CN102504901A - 天然气液化方法 - Google Patents

天然气液化方法 Download PDF

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CN102504901A
CN102504901A CN2011103427039A CN201110342703A CN102504901A CN 102504901 A CN102504901 A CN 102504901A CN 2011103427039 A CN2011103427039 A CN 2011103427039A CN 201110342703 A CN201110342703 A CN 201110342703A CN 102504901 A CN102504901 A CN 102504901A
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薛鲁
江楚标
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SUZHOU XINGLU AIR SEPARATION PLANT SCIENCE AND TECHNOLOGY DEVELOPMENT Co Ltd
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    • 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
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    • 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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
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    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
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Abstract

本发明涉及一种天然气液化方法，将天然气通过换热器来冷却并液化，换热器由制冷工质循环提供冷量，制冷工质经循环压缩机后进入增压透平膨胀机的增压端，冷却后进入换热器中降温，返流制冷工质再经换热器与天然气换热，出换热器的返流制冷工质进入循环压缩机，制冷工质循环包括设置于换热器的热段与中段之间的低温冷冻机换热单元，其包括低温冷冻机、在低温冷冻机中进行循环的制冷剂，低温冷冻机中设置有制冷剂的冷凝器和蒸发器；出换热器的热段的制冷工质进入低温冷冻机中并被制冷剂预冷，再进入换热器的中段。这种天然气液化流程，不仅单位产品的能耗降低，还使制冷循环工质的压缩机厂房不需要采用防爆建筑，从而降低了投资，提高了性价比。

Description

天然气液化方法
技术领域
本发明涉及一种天然气的液化方法，具体地说，涉及一种氮膨胀循环天然气液化流程。
背景技术
现有技术中，中小型天然气液化装置常采用混合冷剂（MRC）流程，氮-甲烷（N2-CH4）流程，氮循环膨胀流程等多种制冷液化流程。氮膨胀流程具有设备简单、防爆要求低、运行操作可靠方便等优点，但液化天然气产品单位能耗偏高，影响了其竞争能力。
发明内容
本发明的目的是提供一种克服氮膨胀流程的缺点，降低液化天然气产品的单位能耗，使其性价比能优于其他流程的天然气液化方法。
为达到上述目的，本发明采用的技术方案是：
一种天然气液化方法，将经净化达到要求的天然气依次通过换热器的热段、中段、冷段来使所述的天然气冷却、液化并过冷，所述的换热器的热段、中段、冷段中由制冷工质循环的制冷提供所述的天然气液化所需的冷量，所述的制冷工质经循环压缩机后进入增压透平膨胀机的增压端增压，再经冷却后依次进入所述的换热器的热段、中段、冷段中降温，出所述的冷段的制冷工质成为返流制冷工质并依次经过所述的换热器的冷段、中段、热段与所述的天然气换热，出所述的热段的返流制冷工质进入所述的循环压缩机完成所述的制冷工质循环，所述的制冷工质循环包括设置于所述的换热器的热段与中段之间的低温冷冻机换热单元，所述的低温冷冻机换热单元包括低温冷冻机、在所述的低温冷冻机中进行循环的制冷剂，所述的低温冷冻机中设置有制冷剂的冷凝器和蒸发器；出所述的换热器的热段的所述的制冷工质进入所述的低温冷冻机中并被所述的制冷剂预冷到规定温度，再进入所述的换热器的中段。
优选的，出所述的循环压缩机的所述的制冷工质经冷却后进入所述的增压透平膨胀机的增压端。
优选的，所述的增压透平膨胀机的增压端包括相串联的第一增压端、第二增压端，出所述的第一增压端（或所述的第二增压端）的所述的制冷工质经冷却后进入所述的第二增压端（或所述的第一增压端），出所述的第二增压端（或所述的第一增压端）的所述的制冷工质经冷却后进入所述的换热器的热段。
优选的，出所述的换热器的中段的所述的制冷工质进入第一增压透平膨胀机的膨胀端降压降温，再进入所述的换热器的冷段。
优选的，出所述的换热器的冷段的所述的制冷工质进入第二增压透平膨胀机的膨胀端降压降温，成为所述的返流制冷工质进入所述的换热器的冷段。
优选的，所述的制冷工质为纯氮气或污氮气。
优选的，所述的循环压缩机的出口压力为1.5-3.9MPa，进口压力为0.15-0.7MPa。
优选的，所述的制冷剂为氟利昂或氨或国家法规允许使用的制冷剂。
优选的，出所述的换热器的冷段的经液化、过冷的天然气经过节流阀节流降压到规定压力后成为液化天然气产品。
由于上述技术方案运用，本发明与现有技术相比具有下列优点：由于本发明采用了低温冷冻机换热单元，既保留了原氮膨胀制冷流程的优点，又降低了液化天然气产品的能耗，提高了性价比。
附图说明
附图1为本发明的天然气液化方法的流程示意图。
以上附图中：1、循环压缩机；2、第一水冷却器；3、第一增压端；4、第二水冷却器；5、第二增压透平膨胀机的膨胀端；6、第一增压透平膨胀机的膨胀端；7、第二增压端；8、第三水冷却器；9、换热器是热段；10、低温冷冻机；11、换热器的中段；12、换热器是冷段；13、节流阀；
101、循环压缩机进气；102、出循环压缩机的制冷工质；103、正流循环的制冷工质；104、出低温冷冻机的制冷工质；105、出第一增压透平膨胀机的膨胀端的制冷工质；106、出第二增压透平膨胀机的膨胀端的返流制冷工质；
201、经净化达到要求的天然气；202、液化过冷后的天然气；203、液化天然气产品。
具体实施方式
下面结合附图所示的实施例对本发明作进一步描述。
实施例一：参见附图1所示。
一种天然气液化方法，将具有压力要求并经净化达到液化要求的天然气201依次通过换热器的热段9、中段11、冷段12来使天然气201冷却、液化并过冷，出换热器的冷段12的液化、过冷后的天然气202经过节流阀13节流降压到规定压力后成为液化天然气产品203。
换热器的热段9、中段11、冷段12中由制冷工质循环中的制冷工质提供天然气201液化所需的冷量。制冷工质为纯氮气或污氮气。
制冷工质经循环压缩机1压缩到规定压力，出循环压缩机的制冷工质102经过第一水冷却器2冷却后进入增压透平膨胀机的增压端增压，循环压缩机1的出口压力为1.5-3.9MPa。增压透平膨胀机的增压端包括相串联的第一增压端3、第二增压端7。出第一增压端3的制冷工质经第二水冷却器4冷却后进入第二增压端7，出第二增压端7的制冷工质经第三水冷却器8冷却后成为正流循环的制冷工质103并进入换热器的热段9中降温。
制冷工质循环包括设置于换热器的热段9与中段11之间的低温冷冻机换热单元，低温冷冻机换热单元包括低温冷冻机10、在低温冷冻机10中进行循环的制冷剂，低温冷冻机10中设置有换热用的制冷剂的冷凝器和蒸发器。出换热器的热段9的制冷工质进入低温冷冻机10中并被制冷剂预冷到规定温度，成为出低温冷冻机的制冷工质104，再进入换热器的中段11降温。制冷剂为氟利昂或氨或国家法规允许使用的制冷剂。
出换热器的中段11的制冷工质进入第一增压透平膨胀机的膨胀端6降压降温，出第一增压透平膨胀机的膨胀端6的制冷工质105再进入换热器的冷段12降温。出换热器的冷段12的制冷工质进入第二增压透平膨胀机的膨胀端5降压降温，成为返流制冷工质106。返流制冷工质106依次经过换热器的冷段12、中段11、热段9复热升温并为正流循环的制冷工质103为天然气201提供冷源。
出热段9的返流制冷工质成为循环压缩机进气101，其进入循环压缩机1完成制冷工质循环，循环压缩机1的进口压力为0.15-0.7MPa。
增压透平膨胀机的增压端与膨胀端可视方便和效率任意组合，例如可以由第一增压端3和第一增压透平膨胀机的膨胀端6组合为一台高温增压透平膨胀机，由第二增压端7和第二增压透平膨胀机的膨胀端5组合为一台低温增压透平膨胀机；也可由第一增压端3和第二增压透平膨胀机的膨胀端5组合为一台低温增压透平膨胀机，由第二增压端7和第一增压透平膨胀机的膨胀端6组合为一台高温增压透平膨胀机。在本实施例中，采用后一种方式。
采用增压透平膨胀机对制冷工质引进串联增压和膨胀，由于每台增压透平膨胀机的压缩比和膨胀比都明显减小，因而可以得到更高的效率，也更加安全可靠。
增压透平膨胀机需要有一定压力的密封气，该密封气可以根据需要从第二水冷却器4或第三水冷却器8后抽取，再从其他气源向循环压缩机2中补充进相同压力、相同气量的制冷工质即可。
低温冷冻机10与增压透平膨胀机是同时运行的。循环压缩机1和第一水冷却器2可安装在非防爆建筑内，冷箱***属于防爆区域，需满足国家标准所规定的各种防爆要求。
上述技术方案的应用，可保留原氮膨胀液化流程的优点，克服氮膨胀液化流程天然气单位产品能耗偏高的缺点，使其具有更好的性价比，在一定的装置规模范围内完全可以与混合冷剂流程、氮-甲烷流程进行竞争。
上述实施例只为说明本发明的技术构思及特点，其目的在于让熟悉此项技术的人士能够了解本发明的内容并据以实施，并不能以此限制本发明的保护范围。凡根据本发明精神实质所作的等效变化或修饰，都应涵盖在本发明的保护范围之内。

Claims (9)

1.一种天然气液化方法，将经净化达到要求的天然气依次通过换热器的热段、中段、冷段来使所述的天然气冷却、液化并过冷，所述的换热器的热段、中段、冷段中由制冷工质循环的制冷提供所述的天然气液化所需的冷量，所述的制冷工质经循环压缩机后进入增压透平膨胀机的增压端增压，再经冷却后依次进入所述的换热器的热段、中段、冷段中降温，出所述的冷段的制冷工质成为返流制冷工质并依次经过所述的换热器的冷段、中段、热段与所述的天然气换热，出所述的热段的返流制冷工质进入所述的循环压缩机完成所述的制冷工质循环，其特征在于：所述的制冷工质循环包括设置于所述的换热器的热段与中段之间的低温冷冻机换热单元，所述的低温冷冻机换热单元包括低温冷冻机、在所述的低温冷冻机中进行循环的制冷剂，所述的低温冷冻机中设置有制冷剂的冷凝器和蒸发器；出所述的换热器的热段的所述的制冷工质进入所述的低温冷冻机中并被所述的制冷剂预冷到规定温度，再进入所述的换热器的中段。
2.根据权利要求1所述的天然气液化方法，其特征在于：出所述的循环压缩机的所述的制冷工质经冷却后进入所述的增压透平膨胀机的增压端。
3.根据权利要求1所述的天然气液化方法，其特征在于：所述的增压透平膨胀机的增压端包括相串联的第一增压端、第二增压端，出所述的第一增压端（或所述的第二增压端）的所述的制冷工质经冷却后进入所述的第二增压端（或所述的第一增压端），出所述的第二增压端（或所述的第一增压端）的所述的制冷工质经冷却后进入所述的换热器的热段。
4.根据权利要求1所述的天然气液化方法，其特征在于：出所述的换热器的中段的所述的制冷工质进入第一增压透平膨胀机的膨胀端降压降温，再进入所述的换热器的冷段。
5.根据权利要求1所述的天然气液化方法，其特征在于：出所述的换热器的冷段的所述的制冷工质进入第二增压透平膨胀机的膨胀端降压降温，成为所述的返流制冷工质进入所述的换热器的冷段。
6.根据权利要求1所述的天然气液化方法，其特征在于：所述的制冷工质为纯氮气或污氮气。
7.根据权利要求1所述的天然气液化方法，其特征在于：所述的循环压缩机的出口压力为1.5-3.9MPa，进口压力为0.15-0.7MPa。
8.根据权利要求1所述的天然气液化方法，其特征在于：所述的制冷剂为氟利昂或氨或国家法规允许使用的制冷剂。
9.根据权利要求1所述的天然气液化方法，其特征在于：出所述的换热器的冷段的经液化、过冷的天然气经过节流阀节流降压到规定压力后成为液化天然气产品。
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