CN100535563C - 用于使富碳氢化合物流液化的方法 - Google Patents
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Abstract
本发明涉及用于使富碳氢化合物流、尤其是天然气流液化的方法，其中，富碳氢化合物流的液化通过一个由三个制冷剂混合物循环回路组成的制冷剂混合物循环回路级联装置来实现，其中，这三个制冷剂混合物循环回路中的第一制冷剂混合物循环回路用于预冷却，第二制冷剂混合物循环回路用于液化及第三制冷剂混合物循环回路用于液化的富碳氢化合物流的过冷却。本发明提出：第三制冷剂混合物循环回路的制冷剂混合物(2c)的压缩借助两个功率彼此相差不大于+/-2%的压缩机(V2，V2’)来实现，第一与第二制冷剂混合物循环回路的制冷剂混合物(3c，3e，4c，4e)的压缩分别借助一个相对第三制冷剂混合物循环回路的压缩机(V2，V2’)功率彼此相差不大于+/-2%的压缩机(V4，V3)来实现。优选第一及第二制冷剂混合物循环回路的压缩机(V4，V3)与第三制冷剂混合物循环回路的压缩机(V2，V2’)借助两个功率彼此相差不大于+/-2%的驱动器来驱动。
Description
技术领域
本发明涉及用于使富碳氢化合物流、尤其是天然气流液化的方法，其中，富碳氢化合物流的液化通过一个由三个制冷剂混合物循环回路组成的制冷剂混合物循环回路级联装置来实现，其中，这三个制冷剂混合物循环回路中的第一制冷剂混合物循环回路用于预冷却，第二制冷剂混合物循环回路用于液化及第三制冷剂混合物循环回路用于液化的富碳氢化合物流的过冷却。
背景技术
以下对于“第一制冷剂混合物循环回路”的概念总是也可理解为二氧化碳制冷剂循环回路。
根据所述类型的用于液化富碳氢化合物流的方法已由德国公开文献197 16 415公开。通过引证德国公开文献197 16 415，其公开的内容将被接收在本专利申请的公开内容中。
天然气液化设备或被设计为所谓的LNG基本负荷设备-即用于提供天然气作为原始能量的天然气液化设备-或被设计为所谓的峰值削幅设备-即用于覆盖峰值需要量的天然气液化设备。
LNG基本负荷设备在通常情况下用由碳氢化合物的混合物组成的制冷剂循环回路来工作。该混合物循环回路比膨胀剂循环回路的能效高及允许在大的液化功率下使基本负荷设备相应地具有相对低的能量消耗。
在根据所述类型的液化方法中，基本上第一混合物循环回路用于预冷却，第二混合物循环回路用于液化及第三混合物循环回路用于液化的富碳氢化合物流或天然气的过冷却。
在预冷却与液化之间-如果需要的话-将发生高沸点的碳氢化合物的分离。它们至少为待液化的富碳氢化合物流或天然气的那些在随后的冷却中将冻结的成分-即C5+碳氢化合物及芳香族。此外通常那些不希望地提高被液化的天然气的热值的碳氢化合物-这里尤其是指丙烷及丁烷-在液化前被分离出来。
由一个未提前公开的德国专利申请103 44 030也已知了一种根据所述类型的液化方法，其中，第二制冷剂混合物循环回路的至少一个制冷剂混合物部分流用于富碳氢化合物流的预冷却。在该德国专利申请103 44 030中所述的液化方法允许经济地利用可支配的压缩机及驱动器，因为第三混合物循环回路的(循环回路)压缩机大致得到相同的驱动功率，即各约为总驱动功率的33.33％。因此尤其是具有的液化能力大于每年5百万吨LNG的大型液化设备可经济地运行，因为通过三个制冷循环回路的驱动器及压缩机的统一化可使经受试验的驱动器或压缩机可达到的液化过程的液化功率最大化。
原则上，压缩机驱动器及这里尤其是燃气轮机仅以离散的挡级可供支配。因此对于企图得到的设备大小或液化功率使用三个基本上相同或相同的驱动器通常不合适。
尤其在冷的环境条件下-指这样的条件，其中空气或冷却水处于小于15至20℃的温度下-用于预冷却所需的能量需要量的部分下降到这样的程度，以致如在上述德国专利申请103 44 030中所述方法的应用那样可被视为不是最佳的。
发明内容
本发明的任务则在于，给出一种根据所述类型的方法，它即使在所述的条件下也可实现在所需能量需要量方面最佳的方法应用。
为了解决该任务提出，第三制冷剂混合物循环回路的制冷剂混合物的压缩借助两个基本上功率相同(功率彼此相差不大于+/-2％)的压缩机来实现，及第一与第二制冷剂混合物循环回路的制冷剂混合物的压缩各借助一个相对第三制冷剂混合物循环回路的压缩机基本上功率相同(功率彼此相差不大于+/-2％)的压缩机来实现。
借助根据本发明的方法现在可作到：使压缩机的功率及由此使驱动器的功率这样地分配，以致对于待液化的富碳氢化合物流或天然气流可提供少量的冷却功率。三个制冷剂混合物循环回路的所需总功率现在可分配在四个压缩机驱动器上。
根据本发明的方法尤其应用于大容量的单线液化设备具有其优点。
根据本发明的用于富碳氢化合物流的液化的方法在其进一步构型上提出，第一及第二制冷剂混合物循环回路的压缩机及第三制冷剂混合物循环回路的压缩机借助两个基本上相同和/或功率相同(功率彼此相差不大于+/-2％)的驱动器来驱动。
根据本发明的方法的构型特别有意义的是，压缩机驱动器可输出所需总功率的50％。在此情况下，预冷却循环回路及液化循环回路的压缩机与过冷却循环回路的压缩机可归结成相同的或基本上相同的功率的两个驱动路径。
对于所使用的概念词组“基本上功率相同的压缩机”或“基本上相同的和/或功率相同的驱动器”应理解为这样的压缩机或驱动器，它们的功率彼此相差不大于+/-2％。
附图说明
以下将借助一个附图中所示的实施例来详细描述根据本发明的方法及本发明的其它构型。
在借助该附图描述的方法中将通过一个由三个制冷剂混合物循环回路组成的制冷剂混合物循环回路级联装置来实现富碳氢化合物流的冷却及液化，该富碳氢化合物流通过导管1被输送到热交换器E1。它们在通常情况下具有不同的组成，就像例如在上面所述的德国公开文献197 16 415中所述的那样。
具体实施方式
待液化的富碳氢化合物流在热交换器E1中逆着第一混合物循环回路4a至4e的两个蒸发的制冷剂混合物部分流4b及4d及第二制冷剂混合物循环回路3a至3e的蒸发的制冷剂混合物部分流3d被冷却及接着通过导管1a输入仅作为黑匣子表示的分离单元S。
如果使用一个(二氧化碳)制冷剂循环回路来替换第一制冷剂混合物循环回路，则取消通过导管4d及4e取出的部分流。此外，在此情况下压缩机V4不具有——如该图中所示的——侧向馈入。
在分离单元S中进行上述的C3+分离，其中，从待液化的富碳氢化合物流分离出的组分通过导管1b被从分离单元S取出。
在通常情况下，第二制冷剂混合物循环回路3a至3e的两个部分流3b及3d之一的至少一个部分流用于在分离单元S中提供冷却，关于该第二制冷剂混合物循环回路在下面还要详细描述。这里由两个部分流3b和/或3d中的哪个再选择出用于提供该冷却的至少一个部分流将由分离单元S中所需的温度水平来确定。
然后待液化的富碳氢化合物流通过导管1c被输送给一个第二热交换器E2及在其中逆着第二制冷循环回路3a至3b的蒸发的制冷剂混合物部分流3b被液化。
该富碳氢化合物流在进行了液化后通过导管1d被输送给一个第三热交换器E3及在其中逆着该第三制冷循环回路2a至2c的制冷剂混合物流2b被过冷却。该过冷却的液态产品接着通过导管1e被输送到其另外的应用部分和/或(中间)存储器。
与上述德国专利申请10344030中所述的方法不同地，现在根据本发明该过冷却-制冷循环回路2a至2c具有两个串联连接的压缩机V2及V2’。预冷却制冷循环回路及液化制冷循环回路仅分别具有一个压缩机V4或V3。此外，根据本发明，所使用的压缩机V2，V2’，V3及V4在其功率方面被相同地或基本上相同地构造。这将导致，每个压缩机V2，V2’，V3及V4的功率需要量可通过相同的或基本上相同的驱动器A2，A2’，A3及A4来提供。
预冷却制冷循环回路及液化制冷循环回路的功率需要量必须相应地适配液化制冷循环回路的两个压缩机V2及V2’的功率需要量。因此每个压缩机V2，V2’，V3及V4或压缩机驱动器A2，A2’，A3及A4必需提供总功率的25％，至少在总功率的23％与27％之间。
优选使用燃气轮机，蒸汽轮机和/或电动机作为用于压缩机V2，V2’，V3及V4的驱动器A2，A2’，A3及A4。
连接在压缩机V2，V2’，V3及V4后面的冷却器或热交换器在该图中未示出，在这些冷却器或热交换器中制冷剂混合物逆着冷却剂-例如水-被冷却及在第一制冷剂(混合物)循环回路4a至4e的情况下被冷凝。
第一混合物循环回路的在压缩机V4中被压缩的制冷剂混合物通过导管4a被输送给热交换器E1及在该热交换器中进行了冷却后被分成两个部分流4b及4d。在这两个部分流4b及4d中的制冷剂混合物在阀d及e或减压装置中减压到不同的压力水平上后在热交换器E1中被蒸发及接着通过导管4c或4e在第一级(部分流4c)前或在一个中间压力水平上(部分流4e)输送给压缩机V4。
第二制冷循环回路3a至3e的在压缩机V3中被压缩的制冷剂混合物通过导管3a被导送穿过热交换器E1及E2及在这些热交换器中被冷却。该制冷剂混合物流的被导送穿过热交换器E2的那个部分流3b在阀b中进行了减压后在热交换器E2中逆着待冷却的处理流被蒸发及接着通过导管3c被输送给压缩机V3的输入级。
第二制冷剂混合物循环回路3a至3e的制冷剂混合物的部分流3d在热交换器E1的后面被取出，在该制冷剂混合物部分流通过导管3e在一个中间压力水平上被输送给循环回路压缩机V3以前，在阀c中被减压及接着在热交换器E1中逆着待冷却的处理流被蒸发。因此所提到的制冷剂混合物部分流3d有助于热交换器E1中富碳氢化合物流的预冷却。
为了能够实现这一点，对于富碳氢化合物流预冷却所使用的第二制冷剂混合物循环回路3a至3e的制冷剂混合物的部分流3d必需在一个压力上被蒸发，该压力高于第二制冷剂混合物循环回路3a至3e的制冷剂混合物部分流3b的蒸发压力。
通过中间压力-在该中间压力上制冷剂混合物部分流3e被蒸发及输送给压缩机V3-的选择及通过两个制冷剂混合物部分流3b及3d的量值分配的调节可使第二制冷剂混合物循环回路的制冷功率在热交换器E1及E2上的分配几乎任意地受到调节，及由此使待液化的富碳氢化合物流的预冷却及液化几乎任意地被调节。
根据本发明的用于富碳氢化合物流的液化的方法在其进一步构型上提出，第一及第二制冷剂混合物循环回路的压缩机V4及V3及第三制冷剂混合物循环回路的压缩机V2及V2’借助两个基本上相同或功率相同的驱动器来驱动。
当压缩机V2，V2’，V3及V4可通过两个功率足够强的驱动器来提供时，根据本发明的方法的在附图中所示的该构型尤其具有其优点。当用于工作所需的驱动器的数目最小化时，通常设备的可支配性更高，当不是使用四个而是使用两个驱动器时就是这种情况。
因此根据本发明的用于液化富碳氢化合物流、尤其是天然气流的方法可实现比公知的液化方法更经济地利用可支配的压缩机。尤其是具有的液化能力大于每年5百万吨LNG的大型的单线液化设备可从根据本发明的方法中受益。
Claims (4)
1.用于使富碳氢化合物流液化的方法，其中，富碳氢化合物流的液化通过一个由三个制冷剂混合物循环回路组成的制冷剂混合物循环回路级联装置来实现，其中，这三个制冷剂混合物循环回路中的第一制冷剂混合物循环回路用于预冷却，第二制冷剂混合物循环回路用于液化及第三制冷剂混合物循环回路用于液化的富碳氢化合物流的过冷却，其特征在于：第三制冷剂混合物循环回路的制冷剂混合物(2c)的压缩借助两个功率彼此相差不大于+/-2％的压缩机(V2，V2’)来实现，第一与第二制冷剂混合物循环回路的制冷剂混合物(3c，3e，4c，4e)的压缩分别借助一个相对第三制冷剂混合物循环回路的压缩机(V2，V2’)功率彼此相差不大于+/-2％的压缩机(V4，V3)来实现。
2.根据权利要求1的方法，其特征在于：第一及第二制冷剂混合物循环回路的压缩机(V4，V3)与第三制冷剂混合物循环回路的压缩机(V2，V2’)借助两个功率彼此相差不大于+/-2％的驱动器来驱动。
3.根据权利要求1或2的方法，其特征在于：使用燃气轮机，蒸汽轮机和/或电动机作为用于这些压缩机(V2，V2’，V4，V3)的驱动器(A2，A2’，A3，A4)。
4.根据权利要求1或2的方法，其特征在于：所述富碳氢化合物流为天然气流。
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| DE200410054674 DE102004054674A1 (de) | 2004-11-12 | 2004-11-12 | Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes |
| DE102004054674.6 | 2004-11-12 |
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| CN102393126A (zh) * | 2011-10-25 | 2012-03-28 | 中国寰球工程公司 | 双循环混合冷剂的天然气液化系统和方法 |
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| DE102005029275A1 (de) * | 2005-06-23 | 2006-12-28 | Linde Ag | Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes |
| US9400134B2 (en) | 2006-08-02 | 2016-07-26 | Shell Oil Company | Method and apparatus for liquefying a hydrocarbon stream |
| BRPI0814619B1 (pt) * | 2007-07-12 | 2019-07-09 | Shell Internationale Research Maatschappij B.V. | Método e aparelho para resfriar uma corrente de hidrocarboneto, e, método e aparelho para resfriar uma corrente de refrigerante mista |
| CN102538391B (zh) * | 2012-02-19 | 2013-09-04 | 中国石油集团工程设计有限责任公司 | 多级单组分制冷天然气液化方法 |
| DE102015002164A1 (de) * | 2015-02-19 | 2016-08-25 | Linde Aktiengesellschaft | Verfahren zum Verflüssigen von Erdgas |
| EP3361197A1 (de) | 2017-02-14 | 2018-08-15 | Linde Aktiengesellschaft | Verfahren zum verflüssigen einer kohlenwasserstoff-reichen fraktion |
| EP3361196A1 (de) | 2017-02-14 | 2018-08-15 | Linde Aktiengesellschaft | Verfahren zum verflüssigen einer kohlenwasserstoff-reichen fraktion |
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| GB0006265D0 (en) * | 2000-03-15 | 2000-05-03 | Statoil | Natural gas liquefaction process |
| FR2826969B1 (fr) * | 2001-07-04 | 2006-12-15 | Technip Cie | Procede de liquefaction et de deazotation de gaz naturel, installation de mise en oeuvre, et gaz obtenus par cette separation |
| DE10226596A1 (de) * | 2002-06-14 | 2004-01-15 | Linde Ag | Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes mit gleichzeitiger Gewinnung einer C3+-reichen Fraktion mit hoher Ausbeute |
| RU2352877C2 (ru) * | 2003-09-23 | 2009-04-20 | Статойл Аса | Способ сжижения природного газа |
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| CN102393126A (zh) * | 2011-10-25 | 2012-03-28 | 中国寰球工程公司 | 双循环混合冷剂的天然气液化系统和方法 |
| CN102393126B (zh) * | 2011-10-25 | 2013-11-06 | 中国寰球工程公司 | 双循环混合冷剂的天然气液化系统和方法 |
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| AU2005303932B2 (en) | 2010-12-23 |
| RU2373465C2 (ru) | 2009-11-20 |
| DE102004054674A1 (de) | 2006-05-24 |
| RU2007121845A (ru) | 2008-12-20 |
| NO20072961L (no) | 2007-06-11 |
| AU2005303932A1 (en) | 2006-05-18 |
| WO2006050913A1 (de) | 2006-05-18 |
| CN101057117A (zh) | 2007-10-17 |
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