CN210220390U - 一种适用于超大规模的三循环天然气液化装置 - Google Patents

一种适用于超大规模的三循环天然气液化装置 Download PDF

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CN210220390U
CN210220390U CN201920872645.2U CN201920872645U CN210220390U CN 210220390 U CN210220390 U CN 210220390U CN 201920872645 U CN201920872645 U CN 201920872645U CN 210220390 U CN210220390 U CN 210220390U
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propane
cmr
heat exchanger
wmr
natural gas
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Liming Pu
蒲黎明
Zhiming Jiang
蒋志明
Chenghua Guo
郭成华
Chunlai Zheng
郑春来
Jiahong Liu
刘家洪
Ke Wang
王科
Yunqiang Chen
陈运强
Yingke Li
李莹珂
Yi Wang
王毅
Xiaoyong Tang
汤晓勇
Yong Huang
黄勇
Jing Tian
田静
Gui Wang
汪贵
Xuan Zhou
周璇
Gang Wang
王刚
Long Li
李龙
Dingshan Xie
谢顶衫
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China National Petroleum Corp
China Petroleum Engineering and Construction Corp
China Petroleum Engineering Co Ltd
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Abstract

本实用新型公开了一种适用于超大规模的三循环天然气液化装置，装置包括天然气液化管路、丙烷预冷循环系统、WMR制冷循环系统和CMR制冷循环系统。与现有技术相比，本实用新型的积极效果是：本实用新型以三循环为基础，分担每级制冷负荷，天然气依次通过1个板翅式换热器和2个绕管式换热器进行冷却，直至液化过冷，工艺设备数量少，天然气液化装置规模能够达到单列600～800万吨/年；液化过程所需的冷量由丙烷、WMR混合冷剂、CMR混合冷剂三个系统提供，系统调节手段丰富，能够为天然气液化过程提供匹配的冷量，操作灵活和对原料适应性好。

Description

一种适用于超大规模的三循环天然气液化装置
技术领域
本实用新型涉及天然气液化深冷技术领域，具体为一种适用于超大规模的三循环天然气液化装置，通过采用三级制冷循环，分配预冷段、液化段和过冷段的负荷，采用高效设备，简化流程，满足单列产能600～800万吨/年超大规模天然气液化装置建设需求。
背景技术
随着LNG技术装备的不断发展，国际上LNG工厂建设总体趋势是向着大型化发展，单列生产能力多在300～550万吨/年规模，最大规模已达780万吨/年。国际上大规模LNG装置建设采用的液化工艺技术主要有APCI公司的C3MR、DMR和AP-X工艺，康菲公司的Optimized Cascade工艺，Linde公司的MFC工艺和Shell公司的DMR工艺。大规模的LNG装置能够降低单位LNG生产成本，实现规模效益。
国内LNG装置单列最大规模为120万吨/年，采用多级单组分制冷液化工艺(MSC工艺)。基于MSC工艺实现了单列350万吨/年天然气液化工艺包开发，但该工艺无法满足单列600～800万吨/年超大规模的LNG装置建设。
因此，开发一种能适用于600～800万吨/年超大规模天然气液化装置的天然气液化工艺非常必要。
发明内容
为了克服现有技术的缺点，本实用新型提供了一种适用于超大规模的三循环天然气液化装置，具有流程简洁、能耗低的优点。
本实用新型所采用的技术方案是：一种适用于超大规模的三循环天然气液化装置，包括天然气液化管路、丙烷预冷循环系统、WMR制冷循环系统和CMR制冷循环系统，其中：
所述天然气液化管路由丙烷换热器、WMR换热器、CMR换热器、LNG膨胀机、LNG闪蒸罐和LNG增压泵依次连接组成；
所述丙烷预冷循环系统包括丙烷换热器、丙烷压缩机、丙烷压缩机出口冷却器、高压丙烷气液分离罐、中压丙烷气液分液罐和低压丙烷气液分离罐，用于对天然气、WMR冷剂和CMR冷剂进行预冷；
所述WMR制冷循环系统包括WMR换热器、WMR压缩机入口缓冲罐、WMR压缩机、WMR压缩机出口冷却器和WMR膨胀机，用于对天然气、CMR冷剂进一步冷却和部分液化；
所述CMR制冷循环系统包括CMR换热器、CMR压缩机入口缓冲罐、CMR压缩机、CMR压缩机出口冷却器和CMR膨胀机，用于为天然气和CMR冷剂全部液化和过冷提供冷量。
与现有技术相比，本实用新型的积极效果是：
本实用新型以三循环为基础，分担每级制冷负荷，天然气依次经过1个板翅式换热器和2个绕管式换热器进行冷却，直至液化过冷，工艺设备数量少，天然气液化装置规模能够达到单列600～800万吨/年；液化过程所需的冷量由丙烷、WMR混合冷剂、CMR混合冷剂三个系统提供，系统调节手段丰富，能够为天然气液化过程提供匹配的冷量，操作灵活和对原料适应性好。与现有技术相比，具有如下特点：
1、本实用新型是在多级单组分液化工艺(MSC工艺)工程应用实践基础上进行的创新和改进，工艺技术具有延续性，与MSC工艺相比，具有如下优点：
1)MSC工艺中采用丙烯预冷+乙烯冷却+混合冷剂液化过冷(混合冷剂以甲烷、氮气为主)。本实用新型中预冷循环采用丙烷，冷却循环采用混合冷剂，以乙烷为主，包括甲烷和丙烷；液化过冷循环冷剂采用混合冷剂，包括氮气、甲烷、乙烷。
2)冷却段、液化过冷段均采用混合冷剂，可结合驱动设备可选机型调节各制冷循环负荷，灵活地调节天然气冷却、液化和过冷温度，操作适应性更好。
3)MSC工艺中丙烯和乙烯制冷系统采用管壳式换热器或CIK换热器进行换热，甲烷制冷循环采用板翅式换热器；本实用新型中丙烷预冷段换热设备采用高效的板翅式换热器，换热系统集成度高，具有工艺流程简化、占地少等优势；本实用新型中WMR和CMR主低温换热器采用绕管式换热器，绕管式换热器具有单台换热面积大的特点，有利于实现天然气液化装置大型化。
2、双混合冷剂液化工艺(DMR工艺)采用2级混合冷剂制冷循环实现天然气预冷、液化和过冷，与DMR工艺相比，本实用新型采用三循环制冷分担各级液化负荷，实现单列600～800万吨/年超大规模天然气液化装置建设。
3、MFC工艺是一种三循环制冷循环工艺，其预冷段、液化段、过冷段均采用混合冷剂制冷；与MFC相比本实用新型预冷段为纯丙烷冷剂。
4、AP-X也是一种三循环制冷循环工艺，其预冷段采用丙烷制冷、液化段采用混合冷剂制冷、过冷段采用氮膨胀制冷；与AP-X工艺比较，本实用新型过冷段采用混合冷剂制冷。
5、本实用新型WMR节流、CMR节流和高压LNG节流均采用液体透平膨胀机，液体透平膨胀机为等熵膨胀，与常规节流阀等焓膨胀相比，膨胀效率高，LNG产品产量可提高1～3％，单位LNG产品能耗降低1～3％。
附图说明
本实用新型将通过例子并参照附图的方式说明，其中：
图1是本实用新型的工艺流程图。
具体实施方式
一种适用于超大规模的三循环天然气液化装置，如图1所示，包括：丙烷预冷板翅式换热器1、WMR绕管式换热器2、CMR绕管式换热器3、LNG液力透平膨胀机4、LNG闪蒸罐5、LNG增压泵6、丙烷压缩机7、丙烷压缩机出口冷却器8、第一高压丙烷节流阀9、第二高压丙烷节流阀10、高压丙烷气液分离罐11、第一中压丙烷节流阀12、第二中压丙烷节流阀13、中压丙烷气液分液罐14、低压丙烷节流阀15、低压丙烷气液分液罐16、WMR压缩机入口缓冲罐17、WMR压缩机18、WMR压缩机出口冷却器19、WMR液力透平膨胀机20、CMR压缩机入口缓冲罐21、CMR压缩机22、CMR压缩机出口冷却器23、CMR液力透平膨胀机24，其中：
丙烷预冷板翅式换热器1、WMR绕管式换热器2、CMR绕管式换热器3、LNG液力透平膨胀机4、LNG闪蒸罐5、LNG增压泵6依次相连。
丙烷压缩机7、丙烷压缩机出口冷却器8、第一高压丙烷节流阀9、丙烷预冷板翅式换热器1、丙烷压缩机7高压吸入口依次相连；
丙烷压缩机出口冷却器8、第二高压丙烷节流阀10、高压丙烷气液分离罐11、第一中压丙烷节流阀12、丙烷预冷板翅式换热器1、丙烷压缩机7中压吸入口依次相连；
高压丙烷气液分离罐11、第二中压丙烷节流阀13、中压丙烷气液分离罐14、低压丙烷节流阀15、丙烷预冷板翅式换热器1、低压丙烷气液分离罐16、丙烷压缩机7低压吸入口依次相连；
高压丙烷气液分离罐11出口气相与丙烷压缩机7高压吸入管线相连；中压丙烷气液分离罐14气相出口与丙烷压缩机7中压吸入管线相连。
WMR压缩机入口缓冲罐17、WMR压缩机18、WMR压缩机出口冷却器19、丙烷预冷板翅式换热器1、WMR绕管式换热器2、WMR液力透平膨胀机20依次相连。
CMR压缩机入口缓冲罐21、CMR压缩机22、CMR压缩机出口冷却器23、丙烷预冷板翅式换热器1、WMR绕管式换热器2、CMR绕管式换热器3、CMR液力透平膨胀机24依次相连。
本实用新型在进行天然气液化时，包括如下内容：
1)丙烷预冷系统对天然气、WMR和CMR进行预冷至-30℃～-39℃：
从丙烷压缩机7增压至1.5MPa.a～2.5MPa.a的丙烷经丙烷冷却器8冷却至20℃～50℃，分成2股，其中一股液相丙烷(约15％～25％)通过第一高压丙烷节流阀9节流，压力降至0.3MPa.a～0.6MPa.a后进入丙烷预冷板翅式换热器1，对天然气、WMR冷剂和CMR冷剂进行冷却(20℃～0℃)，从板翅式换热器1出来的气相丙烷回到丙烷压缩机7高压吸入口；另一股液相丙烷(75％～85％)通过第二高压丙烷节流阀10节流，压力降至0.3MPa.a～0.6MPa.a后进入高压丙烷气液分离罐11进行气液分离，罐顶气相丙烷回到丙烷压缩机7高压吸入口；
高压丙烷气液分离罐11的液相分成2股，其中一股液相丙烷(45％～55％)通过第一中压丙烷节流阀12节流，压力降至0.2MPa.a～0.35MPa.a后进入丙烷预冷板翅式换热器1，对天然气、WMR冷剂和CMR冷剂进行冷却(-10℃～-20℃)，从板翅式换热器出来的气相丙烷回到丙烷压缩机7中压吸入口；另一股液相丙烷(45％～55％)通过第二中压丙烷节流阀13节流，压力降至0.2MPa.a～0.35MPa.a后进入中压丙烷气液分离罐14进行气液分离，罐顶气相丙烷回到丙烷压缩机7中压吸入口；
中压丙烷气液分离罐14的液相通过节流阀15节流，压力降至0.1MPa.a～0.2MPa.a后进入丙烷预冷板翅式换热器1，对天然气、WMR冷剂和CMR冷剂进行冷却(-30℃～-39℃)，从丙烷预冷板翅式换热器1出来的气相丙烷经过低压丙烷气液分离罐16后回到丙烷压缩机7低压吸入口；
低压丙烷、中压丙烷、高压丙烷经丙烷压缩机7增压后进行循环。
2)WMR制冷系统将天然气、CMR冷剂冷却至-65℃～-95℃：
从WMR绕管式换热器2底部出来的WMR冷剂进入WMR压缩机入口缓冲罐17，经WMR压缩机18增压至3MPa.a～5MPa.a后经WMR冷却器19冷却至20℃～50℃，进入丙烷预冷板翅式换热器1冷却到-30℃～-39℃并液化；液态WMR进入WMR绕管式换热器2进一步冷却至-65℃～-95℃从顶部出来，经WMR液力膨胀机20膨胀至0.2MPa.a～0.5MPa.a后(-70℃～-100℃)再进入WMR绕管式换热器2，对天然气、WMR冷剂和CMR冷剂进行冷却(-65℃～-95℃)；从WMR绕管式换热器2底部出来的低压WMR(0.2MPa.a～0.5MPa.a,-35℃～-45℃)回到WMR压缩机入口缓冲罐17后进行循环。
3)CMR制冷系统为天然气和CMR冷剂全部液化和过冷提供冷量：
作为CMR制冷系统制冷剂的CMR冷剂经CMR压缩机22增压至5MPa.a～8MPa.a后经CMR压缩机出口冷却器23冷却至20℃～50℃，经丙烷预冷板翅式换热器1冷却到-30℃～-39℃，经WMR绕管式换热器2冷却至-65℃～-95℃，在CMR绕管式换热器3中冷却到-155℃～-160℃后从顶部出来，再经CMR液力膨胀机24膨胀至0.2MPa.a～0.5MPa.a后再进入CMR绕管式换热器3，为天然气和自身液化过冷提供冷量；从CMR绕管式换热器3底部出来的低压CMR(0.2MPa.a～0.5MPa.a,-75℃～-95℃)回到CMR压缩机入口缓冲罐21后进行循环。
4)高压LNG膨胀闪蒸
从CMR绕管式换热器3顶部出来的天然气已液化并过冷至-155℃～-160℃，过冷后的天然气经LNG液力透平膨胀机4膨胀至(120kPa.a，-160℃～-163℃)后进入LNG闪蒸罐5中闪蒸，闪蒸出的BOG送至下游BOG增压装置，LNG闪蒸罐5罐底LNG经LNG增压泵输6增压后送至LNG存储单元。
所述混合冷剂WMR以乙烷为主，并配一定量的甲烷和丙烷，其中甲烷体积含量为5％～15％、乙烷为70％～85％，丙烷为10％～20％；混合冷剂CMR组成为氮气、甲烷、乙烷，其中氮气体积含量为10％～25％、乙烷为40％～65％，丙烷为30％～45％。
本实用新型的工作原理是：
本实用新型提供的基于高效设备的三循环液化系统可适用于单列年产能达600～800万吨/年超大规模天然气液化装置，其采用三级制冷循环，预冷段采用丙烷冷剂、液化和过冷段采用混合冷剂；预冷循环、液化和过冷循环分别采用一套压缩、冷却、冷凝、透平膨胀和换热过程。
本实用新型中WMR、CMR和LNG节流膨胀选用液力透平膨胀机，其原理为等熵膨胀，制冷效率更高；采用液力透平膨胀机来回收能量，用于发电，从而降低综合能耗。
本实用新型具有如下效果：1)可根据项目建设地环境和原料气条件的变化，合理配置混合冷剂的组成和配比，从而优化冷却和液化温度，使得整个工艺系统的能耗最低，地区适应性广；2)三级制冷循环，采用高效的板翅式换热器和绕管式换热器，换热效率高，可合理分担各级制冷负荷，实现单线LNG装置大型化。3)WMR冷剂、CMR冷剂节流采用液力透平膨胀机，制冷效率高，单位LNG产品能耗更低；4)高压LNG节流采用液力透平膨胀机，节流效应好，天然气液化率更高。

Claims (6)

1.一种适用于超大规模的三循环天然气液化装置，其特征在于：包括天然气液化管路、丙烷预冷循环系统、WMR制冷循环系统和CMR制冷循环系统，其中：
所述天然气液化管路由丙烷换热器、WMR换热器、CMR换热器、LNG膨胀机、LNG闪蒸罐和LNG增压泵依次连接组成；
所述丙烷预冷循环系统包括丙烷换热器、丙烷压缩机、丙烷压缩机出口冷却器、高压丙烷气液分离罐、中压丙烷气液分液罐和低压丙烷气液分离罐，用于对天然气、WMR冷剂和CMR冷剂进行预冷；
所述WMR制冷循环系统包括WMR换热器、WMR压缩机入口缓冲罐、WMR压缩机、WMR压缩机出口冷却器和WMR膨胀机，用于对天然气、CMR冷剂进一步冷却和部分液化；
所述CMR制冷循环系统包括CMR换热器、CMR压缩机入口缓冲罐、CMR压缩机、CMR压缩机出口冷却器和CMR膨胀机，用于为天然气和CMR冷剂全部液化和过冷提供冷量。
2.根据权利要求1所述的一种适用于超大规模的三循环天然气液化装置，其特征在于：所述丙烷预冷循环系统中，丙烷压缩机、丙烷压缩机出口冷却器、第一高压丙烷节流阀、丙烷换热器和丙烷压缩机高压吸入口依次相连；丙烷压缩机出口冷却器、第二高压丙烷节流阀、高压丙烷气液分离罐、第一中压丙烷节流阀、丙烷换热器、丙烷压缩机中压吸入口依次相连；高压丙烷气液分离罐、第二中压丙烷节流阀、中压丙烷气液分离罐、低压丙烷节流阀、丙烷换热器、低压丙烷气液分离罐、丙烷压缩机低压吸入口依次相连；高压丙烷气液分离罐出口气相与丙烷压缩机高压吸入管线相连；中压丙烷气液分离罐气相出口与丙烷压缩机中压吸入管线相连。
3.根据权利要求1所述的一种适用于超大规模的三循环天然气液化装置，其特征在于：所述WMR制冷循环系统中，WMR换热器、WMR压缩机入口缓冲罐、WMR压缩机、WMR压缩机出口冷却器、丙烷换热器、WMR换热器、WMR膨胀机、WMR换热器依次相连。
4.根据权利要求1所述的一种适用于超大规模的三循环天然气液化装置，其特征在于：所述CMR制冷循环系统中，CMR换热器、CMR压缩机入口缓冲罐、CMR压缩机、CMR压缩机出口冷却器、丙烷换热器、WMR换热器、CMR换热器、CMR膨胀机、CMR换热器依次相连。
5.根据权利要求1至4中任一所述的一种适用于超大规模的三循环天然气液化装置，其特征在于：所述LNG膨胀机、WMR膨胀机和CMR膨胀机均为液力透平膨胀机。
6.根据权利要求5所述的一种适用于超大规模的三循环天然气液化装置，其特征在于：所述丙烷换热器为板翅式换热器，所述WMR换热器和CMR换热器均为绕管式换热器。
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110186251A (zh) * 2019-06-11 2019-08-30 中国石油工程建设有限公司 一种适用于超大规模的三循环天然气液化装置及方法
CN114963689A (zh) * 2022-06-22 2022-08-30 中海石油气电集团有限责任公司 一种双循环混合冷剂天然气液化系统

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110186251A (zh) * 2019-06-11 2019-08-30 中国石油工程建设有限公司 一种适用于超大规模的三循环天然气液化装置及方法
CN110186251B (zh) * 2019-06-11 2024-01-26 中国石油集团工程股份有限公司 一种适用于超大规模的三循环天然气液化装置及方法
CN114963689A (zh) * 2022-06-22 2022-08-30 中海石油气电集团有限责任公司 一种双循环混合冷剂天然气液化系统

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