CN103582792A - 用于天然气液化的方法 - Google Patents

用于天然气液化的方法 Download PDF

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CN103582792A
CN103582792A CN201280027025.XA CN201280027025A CN103582792A CN 103582792 A CN103582792 A CN 103582792A CN 201280027025 A CN201280027025 A CN 201280027025A CN 103582792 A CN103582792 A CN 103582792A
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heat exchanger
fluid stream
expander
gas
natural gas
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CN103582792B (zh
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安东尼·D·蒙德
杰弗里·弗雷德里克·斯金纳
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Abstract

一种方法，包括：通过一个热交换器和一个第一膨胀器来冷却天然气。该热交换器将给送天然气冷却至高于该膨胀器出口温度的温度、在该热交换器的一个第一冷通道中将膨胀器出口流束再加热至略微低于通到该热交换器的给送天然气的温度、使来自该热交换器的冷出口流束进入一个第二膨胀器中而使其在该第二膨胀器中被部分地液化、将该第二膨胀器的出口流束分离成液体部分和蒸气部分、收集该液体部分以用作LNG产品、将该蒸气部分在该热交换器的一个第二冷侧通道中再加热至与通到该热交换器的给送天然气的温度基本上相同的温度、将经再加热的蒸气部分进行再循环而一部分作为该第一膨胀器的进料且一部分作为该热交换器的进料。

Description

用于天然气液化的方法
技术领域
本发明涉及一种用于将富含甲烷的气体液化的方法，并且更具体地但并非排他性地涉及用于产生液化天然气（LNG）的方法。
背景技术
天然气的液化实际上可以通过以下方式实现：
-将液体制冷剂蒸发
-在膨胀机（膨胀器）中使气体做功膨胀。
液体制冷剂的蒸发提出了最低功率要求并且是广泛使用的级联和混合制冷剂LNG方法的基础。
基于膨胀器的LNG设施是简单的、紧凑的、重量小的并且可以避免液体制冷剂的输送/制备/储存。这些特征对于小规模应用（特别是离岸的）是有吸引力的，在这些应用中从安全考虑希望小的烃藏有量。然而，膨胀器方法具有若干缺点：
-直到最近，对膨胀器的能力和经验仍有限
-具有较高的功率要求
-较高的内部气体流速，要求有较大的管线直径等等。
对于大多数基于膨胀器的方法而言，工作流体（典型地为氮气）在膨胀器出口处保持处于蒸气相。
使给送气体本身在膨胀器中部分地液化，从而具有一个两相的排出流，这可以减小内部（再循环）气体流量并且减小功率要求。
在一个液化膨胀器中生产LNG不是一个新观点（USP2,903,858-Bocquet）。
本发明的诸位发明人之前披露过一种具有潜在较低功率要求的方法（英国专利2393504B，USP7,234,321），其中将一个液化膨胀器与一个预冷却回路相组合，该预冷却回路含有由给送天然气所产生的一种简单的混合制冷剂。
其他近期的公开文献包括通过一个平行/再循环气体膨胀器后接一个液化膨胀器来进行预冷却：
-WO01/44735（Minta等人），描述了在-112℃由被压缩至“1600帕以上”高压的给送气体来生产加压液化天然气（PLNG）。
-US2006/0213222（Whitesell），描述了由一种以“约1500帕至约3500帕”之间的压力进入工艺中、或在该工艺中被压缩至此压力的给送气体来生产LNG。
发明内容
相对于上述两个专利，本申请的发明性步骤在于：识别这两个膨胀器（预冷却膨胀器和液化膨胀器）的运行条件，这允许在约-161℃实践生产出环境大气压的LNG。此外，不再要求作为上述这些专利的一个特征的非常高压的给送气体。
这产生了一种简化的方法、改进了热效率、具有广阔的潜在应用范围，在这些潜在应用中原料给送气体具有低至40巴（4MPa）的压力。
本发明有助于从较小的气田（特别是离岸的气田）生产LNG，这是由于其简单的流程方案、小的功率消耗、以及不依赖于储存和使用液体制冷剂。该液化方法本身基本上不需要在这样的操作条件下可能较不容易操作的处理柱，例如用于制冷剂制备。
具体实施方式
根据本发明，提供了一种用于将天然气或其他富含甲烷的气体液化的方法。一般处于从40（4Mpa）到100巴（10Mpa）的压力下的这种给送气体通过以上描述的基于膨胀器的设备构型被液化而产生处于约1巴（0.1Mpa）/-161℃的LNG产品，该基于膨胀器的设备构型包括：
-在第一步骤中，将给送气体和再循环气体（下文中提到）通过一个第一热交换器并且在一个第一做功膨胀器中冷却；该热交换器具有在-50℃至-80℃、优选-60℃至-70℃范围内的出口温度；该膨胀器具有低于该热交换器的出口温度；该膨胀器的出口流束在所述热交换器的一个冷通道中被再加热并且然后被再压缩而形成上述再循环气体的一部分。
-使来自所述第一热交换器的经冷却的出口流束一部分进入一个第二热交换器中的热通道中而使其在该热通道中被基本上冷凝、并且一部分进入一个第二做功膨胀器中，所述第二膨胀器具有低于该第二交换器的冷出口的出口温度，该第二膨胀器的出口流束包含显著量的液体（典型地10-15%wt）；该膨胀器出口流束被分离成一个蒸气部分和一个液体部分；该蒸气部分在所述第二和第一热交换器中的多个冷通道中被再加热、然后被再压缩并且返回至该工艺的入口以作为上述再循环气体的一部分。
-将上述分离出的液体以及来自第二热交换器的热通道的冷凝液体（二者典型地处于-120℃左右）的压力降低到大气压力附近；将在上述这些热交换器中的另外多个冷通道中放出的闪发气体进行再加热；去除这些液体来作为LNG产品使用。
已经发现，对再循环气体压缩功率的最低要求归因于要将抽出的机械功集中成该第二膨胀器出口附近处的高于10巴（1Mpa）以上压力范围。这样的一个优点是，来自这两个膨胀器的出口压力可以均等为约10巴（1Mpa），从而将该第一热交换器减少至一种三通道构型。
虽然大多数现有LNG生产都依赖于液体制冷剂的蒸发来冷却并冷凝天然气以便在热交换器中形成LNG产品，但本发明包括一种具有适度功率要求的液化工艺，其中必须的制冷大部分是由给送气体本身的做功膨胀来供应的。因此不需要低温的液体制冷剂或其他辅助工作流体如氮气。以这种方式，在低的温度水平上提取出能量，这导致热力学效率得到改善。因此，除了在由来自一个做功膨胀器的冷气体的再加热而被冷却的交换器中通过冷凝作用形成的之外，直接在该做功膨胀器中形成了显著比例的LNG。
优选实施方式的说明
将参考附图对本发明进行说明，其中图1和图2呈现了展示根据本发明的工艺的流程图。
图1示出了本发明的操作特征。准确的流程图表将取决于给送气体的规格、但一般包含三个基本元素。其中在本申请各处，压力被描述为“巴”，这些是巴的绝对值。
给送天然气（流束1）经过一个预处理阶段A，在该预处理阶段中，将会固化或以其他方式干扰下游液化过程的组分（例如CO2、H2S、水蒸气和汞蒸气）被去除到必要的程度以赋予经预处理的气体（流束2）的适当且常规的最大浓度。流束2与再循环气体（流束3）的一部分（流束4）混合而形成流束6，该流束穿过热交换器B中的一个通道，而作为处于典型在-20℃至-60℃、优选-30℃至-50℃范围内的温度下的流束7而离开。这个温度典型地是足够的低以便冷凝足够的NGL来满足最终LNG产品的规格。在分离器C中任何经冷凝的烃类作为流束8而被去除。来自C的出口蒸气（流束9）在热交换器D的一个通道中被进一步冷却，作为温度在-50℃至-80℃、优选-60℃至-70℃范围内的流束10离开。再循环气体的剩余部分（流束5）在气体膨胀器E中被冷却，该气体膨胀器具有的出口流束11的温度低于流束10的温度。
任选地，经预处理的给送气体的一部分或全部可以通过流束2a离开预处理阶段A而在被划分为流束4和5的这个点的上游汇入气体流束3中。当天然气给送流束1仅具有小含量的重烃时，这个选择可能是适宜的。在这样的情况下，经预处理的给送气体可以与全部的再循环气体进行混合，并且然后将所得的混合物进行划分以通过流束6来供应热交换器B并且通过流束5来供应气体膨胀器E。
流束11的压力典型地在15巴（1.5Mpa）左右。流束11进入热交换器D中的一个第一冷通道中、作为流束12离开，然后该流束穿过热交换器B中的一个第一冷通道、以刚好低于流束6的温度的一个温度出来（流束13）。流束4的流速与流束5的流速之比受到控制，从而使得热交换器B和D的这些复合的热和冷侧之间的温度接近度在其整个长度上是基本上均匀的。
然后流束10的一大部分（流束14）穿过一个第二气体膨胀器F，从这里以3巴（0.3Mpa）与20巴（2Mpa）之间、优选5巴（0.5Mpa）与15巴（1.5Mpa）之间的压力并且以部分液化的状态作为流束15出来。然后流束15进入蒸气-液体分离器G中。来自分离器G的液相（流束16）然后典型地在一个减压装置H（如阀或涡轮机）中被减压。典型地处于或接近于大气压力的来自H的出口流束（流束17）被输送到LNG储罐I中。如果希望减小产品LNG的氮含量，则可以使用一个常规的氮气汽提柱（未图示），典型地采用流束16的感热进行再沸。
任选地并且优选地，流束10的一部分作为流束23流动穿过热交换器J的热侧通道，在其中它通过与来自分离器G的蒸气（流束18）的间接热交换而被液化，从而作为流束24出现。然后其在减压装置K例如阀或涡轮机中典型地被减压。来自K的出口流束被引导至蒸气-液体分离器G中、以虚线示出为流束25a，或是优选地作为流束25b被引导至LNG储罐I。这第二个选择有助于减少再循环气体中氮的累积。已经在热交换器J的第一冷通道中被加热的流束18作为流束19出现。它然后在热交换器D的一个第二冷通道中被进一步加热而作为流束20出现，然后在热交换器B中的一个第二冷通道中被进一步加热而以略低于流束6的温度的一个温度作为流束21出现。
流束13和21在再循环压缩机N中被压缩，来自该再循环压缩机的出口流束34典型地通过冷却器O中的冷却水被冷却。压缩机N可以由具有中冷器的多于一个级组成。流束13和21将不具有相同的压力并且可以在不同的压缩机级处进入。来自O的出口流束形成了上述再循环气体流束3。
经过H的流束16的闪蒸和经过K的流束24的闪蒸将导致放出主要包含甲烷以及给送气体的大部分氮含量的蒸气。典型地这种蒸气（流束26）任选地组合有由向储罐I的热泄漏所产生的汽化损失蒸气，而在热交换器J中的一个第二冷通道中被加热而形成流束27、然后在热交换器D中的一个第三冷通道中被加热而产生流束28并且最后在热交换器B中的一个第三冷通道中被加热而以略低于流束6的温度的一个温度作为流束29出现。在流束26中可以提供一个常规的增压鼓风机（也未图示）以便确保流束29的压力不落到大气压力以下。流束29典型地可以用作燃料气体。
流束29的一部分或全部（流束30）任选地可以被压缩以便返回成一个低压压缩机L中的再循环气体，从而作为流束31离开。这个流束在冷却器M中被冷却，来自该冷却器的出口流束（流束32）汇入流束21中以形成流束22，该流束接着进入再循环压缩机N的吸入端，而不是在不使用这种选择的情况下的只有流束21单独进入。另一个选择是在一个适宜的点处从压缩机N中抽出再循环气体（流束33）以典型地用作气体涡轮机燃料。可能适宜的是使用流束29或流束33作为汽提气体来将预处理阶段A中的吸附剂在其最终作为燃料燃烧之前进行再生。
图2示出了本发明的一个优选实施例，其中膨胀器E和F具有在3巴（0.3Mpa）与20巴（2Mpa）之间、优选在5巴（0.5Mpa）与15巴（1.5Mpa）之间的基本上相同的出口压力。来自膨胀器F的出口流束（流束11）接着与流束19合并而形成流束19a，该流束代替图1中的流束19进入热交换器D中。热交换器B和D则具有仅三个通道，从而简化了热交换器的构造和该设备的运行。
虽然在大多数应用中预期的是流束2和3将具有接近于环境温度的温度，但冷却到此水平以下可能是有利的。可行的是通过一个机械制冷循环或通过一个吸收制冷系统（典型地使用溴化锂（LiBr））来冷却这些流束、以及任选地来自压缩机中冷器和后冷器的出口流束，该系统可以接收来自一个气体涡轮机、气体发动机或组合的循环或任何其他适当方式的排气作为其热供应。

Claims (8)

1.一种用于将天然气或其他富含甲烷的气体液化的方法，包括：
-通过一个热交换器和一个第一气体膨胀器将给送天然气冷却至-50℃至-80℃的温度，该热交换器接收该给送天然气并且具有高于该膨胀器的出口温度的一个出口温度；
-将该膨胀器出口流束在所述热交换器的一个第一冷通道中再加热至刚好低于通到所述热交换器的该给送天然气的入口温度、进行压缩和再循环；
-使来自所述热交换器的该冷出口流束的一部分或全部进入一个第二膨胀器中而使其在该第二膨胀器中部分地液化；
-将所述第二膨胀器的出口流束分离成为蒸气部分和液体部分；
-收集该液体部分以作为LNG产品来使用，
-将该蒸气部分在所述热交换器的一个第二冷侧通道中再加热至刚好低于通到所述热交换器的该给送天然气的入口温度；
-将所述经再加热的蒸气部分在压缩之后以一部分再循环到所述第一膨胀器而以一部分再循环到所述热交换器。
2.如权利要求1所述的方法，其中，该热交换器接收全部的给送天然气。
3.如权利要求1所述的方法，其中，该热交换器接收大部分的、至少30%的给送天然气。
4.如以上任一项权利要求所述的方法，其中，给送天然气被冷却至-60℃至-70℃的温度。
5.如以上任一项权利要求所述的方法，其中，所述第一和第二气体膨胀器具有在3巴（0.3Mpa）与20巴（2Mpa）之间、优选5巴（0.5Mpa）与15巴（1.5Mpa）之间的相同出口压力，并且来自这两个膨胀器的这些出口流束在最终的再加热、压缩和再循环之前被合并。
6.如以上任一项权利要求所述的方法，其中，该给送流束和/或压缩机排出流束和/或再循环流束的任何一部分或全部典型地通过使用吸收制冷循环如溴化锂（LiBr）而被冷却。
7.如以上任一项权利要求所述的方法，其中，一个吸收制冷系统所要求的热是通过气体发动机或气体涡轮机废热来提供的，该气体发动机或气体涡轮机例如是可以用于向该方法的压缩机提供功率的气体发动机或涡轮机。
8.如以上任一项权利要求所述的方法，其中，给送流束和/或再循环流束的此种冷却与从该给送气体中去除二氧化碳和/或杂质相组合。
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