CN108474613A - 用于液化天然气和氮气的方法 - Google Patents

用于液化天然气和氮气的方法 Download PDF

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CN108474613A
CN108474613A CN201680077539.4A CN201680077539A CN108474613A CN 108474613 A CN108474613 A CN 108474613A CN 201680077539 A CN201680077539 A CN 201680077539A CN 108474613 A CN108474613 A CN 108474613A
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natural gas
low temperature
unit
generating
nitrogen stream
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CN108474613B (zh
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尼古拉斯·卡姆布朗
理查德·杜巴特尔格勒尼耶
卢瓦克·若利
维亚内·默尼耶
克里斯多夫·萨莫莱夫斯基
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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    • 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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Abstract

一种用于产生液化天然气和液氮流的方法，该方法包括至少以下步骤：步骤a)：通过空气分离单元(ASU)产生气态氮气；步骤b)：在天然气液化单元中液化天然气流，该天然气液化单元包括主热交换器和用于产生低温的系统；步骤c)：在天然气液化单元的所述主交换器中将由步骤a)产生的氮气流与步骤b)中的液化天然气并行液化；其特征在于，用于液化氮气流和用于液化天然气所需的所有低温由天然气液化单元的所述用于产生低温的系统供应。

Description

用于液化天然气和氮气的方法
本发明涉及一种用于液化诸如天然气等烃流的方法、尤其是一种用于产生液化天燃气和液氮流的方法。在用于使用混合制冷剂级联液化天然气的典型工厂中，制冷剂流用于通过相对于待液化的烃流(通常为天然气)进行蒸发而在主热交换器的不同水平产生低温。
本发明特别适用于存在空气分离单元(ASU)和天然气液化单元的场所。
出于多种原因，天然气液化是可取的。例如，天然气可以在液态下比在气态形式下更容易储存和长距离运输，因为它对于给定的质量占据较小的体积并且不需要在高压下储存。
将空气分离单元与天然气液化单元热组合，其中，天然气液化所需的低温由空气分离单元经由液氮产生，这在现有技术中是已知的，尤其从专利申请EP 1435497中已知。
这种系统的缺点是，通常由空气分离单元产生的液氮量不足以避免用于天然气液化单元的产生低温的系统(例如涡轮机械)上的资本支出。
此外，通过液氮的天然气液化比使用制冷循环(诸如基于逆布雷顿循环的原理的氮气循环，或者基于液化交换器中不同水平的不同烃流的蒸发而使用混合制冷剂的循环)在能量上效率低得多。
本发明的诸位发明人已经开发出用于解决上述问题的解决方案，即，使空气分离单元中的用于产生低温的系统的资本支出最小化，并且因此在维持用于液化单元中天然气液化的最优效率的同时使资本支出最优化。
本发明涉及一种用于产生液化天然气和液氮流的方法，该方法包括至少以下步骤：
-步骤a)：在空气分离单元(ASU)中产生气态氮气；
-步骤b)：在天然气液化单元中液化天然气流，该天然气液化单元包括主热交换器和用于产生低温的系统；
-步骤c)：在天然气液化单元的所述主交换器中将由步骤a)产生的氮气流与步骤b)中的液化天然气并行液化；
其特征在于，用于液化氮气流和用于液化天然气所需的所有低温由天然气液化单元的所述用于产生低温的系统供应。
根据其他实施例，本发明还涉及：
一种如上所述的方法，其特征在于，空气分离单元包括至少一个所谓的高压柱和至少一个所谓的低压柱，步骤a)中产生的气态氮气在低压柱的顶部产生。
一种如上所述的方法，其特征在于，由步骤c)产生的液化氮的一部分以该低压柱的顶部水平再循环至该空气分离单元。
一种如上所述的方法，其特征在于，所述用于产生低温的系统包括至少一个压缩机和至少一个涡轮-增压器系统。
一种如上所述的方法，其特征在于，该液化单元包括制冷循环，该制冷循环供应有包含选自氮气、甲烷、乙烯、乙烷、丁烷、以及戊烷的成分中的至少一种的制冷剂流。
本发明还涉及一种用于产生液化天然气和液氮的装置，该装置包括产生至少一个气态氮气流的空气分离单元和天然气液化单元，所述天然气液化单元包括至少一个主热交换器和用于产生低温的系统，其特征在于，该用于产生低温的系统适合于并且被设计成用于对来自该空气分离单元的氮气流和在该天然气液化单元中循环的该天然气流进行液化。
根据具体实施例，本发明涉及一种如上所述的装置，其特征在于，所述用于产生低温的系统包括至少一个压缩机和至少一个涡轮-增压器系统。
本发明的目的是用于液化富含烃的气体(通常为天然气)的单元与空气分离单元(ASU)的热耦合。
“热耦合”是指将用于产生低温的装置进行组合，以确保两个单元(通常为空气压缩机、制冷循环压缩机、以及可选的涡轮/增压器系统)的热平衡。
“涡轮/增压器系统”是指涡轮(经由公共轴)机械地联接到单级压缩机，涡轮产生的动力直接传输到单级压缩机上。
由于天然气液化单元的低温需求通常大于空气分离单元的低温需求，利用天然气液化单元的机器(压缩机和/或涡轮/增压器)有利于至少部分地确保空气分离单元的低温需求并显著地利于限制ASU的机器上的资本支出。
具体地，用于提高烃液化器的液化能力的增量支出远远低于用于提高空气分离单元的液体生产能力的增量支出。
本发明尤其适用于产生一个或多个气态流的空气分离单元，所述气态流包括至少一个气态氮气流。
此气态氮气流被送至天然气液化单元的主交换器，在该主交换器中该氮气流与天然气流并行液化。用于液化此气态氮气流所需的低温由天然气液化循环本身的用于产生低温的装置供应，典型地，可选地具有涡轮/增压器的循环压缩机。
气态氮气流可以可选地在被送至用于液化天然气的单元之前进行压缩以促进其液化。
一旦液化，氮气流至少部分返回到空气分离单元(通常返回到低压柱的顶部)以在那里提供冷平衡。
此解决方案的优点之一是利用天然气液化器的冷量来增加ASU的氧气和氩气的产量，同时限制其上的资本支出。此解决方案还可以用于ASU(在其初始配置中几乎仅产生气态流并且仅产生少量液体)以产生更大量的液体流，同时限制过度投资。
在使用氮气的天然气液化循环的特定情况下，由循环压缩机以及由至少一个涡轮/增压器系统提供低温，来自ASU的气态氮气流将优选地被引入循环压缩机的上游，以便在天然气液化单元的主交换器中进行液化之前在那里进行压缩。
尽管根据本发明的方法适用于各种烃供料流，但它尤其适用于待液化的天然气流。进一步地，本领域技术人员将容易理解，在液化之后，如果需要，可以进一步处理液化天然气。举例来讲，获得的液化天然气可以通过焦耳-汤姆逊阀或通过涡轮减压。
进一步地，其他中间处理步骤可以在气/液分离与冷却之间进行。待液化的烃流通常是从天然气田或油罐获得的天然气流。作为替代方案，天然气流还可以从其他源获得，也包括诸如费歇尔-特罗普希(Fischer-Tropsch)法的合成源。
通常，天然气流基本上由甲烷组成。优选地，供料流包含至少60mol％的甲烷、优选地至少80mol％的甲烷。根据来源，天然气可能包含大量的比甲烷重的烃，比如乙烷、丙烷、丁烷和戊烷、以及特定的芳香烃。天然气流还可以包含非烃产品，诸如H2O、N2、CO2、H2S以及其他含硫化合物等。
包含天然气的供料流可以在其被供给到热交换器中之前进行预处理。此预处理可以包括减少和/或去除不需要的成分(诸如CO2和H2S)或其他步骤(诸如预冷和/或加压)。由于这些措施为本领域技术人员所熟知，因此在此不再详细描述。
在本申请中使用的表述“天然气”是指含有至少包括甲烷的烃的任何组合物。这包括“未加工的”组合物(在任何诸如清洁或洗涤等处理之前)以及已经部分地、基本上或完全地用于减少和/或去除一种或多种化合物的任何组合物，所述化合物包含但不限于硫、二氧化碳、水以及具有两个或更多个碳原子的烃。
热交换器可以是任何适于允许一定数量的流通过的柱、单元或其他布置，并且因此允许一个或多个制冷剂管线与一个或多个供料流之间的直接或间接热交换。
将参照附图更详细地描述本发明，该附图展示了根据本发明的方法的实现方式的特定实施例的方案。
附图中，天然气流1被供给到天然气液化单元3的主交换器2中以便进行液化。液化天然气流20从液化单元3排出。制冷剂流在此热交换器2中以闭合循环方式循环，以便供给用于液化所述天然气流1所需的低温。
具体地，本附图描述了使用氮气的液化循环。
然而，也可以使用其他类型的天然气液化循环，例如逆布雷顿循环(特别是供应有氮气，但也可以使用NG循环本身)或基于一种或多种混合制冷剂的循环。
在同一场所，包含至少一个所谓的高压柱6和所谓的低压柱5的空气分离单元(ASU)4产生气态氮气流7。该氮气流7经由压缩机9被供给到液化单元3的用于产生低温的系统8中。在压缩机的出口处，氮气流被供给到与压缩机9串联的至少一个增压器10中。来自此至少一个增压器10的流动的至少一部分连接到至少一个涡轮11上，涡轮11连接到增压器10上，从而形成本申请中所谓的涡轮/增压器系统。在增压器10的出口处，氮气流被供给到主热交换器2中以与此交换器2中的液化天然气流1并行冷却。这样被冷却的气态流的一部分12在中间水平13处从交换器2中排出，以便被供给到与增压器10相连接的涡轮11中，由此获得先前被供给到交换器2中的气态流。在涡轮11的出口处，氮气流在热交换器2的最冷端(即入口14，其温度水平为交换器2的温度水平的最低水平)被供给回到热交换器中。然后这样被供给到交换器中的氮气流被加热至交换器2的出口15(其温度水平是最高的)的水平，然后被送至压缩机9，以便遵循与气流7相同的路径。
在增压器10的出口处被供给到热交换器2中的氮气流的其他部分16(未在中间水平13处排出)与天然气流1并行液化。一旦液化，液氮流17被分成至少两个流18和19。液氮流18通过被供给到单元4的低压柱5的顶部而再循环至空气分离单元4。就其本身而言，液氮流19旨在用于生产。
根据本发明的方法的变体包括将从空气分离单元4中排出的气态氮气流7的至少一部分7′直接供给到主热交换器2中，以便与天然气流1并行液化，并且在交换器的温度水平最低的出口21处以液体形式排出，并因此重新加入用于生产的液氮流19。

Claims (7)

1.一种用于产生液化天然气和液氮流的方法，该方法包括至少以下步骤：
-步骤a)：在空气分离单元(ASU)(4)中产生气态氮气(7)；
-步骤b)：在天然气液化单元(3)中液化天然气流(1)，该天然气液化单元包括主热交换器(2)和用于产生低温的系统(8)；
-步骤c)：在该天然气液化单元(3)的所述主交换器(2)中将由步骤a)产生的该氮气流(7)与步骤b)中的该液化天然气(20)并行液化；
其特征在于，用于液化该氮气流和用于液化该天然气所需的所有低温由该天然气液化单元(3)的用于产生低温的所述系统(8)供应。
2.如前一项权利要求所述的方法，其特征在于，该空气分离单元(4)包括至少一个所谓的高压柱(6)和至少一个所谓的低压柱(5)，步骤a)中产生的该气态氮气在该低压柱(5)的顶部产生。
3.如前一项权利要求所述的方法，其特征在于，由步骤c)产生的该液化氮的一部分以该低压柱(5)的顶部水平再循环至该空气分离单元(4)。
4.如前述权利要求之一所述的方法，其特征在于，所述用于产生低温的系统(8)包括至少一个压缩机(9)和至少一个涡轮-增压器系统(10，11)。
5.如前述权利要求之一所述的方法，其特征在于，该液化单元(3)包括制冷循环，该制冷循环供应有包含选自氮气、甲烷、乙烯、乙烷、丁烷、以及戊烷的成分中的至少一种的制冷剂流。
6.一种用于产生液化天然气和液氮的装置，该装置包括产生至少一个气态氮气流(7)的空气分离单元(4)和天然气液化单元(3)，所述天然气液化单元(3)包括至少一个主热交换器(2)和用于产生低温的系统(8)，其特征在于，该用于产生低温的系统(8)适合于并且被设计成用于对从该空气分离单元(4)获得的该氮气流(7)和在该天然气液化单元(3)中循环的该天然气流(1)进行液化。
7.如前一项权利要求所述的装置，其特征在于，所述用于产生低温的系统(8)包括至少一个压缩机(9)和至少一个涡轮-增压器系统(10，11)。
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EA201891282A1 (ru) 2018-10-31
CN108474613B (zh) 2020-10-23
WO2017098099A1 (fr) 2017-06-15

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