CN101033910B - 集成空气分离与液化天然气冷量回收系统 - Google Patents

集成空气分离与液化天然气冷量回收系统 Download PDF

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CN101033910B
CN101033910B CN2007100680607A CN200710068060A CN101033910B CN 101033910 B CN101033910 B CN 101033910B CN 2007100680607 A CN2007100680607 A CN 2007100680607A CN 200710068060 A CN200710068060 A CN 200710068060A CN 101033910 B CN101033910 B CN 101033910B
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nitrogen
liquid
heat exchanger
liquefied natural
natural gas
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CN101033910A (zh
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卢杰
毛绍融
朱朔元
何晖
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Hang Yang Group Co ltd
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Hangzhou Hangyang Co Ltd
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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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0234—Integration with a cryogenic air separation unit
    • 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
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—Nitrogen
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
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    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
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    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
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Abstract

一种集成空气分离和液化天然气冷量回收系统，它至少包括一主要由分馏塔组成的空气分离装置及至少包括一主要由液化天然气换热器组成的液化天然气冷量回收装置，所述的空气分离装置中还配置有主换热器、液氧换热器和液氮液空过冷器；从分馏塔的分馏上塔顶部引出的氮气经过液氮液空过冷器、主换热器的复热后，经压缩增压后至少进入液化天然气换热器进行预冷换热；所述的液化天然气冷量回收装置中还至少配置有汽液分离器和液氮过冷器，且被置于一独立的第二冷箱内；而主换热器、液氧换热器、液氮液空过冷器和由分馏下塔，分馏上塔和主冷凝蒸发器连接组成的分馏塔被置于一独立的第一冷箱内；它充分利用了液化天然气高品位的冷量，使空气分离装置的能耗显著降低，能保证空气分离装置的安全运行，能获得极大的社会和经济效益。

Description

集成空气分离与液化天然气冷量回收系统
技术领域
本发明涉及一种集成空气分离与液化天然气冷量回收的系统，特别适用于液氧、液氮和氩馏分的大量生产；这种系统利用液化天然气气化过程中释放出的冷量，在低温条件下将空气中氧、氮分离并且最终液化，可以大幅度地降低空气分离装置的能耗。
背景技术
空气是一种均匀的多组分混合气体，主要由氧、氮、氩组成，它们所占空气的容积百分比分别为20.95％，78.118％，0.932％。氧、氮、氩和其它物质一样，具有气、液、固三态。在常温常压下它们呈气态。在标准大气压下，氧被冷却到90.188K，氮被冷却到77.36K，氩被冷却到87.29K，它们都分别变成液态。如果遇热又可变成气态。氧和氮的沸点相差约13K，氩和氮的沸点相差约10K，这是低温分馏法将空气分离为氧、氮和氩的基础。通常，原料空气被冷却到液化温度后进行分馏塔过程，可以获得各种气态或液态的氧、氮、氩。氧、氮、氩产品在国防、科研、工业生产中都有着广泛的用途，但是，空气分离过程通常在80～100K低温条件下进行，创造和维持低温需要消耗大量的能耗，特别是在生产大量液氧、液氮和液氩时，能耗将急剧增加。例如，生产液氧、液氮或液氩的大型空气分离装置的单位耗电量达到1.0～1.25千瓦时/公斤液氧，日耗电达到33～41万千瓦时。因此，在能源日益紧缺的今天，随着各行业对液氧、液氮的需求日益增长，空气分离装置的节能降耗引起人们广泛的关注。
液化天然气(Liquefied Natural Gas，LNG)是一种十分洁净的燃料，主成分为甲烷、乙烷等。LNG蕴藏有巨大的高品质冷量，LNG在输送给天然气分配系统前，必须将其气化到环境温度并提高到高压，通常采用开架式气化器，用海水做热源对LNG加热气化，使得LNG的冷量没有被回收而大量浪费。例如，在8MPa压力下，LNG温度从-161℃升高到27℃时释放的冷量约为830kJ/kg。因此，合理回收和利用LNG冷量，也是天然气利用领域非常关注的问题。
通常，空气的液化温度为-173℃，低于液化天然气的温度-161℃，必须向空气分离装置内补充足够的冷量，才能使原料空气冷却达到其液化温度，以便进一步的空气分离。这种冷量可以由外界的低温液体或气体供给，也可以由装置本身通过节流膨胀、等熵膨胀制冷等方法获得。空气分离装置内部是一个氧气富集区，液化天然气富含甲烷等碳氢化合物，属于易燃、易炸的物质。因此，利用液化天然气冷量补充空气分离必要的的冷量外，首先应保证空气分离装置的安全运行，而现有利用液化天然气冷量的空气分离装置普遍存在安全隐患的问题。
美国专利US5,220,798A描述了一种利用液化天然气和液态惰性物质的气化共同补充冷量的空气分离装置。分馏塔内产生的氮气被压缩后，在换热器中与高压液化天然气换热，液化天然气将冷量传递给氮气，氮气被冷却并被液化，送入分馏塔内提供空气分离的冷量。
美国专利US5,137,558A描述了一种空气分离装置。来自分馏塔内氮气被压缩后，在换热器中与高压液化天然气换热而被预冷，节流后可以获得含有液氮的汽液混合物，液氮进入分馏塔内作为回流液体，提供空气分离的冷量。
与之类似，中国实用新型专利CN2,499,774Y描述了一种采用液化天然气的空气分离装置。来自分馏塔的低压氮气被压缩到高压，中间有中压压缩机串连，压缩前高压液化天然气在换热器中对氮气预冷，高压氮气节流产生含有液氮的汽液混合物，液氮进入分馏塔内部作为回流液体，提供空气分离的冷量，并生产液氧、液氮、液氩产品。
上面描述的空气分离方法和装置利用了液化天然气冷量，可以大幅度降低了空气分离的能耗。但应当指出，空气分离装置属于长期运行的设备，其对安全性要求十分高。利用液化天然气冷量的过程中，返流的液氮提供空气分离的冷量，而返流的液氮通常与高压的液化天然气在换热器中换热过，一旦高压的液化天然气泄漏，污染进分馏塔提供空气分离冷量的液氮，空气分离装置将会有爆炸危险。本发明利用液化天然气冷量，生产液氧、液氮和氩馏分，液氮直接作为产品排放出空气分离装置，不再进入分馏塔作为空气分离的冷源，彻底解决了空气分离过程的安全性问题。
发明内容
本发明的目的是针对目前利用液化天然气冷量的空气分离方法和装置存在的安全性问题，提供一种集成空气分离和液化天然气冷量回收系统，以低能耗获得液氧、液氮和氩馏分等产品。
本发明的目的是通过如下技术方案来完成的，它至少包括一主要由分馏塔组成的空气分离装置及至少包括一主要由液化天然气换热器组成的液化天然气冷量回收装置，所述的空气分离装置中还配置有主换热器、液氧换热器和液氮液空过冷器；从分馏塔的分馏上塔顶部引出的氮气经过液氮液空过冷器、主换热器的复热后，经压缩增压后至少进入液化天然气换热器进行预冷换热；所述的液化天然气冷量回收装置中还至少配置有汽液分离器和液氮过冷器，且被置于一独立的第二冷箱内；而主换热器、液氧换热器、液氮液空过冷器和由分馏下塔，分馏上塔和主冷凝蒸发器连接组成的分馏塔被置于一独立的第一冷箱内；其特征在于所述的由分馏上塔顶部引出氮气，经液氮液空过冷器复热后，进入主换热器的氮气换热通道复热，部分被引入独立的第二冷箱，与出液氮过冷器并经复热的循环氮气合并，作为氮气液化的原料氮气，随后进入低压氮透平压缩机中压缩，与来自汽液分离器的出汽液分离器的循环氮气汇合，进入中压氮透平压缩机中压缩，随后进入液化天然气换热器被进液化天然气换热器的液化天然气和所述出汽液分离器的循环氮气预冷，进液化天然气换热器的液化天然气在液化天然气换热器中被复热后引出独立的第二冷箱用于其它用途；离开液化天然气换热器的氮气一部分节流膨胀，产生含有液氮的湿蒸气，去汽液分离器；另一部分引出液化天然气换热器换热的循环氮气也节流膨胀，返回液化天然气换热器复热，去中压氮透平压缩机，完成氮气制冷循环。
由汽液分离器分离出的出汽液分离器的循环氮气返回液化天然气换热器复热，与所述另一部分返回液化天然气换热器复热的循环氮气合并去中压氮透平压缩机；由汽液分离器分离出的液氮经液氮过冷器过冷后，一部分节流膨胀后的循环氮气，依次返回液氮过冷器、液化天然气换热器复热，与独立的第一冷箱引出的氮气汇合去低压氮透平压缩机，完成一路氮气循环；一部分引出独立的第二冷箱，作为出液氮过冷器的液氮产品，并送往液氮贮槽；其余出液氮过冷器的液氮节流膨胀后返回独立的第一冷箱，依次在液氧换热器、主换热器中复热，去低压氮透平压缩机，完成另一路氮气循环。
中压氮透平压缩机的工作压力在2.5～5.0MPa范围内。
低压氮透平压缩机，中压氮透平压缩机，节流阀，液化天然气换热器的换热通道，以及主换热器的换热通道构成氮气制冷循环回路。
液化天然气的压力在4.0～9.5MPa范围内，进入液化天然气换热器的换热通道，复热后引出独立的第二冷箱。
本发明利用了带液化天然气预冷的氮气循环制冷提供了用于获得氧气，氮气，液氧，液氮，以及氩馏分的冷量，充分利用了液化天然气高品位的冷量，空气分离装置的能耗显著降低。本发明所提出的空气分离装置生产1kg液氧的电消耗为0.42～0.45kwh，而同等规模传统的空气分离装置生产1kg液氧的电消耗为1.0～1.25kwh，其单位耗电量是本发明所提出的空气分离装置单位耗电量的2.4～3倍；本发明利用空气分离出来的氮气作为冷量传递的冷媒，与液化天然气换热后不再进入分馏上塔，或者分馏下塔，保证空气分离装置的安全运行；因此本发明如能推广应用，必将获得极大的社会和经济效益。
附图说明
附图1是本发明的实施例1的示意图。
附图2是本发明的实施例2的示意图。
附图3是本发明的实施例3的示意图。
具体实施方式
图中序号名称：1-独立的第一冷箱，2-独立的第二冷箱，3-主换热器，4-分馏下塔，5-主冷凝蒸发器，6-分馏上塔，7-液空液氮过冷器，8-液氮节流阀，9-液空节流阀，10-液氧换热器，11-液氮过冷器，12-气液分离器，13，14-节流阀，15-液化天然气换热器，16-低压氮透平压缩机，17-中压氮透平压缩机，18-液氧贮槽，19-液氮贮槽，20-增压透平膨胀机，21-水冷却器。
相关物流编号：100-中压氮透平压缩机压缩，并经液化天然气换热器换热的氮气，101-中压氮透平压缩机压缩，引出液化天然气换热器换热的循环氮气，102-节流后，引入液化天然气换热器换热的循环氮气，103-出气液分离器的循环氮气，104-出液氮过冷器的液氮产品，105-出液氮过冷器引入冷箱I的液氮，106-出气液分离器，引入液氮过冷器复热的氮气，107-出液氮过冷器的循环氮气，108-出分馏上塔，经主换热器复热后的原料氮气，109-出分馏上塔，经主换热器复热后的污氮气，110-出液氧换热器，经主换热器复热后的循环氮气，111-进天然气换热器的液化天然气，112-出天然气换热器的液化天然气，113-进入主换热器的原料空气，114-从分馏上塔引出的氩馏分，115-从外界引入并送入分馏上塔的液氮，116-从分馏上塔引出的氧气。
以下结合附图对本发明作进一步的详细说明。
实施例1：如图1所示，去除二氧化碳、水、乙炔和其它碳氢化合物杂质的原料空气113被送入独立的第一冷箱1内的主换热器3的换热通道A1-A2，与其它换热通道的返流气体换热，冷却降温到合适分馏的温度后，送入分馏下塔4的底部。
主换热器3、分馏塔和液氧换热器10位于独立的第一冷箱1内部。分馏塔由分馏下塔4，分馏上塔6和主冷凝蒸发器5连接组成。冷却降温的原料空气进入分馏下塔4的底部，与从分馏下塔4顶部流下的回流液体在多层塔板上发生传热与传质过程。氧组分较高的富氧液体空气(简称液空)汇集于分馏下塔4的底部，氮气汇集于分馏下塔4的顶部，并被分馏下塔4与分馏上塔6之间的主冷凝蒸发器5的液氧所冷凝。
从分馏下塔4顶部引出液氮分成两部分，一部分返回分馏下塔4作为回流液体，另一部分在液氮液空过冷器7中过冷，经液氮节流阀8降压至分馏上塔6顶部的压力，并被送入分馏上塔6顶部，作为分馏上塔6的回流液体。
从分馏下塔4底部引出富氧液空，在液氮液空过冷器7中过冷，经液空节流阀9降压至分馏上塔6中部的压力，并被送入分馏上塔6的中部，也作为分馏上塔的回流液体。
上述两股回流液体成为分馏上塔6的回流液体，与从塔内上升气流在多层塔板上发生传热与传质过程，在分馏上塔6的底部获得液氧，顶部获得氮气。液氧在主冷凝蒸发器5中被分馏下塔4顶部的氮气加热成氧气，氧气成为分馏上塔6的主要上升气流，部分氧气被引出分馏上塔6进行下一步的液化，或者作为产品引出独立的第一冷箱1。
由分馏上塔顶部6引出氮气，经液氮液空过冷器7复热后，进入主换热器3的氮气换热通道M1-M2复热，部分被引入独立的第二冷箱2，与其它氮气一并送入低压氮透平压缩机16压缩。
由分馏上塔6上部引出污氮气，经液氮液空过冷器7复热后，进入主换热器3的污氮气换热通道B1-B2继续复热，之后引出独立的第一冷箱1。出独立的第一冷箱1的污氮气可以被电热器或蒸汽加热后，送到分子筛纯化器中作为再生气体，脱附分子筛吸附的水、二氧化碳，然后排放大气环境。
由分馏上塔6的中下部引出含氩量较高的氩馏分114，去制氩装置作为获得液氩或其它形式氩产品的原料。
从分馏上塔6顶部引出的氮气110经液氮液空过冷器7，主换热器3复热后，与来自汽液分离器12并经复热的氮气107合并，作为氮气液化的原料氮气，随后进入低压氮透平压缩机16中压缩，与来自汽液分离器12的循环氮气107汇合，进入中压氮透平压缩机17中压缩，随后进入液化天然气换热器15被液化天然气110和来自汽液分离器12的氮气预冷，液化天然气110在液化天然气换热器15中被复热后引出独立的第二冷箱2用于其它用途。离开液化天然气换热器15的氮气一部分节流膨胀，产生含有液氮的湿蒸气，去汽液分离器12；另一部分氮气101也节流膨胀，返回液化天然气换热器15复热，去中压氮透平压缩机17，完成氮气循环制冷。
中压氮透平压缩机17的工作压力可以在2.5～5.0MPa范围内。
由汽液分离器12分离出的氮气103返回液化天然气换热器15复热，与循环氮气102合并去中压氮透平压缩机。由汽液分离器12分离出的液氮经液氮过冷器11过冷后，一部分节流膨胀，依次返回液氮过冷器11、液化天然气换热器15复热，与独立的第一冷箱1引出的氮气汇合去低压氮透平压缩机16，完成氮气循环；一部分引出独立的第二冷箱2，作为液氮产品104，并送往液氮贮槽18；其余氮气105节流膨胀后返回独立的第一冷箱1，依次在液氧换热器10、主换热器3中复热，去低压氮透平压缩机16，完成氮气循环。氧气在液氧换热器10中被冷却液化，引出独立的第一冷箱1，作为液氧产品103，并送往液氧贮槽19。
液化天然气换热器15、汽液分离器12、液氮过冷器11位于独立的第二冷箱2内部。
低压氮透平压缩机16，中压氮透平压缩机17，节流阀14，液化天然气换热器15的换热通道D1-D2、E1-E2、F1-F2、G1-G2、H1-H2，以及主换热器3的换热通道C1-C2、M1-M2构成氮气制冷循环回路。
液化天然气111的压力可以在4.0～9.5MPa范围内，进入液化天然气换热器15的换热通道I1-I2，复热后以液态形式引出冷箱II2用于其它用途。
实施例2。利用液化天然气冷量分离空气的系统和装置如图2所示，本实施例2与实施例的区别在于：当液化天然气111由于突发事件导致供应不足时，可以向装置提供额外的低温液体，低温液体可以是液氮。
当液化天然气111由于突发事件导致供应不足时，可以是从外界引入并送入分馏上塔的液氮115。液氮115可以直接送入分馏上塔6，或者可以与分馏下塔4抽出经过液氮液空过冷器7过冷后的液氮合并后送入分馏上塔6。
当液化天然气111由于突发事件导致供应不足时，可以从外界引入并送入分馏上塔的液氮115，从分馏上塔引出的氧气116，而不产生液氮和液氧。
实施例3。利用液化天然气冷量分离空气的系统和装置如图3所示。本实施例与实施例1与实施例2的区别在于：增加了增压透平膨胀机20和水冷却器21。从中压氮透平压缩机17出来的氮气经过增压透平膨胀机20的增压部分继续压缩，该增压部分位于独立的第二冷箱2的外部，氮气压缩后经过水冷却器21预冷，分成两股进入液化天然气换热器15，一股从液化天然气换热器15的中部抽出，进入增压透平膨胀机20的膨胀部分膨胀降压，与汽液分离器12出来的氮气汇合返回液化天然气换热器15复热，并回到中压氮透平压缩机17的入口，完成氮气循环；另一股氮气则经过液化天然气换热器15预冷后，节流膨胀，进入汽液分离器12。
增加了增压透平膨胀机20也可以布置在独立的第一冷箱1内，一部分原料空气113可以经过压透平膨胀机20的增压部分继续压缩，进入主换热器3预冷后从主换热器3的适当部位抽出，并进入增压透平膨胀机20的膨胀部分膨胀降压，为空气分离装置提供冷量。
当液化天然气111由于突发事件导致供应不足时，本空气分离装置可以向装置提供额外的低温液体，低温液体可以是液氮，液体通道可以与实施例2相同。
当液化天然气111由于突发事件导致供应不足时，可以从外界引入并送入分馏上塔的液氮115，从分馏上塔引出的氧气116，而不产生液氮和液氧。
上述实施例1，实施例2，实施例3仅仅是本发明的优选实施方式。对于本利用液化天然气的空气分离装置而言，可以作出各种变型或优化，这些也是本发明的保护范围。

Claims (5)

1.一种集成空气分离与液化天然气冷量回收系统，它至少包括一主要由分馏塔组成的空气分离装置及至少包括一主要由液化天然气换热器组成的液化天然气冷量回收装置；所述的空气分离装置中还配置有主换热器(3)、液氧换热器和液氮液空过冷器；从分馏塔的分馏上塔顶部引出的氮气经过液氮液空过冷器、主换热器(3)的复热后，经压缩增压后至少部分进入液化天然气换热器进行预冷换热；所述的液化天然气冷量回收装置中还至少配置有汽液分离器(12)和液氮过冷器(11)，且被置于一独立的第二冷箱(2)内；而主换热器(3)、液氧换热器、液氮液空过冷器和由分馏下塔(4)，分馏上塔(6)和主冷凝蒸发器(5)连接组成的分馏塔被置于一独立的第一冷箱(1)内；其特征在于所述的由分馏上塔顶部(6)引出氮气，经液氮液空过冷器(7)复热后，进入主换热器(3)的氮气换热通道(M1-M2)复热，部分被引入独立的第二冷箱(2)，与出液氮过冷器并经复热的循环氮气(107)合并，作为氮气液化的原料氮气，随后进入低压氮透平压缩机(16)中压缩，与来自汽液分离器(12)的出汽液分离器的循环氮气(103)汇合，进入中压氮透平压缩机(17)中压缩，随后进入液化天然气换热器(15)被进液化天然气换热器的液化天然气(111)和所述出汽液分离器的循环氮气(103)预冷，进液化天然气换热器的液化天然气(111)在液化天然气换热器(15)中被复热后引出独立的第二冷箱(2)用于其它用途；离开液化天然气换热器(15)的氮气一部分节流膨胀，产生含有液氮的湿蒸气，去汽液分离器(12)；另一部分引出液化天然气换热器换热的循环氮气(101)也节流膨胀，返回液化天然气换热器(15)复热，去中压氮透平压缩机(17)，完成氮气制冷循环。
2.根据权利要求1所述的集成空气分离与液化天然气冷量回收系统，其特征在于由汽液分离器(12)分离出的出汽液分离器的循环氮气(103)返回液化天然气换热器(15)复热，与所述另一部分返回液化天然气换热器复热的循环氮气(101)合并去中压氮透平压缩机(17)；由汽液分离器(12)分离出的液氮经液氮过冷器(11)过冷后，一部分节流膨胀后的循环氮气(107)，依次返回液氮过冷器(11)、液化天然气换热器(15)复热，与独立的第一冷箱(1)引出的氮气汇合去低压氮透平压缩机(16)，完成一路氮气循环；一部分引出独立的第二冷箱(2)，作为出液氮过冷器的液氮产品(104)，并送往液氮贮槽(18)；其余出液氮过冷器的液氮(105)节流膨胀后返回独立的第一冷箱(1)，依次在液氧换热器(10)、主换热器(3)中复热，去低压氮透平压缩机(16)，完成另一路氮气循环。
3.根据权利要求1所述的集成空气分离与液化天然气冷量回收系统，其特征在于中压氮透平压缩机(17)的工作压力在2.5～5.0MPa范围内。
4.根据权利要求1或3所述的集成空气分离与液化天然气冷量回收系统，其特征在于低压氮透平压缩机(16)，中压氮透平压缩机(17)，节流阀(14)，液化天然气换热器(15)的换热通道(D1-D2、E1-E2、F1-F2、G1-G2、H1-H2)，以及主换热器(3)的换热通道(C1-C2、M1-M2)构成氮气制冷循环回路。
5.根据权利要求1所述的集成空气分离与液化天然气冷量回收系统，其特征在于液化天然气(111)的压力在4.0～9.5MPa范围内，进入液化天然气换热器(15)的换热通道(I1-I2)，复热后引出独立的第二冷箱(2)。
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