CN201532077U - 基于低温液体制冷的天然气液化装置 - Google Patents

基于低温液体制冷的天然气液化装置 Download PDF

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CN201532077U
CN201532077U CN2009202680841U CN200920268084U CN201532077U CN 201532077 U CN201532077 U CN 201532077U CN 2009202680841 U CN2009202680841 U CN 2009202680841U CN 200920268084 U CN200920268084 U CN 200920268084U CN 201532077 U CN201532077 U CN 201532077U
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natural gas
subcooler
heat exchanger
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舒水明
孙川
丁国忠
胡兴华
张晓青
江蓉
黄罡
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Huazhong University of Science and Technology
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Abstract

本实用新型提供了一种基于低温液体制冷的天然气液化装置，主要包括主换热器、天然气节流制冷单元和低温液体制冷单元，创新之处在于在低温液体制冷单元中使用低温液体气化潜热和显热作为冷源冷却、液化及过冷天然气，降低或消除液化天然气的汽化率，减少了对灌装设备及操作的技术要求，可实现大制冷量和制冷与液化远距离分离的天然气液化循环。

Description

基于低温液体制冷的天然气液化装置
技术领域
本实用新型涉及气体液化领域，特别是涉及一种天然气液化装置。
背景技术
以甲烷为主的天然气液化后的体积只有原来的1/625左右，对天然气进行液化是大量贮存和远距离输送的一种经济而有效的方法。目前天然气液化循环主要有三种类型：复叠式制冷循环(或称“阶式”循环)、混合制冷剂液化循环和带膨胀机的液化循环。以上方法均有广泛应用，技术较成熟。但其中压缩机等关键动力设备的制造水平限制了液化天然气(liquefied natural gas，LNG)生产规模，且造成系统设计、运行和维护的难度加大。
实用新型内容
本实用新型提出了基于低温液体制冷的天然气液化装置，采用低温液体作为冷源液化天然气，克服了LNG产量增加时对关键动力设备的制造限制，可实现大制冷量和远距离的天然气液化循环。
基于低温液体制冷的天然气液化装置，包括主换热器1和与其相连接的重烃分离器2，其特征在于，所述主换热器1还连接第一过冷器3，第一过冷器3依次连接节流阀4、第一过冷器3、天然气贮槽5、液化天然气泵6和第二过冷器7，从第二过冷器7输出的液化天然气传送给空分设备9；第一过冷器3与第二过冷器7相连接，第一过冷器3和第二过冷器7均与低温液体泵13相连接，低温液体泵13连接低温液体收集站；低温液体收集站中的低温液体由空分设备9提供。
本实用新型的技术效果体现在：本实用新型利用了空分产业生产的液氮以及其它可收集的集中或分散的低温液体的冷能，充分利用了能源；因为低温液体的温度比LNG温度低，使LNG过冷，这样可以降低或消除LNG的汽化率和对灌装设备及操作技术的要求；该方法涉及到的LNG冷能利用系统主要应用LNG的冷能，该冷能可梯级利用，能实现制取和收集低温液体，大幅度节能。
附图说明
图1是本实用新型一种具体实施方式结构示意图；
图2是本实用新型另一种具体实施方式结构示意图。
具体实施方式
下面结合附图和具体实施方式对本实用新型作进一步的详细说明。
如图1所示，本实用新型包括主换热器1、低温液体制冷单元、天然气节流制冷单元。
主换热器1是天然气液化的关键场所，其型式首选板翅式换热器，也可是绕管式换热器或其它换热器，可以是一个或多个串、并联的板翅式换热器，或者一个或多个串、并联的板翅式换热器与绕管式换热器的组合。
所用低温液体指制造成本低，制取工艺成熟的液氮(也可是液空、液氧或液氩，利用液氧或液氩冷量，适用于氧气或氩气用量大的场合)等低温液体，其制取可通过LNG冷能利用系统实现，或收集零散的低温液体，可通过管道、车、船等工具运送这些液体。
以液氮为例，低温液体制冷单元构成为：空分设备9的出口端接第一液氮收集站10的进口端，第一液氮收集站10的出口端通过管道或车船运输方式连接第二液氮收集站12的进口端。第二液氮收集站12位于天然气液化场地，第一液氮收集站10位于低温液体生产场地，两场地可相距很远。第二液氮收集站12的出口端连接液氮泵13的进口端，液氮泵13出口端再分别连接过冷器3和7的液氮进口端，过冷器3的液氮出口端接入主换热器1，主换热器1中对应的出口气体则排空。运行过程为：液氮从空分设备9输出，进入第一液氮收集站10，然后通过管道或车船运输方式传送给第二液氮收集站12以储存。在液氮泵13的作用下，液氮收集站12内的液氮被压入第一过冷器3和第二过冷器7中，与经过过冷器3，7的LNG进行换热，使LNG过冷。然后，液氮出过冷器3和7，汇合后进入主换热器1中，释放冷量。出主换热器1的氮气已升温气化，排空(或被他它用)。
LNG单元为天然气首先进入主换热器1，主换热器1的LNG通道在特定位置开口，抽出LNG。LNG在重烃分离器2中进行重烃分离，并返回主换热器1，出主换热器1后，LNG进入过冷器3过冷，出过冷器的LNG经过天然气节流制冷单元即节流阀4进行节流。节流后LNG的温度降低，重新送回过冷器3释放冷量，出过冷器的LNG经过LNG贮槽5，放出闪蒸气，然后通过液化天然气泵6升压，在过冷器7被液氮进一步冷却，再送入LNG与液氮两用船8，最后，LNG被运输到空分设备9，其冷能在空分装置中得到利用，并升温气化，输送给天然气用户使用。
流程中冷量来自液氮的气化潜热和显热，以及LNG节流冷量，通过调节液氮冷量可改变装置产量。LNG冷能可充分利用，如用于生产低温液氮等。该系统实现冷量循环分级利用，可大幅度节能。
流程中主换热器和其它换热器内液氮等低温液体(LTL)与原料天然气是进行逆流换热的。
流程中LNG过冷器可充分利用液氮等冷源的低温冷量，并且过冷LNG灌装时可降低或消除LNG的汽化率和对灌装设备及操作技术的要求。
作为本实用新型优化的另一实施方式如图2所示，在图1的基础上增设了混合工质制冷单元。混合工质制冷单元构成为：压缩机14通过管路依次连接冷却器16、主换热器1、截流阀17(或19/21)、主换热器1、气流缓冲罐18(或20/22)和接压缩机14构成回路。三个制冷循环回路(回路14-16-17-18、回路14-16-19-20、回路14-16-20-22)中的制冷剂均为混合工质。运行过程为：各制冷循环回路中气流缓冲罐中的气体制冷剂进入压缩机14，在压缩机驱动15的作用下，压缩机对气体制冷剂进行压缩，压缩得到的高压制冷剂进入冷却器16预冷，然后进入主换热器1冷凝转变为液体制冷剂，液体制冷剂输出经过节流阀17/19/21后，温度降低，接着再返回进入主换热器1释放冷量，释放后蒸发为气体回到气流缓冲罐18/20/22。因为空分设备的液体产品如液氮具有温度低、冷量大的特性，因此本实用新型提出使用低温液体为天然气液化提供冷量，在满足液化效果的条件下，减小了对混合工质制冷循环的负荷要求，采用小容积的压缩机即可。
图2中的液化天然气冷量一部分来自于混合工质节流冷量。混合工质制冷单元的混合工质组分可以根据产量及现场需求进行配比。当低温液体(LTL)供给充足或LNG产量减小时可以调节或停止运行混合工质(MR)制冷系统或减少低温液氮的制冷量。按LNG产量要求，混合工质制冷系统和液氮制冷系统可组合对天然气供冷，也可各自独立对天然气供冷；混合工质制冷系统和液氮制冷系统可对天然气等量供冷，也可按比例供冷，还可以分置多个液氮制冷系统液化天然气。
混合工质制冷量和低温液体制冷量可同时在相应换热器中与天然气换热，也可各自独立与天然气换热。
主换热器内混合工质与原料天然气是进行逆流换热的。

Claims (2)

1.基于低温液体制冷的天然气液化装置，包括主换热器(1)和与其相连接的重烃分离器(2)，其特征在于，所述主换热器(1)还连接第一过冷器(3)，第一过冷器(3)依次连接节流阀(4)、第一过冷器(3)、天然气贮槽(5)、液化天然气泵(6)和第二过冷器(7)，从第二过冷器(7)输出的液化天然气传送给空分设备(9)；第一过冷器(3)与第二过冷器(7)相连接，第一过冷器(3)和第二过冷器(7)均与低温液体泵(13)相连接，低温液体泵(13)连接低温液体收集站；低温液体收集站中的低温液体由空分设备(9)提供。
2.根据权利要求1所述的天然气液化装置，其特征在于，所述主换热器(1)还连接混合工质制冷单元。
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CN101709912B (zh) * 2009-11-17 2011-05-18 华中科技大学 基于低温液体制冷的天然气液化装置
CN105102913A (zh) * 2013-11-07 2015-11-25 俄罗斯天然气工业公开股份公司 天然气液化方法和装置
CN110418929A (zh) * 2017-03-16 2019-11-05 诺瓦泰克公共股份公司 用于天然气液化的设备和方法
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CN113446872A (zh) * 2021-06-23 2021-09-28 中国科学院广州能源研究所 一种高压低温液体气化升温过程冷能回收装置
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CN101709912B (zh) * 2009-11-17 2011-05-18 华中科技大学 基于低温液体制冷的天然气液化装置
CN105102913A (zh) * 2013-11-07 2015-11-25 俄罗斯天然气工业公开股份公司 天然气液化方法和装置
CN105102913B (zh) * 2013-11-07 2017-04-05 俄罗斯天然气工业公开股份公司 天然气液化方法和装置
CN110418929A (zh) * 2017-03-16 2019-11-05 诺瓦泰克公共股份公司 用于天然气液化的设备和方法
CN110418929B (zh) * 2017-03-16 2021-11-23 诺瓦泰克公共股份公司 用于天然气液化的设备和方法
US11566840B2 (en) 2017-03-16 2023-01-31 Publichnoe Aktsionernoe Obshchestvo “NOVATEK” Arctic cascade method for natural gas liquefaction in a high-pressure cycle with pre-cooling by ethane and sub-cooling by nitrogen, and a plant for its implementation
US11774173B2 (en) 2017-03-16 2023-10-03 Publichnoe Aktsionernoe Obshchestvo “NOVATEK” Arctic cascade method for natural gas liquefaction in a high-pressure cycle with pre-cooling by ethane and sub-cooling by nitrogen, and a plant for its implementation
WO2020242782A1 (en) * 2019-05-24 2020-12-03 Praxair Technology, Inc. Dual mode liquefied natural gas (lng) liquefier
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DE102020006396A1 (de) 2020-10-17 2022-04-21 Linde Gmbh Verfahren und Anlage zur Erzeugung eines verflüssigten Kohlenwasserstoffprodukts
CN113446872A (zh) * 2021-06-23 2021-09-28 中国科学院广州能源研究所 一种高压低温液体气化升温过程冷能回收装置

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