CN110418929A - 用于天然气液化的设备和方法 - Google Patents

用于天然气液化的设备和方法 Download PDF

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CN110418929A
CN110418929A CN201780088426.9A CN201780088426A CN110418929A CN 110418929 A CN110418929 A CN 110418929A CN 201780088426 A CN201780088426 A CN 201780088426A CN 110418929 A CN110418929 A CN 110418929A
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nitrogen
ethane
natural gas
gas
compressor
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CN110418929B (zh
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R·M·米尼古罗夫
S·V·鲁登科
O·E·瓦辛
D·N·格里茨辛
E·I·索伯列夫
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Novatek PAO
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Abstract

本发明涉及液化天然气的技术。一种液化天然气的方法，其中，通过乙烷蒸发将经处理的天然气预冷却，利用冷却氮作为制冷剂对液化气体进行过冷，将液化气体的压力降低，将非液化的气体分离，排出液化天然气。此外，在预冷却之前，将天然气压缩，在液化气体的多级预冷却过程中蒸发乙烷，同时使用冷却的乙烷作为制冷剂来蒸发乙烷。在蒸发过程中产生的乙烷被压缩、冷凝并在液化气体和氮气的冷却过程中用作制冷剂，其中氮气被压缩、冷却、膨胀并进料到天然气的过冷阶段。本发明简化了液化天然气的工艺流程。

Description

用于天然气液化的设备和方法
技术领域
本发明涉及天然气液化技术，用于其进一步通过河流或海洋运输并随后再气化。
背景技术
有许多方法可以液化天然气，主要是基于外部制冷剂的热量去除，其中C3MR、Philips Cascade、Shell DMR和Linde MFCP液化技术用于北极气候。
C3MR技术在亚马尔液化天然气(LNG)项目Sabetta的亚马尔半岛的NOVATEK,JSC工厂中采用。
最初，C3MR工艺(GB 1291467A，04.10.1972)由Air Products为文莱的LNG工厂开发。该技术基于天然气冷却顺序：首先，在三个热交换器中使用独立的基于丙烷的蒸气压缩循环，然后在双区多段热交换器中使用基于制冷剂混合物的循环，其也可以在两个热交换器中使用丙烷循环进行预冷却。
C3MR工艺的使用率超过生产线(process train)总数的80％。
北极气候下该工艺的一个缺点是环境寒冷的不完整使用。如果在赤道气候下，丙烷回路中的气体和混合制冷剂(MR)的热量去除在+45℃至-34℃的温度范围内实现，而在北极气候下，此范围可能从+10℃开始。结果，主压缩机功率用于压缩第二回路的混合制冷剂。压缩机容量与气体驱动器的大小有关。对于每年容量为500万吨液化天然气(LNG)的生产线，使用86兆瓦的驱动器。只有通过增加主低温热交换器的重量和尺寸，才能最大限度地利用这种动力，并将其消耗平衡转向MR。
Conoco Phillips在几家LNG工厂(阿拉斯加州、特立尼达和多巴哥等)使用Phillips Cascade技术。
该技术基于丙烷、乙烯和甲烷在三个回路中连续冷却气体。丙烷冷凝在空气冷却器中进行，而乙烯通过丙烷蒸气冷凝，甲烷通过乙烯蒸气冷凝。
经过水分和二氧化碳预净化的天然气在41巴的压力下进料到热交换器，并在冷却和节流后供给到罐。每个回路提供制冷剂的三倍膨胀，其中返回流进料到热交换器下游的多级离心压缩机的相应级。压缩机丙烷级的喷射压力为15.2巴，节流以5.5、3.15和1.37巴的压力进行。在乙烯级，压力从20.5降至5.5、2.05和1.72巴，在最后一回路，压力从37.2巴的压力下降到14.8、5.8和2.05巴的压力。
所述技术的缺点是液化气体的低压(41巴)，这增加了液化工艺的特定能量消耗，大量设备，需要第三方乙烯制冷剂供应，制冷剂流控制的复杂方案包括3个三级压缩机，9个防喘振电路。
壳牌(Shell)在萨哈林LNG工厂实施了Shell DMR技术(US6390910A，21.05.2002)。
DMR工艺使用2种混合制冷剂。气体在两个回路中液化，在每个回路中，气体由不同组成的混合制冷剂冷却。每个回路使用多线程线圈热交换器。在第一回路中，气体由制冷剂蒸气冷却，制冷剂蒸气预先冷凝在热交换器管侧，并且第二回路的冷却剂也被冷却。在第二热交换器中，气体在2级管道中进行过冷(sub-cooling)，第二回路制冷剂的蒸气在管束中冷凝。
该工艺与寒冷气候最匹配。该工艺的缺点是MR的2个回路的复杂控制方案。实际上，根据一年中的时间，从一种MR组合转换到另一种MR组合的结果难以预测，并且在萨哈林LNG工厂每年应用不超过2～3次。
林德(Linde)MFCP技术(US6253574A，07/03/2001)由挪威国家石油公司(Statoil)用于挪威哈默菲斯特(Hammerfest)工厂的天然气液化。
MFCP液化工艺基于三个回路中的顺序气体冷却，并使用三种不同组成的混合制冷剂。第一回路使用两个连续的板式热交换器，其在两种压力水平下运行。第一回路制冷剂是丙烷-乙烷。丙烷-乙烷混合物蒸气通过海水冷凝，在第一回路的板式热交换器中冷却，并将寒冷分散到第二回路的液化气体和制冷剂。
第二回路设计成使用丙烷-乙烷-甲烷混合物作为制冷剂在线圈热交换器中液化天然气。在第三回路中，液化气体用氮-甲烷-乙烷蒸气进行过冷。与第二回路一样，线圈绕制的热交换器用于过冷。所有三个回路都使用海水进行初步气体冷却。
由于使用三种类型的混合制冷剂，以及大量类型的热交换和压缩机设备，该方法的缺点是复杂的控制方案。
OAO Gazprom获得了天然气液化方法的专利，该方法包括在经预处理和干燥的天然气的预冷器中冷却和冷凝，该天然气进一步与送至分馏的液体乙烷馏分分离，同时来自第一分离器的气流依次在液化剂热交换器中使用混合制冷剂冷却，在过冷热交换器中通过气态氮进行过冷，同时在液体膨胀机中降低经过冷LNG的压力，并将经过冷LNG送去分离，之后将液化气体输送到LNG储罐，同时将分离的气体排放到燃料气体系统。天然气液化设备包括预冷器，五个分离器，两个节流器，液化剂-交换器，三个用于压缩混合制冷剂的压缩机，五个空气冷却器，两个泵，液体膨胀机，过冷热交换器，包括膨胀机和压缩机的透平(turbo)膨胀机单元，两个氮循环压缩机(RU 2538192 C1，发布于10.01.2017)。
RU 2538192 C1的方法和设备的缺点是预冷却回路的复杂控制。在每个压缩阶段下游存在液相导致在任何参数如空气温度、制冷剂压缩比、生产率的降低/增加的变化的情况下难以预测主要气体冷却回路的功能变化。
与所提出的方法最接近的用于天然气液化的技术和设备是OAO Gazprom专利RU2538192 C1的天然气体液化技术和设备。
发明内容
所提出的天然气液化技术解决的技术问题是简化工艺过程，改变液化过程参数下的操作稳定性和减少设备的资本支出。
该技术问题通过天然气的液化方法解决，该方法包括通过乙烷分离来对经处理的天然气预冷却，使用冷却氮作为制冷剂对液化气体进行过冷，将液化气体的压力降低，将非液化的气体分离并将液化天然气(LNG)移除。该方法的特点是在预冷却之前将天然气压缩，在液化气体的多级预冷却期间分离乙烷，同时使用冷却的乙烷作为制冷剂来蒸发乙烷，而通过蒸发产生的乙烷被压缩、冷凝并在液化气体和氮气冷却过程中用作制冷剂，氮气被压缩、冷却、膨胀并进料到天然气的过冷阶段。
此外，乙烷在串联连接的蒸发器中蒸发，氮气通过交替进料到蒸发器和氮-氮热交换器来冷却，而来自经压缩气体热交换器的氮气返回流被用作氮-氮热交换器中的制冷剂。
此外，天然气在单相状态下在高压下冷却，从而防止相变过程。
此外，对于天然气的预冷却，使用来自北极、南极或近地流域的环境空气或水。
此外，天然气过冷却过程使用单相临界状态的液化气体以及气态氮。
此外，每个冷却设备是使用环境空气或水的空气或水冷却器。
天然气的液化设备也解决了该技术问题，该设备包括天然气液化管线、乙烷回路和氮气回路；天然气液化管线包括串联连接的天然气压缩机、空气冷却器、乙烷蒸发器、封闭式过冷热交换器和分离器；乙烷回路包括串联连接的至少一个乙烷压缩机、空气冷却器、所述乙烷蒸发器，所述乙烷蒸发器的出口连接到至少一个压缩机的入口；氮气回路包括串联连接的至少一个氮气压缩机、空气冷却器、所述乙烷蒸发器、连接在所述乙烷蒸发器之间的氮-氮热交换器、透平膨胀机、所述封闭式过冷热交换器、所述氮-氮热交换器和连接到氮气压缩机入口的透平压缩机。
此外，用于非液化蒸发气(BOG)的分离器出口与封闭式过冷热交换器连接，该封闭式过冷热交换器的BOG出口连接到BOG压缩机。
此外，透平膨胀机和透平压缩机组合成膨胀机-压缩机单元。
此外，所有压缩机的驱动器是连接到倍增器的燃气涡轮发动机，所述倍增器连接到每个压缩机。
使用所提出的方法和设备时获得的技术结果如下。
与OAO Gazprom技术相比，所提出的“北极瀑布”(Arctic Cascade)技术在第一液化回路中使用纯乙烷制冷剂代替混合制冷剂(MR)。该解决方案大大简化了液化工艺，允许使用简单的蒸发器代替复杂的用于混合制冷剂的多线程热交换器，扩大了能够制造必要设备的工厂清单。
使用乙烷代替MR进行预冷却有助于降低制冷剂分馏单元的资金成本，减少存储仓库的尺寸，从而从方案中排除用于MR制备的纯制冷剂混合单元。
采用更简单的工艺方案，“北极瀑布”(Arctic Cascade)技术与RU 2538192 C1的液化工艺的能耗相似，环境空气温度为+5℃，每吨LNP约为240kW。
“北极瀑布”(Arctic Cascade)技术为一条生产线实现单一驱动，通过倍增器分配其功率，而RU 2538192 C1专利技术应用两个驱动器，这增加了成本和设备数量。
附图说明
图1所示为所提出的设备的示意图，解释了所提出的天然气液化方法。
具体实施方式
天然气液化管线包括串联连接的天然气压缩机2、空气冷却器5、乙烷蒸发器7、封闭式过冷热交换器9(例如多线程)以及分离器10。
乙烷回路包括串联连接的至少一个乙烷压缩机4(图1中示出两个串联连接的压缩机4)、空气冷却器13和所述蒸发器7，其出口连接到至少一个压缩机4的入口。如图所示，第一蒸发器7的出口连接到第二压缩机4的入口，而剩余蒸发器7的出口梯次连接到第一压缩机4。
氮气回路包括至少一个氮气压缩机3(图1中示出两个串联连接的压缩机3)、空气冷却器14、所述乙烷蒸发器7(其间连接有氮-氮热交换器8)、膨胀机-压缩机单元10的透平膨胀机、所述封闭式过冷热交换器9、所述氮-氮热交换器8和膨胀机-压缩机单元10的透平压缩机，其连接到第一氮气压缩机3的入口。
分离器11的BOG出口与封闭式过冷热交换器9连接，该封闭式过冷热交换器9的BOG出口连接到BOG压缩机15。
此外，所有压缩机2、3、4的驱动器是连接到倍增器6的燃气涡轮发动机1，该倍增器6将动力分配到每个压缩机2、3、4。
天然气的液化方法如下。
将用于液化的经预处理的天然气(NG)(除去水、二氧化碳和其他污染物的蒸气)进料到天然气压缩机2，压缩至所需压力，由空气或水冷却器单元5中的冷环境来冷却至约+10℃的温度，然后送至乙烷蒸发器7进行预冷却。在蒸发器7中顺序冷却后，将温度为约-84℃的气体进料到封闭式气体过冷热交换器9，在该处用氮气和BOG将其过冷至约-137℃的温度。然后在节流器处将气体压力降低到约0.15MPag，同时其温度降至约-157℃，之后，气液流进入到末端分离器11。通过泵12将LNG从分离器11供应到储罐，同时将气体的非液化部分输送到末端热交换器9，将寒冷分散到液化气流，并被BOG压缩机13压缩至约3.0MPag的压力。部分蒸发气被输送到单元燃料系统，而另一部分则再循环到液化工艺的开始处。
预冷却回路使用乙烷作为制冷剂。来自具有不同压力的蒸发器7的气态乙烷进入到多级压缩机4(压缩机)，在该处它被压缩到约3MPag的压力，并在+10℃或更低的温度下在空气冷却器13中冷凝。将液体乙烷送至蒸发器7，其中氮气以各种压力水平将气体冷却至约-84℃的温度。来自蒸发器7的气态乙烷进料到压缩机4(压缩机)并进一步循环。
由压缩机3压缩至约10MPa的氮气在空气冷却器14中冷却，交替地进入乙烷蒸发器7和氮-氮热交换器8，并且通过氮气返回流在乙烷蒸发器7冷却至约-84℃的温度，进入透平膨胀机，其中氮气增压透平压缩机在膨胀机-压缩机单元10中作为负载。在将膨胀机压力降至2.6MPa并冷却至-140℃后，氮气进入封闭式多线程过冷热交换器9。在将寒冷分散给液化气流之后，氮气通过同流换热式氮-氮热交换器8，进入膨胀机-压缩机单元10的透平压缩机，被压缩到约3MPag的压力，进入压缩机3的入口，另外压缩至10MPag并送至循环。
该工艺在标称模式下在+5℃及更低的环境温度下运行。在温度高于+5℃时，生产线的性能开始下降。由于该技术是针对北极和南极纬度而开发的，北极或南极海域、海湾和其他水体的水即使在夏季也是低温，因此也可在炎热的夏季用于单元13中的乙烷冷凝。
为了优化运动回路并减少周转设备的数量，用于气体、乙烷和氮气压缩的所有压缩机2、3、4可以由单个燃气涡轮发动机1驱动，通过倍增器6将动力分配给每个压缩机。
通过使用“北极瀑布”(Arctic Cascade)技术，LNG生产的估算能耗为约每吨220kW。
权利要求书(按照条约第19条的修改)
1.一种天然气的液化方法，包括通过乙烷蒸发来对经处理的天然气预冷却，使用冷却氮作为制冷剂对液化气体进行过冷，将液化气体的压力降低，将非液化的气体分离并分流液化天然气，其中在预冷却之前将天然气压缩，在液化气体的多级预冷却期间蒸发乙烷，同时使用冷却的乙烷作为制冷剂来蒸发乙烷，而通过蒸发产生的乙烷被压缩、冷凝并在液化气体和氮气的冷却过程中用作制冷剂，氮气被压缩、冷却、膨胀并进料到天然气的过冷阶段。
2.根据权利要求1所述的方法，其中乙烷在串联连接的蒸发器中蒸发，氮气通过交替进料到蒸发器和氮-氮热交换器来冷却，而来自经压缩气体热交换器的氮气返回流被用作氮-氮热交换器中的制冷剂。
3.根据权利要求1所述的方法，其中该天然气在单相状态下在高压下冷却，从而防止相变过程。
4.根据权利要求1所述的方法，其中对于天然气的预冷却，使用来自北极、南极或近地流域的环境空气或水。
5.根据权利要求1所述的方法，其中该天然气的过冷却过程使用处于单相临界状态的液化气体以及气态氮。
6.一种天然气的液化设备，包括天然气液化管线、乙烷回路和氮气回路；天然气液化管线包括串联连接的天然气压缩机、空气冷却器、乙烷蒸发器、封闭式过冷热交换器和分离器；乙烷回路包括串联连接的至少一个乙烷压缩机、空气冷却器、所述乙烷蒸发器，所述乙烷蒸发器的出口连接到至少一个压缩机的入口；氮气回路包括串联连接的至少一个氮气压缩机、空气冷却器、所述乙烷蒸发器、连接在所述乙烷蒸发器之间的氮-氮热交换器、透平膨胀机、所述封闭式过冷热交换器、所述氮-氮热交换器和连接到氮气压缩机入口的透平压缩机。
7.根据权利要求6所述的设备，其中用于非液化蒸发气(BOG)的分离器出口与所述封闭式过冷热交换器连接，所述封闭式过冷热交换器的BOG出口连接到BOG压缩机。
8.根据权利要求6所述的设备，其中所述透平膨胀机和所述透平压缩机组合成膨胀机-压缩机单元。
9.根据权利要求6所述的设备，其中所有压缩机的驱动器是连接到倍增器的燃气涡轮发动机，所述倍增器连接到每个压缩机。
10.根据权利要求6所述的设备，其中每个冷却设备是使用环境空气或水的空气或水冷却器。
说明或声明(按照条约第19条的修改)
将权利要求1第13页第3行和第13页第8行“分离”改为“蒸发”。其他无改变。
修改依据购见PCT申请第10页第16～18行的记载；
“然后送至乙烷蒸发器7进行预冷却。在蒸发器7中顺序冷却后”该修改更准确地表证了乙烷的操作。
申请人还要求对摘要进行相应修改。

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1.一种天然气的液化方法，包括通过乙烷分离来对经处理的天然气预冷却，使用冷却氮作为制冷剂对液化气体进行过冷，将液化气体的压力降低，将非液化的气体分离并分流液化天然气，其中在预冷却之前将天然气压缩，在液化气体的多级预冷却期间分离乙烷，同时使用冷却的乙烷作为制冷剂来蒸发乙烷，而通过蒸发产生的乙烷被压缩、冷凝并在液化气体和氮气的冷却过程中用作制冷剂，氮气被压缩、冷却、膨胀并进料到天然气的过冷阶段。
2.根据权利要求1所述的方法，其中乙烷在串联连接的蒸发器中蒸发，氮气通过交替进料到蒸发器和氮-氮热交换器来冷却，而来自经压缩气体热交换器的氮气返回流被用作氮-氮热交换器中的制冷剂。
3.根据权利要求1所述的方法，其中该天然气在单相状态下在高压下冷却，从而防止相变过程。
4.根据权利要求1所述的方法，其中对于天然气的预冷却，使用来自北极、南极或近地流域的环境空气或水。
5.根据权利要求1所述的方法，其中该天然气的过冷却过程使用处于单相临界状态的液化气体以及气态氮。
6.一种天然气的液化设备，包括天然气液化管线、乙烷回路和氮气回路；天然气液化管线包括串联连接的天然气压缩机、空气冷却器、乙烷蒸发器、封闭式过冷热交换器和分离器；乙烷回路包括串联连接的至少一个乙烷压缩机、空气冷却器、所述乙烷蒸发器，所述乙烷蒸发器的出口连接到至少一个压缩机的入口；氮气回路包括串联连接的至少一个氮气压缩机、空气冷却器、所述乙烷蒸发器、连接在所述乙烷蒸发器之间的氮-氮热交换器、透平膨胀机、所述封闭式过冷热交换器、所述氮-氮热交换器和连接到氮气压缩机入口的透平压缩机。
7.根据权利要求6所述的设备，其中用于非液化蒸发气(BOG)的分离器出口与所述封闭式过冷热交换器连接，所述封闭式过冷热交换器的BOG出口连接到BOG压缩机。
8.根据权利要求6所述的设备，其中所述透平膨胀机和所述透平压缩机组合成膨胀机-压缩机单元。
9.根据权利要求6所述的设备，其中所有压缩机的驱动器是连接到倍增器的燃气涡轮发动机，所述倍增器连接到每个压缩机。
10.根据权利要求6所述的设备，其中每个冷却设备是使用环境空气或水的空气或水冷却器。
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