CN102575896B - 液化富烃馏分的方法 - Google Patents
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Abstract
描述了一种液化富烃馏分的方法，其中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，将该制冷剂混合物以至少两级进行压缩并在每个压缩级之后分离成气态和液态馏分，其中将最后压缩级的气态馏分冷却至最低温度水平，同时将一个或至少一个中间压缩级的液态馏分冷却至高于最低温度水平的温度水平，其特征在于，将被冷却至高于最低温度水平的液态馏分(3)在与待液化的富烃馏分(20)的间接热交换(E)上游进行冷却(E3)。
Description
技术领域
本发明涉及液化富烃馏分的方法，其中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，将该制冷剂混合物以至少两级进行压缩并在每个压缩级之后分离成气态和液态馏分，其中将最后压缩级的气态馏分冷却至最低温度水平，同时将一个或至少一个中间压缩级的液态馏分冷却至高于最低温度水平的温度水平。
背景技术
在具有30,000至3百万吨/年的LNG生产率的天然气液化过程中，经常使用仅具有一个也称作SMR(单级混合制冷剂Single MixedRefrigerant)过程的循环压缩机的混合物回路。
下面依据在图1中所示的液化过程更详细地阐述液化富烃馏分的此类方法。
该液化过程所需的循环压缩机具有两个压缩级V1和V2。在第一压缩级V1中压缩的制冷剂混合物通常实施压缩到10至40巴、优选15至25巴，其在后期冷却器或热交换器E1中优选与周围空气或水相对地进行部分冷凝，并经过管道1送至分离塔D1。在其中分离成气态和液态馏分。将气态馏分经过管道2送至第二压缩级V2，并在其中压缩至通常为25至80巴、优选30至50巴的所期望的最终压力。
在该第二压缩级V2下游还设置有后期冷却器E2，在其中将经压缩的制冷剂馏分优选与周围空气或水相对地进行冷却。随后，将该制冷剂馏分经过管道4送至另一个分离塔D2。
在分离塔D2的塔顶经过管道5排出的气态制冷剂馏分被送至主热交换器E，在其中与待加温的工艺流相对地进行冷却，并在热交换器E的冷端经过管道7排出。该热交换器E优选被设计成多流式热交换器，尤其是板式热交换器或绕管式热交换器。
将待液化的富烃馏分例如是天然气流经过管道20送至热交换器E。在实施液化之后将液化的产品流经过管道21从热交换器E排出，并送至其另外的应用或暂时储存。
将经过管道7从热交换器E排出的制冷剂馏分在阀门a中进行制冷做功膨胀(entspannt)，并经过管道8在相对于待冷却和待液化的富烃馏分20的逆流中引导通过热交换器E。随后，将该制冷剂馏分经过管道区段8和8′送至第一压缩级V1。
从分离塔D1的塔底经过管道3排出的液态馏分在热交换器E中冷却之后经过管道9从该热交换器排出，在阀门b中进行制冷做功膨胀，随后经过管道10在相对于待冷却和待液化的富烃馏分的逆流中引导通过热交换器E。随后，将该制冷剂馏分混入至前述的在管道8中的制冷剂馏分，并与其一起经过管道8′送至第一压缩级V1。
将在第二分离塔D2的塔底中产生的液态馏分在阀门c中进行制冷做功膨胀至第一分离塔D1的压力，并送回至其上游。
经过管道3从分离塔D1排出的液态制冷剂馏分通常处于沸腾状态。但是，沸腾的制冷剂液体通常由于摩擦和/或由于升高的管道引导而导致压力损失。该压力损失必然导致该制冷剂馏分的轻质成分的部分除气。因此，导致非期望地形成两相流。这会导致管道中不稳定的流量比例和/或导致下游装置中的错误分配，其应理解为气体和液体在平行的流动途径如热交换器中的不相等比例。
发明内容
本发明的目的是，提供液化富烃馏分的此类方法，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，其特征在于，将被冷却至高于最低温度水平的温度水平的液态馏分在与待液化的富烃馏分的间接热交换上游进行冷却。
由于根据本发明设置的液态制冷剂馏分的冷却或过冷，可以有效地避免产生两相流以及与此相关的缺点。
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，
-将被冷却至更高温度水平的液态馏分在与待液化的富烃馏分的间接热交换上游冷却到比经压缩的制冷剂混合物在分离成气态和液态馏分时所具有的温度还要低2至15℃、优选4至7℃的温度，
-将被冷却至更高温度水平的液态馏分在与沸腾的馏分相对的间接热交换中进行冷却，所述沸腾的馏分来自于设置在一个下游压缩级的下游的分离成气态和液态馏分的过程，
-在待液化的富烃馏分与制冷剂混合物之间的热交换是在多流式热交换器中进行的，该多流式热交换器优选被设计成板式热交换器或绕管式热交换器，及
-至少暂时地使被冷却至最低温度水平的馏分的至少一个支流减压，并混入至被冷却至高于最低温度水平的温度水平的馏分的经减压的液态馏分。
具体实施方式
下面依据在图2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另外的实施方案。在描述在图2中所示的实施例时，下面仅探讨相对于在图1中所示的工艺流程的差异。
现在根据本发明设置热交换器E3，其能够在两个从分离塔D1和D2经过管道3和6排出的液态馏分之间实施热交换。因为经过管道6从分离塔D2排出的液态馏分在阀门c中减压至分离塔D1的压力，所以该液态馏分通过部分蒸发而被冷却至低于在后期冷却器E1和E2中可达到的工艺温度的温度。如此冷却的、在阀门c下游存在于管道6中的液态馏分现在于热交换器E3中使经过管道3从分离塔D1排出的液态馏分冷却或过冷。
在此，使液态馏分3冷却或过冷而比在后期冷却器E1和E2中可达到的工艺温度还要低2至15℃、优选4至7℃。
现在可以将如此冷却的、经过管道3从分离塔D1排出的液态馏分送至热交换器E，并引导通过其中，而不产生开始时所述的不利效应。
热交换器E3优选被设计成逆流热交换器，例如直管交换器(Geradrohrtauscher)。有利地，在实践中以如下方式设置热交换器E3，设置其低于阀门c且高于分离塔D1。在阀门c、热交换器E3和分离塔D1之间的落差使得在阀门c中减压之后的流6的两相流保持稳定。
进一步建议根据本发明液化富烃馏分的方法，使至少暂时地使被冷却至最低温度水平的馏分的至少一个支流减压，并混入至被冷却至高于最低温度水平的温度水平的馏分的经减压的液态馏分。此类工艺流程例如是通过如下方式实现的，经过管道11和/或12将制冷剂混合物-支流在热交换器E的冷端或在合适的中间温度下排出，在阀门d或e中减压，并混入至经减压的液态馏分9。若制冷剂馏分5相对于沸腾状态的过冷度为至少5℃、优选至少10℃，则存在合适的中间温度。在实践中在大多数情况下设置阀门d或e。此类工艺流程能够改善在热交换器E中的温度或温度分布的调节。
在图2中所示的实施方案由于在其中实现了将液态馏分3的过冷整合到压缩V1/V2中而具有以下优点，液态馏分3在被送至热交换器E中之前可以达到的温度低于在与周围空气或冷水相对地进行冷却的情况下可以达到的温度，无需为此通过分离的冷却设备和/或通过另一个冷的工艺流额外地进行冷却。
在图2中所示的方法使得在热交换器E3中实现的制冷剂3的过冷与其他设备部件的运行之间值得期待的分离成为可能。这一分离尤其是在液化过程开始时是有意义的，这是因为冷的工艺流通常在该过程开始之后才是可动用的，因此也无法从开始就考虑进行过冷。
根据本发明液化富烃馏分的方法能够以低的额外建设成本，即在仅设置一个额外的热交换器E3的情况下，消除开始时所述的问题，如其在属于现有技术的液化过程中所出现的问题。
Claims (6)
1.液化富烃馏分的方法，其中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，将该制冷剂混合物以至少两级进行压缩并在每个压缩级之后分离成气态和液态馏分，其中将最后压缩级的气态馏分冷却至最低温度水平，同时将一个或至少一个中间压缩级的液态馏分冷却至高于最低温度水平的温度水平，将被冷却至高于最低温度水平的温度水平的液态馏分(3)在与待液化的富烃馏分(20)的间接热交换上游进行冷却(E3)，其特征在于，将被冷却至高于最低温度水平的温度水平的液态馏分(3)在与沸腾的馏分(6)相对的间接热交换中进行冷却(E3)，所述沸腾的馏分来自于设置在一个下游压缩级(V2)的下游的分离成气态和液态馏分的过程(D2)。
2.根据权利要求1的方法，其特征在于，将被冷却至高于最低温度水平的温度水平的液态馏分(3)在与待液化的富烃馏分(20)的间接热交换上游冷却(E3)到比经压缩的制冷剂混合物在分离成气态和液态馏分时所具有的温度还要低2至15℃的温度。
3.根据权利要求2的方法，其特征在于，将被冷却至高于最低温度水平的温度水平的液态馏分(3)在与待液化的富烃馏分(20)的间接热交换上游冷却(E3)到比经压缩的制冷剂混合物在分离成气态和液态馏分时所具有的温度还要低4至7℃的温度。
4.根据权利要求1至3之一的方法，其特征在于，在待液化的富烃馏分(20)与制冷剂混合物之间的热交换是在多流式热交换器中进行的。
5.根据权利要求4的方法，其特征在于，所述多流式热交换器被设计成板式热交换器或绕管式热交换器。
6.根据权利要求1至3之一的方法，其特征在于，至少暂时地使被冷却至最低温度水平的馏分(5，7)的至少一个支流(11，12)减压(d，e)，并混入至被冷却至高于最低温度水平的温度水平的馏分的经减压的液态馏分。
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| DE102011010633A1 (de) * | 2011-02-08 | 2012-08-09 | Linde Ag | Verfahren zum Abkühlen eines ein- oder mehrkomponentigen Stromes |
| DE102014018412A1 (de) * | 2014-12-09 | 2016-06-09 | Linde Aktiengesellschaft | Abfackelfreies Anfahren eines Erdgasverflüssigungsprozesses |
| DE102015004125A1 (de) * | 2015-03-31 | 2016-10-06 | Linde Aktiengesellschaft | Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion |
| US10323880B2 (en) | 2016-09-27 | 2019-06-18 | Air Products And Chemicals, Inc. | Mixed refrigerant cooling process and system |
| US10852059B2 (en) | 2017-09-28 | 2020-12-01 | Air Products And Chemicals, Inc. | Multiple pressure mixed refrigerant cooling system |
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2010
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- 2010-03-30 PE PE2011001669A patent/PE20120848A1/es not_active Application Discontinuation
- 2010-03-30 AU AU2010230576A patent/AU2010230576B2/en not_active Ceased
- 2010-03-30 WO PCT/EP2010/002034 patent/WO2010112206A2/de active Application Filing
- 2010-03-30 RU RU2011144360/06A patent/RU2538156C2/ru not_active IP Right Cessation
- 2010-03-30 BR BRPI1013386A patent/BRPI1013386A2/pt not_active Application Discontinuation
- 2010-03-30 MY MYPI2011004663A patent/MY161644A/en unknown
- 2010-03-30 CN CN201080015211.2A patent/CN102575896B/zh not_active Expired - Fee Related
-
2011
- 2011-09-27 CL CL2011002391A patent/CL2011002391A1/es unknown
- 2011-10-18 NO NO20111413A patent/NO20111413A1/no not_active Application Discontinuation
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| US4586942A (en) * | 1983-02-08 | 1986-05-06 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and plant for the cooling of a fluid and in particular the liquefaction of natural gas |
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| GB2326464A (en) * | 1997-06-12 | 1998-12-23 | Costain Oil Gas & Process Limi | A refrigeration cycle utilising a multi-component refrigerant |
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Also Published As
| Publication number | Publication date |
|---|---|
| RU2538156C2 (ru) | 2015-01-10 |
| RU2011144360A (ru) | 2013-05-10 |
| AR076136A1 (es) | 2011-05-18 |
| NO20111413A1 (no) | 2011-10-18 |
| DE102009016046A1 (de) | 2010-10-07 |
| CN102575896A (zh) | 2012-07-11 |
| BRPI1013386A2 (pt) | 2016-03-29 |
| PE20120848A1 (es) | 2012-07-11 |
| MY161644A (en) | 2017-04-28 |
| CL2011002391A1 (es) | 2012-02-10 |
| WO2010112206A2 (de) | 2010-10-07 |
| AU2010230576A1 (en) | 2011-09-15 |
| AU2010230576B2 (en) | 2016-02-18 |
| WO2010112206A3 (de) | 2012-10-11 |
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