JP5411496B2 - 液化天然ガス流の希薄化方法及び装置 - Google Patents
液化天然ガス流の希薄化方法及び装置 Download PDFInfo
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Description
液化天然ガスは、メタンの他、通常、エタン、プロパン、及びブタンの各種異性体形態等、更に高級の炭化水素化合物を含有する。これらの付加的化合物は、メタンより高い熱量を有する。液化天然ガスには、特に熱量に関して異なる規格が各種市場で要求されている。
希薄化の一形成方法は、液化天然ガス流から天然ガス液を回収するというものである。
前述の方法は、必ずしも効率的ではないことが見出された。
本発明の目的は、前記問題を最小限にすることである。
本発明の更なる目的は、液化天然ガス流を希薄化する代わりの方法を提供することである。
液化天然ガス流を含む原料流を第一熱交換器配列中で加熱して、中間原料流を形成する工程、
中間原料流を少なくとも第一部分と第二部分とに分割する工程、
第一部分を蒸留塔に通すと共に、該第一部分を第一供給点経由で供給する工程、
第二部分を第二熱交換器配列に通し、ここで第二部分を更に加熱し、次いで、加熱された第二部分を第二供給点経由で蒸留塔に供給する工程、
蒸留塔の下部から天然ガス液含有液体流を取出す工程、
蒸留塔の上部から塔頂蒸気流を取出す工程、
塔頂蒸気流を第二熱交換器配列に通し、ここで塔頂蒸気流を、中間原料流の第二部分により冷却して、中間希薄化流を形成し、次いで、該中間希薄化流の少なくとも一部を第一熱交換器配列に通して更に原料流により冷却し、希薄化天然ガスの生成物流を形成する工程、
を含む。ここで第二熱交換器配列での塔頂蒸気流の冷却中、該蒸気流は部分的に凝縮されて、中間凝縮物及び中間蒸気を形成し、該中間凝縮物の少なくとも一部は、第三供給点経由で蒸留塔に通され、該中間蒸気は第一熱交換器配列に通される。
以上説明した本発明の特徴及びその他の特徴を、実施例により、また添付の非限定的な図面を参照して更に説明する。
添付図面において、図1及び図2は、本発明の全ての特徴は含まないが、説明目的のために取り入れた系統工程及び装置の概略を示す。
図3は、本発明の系統工程及び装置の概略を示す。
この説明目的のため、同様な符号は同様な部品に対応する。ラインに対応する符号もこれらのラインに流れるそれぞれの流れを言うのに用いた。
図1は、液化天然ガス流から天然ガス液を抽出して、液化天然ガス流を希薄化する装置の概略図である。原料ライン1は、液化天然ガスの供給源に接続可能である。任意のポンプ3は、原料ライン1中に備えられ、その高圧出口はライン2を介して第一熱交換器配列5と流通可能である。
操作時、メタン、エタン及びプロパンを含有する、液化天然ガスの原料流を本プロセスに供給する場合、プロパンの大部分は蒸留塔21で回収される。塔頂蒸気流40中に存在する可能性がある残りのプロパン成分を第二熱交換器26中で凝縮すれば、プロパンの選択的回収量は増加できる。還流分離容器43から中間凝縮物49が抜き出され、冷還流流として蒸留塔21にフィードバックされる。プロパンは、その他、出口31経由で本プロセスを離れる機会もある。
本発明に関連して、熱交換器配列は、1つの熱交換器、或いは複数の熱交換器を並列及び/又は直列に備えることができる。
5 第一熱交換器配列
6 第一熱交換器配列の出口
7 中間原料流
9 第二気体/液体分離器
11 第二気体/液体分離器の出口
14 分配器
15 液体中間原料フラクション
17 中間原料流の第一部分
19 中間原料流の第二部分
20 加熱された第二部分
21 蒸留塔
25 第一供給点
26 第二熱交換器配列
29 第二供給点
35 天然ガス液含有液体流又は天然ガス液
39 塔頂蒸気出口
40 塔頂蒸気流
43 第一気体/液体分離器又は第一分離器
45 第一分離器の出口
47 第一分離器の出口
48 中間希薄化流
49 中間凝縮物の少なくとも一部
51 第三供給点
55 希薄化天然ガスの生成物流
57 蒸気状中間原料フラクション
63 圧縮機
Claims (11)
- 液化天然ガス流から、メタンより高級の炭化水素化合物を天然ガス液(35)の形態で除去することにより、液化天然ガス流(1)を希薄化する方法において、
液化天然ガス流を含む原料流(1)を第一熱交換器配列(5)中で加熱して、中間原料流(7)を形成する工程、
中間原料流(7)を少なくとも第一部分(17)と第二部分(19)とに分割する工程、
第一部分(17)を蒸留塔(21)に通すと共に、該第一部分(17)を第一供給点(25)経由で供給する工程、
第二部分(19)を第二熱交換器配列(26)に通し、ここで第二部分を更に加熱し、
次いで、加熱された第二部分(20)を第二供給点(29)経由で蒸留塔(21)に供給する工程、
蒸留塔(21)の下部から天然ガス液含有液体流(35)を取出す工程、
蒸留塔(21)の上部から塔頂蒸気流(40)を取出す工程、
塔頂蒸気流(40)を第二熱交換器配列(26)に通し、ここで塔頂蒸気流(40)を、中間原料流(7)の第二部分(19)により冷却して、中間希薄化流(48)を形成し、次いで、該中間希薄化流の少なくとも一部を第一熱交換器配列(5)に通して更に原料流(1)により冷却し、希薄化天然ガスの生成物流(55)を形成する工程、
を含み、第二熱交換器配列(26)での塔頂蒸気流(40)の冷却中、該蒸気流は部分的に凝縮されて、中間凝縮物及び中間蒸気を形成し、該中間凝縮物の少なくとも一部(49)は、第三供給点(51)経由で蒸留塔(21)に通され、該中間蒸気は第一熱交換器配列(5)に通される該方法。 - 第一熱交換器配列(5)での前記原料流の加熱工程が、原料流を部分的に気化する工程を含み、これにより中間原料流(7)は液体中間原料フラクションと蒸気状中間原料フラクションとの混合物を含むと共に、少なくとも液体中間原料フラクション(15)は、少なくとも前記第一部分と第二部分(17、19)とに分割される請求項1に記載の方法。
- 前記混合物が原料分離容器(9)に通され、ここから、液体中間原料フラクション(15)及び蒸気状中間原料フラクション(57)は、前記少なくとも第一部分と第二部分(17、19)とに分割する前に、それぞれ抜き出される請求項2に記載の方法。
- 前記第二供給点(29)が、第一供給点(25)より重力的に低い位置に配置される請求項1〜3のいずれか1項に記載の方法。
- 前記第三供給点(51)が、第一供給点(25)より重力的に低い位置にある請求項1〜4のいずれか1項に記載の方法。
- 前記第三供給点(51)が、第二供給点(29)より重力的に高い位置にある請求項1〜4のいずれか1項に記載の方法。
- 前記塔頂蒸気流(40)が、第二熱交換器配列(26)に通す前に、圧縮される請求項1〜6のいずれか1項に記載の方法。
- 前記希薄化天然ガスの生成物流が、引続き再ガス化される請求項1〜7のいずれか1項に記載の方法。
- 液化天然ガス流から、メタンより高級の炭化水素化合物を天然ガス液(35)の形態で除去することにより、液化天然ガス流(1)を希薄化する装置において、
第一熱交換器配列(5)中で液化天然ガス流を含む原料流(1)を加熱することにより形成される中間原料流(7)の排出用出口(6)を備え、液化天然ガス流を含む原料流(
1)を受けるために配置された該第一熱交換器配列(5);
第一熱交換器配列(5)の出口(6)と流通可能な第二熱交換器配列(26);
少なくとも第一、第二及び第三の供給点(25、29、51)を有し、下部に天然ガス液含有液体流(35)の取出し用排出口(31)を備えると共に、上部に、少なくとも第二熱交換器配列(26)を介して第一熱交換器配列(5)と流通可能な塔頂蒸気出口(39)を備えた蒸留塔(21);
蒸留塔(21)の第一供給点(25)に接続した第一出口、及び第二熱交換器配列(26)を介して蒸留塔(21)の第二供給点(29)に接続した第二出口を有すると共に、第一熱交換器配列(5)の出口(6)に接続した分配器(14);及び
第一分離器(43)は蒸留塔(21)の第三供給点(51)に接続した出口(45)、及び第一熱交換器配列(5)と流通可能な出口(47)を備えると共に、塔頂蒸気出口(39)の下流で、かつ第二熱交換器配列(26)と第一熱交換器配列(5)との間にある第一気液分離器(43);
を有する該装置。 - 第一熱交換器配列(5)の出口(6)に接続した入口、及び分配器(14)に接続した底部出口(11)を備えた第二気液分離器(9)を更に有する請求項9に記載の装置。
- 蒸留塔(21)の出口(39)と第二熱交換器配列(26)との間に圧縮機(63)を更に有する請求項9又は10に記載の装置。
Applications Claiming Priority (3)
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EP05102252.3 | 2005-03-22 | ||
EP05102252 | 2005-03-22 | ||
PCT/EP2006/060867 WO2006100218A1 (en) | 2005-03-22 | 2006-03-20 | Method and apparatus for deriching a stream of liquefied natural gas |
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JP5411496B2 true JP5411496B2 (ja) | 2014-02-12 |
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EP (1) | EP1861671B1 (ja) |
JP (1) | JP5411496B2 (ja) |
ES (1) | ES2561808T3 (ja) |
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US20080148771A1 (en) * | 2006-12-21 | 2008-06-26 | Chevron U.S.A. Inc. | Process and apparatus for reducing the heating value of liquefied natural gas |
AU2009344225B2 (en) * | 2009-04-07 | 2013-04-04 | Twister B.V. | Separation system comprising a swirl valve |
EP3604222A1 (en) * | 2018-07-30 | 2020-02-05 | Evonik Operations GmbH | Process for the purification of hydrogen cyanide |
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FR1501013A (fr) * | 1966-09-13 | 1967-11-10 | Air Liquide | Procédé de production d'un gaz riche en méthane, sous pression élevée à partirde gaz naturel liquide sous basse pression |
US3452548A (en) * | 1968-03-26 | 1969-07-01 | Exxon Research Engineering Co | Regasification of a liquefied gaseous mixture |
US3837821A (en) * | 1969-06-30 | 1974-09-24 | Air Liquide | Elevating natural gas with reduced calorific value to distribution pressure |
US5114451A (en) * | 1990-03-12 | 1992-05-19 | Elcor Corporation | Liquefied natural gas processing |
US6510706B2 (en) * | 2000-05-31 | 2003-01-28 | Exxonmobil Upstream Research Company | Process for NGL recovery from pressurized liquid natural gas |
US7069743B2 (en) * | 2002-02-20 | 2006-07-04 | Eric Prim | System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas |
US6941771B2 (en) * | 2002-04-03 | 2005-09-13 | Howe-Baker Engineers, Ltd. | Liquid natural gas processing |
US6564579B1 (en) * | 2002-05-13 | 2003-05-20 | Black & Veatch Pritchard Inc. | Method for vaporizing and recovery of natural gas liquids from liquefied natural gas |
US6964181B1 (en) * | 2002-08-28 | 2005-11-15 | Abb Lummus Global Inc. | Optimized heating value in natural gas liquids recovery scheme |
AU2003258212B2 (en) * | 2003-06-05 | 2009-03-19 | Fluor Technologies Corporation | Liquefied natural gas regasification configuration and method |
US6907752B2 (en) * | 2003-07-07 | 2005-06-21 | Howe-Baker Engineers, Ltd. | Cryogenic liquid natural gas recovery process |
US7155931B2 (en) * | 2003-09-30 | 2007-01-02 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
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US20060130520A1 (en) * | 2004-12-17 | 2006-06-22 | Abb Lummus Global Inc. | Method for recovery of natural gas liquids for liquefied natural gas |
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RU2007138916A (ru) | 2009-04-27 |
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RU2386091C2 (ru) | 2010-04-10 |
JP2008535961A (ja) | 2008-09-04 |
ES2561808T3 (es) | 2016-03-01 |
EP1861671B1 (en) | 2015-12-23 |
US20090056371A1 (en) | 2009-03-05 |
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