CN107407519A - 用于液化富烃馏出物的方法 - Google Patents
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Abstract
本发明描述了一种用于液化富烃馏出物、尤其天然气的方法，其中富烃馏出物在其液化前被预冷，经受脱水和紧接其的干燥过程并且富烃馏出物相对于至少一个混合冷却循环被液化，其中，在混合冷却循环中循环的冷却剂被至少二级地压缩，紧接着至少部分地冷凝并且在此产生的液体馏出物至少部分地混合至被压缩到中间压力上的冷却剂。根据本发明，液体馏出物(17)的部分流用于待液化的富烃馏出物(1,2)在其输送到脱水(D4)中前的预冷，其中，在液体馏出物(17)和待液化的富烃馏出物(1,2)之间的热交换经由至少一个热交换系统(E4)实现。
Description
技术领域
本发明涉及一种用于液化富烃馏出物、尤其天然气的方法，其中
- 富烃馏出物在其液化前被预冷，经受脱水和紧接着其的干燥过程，并且
- 富烃馏出物相对于至少一个混合冷却循环被液化，
- 其中，在混合冷却循环中循环的冷却剂被至少二级地压缩，紧接着至少部分地冷凝并且在此产生的液体馏出物至少部分地混合至被压缩到中间压力上的冷却剂，并且
- 其中，液体馏出物的部分流用于待液化的富烃馏出物在其输送到脱水中前的预冷。
背景技术
为了液化富烃的气体馏出物、尤其天然气，此外应用带有由轻烃以及氮组成的冷却剂混合物的方法，其中，冷却剂混合物相对于周围环境在提高的压力下至少部分地冷凝。为了液化天然气，液态的冷却剂紧接着在降低的压力下在与天然气的间接的热交换中气化。因为在(非共沸的)混合物中露点温度(Tautemperatur)在给出的压力中一直处于沸腾温度(Siedetemperatur)之上，冷却剂气化根据组分平滑地在这样的温度范围之上发生，该温度范围根据方法在至少20℃上、部分地甚至在200℃上延伸。
当用于天然气液化设备的投资费用应被保持较低时，仅仅前述的类型的混合循环用于在周围环境温度和LNG(液化天然气，Liquefied Natural Gas)-产物温度(大约-160℃)之间的总温度范围。在此放弃了对于在周围环境温度和大概-50℃之间的温度范围的特别的预冷循环的使用。
在通常称为SMR(单混合冷却，Single Mixed Refrigerant)-过程的该类型的方法执行中，那么仅一冷却剂、或其部分流供使用，该冷却剂具有平滑的气化。这样的天然气-液化方法例如从文件DE 197 22 490中已知。
在液化前，天然气通常借助于化学洗涤、例如胺类洗涤，来清洁掉酸性气体成分例如CO2和H2S。由此天然气是水(蒸气)饱和的。为了实现经济地设计紧接着的干燥(其通常基于在沸石分子筛处的吸附)，天然气尽可能广地被冷却并且通过部分的水冷凝以及紧接着的脱水在水浓度上降低，直到水合物或冰的随后的形成设置一界限。该界限根据气体组分在直到20℃的温度中实现。
在许多气候条件下不可能的是，天然气相对于空气和/或冷却水冷却到足够接近(在水合温度之上最高10℃、优选地5℃)于前述的界限温度处。
在文件DE 10 2006 021 620中因此提出了在文件DE 197 22 490中公开的改进方案用于液化富烃馏出物，在其中冷却剂的液体馏出物的部分流用于待液化的富烃馏出物在其输送到脱水中之前的预冷。
混合冷却剂然而由于平滑的气化不太适合于，在干燥前以经济的方式尽可能准确地达到湿润的天然气的最优的温度，而同时至少在应用的热交换器的部分中不低于水合温度。
发明内容
本发明的任务在于，说明一种用于液化富烃馏出物的这种类型的方法，其使如下成为可能，即，待液化的富烃馏出物在不应用完全的预冷循环的情形下(也就是说没有附加的压缩机)在干燥前预冷。尤其富烃馏出物应预冷到在水合温度之上最高10℃、优选地最高5℃的温度上，而湿润的富烃馏出物不与水合点之下的温度产生热接触。
为了解决本任务提出了用于液化富烃馏出物的这种类型的方法，其特征在于，在液体馏出物和待液化的富烃馏出物之间的热交换经由至少一个热交换系统实现。
改进地提出了用于液化富烃馏出物的根据本发明的方法，即冷却剂的液体馏出物的部分流被卸压到在第二或最后的压缩机级的吸取压力之上至少0.3bar、优选地至少0.7bar的压力上并且仅仅在此产生的液体份额用于待液化的富烃馏出物在其输送到脱水中前的预冷。
待液化的富烃馏出物在其输送到脱水中前的预冷相对于在被压缩的冷却剂的部分的冷凝中产生的液体馏出物的部分流实现。在此根据本发明，在该液体馏出物和待液化的富烃馏出物之间的热交换经由热交换系统实现。热交换系统用于在待液化的富烃馏出物和平滑地气化的冷却剂之间的间接的热传递。
概念“热交换系统”理解为这样的任意的系统，在其中在至少两种介质之间的间接的热传递借助于热承载流体实现。这样的热交换系统例如从美国专利文件中2,119,091中已知。
这样的热交换系统优选地应用沸腾的、在0与30℃之间的温度范围中液态地存在的纯净物作为热承载流体，在其中该热承载流体例如可为乙烷、乙烯、丙烷、丙烯、丁烷、二氧化碳或氨。
热交换系统优选地由两个直管束、两个卷绕的热交换器、两个板交换器或这些结构形式的任意组合实现，其中，前述的热交换器构件优选地装入在含有沸腾的热承载流体的储压器中。
通过合适地选择纯净物-热承载流体以及通过调节其运行压力和因此其沸腾温度，富烃馏出物可冷却到非常接近于水合温度处，而不与不允许地冷的冷却剂流直接产生热接触。热承载流体相对来说有效地通过在冷却剂侧处的持续的冷凝和在富烃馏出物侧处的气化实现追求的热交换。不同于平滑地气化的混合冷却剂，热承载流体在恒定的沸腾温度和由此露点温度的情形下工作。即使热承载流体的冷凝至少部分地相对于在富烃馏出物的水合温度之下气化的混合冷却剂实现，那么富烃馏出物和混合冷却剂也有效地通过热承载流体而热分离。
借助于根据本发明的方法途径干燥过程的最优的减压(Entlastung)可通过待液化的富烃馏出物或待液化的天然气冷却直到接近于水合点处并且脱水来实现。
附图说明
用于液化富烃馏出物的根据本发明的方法以及其另外的有利的设计方案根据在图1和2中呈现的实施例更详细地被解释。
具体实施方式
在图1和2中呈现的仅仅在实际的液化过程中相区分的实施例中，通常具有40和80℃之间的温度的待液化的富烃馏出物1在热交换器E3中相对于冷却空气和/或冷却水被冷却到30和60℃之间的温度上。紧接着待液化的富烃馏出物2输送给热交换系统E4并且在其中被预冷到在其水合温度之上最高10℃、优选地最高5℃的温度上。如此被预冷的富烃馏出物3被输送给分离器D4，在其底壳中产生冷凝出的水4。在分离器D4的头部处抽出的富烃馏出物5从现在起输送给仅仅作为黑箱呈现的干燥过程T。所述干燥过程T通常为吸附过程，在其中通常应用沸石分子筛(zeolithisches Molekularsieb)作为吸附剂。如此被预处理的、待液化的富烃馏出物6紧接着在热交换器E中相对于还待解释的冷却循环被冷却、液化并且若有可能过冷，从而经由管路7在天然气-液化的情况下可抽出LNG-产物流。
富烃馏出物的液化在图1和2中呈现的实施例中相对于混合冷却循环实现。这样的混合冷却循环通常具有氮和至少一种C1+-烃作为冷却剂。待压缩的冷却剂10在第一压缩机级C1中被压缩到中间压力上。紧接着压缩的冷却剂11在后冷却器E1中部分地冷凝并且在分离器D2中拆分成低沸点的气体馏出物12和高沸点的液体馏出物15。仅仅低沸点的气体馏出物12在第二压缩机级C2中被压缩到最大的循环压力上。被压缩的冷却剂13在后冷却器E2中重新部分地冷凝并且在分离器D3中拆分成气体馏出物14以及液体馏出物17/17'。在图1中呈现的实施例中气体馏出物14以及前面提及的、高沸点的冷却剂-液体馏出物15(其借助于泵P被泵到冷却剂-气体馏出物14的压力上)共同在热交换器E中相对于本身冷却并且紧接着在卸压阀V4中以提供冷的方式卸压。以提供冷的方式卸压的冷却剂16此后在热交换器E中相对于待液化的富烃馏出物6完全地气化并且重新输送给前接于第一压缩机级C1的分离器D1；其用于保护压缩机级C1，因为在其中若有可能被连带引导的液体份额被分离。
当在属于现有技术的方法途径中从分离器D3中抽出的冷却剂-液体馏出物17'经由卸压阀V1完全地被引回到分离器D2前期间，从现在起该液体馏出物的部分流17被用于待液化的富烃馏出物1/2的预冷。对此液体馏出物的前面描述的部分流17在阀V2中优选地被卸压到在第二压缩机级C2的吸取压力之上至少0.3bar、尤其至少0.7bar的压力上并且由此产生的二级的流被输送给分离器D5。在其中产生的气体馏出物19经由调节阀V3被引回到分离器D2前，而在分离器D5中产生的液体份额18被用于待液化的富烃馏出物1/2的预冷并且紧接着同样被引回到分离器D2前。
在液体馏出物17或在卸压后在阀V2中产生的液体份额18和待液化的富烃馏出物1/2之间的热交换经由热交换系统E4实现。
在图2中呈现的实施例中，冷却剂的从分离器D2中抽出的高沸点的液体份额50和从分离器D3中抽出的冷却剂-气体馏出物40分离地在热交换器E'的预冷地带a中被冷却。在高沸点的液体馏出物50在阀V5中以提供冷的方式被卸压并且紧接着在相对于待液化的富烃馏出物6的逆流中气化期间，前述的气体馏出物40部分地冷凝并且在分离器D6中拆分成另一气体馏出物41以及另一液体馏出物42。气体馏出物41在热交换器E'的液化地带b和过冷地带c中被冷却并且部分地冷凝。紧接着其在卸压阀V7中以提供冷的方式被卸压并且在相对于待液化的并且若有可能待过冷的富烃馏出物6的逆流中完全地气化。在分离器D6中产生的液体馏出物42在热交换器E'的液化地带b中进一步被冷却，在卸压阀V6中以提供冷的方式卸压并且在相对于待液化的富烃馏出物6的逆流中完全地气化。假如在图2中呈现的热交换器E'构造为所谓的卷绕的热交换器，则在卷绕的热交换器的外套中实现前述的冷却剂流41,42和50的气化。在热交换器E'中合并的并且在其中完全地气化的冷却剂流41,42和50经由管路43输送给前接于第一压缩机级C1的分离器D1。
Claims (5)
1. 一种用于液化富烃馏出物、尤其天然气的方法，其中
- 所述富烃馏出物在其液化前被预冷，经受脱水和紧接其的干燥过程，并且
- 所述富烃馏出物相对于至少一个混合冷却循环被液化，
- 其中，在所述混合冷却循环中循环的冷却剂被至少二级地压缩，紧接着至少部分地冷凝并且在此产生的液体馏出物至少部分地混合至被压缩到中间压力上的冷却剂，并且
- 其中，所述液体馏出物的部分流用于待液化的富烃馏出物(1,2)在其输送到脱水中前的预冷，
其特征在于，在所述液体馏出物(17)和所述待液化的富烃馏出物(1,2)之间的热交换经由至少一个热交换系统(E4)实现。
2.根据权利要求1所述的方法，其特征在于，所述液体馏出物(17)的部分流卸压到在第二或最后的压缩机级的吸取压力之上至少0.3bar、优选地至少0.7bar的压力上(V2)并且仅仅在此产生的液体份额(18)用于所述待液化的富烃馏出物(1,2)在其输送给所述脱水(D4)前的预冷。
3.根据权利要求1或2所述的方法，其特征在于，作为热交换系统(E4)的热承载流体应用沸腾的、在0与30°C之间的温度范围中液态地存在的纯净物，优选地乙烷、乙烯、丙烷、丙烯、丁烷、CO2或NH3。
4.根据权利要求1至3中任一项所述的方法，其特征在于，所述热交换系统(E4)由两个直管束、两个卷绕的热交换器、两个板交换器或这些结构形式的任意组合实现，其中，热交换器构件优选地装入到含有沸腾的热承载流体的储压器中。
5.根据权利要求1至4中任一项所述的方法，其特征在于，在所述混合冷却循环中循环的冷却剂具有氮和至少一种C1+-烃。
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| PCT/EP2016/000231 WO2016138978A1 (de) | 2015-03-05 | 2016-02-11 | Verfahren zum verflüssigen einer kohlenwasserstoff-reichen fraktion |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1049713A (zh) * | 1989-08-21 | 1991-03-06 | 气体产品与化学公司 | 使用操作负载膨胀器之天然气液化 |
| DE102006021620A1 (de) * | 2006-05-09 | 2007-11-15 | Linde Ag | Vorbehandlung eines zu verflüssigenden Erdgasstromes |
| CN101880560A (zh) * | 2009-05-05 | 2010-11-10 | 气体产品与化学公司 | 预冷却的液化方法 |
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| US2119091A (en) | 1935-11-29 | 1938-05-31 | Standard Oil Dev Co | Process and apparatus for indirect heat transfer between two liquid materials |
| FR2471566B1 (fr) * | 1979-12-12 | 1986-09-05 | Technip Cie | Procede et systeme de liquefaction d'un gaz a bas point d'ebullition |
| DE19722490C1 (de) | 1997-05-28 | 1998-07-02 | Linde Ag | Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes |
| DE102009018248A1 (de) * | 2009-04-21 | 2010-10-28 | Linde Aktiengesellschaft | Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion |
| US20150300731A1 (en) * | 2012-11-21 | 2015-10-22 | Shell Oil Company | Method of treating a hydrocarbon stream comprising methane, and an apparatus therefor |
| RU2538192C1 (ru) * | 2013-11-07 | 2015-01-10 | Открытое акционерное общество "Газпром" | Способ сжижения природного газа и установка для его осуществления |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1049713A (zh) * | 1989-08-21 | 1991-03-06 | 气体产品与化学公司 | 使用操作负载膨胀器之天然气液化 |
| DE102006021620A1 (de) * | 2006-05-09 | 2007-11-15 | Linde Ag | Vorbehandlung eines zu verflüssigenden Erdgasstromes |
| CN101880560A (zh) * | 2009-05-05 | 2010-11-10 | 气体产品与化学公司 | 预冷却的液化方法 |
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| DE102015002822A1 (de) | 2016-09-08 |
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| RU2705130C2 (ru) | 2019-11-05 |
| AU2016227946A1 (en) | 2017-09-28 |
| US20180045459A1 (en) | 2018-02-15 |
| RU2017132312A3 (zh) | 2019-04-08 |
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