然气。
10.根据权利要求9所述的方法，其特征在于，所述第一温度为约-40至约-120°F。
11.根据权利要求9所述的方法，其特征在于，所述第一液体流在约-40至约-120°F的温度下进入甲烷分离器。
12.根据权利要求9所述的方法，其特征在于，所述甲烷分离器处在约-100至约-120°F的温度和低于约650psig的压力下。
13.根据权利要求9所述的方法，其特征在于，所述第二液体流进入一分馏塔以产生第三气体流和包含天然气液体的流。
14.根据权利要求13所述的方法，其特征在于，所述第三气体流经冷却、液化并被泵送以与压缩的气体流组合。
15.根据权利要求9所述的方法，其特征在于，所述压缩机还由一马达驱动。
16.根据权利要求9所述的方法，其特征在于，所述减压气体流进入第二分离区域以产生第三气体流和第三液体流，使第三气体流进入压缩机并使第三液体流进入甲烷分离塔。
17.一种系统，用于液化具有高于约500psig的压力的天然气流，该系统包括：
a)一致冷单元，其适合于将天然气冷却到足以液化至少大部分的天然气的温度，致冷单元具有一中间的气体出口、一中间的气体入口和一液化的天然气产品出口；
b)一分离器，该分离器与所述中间的气体出口流体连通并且具有一气体出口和一液体出口；
c)一甲烷分离塔，该甲烷分离塔与所述液体出口流体连通并且具有一顶部的气体出口、一底部的液体出口和一气体入口；
d)一涡轮膨胀器，其与来自所述分离器的气体出口和进入甲烷分离塔的气体入口流体连通；以及
e)一压缩机，该压缩机由涡轮膨胀器驱动，并且流体连通于所述顶部的气体出口，以及具有一与所述中间的气体入口流体连通的压缩气体出口。
18.根据权利要求17所述的系统，其特征在于，该系统还包括一分馏器，其流体连通于所述底部的液体出口并具有一分离的气体出口和一天然气液体出口。
19.根据权利要求18所述的系统，其特征在于，所述分离的气体出口经由一热交换器、一泵和一管线流体连通于所述中间的气体入口。
20.根据权利要求17所述的系统，其特征在于，所述致冷单元包括多个热交换区域。
21.一种方法，用于在高于约500psig的压力下从天然气流中有效地分离天然气液体，以便生产高压气体流和天然气液体流，该方法包括：
a)将天然气流冷却到低于约-40°F的第一温度以产生冷却的天然气流；
b)使冷却的天然气流进入一液体分离区域以产生第一气体流和第一液体流；
c)使第一液体流在低于约-40°F的温度和低于约650psig的压力下进入一甲烷分离容器，以产生包含甲烷的第二气体流和包含天然气液体的第二液体流；
d)使第一气体流进入一涡轮膨胀器以将第一气体流的压力降到低于约650psig的压力，以便产生减压的气体流并使该减压的气体流进入甲烷分离塔；
e)由所述涡轮膨胀器驱动一压缩机；以及
f)使第二气体流进入压缩机并压缩第二气体流以产生高压压缩的气体流。
22.根据权利要求21所述的方法，其特征在于，所述第二液体流进入一分馏塔以产生第三气体流和包含天然气液体的流。
23.根据权利要求21所述的方法，其特征在于，所述减压气体流进入第二分离区域以产生第三气体流和第三液体流，使第三气体流进入压缩机并使第三液体流进入甲烷分离塔。
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