CN102575897B - 液化富烃馏分的方法 - Google Patents

液化富烃馏分的方法 Download PDF

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CN102575897B
CN102575897B CN201080017277.5A CN201080017277A CN102575897B CN 102575897 B CN102575897 B CN 102575897B CN 201080017277 A CN201080017277 A CN 201080017277A CN 102575897 B CN102575897 B CN 102575897B
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H·鲍尔
H·弗兰克
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0095—Oxides of carbon, e.g. CO2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • F25J1/0215—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
    • F25J1/0216—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle using a C3 pre-cooling cycle

Abstract

描述了一种液化富烃馏分的方法。根据本发明，富烃馏分(1，2)在与制冷剂混合物回路(5-9)的制冷剂混合物相对的间接热交换中进行冷却(E6)和液化(E7)，富烃馏分(1，2)在与制冷剂混合物回路(5-9)的完全蒸发的制冷剂混合物相对的间接热交换中进行冷却(E6)，制冷剂混合物回路(5-9)的经压缩的制冷剂混合物借助于纯物质制冷回路(10-19)进行预先冷却，及选择制冷剂混合物的组成和/或制冷剂混合物回路(5-9)的压缩机最终压力，从而通过纯物质制冷回路(10-19)使制冷剂混合物完全液化。

Description

液化富烃馏分的方法
技术领域
本发明涉及液化富烃馏分的方法。
背景技术
US 3,763,658公开了一种液化富烃馏分的方法，该方法尤其是应用于天然气液化过程中。在此，制冷剂混合物回路用于天然气的液化和过冷，同时还额外设置有纯物质回路，其预先冷却待液化的天然气并且使制冷剂混合物回路的制冷剂混合物预先冷却和部分液化。此类液化方法尤其是适合于具有1至6百万吨/年的LNG产量的天然气液化过程。
待液化的天然气在真正的冷却和液化之前通常被送至水性胺洗装置，在其下游通常设置有干燥单元。尤其是在暖的气候带，可以将前述的纯物质回路的一个支流用于冷凝天然气中所含的水，由此减轻了设置在胺洗装置下游的干燥器的负担。
但是，该液化过程需要比较高的设备成本。因此取决于实施方案设置直至新的壶型纯物质蒸发器以及两个绕管式热交换器束。尤其是在更小的液化产量的情况下，在此其理解为少于3百万吨/年的LNG产量，前述的方法过程相对于不具有分离的预冷却回路的所谓的SMR(单级混合制冷剂Single Mixed Refrigerant)液化过程而言具有缺点，这是因为前述的液化过程造成更高的投资成本，即使通过其更低的能量消耗也无法得到补偿。
发明内容
本发明的目的是提供液化富烃馏分的方法，其避免了前述的缺点。
为了实现该目的，建议液化富烃馏分的方法，其中
a)富烃馏分在与制冷剂混合物回路的制冷剂混合物相对的间接热交换中进行冷却和液化，
b)富烃馏分在与制冷剂混合物回路的完全蒸发的制冷剂混合物相对的间接热交换中进行冷却，
c)制冷剂混合物回路的经压缩的制冷剂混合物借助于纯物质制冷回路进行预先冷却，及
d)选择制冷剂混合物的组成和/或制冷剂混合物回路的压缩机最终压力，从而通过纯物质制冷回路使制冷剂混合物完全液化。
术语“纯物质制冷回路”应理解为其中制冷剂浓度为至少95体积％的制冷回路。
与前述的液化方法不同，现在仅在与制冷剂混合物回路的制冷剂混合物相对的间接热交换中使富烃馏分冷却和液化。此外设置的纯物质制冷回路根据本发明仅用于使制冷剂混合物回路的经压缩的制冷剂混合物预先冷却。在此，选择制冷剂混合物的组成和/或制冷剂混合物回路的压缩机最终压力，从而可以使制冷剂混合物通过纯物质制冷回路进行冷却，直至其完全液化。
因此，可以将制冷剂混合物直接送至用于使富烃馏分液化和过冷的热交换器，无需在该热交换器上游设置分离塔。
但是，对于根据本发明的方法，基本上可以保留借助于纯物质制冷回路的预先冷却在能量消耗和对于减轻任选设置的干燥单元负担的适应性方面的优点。但是，与前述的液化方法相比，根据本发明的液化方法的设备成本明显更低，这是因为明显减少了热交换器的数量。
虽然根据本发明的方法导致能量消耗的小幅增加，增加量为最大5％，但是改善了液化过程的总体经济性，因此根据本发明的方法尤其是在0.5至3百万吨/年的LNG产量范围内比已知的液化过程更经济。
根据本发明液化富烃馏分的方法的其他有利的实施方案，作为从属权利要求的主题，其特征在于，
-纯物质制冷回路的制冷剂的至少95体积％由C3H8、C3H6、C2H6、C2H4或CO2组成，
-制冷剂混合物回路的制冷剂混合物包含氮、甲烷和至少两种选自C2H4、C2H6、C3H8、C4H10和C5H12的组分，及
-制冷剂混合物回路的制冷剂混合物在富烃馏分液化时完全蒸发。
具体实施方式
下面依据在附图中所示的实施例更详细地阐述根据本发明液化富烃馏分的方法及其作为从属权利要求主题的其他有利的实施方案。
将待液化的富烃馏分经过管道1送至胺洗装置A，该待液化的富烃馏分在下面应当是天然气流。在胺洗装置下游设置有干燥单元T，在干燥单元上游设置有热交换器E1。于其中使在天然气中所含的水部分冷凝，以减轻干燥单元T的负担。
将如此预处理的天然气流经过管道2送至热交换器E6，并在其中与制冷剂混合物回路的完全蒸发的制冷剂混合物相对地进行冷却，下面对此仍要进行探讨。热交换器E6优选被设计成板式热交换器。
将冷却的天然气流经过管道3送至优选被设计成绕管式热交换器的热交换器E7。于其中在与制冷剂混合物回路的制冷剂混合物的间接热交换中使天然气流液化和过冷。将过冷的LNG产品流经过管道4排出，并送至暂时储存或者直接送至其另外的应用。
将制冷剂混合物回路的制冷剂混合物在单级或多级压缩单元中压缩至所期望的压缩机最终压力；在附图中显示了两个压缩级V2和V2′，其中在压缩级之间优选设置一个未在图中示出的中间冷却器。在后期冷却器E9中冷却之后，将压缩的制冷剂混合物经过管道5引导通过四个彼此前后连接的热交换器E2至E5。于其中该制冷剂混合物在与纯物质制冷回路的制冷剂的间接热交换中进行冷却，下面对此仍要更详细地进行探讨，直至其在最后的热交换器E5的出口处呈液态并因此以单相存在。
为了在最后的热交换器E5的出口处实现制冷剂混合物回路的制冷剂混合物的完全冷凝，相应地选择制冷剂混合物的组成和/或制冷剂混合物回路的压缩机最终压力。
优选使用C3H8、C3H6、C2H6、C2H4或CO2作为纯物质制冷回路的制冷剂。该制冷剂混合物回路的制冷剂混合物优选包含氮、甲烷和至少两种选自C2H4、C2H6、C3H8、C4H10和C5H12的组分。
通过纯物质制冷回路液化的制冷剂混合物现在可以经过管道6直接送至热交换器E7。由此省略了位于热交换器E7上游的分离塔的设置。将液态制冷剂混合物在热交换器E7中进行过冷，然后将其经过管道7排出，并在阀门a中减压至最低压力。
作为在附图中所示的阀门a的替代，可以设置液体膨胀机，其用于在热交换器E7的冷端使制冷剂混合物进行做功膨胀(arbeitsleistendenEntspannung)。
经减压并经过管道7重新送至热交换器E7的制冷剂混合物在热交换器E7中用于使天然气流液化和过冷。有利地，该制冷剂混合物在天然气流液化和过冷时完全蒸发，从而经过管道8从热交换器E7排出完全蒸发的制冷剂混合物流，并送至热交换器E6。于其中将该制冷剂混合物与待冷却的天然气流相对地进行过热，然后将其经过管道9重新送至循环压缩单元V2/V2′的入口。
已述的纯物质制冷回路同样具有多级压缩单元V1，其被分配给液化器E8。将被压缩至所期望的最终压力的制冷剂经过管道10送至分支点，在此处将制冷剂的一个支流经过阀门b减压进入已述的热交换器E1中，并由此处经过管道11和13再次送至压缩单元V1。第二个支流经过管道12和阀门c减压进入热交换器E2中。
将制冷剂的气态部分经过管道13从热交换器E2排出并送至压缩单元V1的中间压力级，同时将该制冷剂的液态部分经过管道14从热交换器E2排出并经过阀门d减压进入热交换器E3中。重新分离成气态制冷剂部分，将其经过管道15送至压缩单元V1的中间压力级，同时将液态制冷剂部分经过管道16排出并经过阀门e减压进入热交换器E4中。由此处还将气态制冷剂部分经过管道17送至压缩单元V1的中间压力级，同时将液态制冷剂部分经过管道18排出并经过阀门f减压进入最后的热交换器E5中。将完全蒸发的制冷剂经过管道19送至压缩单元V1的最低压力级。
代替在附图中所示的制冷剂混合物在热交换器E2至E5中的冷却，在实践中还可以实现少于四个热交换器。热交换器的数量主要通过环境温度和涡轮压缩机V1中叶轮的数量来确定。
根据本发明液化富烃馏分的方法设立一种液化过程，其在减少的设备成本的情况下具有改善的总体经济性，这必须用能量消耗的小幅增加来换取。根据本发明的方法尤其是适合于0.5至3百万吨/年的LNG产量范围。

Claims (4)

1.液化富烃馏分的方法，其中
a)富烃馏分(1，2)在与制冷剂混合物回路(5–9)的制冷剂混合物相对的间接热交换中进行冷却(E6)和液化(E7)，
b)富烃馏分(1，2)在与制冷剂混合物回路(5–9)的完全蒸发的制冷剂混合物相对的间接热交换中进行冷却(E6)，
c)制冷剂混合物回路(5–9)的经压缩的制冷剂混合物借助于纯物质制冷回路(10–19)进行预先冷却，及
d)选择制冷剂混合物的组成和/或制冷剂混合物回路(5–9)的压缩机最终压力，从而通过纯物质制冷回路(10–19)使制冷剂混合物完全液化。
2.根据权利要求1的方法，其特征在于，纯物质制冷回路(10–19)的制冷剂的至少95体积％由C3H8、C3H6、C2H6、C2H4或CO2组成。
3.根据权利要求1或2的方法，其特征在于，制冷剂混合物回路(5–9)的制冷剂混合物包含氮、甲烷和至少两种选自C2H4、C2H6、C3H8、C4H10和C5H12的组分。
4.根据权利要求1或2的方法，其特征在于，制冷剂混合物回路(5–9)的制冷剂混合物在富烃馏分(3)液化(E7)时完全蒸发。
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