CN101223410A - 用于液化富烃流的方法 - Google Patents

用于液化富烃流的方法 Download PDF

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CN101223410A
CN101223410A CNA2006800223253A CN200680022325A CN101223410A CN 101223410 A CN101223410 A CN 101223410A CN A2006800223253 A CNA2006800223253 A CN A2006800223253A CN 200680022325 A CN200680022325 A CN 200680022325A CN 101223410 A CN101223410 A CN 101223410A
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H·鲍尔
R·扎佩尔
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Abstract

本发明涉及一种用于液化富烃流、特别是天然气流的方法，其中，富烃流的液化逆着一个由三个混合制冷剂循环组成的混合制冷剂循环级联装置来实现。根据本发明，第一和第二混合制冷剂循环(2a－2b，3a－3b)用于预冷，第三混合制冷剂循环(4a－4b)用于液化和过冷该富烃流。在此，第一和/或第二混合制冷剂循环(2a－2b，3a－3b)优选被设计为单级的混合制冷剂循环，而第三混合制冷剂循环(4a－4b)优选被设计为两级的混合制冷剂循环。

Description

用于液化富烃流的方法
技术领域
本发明涉及一种用于液化富烃流、特别是天然气流的方法，其中，富烃流的液化逆着由三个混合制冷剂循环组成的混合制冷剂循环级联装置来实现。
下面对于术语“第一混合制冷剂循环”应该总是被理解为二氧化碳制冷剂循环。
背景技术
由德国公开文献197 16 415公开了一种所述类型的用于液化富烃流的方法。通过引用该德国公开文献197 16 415，其公开内容被纳入在本专利申请的公开内容中。
天然气液化装置或者被设计为所谓的LNG基荷型设备-也就是用于以天然气作为原始能量供给的天然气液化设备-或者被设计为所谓的调峰设备-也就是用于满足峰值要求的天然气液化设备。
LNG基荷型设备在一般情况下以制冷循环来驱动，这些制冷循环由烃混合物组成。这些混合物循环比膨胀机循环更节能而且在基荷型设备的大液化功率时实现对应的相对较小的能量消耗。
在这种类型的液化方法中目前基本上是以第一混合物循环用于预冷，第二混合物循环用于液化，第三混合物循环用于过冷富烃流或者天然气。
在预冷和液化之间-如果必要的话-进行高沸点烃的分离。它们至少是待液化的富烃流或天然气这种组分，这些组分在随后的冷却中将被冻结-即C5+烃或者芳香烃。此外，经常是将那些使待被液化的天然气的热值不期望地升高的烃-在此特别是指丙烷和丁烷-在液化之前分离出去。
由德国专利申请103 44 030同样公开了一种所述类型的方法，其中至少使用第二混合制冷剂循环的混合制冷剂的分流来预冷富烃流。该液化方法实现了可使用的压缩机和驱动装置更经济的利用，因为这三个混合物循环的(循环)压缩机得到几乎相同的驱动功率，也就是各为总功率的33.33％。因此特别是每年制取大于五百万吨液化天然气的具有大液化功率的大型液化设备能够更经济地运行，因为通过整合这三个制冷循环的压缩机和驱动装置可使得液化过程的用试验的驱动装置或压缩机所能实现的液化功率最大化。
第一混合制冷剂循环的用于预冷的混合制冷剂在上述类型的液化方法中通常在两个或者多个不同的压力水平上蒸发。从而达到供冷对热过程流的冷却要求的良好适应并且减少能耗。因此，特别是对所谓的基荷型设备或-过程来说，单级预冷是罕见的，这是因为其与高能耗相关。
上述属于现有技术的方法具有以下结果：使得至少一个用于预冷的混合制冷剂分流在一个小于剩余混合制冷剂分流的压力下被蒸发。但是，使用低压蒸发的制冷剂必然导致较大的并且从而成本高的设备、机器和管道。
发明内容
本发明的任务在于，给出一种所述类型的方法，它避免了上述的缺点。
为了解决这个任务，提出了一种所述类型的用于液化富烃流的方法，其特征在于，第一和第二混合制冷剂循环用于预冷，而第三混合制冷剂循环用于液化和过冷富烃流。
根据本发明的用于液化富烃流的方法的其他有利构型的特征在于：
-第一和/或第二混合制冷剂循环被设计为单级混合制冷剂循环，
-第三混合制冷剂循环被设计为两级混合制冷剂循环，
-第一和第二混合制冷剂循环的压缩机的功率消耗与该两级的第三混合制冷剂循环的压缩机的功率消耗相同或者基本相同，
-其中，优选这些混合制冷剂循环所有的压缩机具有相同或者基本相同的功率消耗，
-第一和第二混合制冷剂循环的压缩机的功率消耗与该两级的第三混合制冷剂循环的两个压缩机中的每一个压缩机的功率消耗相同或者基本相同，
-优选使用燃气轮机、蒸汽轮机和/或电动机作为用于压缩机的驱动装置。
对于术语“预冷”应理解为使待液化的富烃流冷却到至少-30℃至-70℃，优选-40℃至-60℃的温度上。
现在，根据本发明，为了预冷富烃流，用两个独立的单级混合制冷剂循环来代替在现有液化方法中实现的两级预冷循环。借助于方法条件的合适选择、比如混合物的组成、压力剖面形状等等，能够使本发明液化方法的两个预冷循环的抽吸压力大大升高，也就是典型地提高到5巴或者更高。与此相比，一个两级预冷循环低压级的抽吸压力为2-3巴。
由于用于预冷的混合制冷剂循环具有较高的气体密度，因此本发明的方法实现了更紧凑的设备或过程。此外，与只使用两个混合物循环的液化方法相比，本发明的具有三个混合物循环的方法具有较低的单位能耗。
附图说明
下面借助附图所示的实施例详细描述本发明的方法及其构成从属权利要求主题的构型。
在图示的方法中，经由管道1输送到换热器E1的富烃流的冷却和液化逆着一个由三个混合制冷剂循环组成的混合制冷剂循环级联装置来实现。这些混合制冷剂循环通常具有不同的组成，例如在前述德国公开文献197 16415中所描述的那样。
具体实施方式
待液化的富烃流在换热器E1中逆着第一混合物循环2a-2c的蒸发了的混合制冷剂流2b冷却。接下来，富烃流通过管道1a被输送到换热器E2并且在该换热器中逆着第二混合物循环3a-3c的蒸发的混合制冷剂流3b进一步冷却。
在换热器E2的出口上，被冷却了的富烃流的温度为-30℃到-70℃，优选-40℃到-60℃。现在它通过管道1b被输送到一个仅作为黑箱表示的分离单元S。
在该分离单元S中进行上述的C3+分离，其中，被从待液化的富烃流中分离出的组分通过管道1c从该分离单元S排出。
然后，待液化的富烃流通过管道1d输送到第三换热器E3并且在该换热器中逆着第三制冷剂循环4a到4c的混合制冷剂流4b被液化和过冷。
接下来，被过冷的液态产物通过管道1e输入到它的另外的用途和/或(中间)储存装置中。
如已经提及的那样，用于预冷待液化富烃流的两个混合制冷剂循环2a-2c和3a-3c分别是单级的混合制冷剂循环。
在各自的循环压缩机V2或者V3中压缩的混合制冷剂经由管道2a或3a流经换热器E1(在第一混合制冷剂循环的情况下)或者流经这两个换热器E1和E2(在第二混合制冷剂循环的情况下)。在减压阀a或b中减压后，混合制冷剂流在换热器E1或E2中逆着待冷却的过程流蒸发并且紧接着经由管道2c或3c又输送到循环压缩机V2或V3。
同样的也适用于第三混合制冷剂循环，在该第三混合制冷剂循环中，被压缩了的混合制冷剂4a在换热器E1、E2和E3中冷却后经由管道4b输送到减压装置c、在该减压装置中减压、接着在换热器E3中捏着待冷却的过程流蒸发并且然后经由管道4c输送到低压压缩机级V4的入口，高压压缩机级V4连接在该低压压缩机级后面。
运行压力的与本发明方法相关联的升高以及用于预冷的第二混合制冷剂分流3a-3c的气体密度的升高对于换热器E2促进了缠绕式换热器的使用，在这种缠绕式换热器中，混合制冷剂外套侧被蒸发。迄今为止，在这种类型的、属于现有技术的液化方法中经常没有应用这种缠绕式换热器，因为这种缠绕式换热器结构太大，但是其允许的最大直径通常由于制造-和运输尺寸的原因而受到限制。
在图中没有示出连接在压缩机V2、V3、V4和V4′后面的冷却器或换热器，在所述冷却器或换热器中，混合制冷剂逆着冷却介质、例如水或者空气被冷却并且在第一混合制冷剂循环2a-2c情况下被冷凝。第二混合制冷剂循环的混合制冷介质通常在压缩之后逆着冷却介质、例如水或者空气至少部分地冷凝。
根据本发明方法的另一有利的构型，第一和第二混合制冷剂循环2a-2b和3a-3b的压缩机V2和V3的功率消耗与所述两级的第三混合制冷剂循环4a-4b的压缩机V4和V4′的功率消耗相同或者基本相同地设计。在这种情况下，这些混合制冷剂循环2a-2b、3a-3b和4a-4b的所有压缩机V2、V3、V4和V4′具有相同的或者基本相同的功率消耗。
在本发明方法该构型中，可以设置两个相同的驱动装置(一个配置给压缩机V2和V3，一个配置给压缩机V4和V4′)或者四个相同的驱动装置(分别驱动一个压缩机V2、V3、V4及V4′)。
对于术语“基本相同”应理解为功率消耗相差不超过+/-2％。
替代本发明方法的上述构型地，第一和第二混合制冷剂循环2a-2b和3a-3b的压缩机V2和V3的功率消耗与所述两级的第三混合制冷剂循环4a-4b的两个压缩机V4和V4′每一个压缩机的功率消耗相同或者基本相同地设计。在本发明方法的该构型中，优选使用三个相同的驱动装置A2/3、A4和A4′，其中A2/3配置给压缩机V2和V3，而A4和A4′配置给压缩机V4和V4′。
因此，主要在大驱动装置、尤其是燃气轮机的以单级方式可供使用的情况下，可以满足设备尺寸的多样化。上面最后提及的替换方案特别适合于冷的冷却介质，因为在这种情况下预冷的能量需求降低。
因此，本发明方法的上述构型特别的具有如下优点，即在其功率方面可以使用相同的或者基本相同的驱动装置A2/3、A4和A4′。

Claims (7)

1.用于液化富烃流、特别是天然气流的方法，其中，富烃流的液化逆着一个由三个混合制冷剂循环组成的混合制冷剂循环级联装置来实现，其特征在于，第一和第二混合制冷剂循环(2a-2b，3a-3b)用于预冷，第三混合制冷剂循环(4a-4b)用于液化和过冷该富烃流。
2.如权利要求1所述的方法，其特征在于，第一和/或第二混合制冷剂循环(2a-2b，3a-3b)被设计为单级的混合制冷剂循环。
3.如权利要求1或2所述的方法，其特征在于，第三混合制冷剂循环(4a-4b)被设计为两级的混合制冷剂循环。
4.如权利要求3所述的方法，其特征在于，第一和第二混合制冷剂循环(2a-2b，3a-3b)的压缩机(V2，V3)的功率消耗与所述两级的第三混合制冷剂循环(4a-4b)的压缩机(V4，V4′)的功率消耗相同或者基本相同。
5.如权利要求4所述的方法，其特征在于，这些混合制冷剂循环(2a-2b，3a-3b，4a-4b)的所有压缩机(V2，V3，V4，V4′)具有相同的或者基本相同的功率消耗。
6.如权利要求3所述的方法，其特征在于，第一和第二混合制冷剂循环(2a-2b，3a-3b)的压缩机(V2，V3)的功率消耗与所述两级的第三混合制冷剂循环(4a-4b)的两个压缩机(V4，V4′)中的每一个压缩机的功率消耗相同或者基本相同。
7.如权利要求1-6之一所述的方法，其特征在于，使用燃气轮机、蒸汽轮机和/或电动机作为用于压缩机(V2，V3，V4，V4′)的驱动装置(A2/3，A4，A4′)。
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US9163873B2 (en) 2008-08-29 2015-10-20 Wärtsilä Oil & Gas Systems As Method and system for optimized LNG production
CN102203531A (zh) * 2008-11-04 2011-09-28 海威气体***公司 用于低温液化工艺中的组合式循环机械驱动的***
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