JP2007526924A - 天然ガスの液化及び天然ガスからの液状副生成物を生産するための方法及び設備 - Google Patents
天然ガスの液化及び天然ガスからの液状副生成物を生産するための方法及び設備 Download PDFInfo
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- JP2007526924A JP2007526924A JP2006508346A JP2006508346A JP2007526924A JP 2007526924 A JP2007526924 A JP 2007526924A JP 2006508346 A JP2006508346 A JP 2006508346A JP 2006508346 A JP2006508346 A JP 2006508346A JP 2007526924 A JP2007526924 A JP 2007526924A
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- natural gas
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- purified
- cooled
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- 238000000926 separation method Methods 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 8
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- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 5
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- 239000001282 iso-butane Substances 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 4
- 239000012808 vapor phase Substances 0.000 description 4
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 3
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- XTFIVUDBNACUBN-UHFFFAOYSA-N 1,3,5-trinitro-1,3,5-triazinane Chemical compound [O-][N+](=O)N1CN([N+]([O-])=O)CN([N+]([O-])=O)C1 XTFIVUDBNACUBN-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- GJVFBWCTGUSGDD-UHFFFAOYSA-L pentamethonium bromide Chemical compound [Br-].[Br-].C[N+](C)(C)CCCCC[N+](C)(C)C GJVFBWCTGUSGDD-UHFFFAOYSA-L 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
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Abstract
Description
(a)原料天然ガスは前処理天然ガスを得るため前処理され、
(b)工程(a)で得られる前処理天然ガスはその凝縮点に近い温度に冷却され、
(c)工程(b)で得られる冷却された前処理天然ガスは膨張され、膨張された該天然ガスは、一方で塔頂生成物として精製天然ガスを、及び他方で前記LGN留分を製造するために少なくとも1つの主蒸留塔を有するLGN回収ユニットに導入され、並びに
(d)液化天然ガスは、工程(c)で得られる精製天然ガスから製造される、
以上の工程を有するタイプである。
(a1)原料天然ガスはその凝縮点に近い温度に冷却され、
(a2)工程(a1)で得られる冷却された原料天然ガスは還流を行うオーバーヘッド還流冷却器を設けられた補助蒸留塔に導入され、補助蒸留塔は45から65バールの間の圧力で操作され塔頂生成物として前処理天然ガスを製造し、前処理天然ガスはC6 + 炭化水素を実質的に含まず、補助蒸留塔は更にC6 + 重質炭化水素の留分を必然的に生じる
という副工程を有することを特徴とする。
− 工程(d)が以下の
(d1)主塔の塔頂から抽出された精製天然ガスは、少なくとも第1圧縮機では液化圧力に圧縮され、
(d2)工程(d1)で得られる圧縮された精製天然ガスは、液化天然ガスを製造するために、第1熱交換器で主塔の塔頂から抽出された精製天然ガスと熱交換することによって冷却される
という副工程を有する。
− 工程(b)が以下の
(b1)工程(a)で得られる前処理天然ガスは、第2熱交換器で第2主塔から抽出された精製天然ガスと熱交換することによって冷却される
という副工程を有する。
− 工程(c)が以下の
(c1)工程(b)で得られる冷却された前処理天然ガスは、液体ストリーム及びガスストリームを得るために分離ドラムに導入され、
(c2)工程(c1)で得られるガスストリームは、第1圧縮機に結合しているタービンで膨張され、
(c3)工程(c2)で得られるストリームは中間のレベルN3で主塔に導入され、
(c4)工程(c1)で得られる液体ストリームは膨張され、膨張された液体ストリームは、レベルN3の下のレベルN2で主塔に導入される
という副工程を有する。
− 工程(d1)において、第1圧縮機から得られる圧縮された精製天然ガスは、前記液化圧力に達するように、外部エネルギー源が供給されている第2圧縮機で圧縮される。
− 主蒸留塔の圧力は35バールより大きい。
− 液化天然ガスは更に工程(a)に直接由来する前処理天然ガスの一部を含む。
− 液化天然ガスが殆ど又は完全に工程(a)に直接由来する前処理天然ガスからなり、前記液化天然ガスが比較的C2 乃至C5 の炭化水素に富む始動段階を有し、
液化天然ガスに所望のC2 乃至C5 の炭化水素含有量に従って、工程(a)に直接由来する前処理天然ガスの一部が液化天然ガスに混合調整される製造段階を引き続き有する。
− 補助塔によって製造される液体は膨張され、主塔に導入される。
以上の特徴から個別に選択され、又は任意に組み合わせられ、1つ以上の特徴を有してよい。
(a)前処理天然ガスを得るため原料天然ガスを前処理するユニット、
(b)その凝縮点に近い温度に前処理天然ガスを冷却する手段、
(c)冷却された前処理天然ガスを膨張する手段を有し、一方で塔頂生成物として精製天然ガスを、及び他方で前記LGN留分を製造する少なくとも1つの主蒸留塔を有する、LGNを回収するユニット、及び
(d)工程(c)で得られる精製天然ガスから液化天然ガスを製造する手段
を備えるタイプであり、
前処理ユニットは、
(a1)その凝縮点に近い温度に原料天然ガスを冷却する手段、及び
(a2)補助塔は還流を行うオーバーヘッド還流冷却器を設けられ、補助蒸留塔は45から65バールの間の圧力で操作され塔頂生成物としてC6 + 炭化水素を実質的に含まない前処理天然ガスを製造し、補助蒸留塔は更にC6 + 重質炭化水素の留分を必然的に生じる、冷却された原料天然ガスを蒸留する補助蒸留塔を有することを特徴とする。
− 液化天然ガスを製造する手段は、
(d1)主塔の塔頂から抽出された精製天然ガスを液化圧力に圧縮し、少なくとも第1圧縮機を有する手段、及び
(d2)圧縮手段由来の圧縮された精製天然ガスを主塔の塔頂から抽出された精製天然ガスと熱交換させる第1熱交換器であって、液化天然ガスを製造するために、圧縮された精製天然ガスを冷却する第1熱交換器
である。
− 前処理天然ガスを冷却する手段は、このガスを主塔から抽出された精製天然ガスと熱交換させる第2熱交換器を有する。
− LGNを回収するユニットは、
(c1)そのドラムは液体ストリーム及びガスストリームを製造する、冷却された前処理天然ガスを分離する分離ドラム、
(c2)第1圧縮機に結合されている、前記ガスストリームを膨張する第1膨張タービン、
(c3)膨張されたガスストリームを中間のレベルN3で主塔に導入する手段、
(c4)液体ストリームを膨張する手段、及び膨張された液体ストリームをレベルN3の下のレベルN2で主塔に導入する手段
を有する。
− 主塔の塔頂から抽出された精製天然ガスを圧縮する手段は更に、外部エネルギー源で駆動される第2圧縮機を有し、圧縮された精製天然ガスの圧力を前記液化圧力に達するよう増加するべくなされている。
− 精製天然ガスを製造する手段は、前処理ユニットに直接由来する前処理天然ガスの調整可能な部分を液化天然ガスのラインに選択的に導入する手段を有する。
以上の特徴から個別に選択され、又は任意に組み合わせられ、1つ以上の特徴を有してよい。
Claims (13)
- 窒素、メタン、C2 乃至C5 の炭化水素及びC6 + 重質炭化水素を有する原料天然ガス(101)から液化天然ガス(161)と天然ガス液(NGL)留分(15)とを同時に製造する方法であって、
(a)原料天然ガス(101)は前処理天然ガス(111)を得るため前処理され、
(b)工程(a)で得られる前処理天然ガス(111)はその凝縮点に近い温度に冷却され、
(c)工程(b)で得られる冷却された前処理天然ガス(117)は膨張され、膨張された該天然ガス(121、127、129)は、一方で塔頂生成物として精製天然ガス(151)を、及び他方で前記NLG留分(15)を製造するために少なくとも1つの主蒸留塔(49)を有するNGL回収ユニット(19)に導入され、並びに
(d)液化天然ガス(161)は、工程(c)で得られる精製天然ガス(151)から製造される
以上の工程を有するタイプであり、
工程(a)は以下の
(a1)原料天然ガス(101)はその凝縮点に近い温度に冷却され、
(a2)工程(a1)で得られる冷却された原料天然ガス(103)は還流を行うオーバーヘッド還流冷却器(32)を設けられた補助蒸留塔(31)に導入され、補助蒸留塔(31)は45から65バールの間の圧力で操作され塔頂生成物として前処理天然ガス(111)を製造し、前処理天然ガス(111)はC6 + 炭化水素を実質的に含まず、補助蒸留塔(31)は更にC6 + 重質炭化水素の留分(105)を必然的に生じる
という副工程を有し、
工程(c)は以下の
(c1)工程(b)で得られる冷却された前処理天然ガス(117)は、液体ストリーム(121)及びガスストリーム(125)を得るために分離ドラム(47)に導入され、
(c2)工程(c1)で得られるガスストリーム(125)は、第1圧縮機(53)に結合しているタービン(51)で膨張され、
(c3)工程(c2)で得られるストリーム(129)は中間のレベルN3で主塔(49)に導入され、
(c4)工程(c1)で得られる液体ストリーム(121)は膨張され、膨張された液体ストリーム(121)は、レベルN3の下のレベルN2で主塔(49)に導入される
という副工程を有し、及び
液化天然ガス(161)は更に工程(a)に直接由来する前処理天然ガス(111)の一部(115)を含む
ことを特徴とする方法。 - 工程(d)が以下の
(d1)主塔(49)の塔頂から抽出された精製天然ガス(151)は、少なくとも第1圧縮機(53)では液化圧力に圧縮され、
(d2)工程(d1)で得られる圧縮された精製天然ガス(155)は、液化天然ガス(161)を製造するために、第1熱交換器(41)で主塔(49)の塔頂から抽出された精製天然ガス(151)と熱交換することによって冷却される
という副工程を有することを特徴とする請求項1に記載の方法。 - 工程(b)が以下の
(b1)工程(a)で得られる前処理天然ガス(113)は、第2熱交換器(43)で第2主塔(49)から抽出された精製天然ガス(151)と熱交換することによって冷却される
という副工程を有することを特徴とする請求項2に記載の方法。 - 工程(d1)において、第1圧縮機(53)から得られる圧縮された精製天然ガス(153)は、前記液化圧力に達するように、外部エネルギー源(56)が供給されている第2圧縮機(55)で圧縮されることを特徴とする請求項2又は3に記載の方法。
- 主蒸留塔(49)の圧力は35バールより大きいことを特徴とする請求項1乃至4の何れか1つに記載の方法。
- 液化天然ガス(161)が殆ど又は完全に工程(a)に直接由来する前処理天然ガス(111)からなり、前記液化天然ガス(161)が比較的C2 乃至C5 の炭化水素に富む始動段階を有し、
液化天然ガス(161)に所望のC2 乃至C5 の炭化水素含有量に従って、工程(a)に直接由来する前処理天然ガス(111)の一部(115)が液化天然ガス(161)に混合調整される製造段階を引き続き有する
ことを特徴とする請求項1乃至5の何れか1つに記載の方法。 - 補助塔(31)によって製造される液体(105)は膨張され、主塔(49)に導入されることを特徴とする先行する請求項の何れか1つに記載の方法。
- 補助蒸留塔(31)は、原料天然ガス(101)が有するC6 + 炭化水素の約98モル%を抽出するように設計されていることを特徴とする先行する請求項の何れか1つに記載の方法。
- 前処理天然ガス(111)中のC6 + 炭化水素のモル組成は約57ppmに等しいことを特徴とする先行する請求項の何れか1つに記載の方法。
- 窒素、メタン、C2 乃至C5 の炭化水素及びC6 + 重質炭化水素を有する原料天然ガス(101)から液化天然ガス(161)と天然ガス液(LGN)留分(15)とを同時に製造する設備であって、
(a)前処理天然ガス(111)を得るため原料天然ガス(11)を前処理するユニット(17)、
(b)その凝縮点に近い温度に前処理天然ガス(111)を冷却する手段(43)、
(c)冷却された前処理天然ガス(117)を膨張する手段(51,123,131)を有し、一方で塔頂生成物として精製天然ガス(151)を、及び他方で前記LGN留分(15)を製造する少なくとも1つの主蒸留塔(49)を有する、LGNを回収するユニット(19)、及び
(d)工程(c)で得られる精製天然ガス(151)から液化天然ガスを製造する手段(53,55,41)
を備えるタイプであり、
前処理ユニット(17)は、
(a1)その凝縮点に近い温度に原料天然ガス(101)を冷却する手段(25,27,29)、及び
(a2)補助塔は還流を行うオーバーヘッド還流冷却器(32)を設けられ、補助蒸留塔(31)は45から65バールの間の圧力で操作され塔頂生成物としてC6 + 炭化水素を実質的に含まない前処理天然ガス(111)を製造し、補助蒸留塔は更にC6 + 重質炭化水素の留分(105)を必然的に生じる、冷却された原料天然ガス(103)を蒸留する補助蒸留塔(31)
を有し、
LGNを回収するユニット(19)は、
(c1)ドラム(47)は液体ストリーム(121)及びガスストリーム(119)を製造する、冷却された前処理天然ガス(117)を分離する分離ドラム、
(c2)第1圧縮機(53)に結合されている、前記ガスストリームを膨張する第1膨張タービン(51)、
(c3)膨張されたガスストリーム(129)を中間のレベルN3で主塔(49)に導入する手段、
(c4)液体ストリーム(121)を膨張する手段(123)、及び膨張された液体ストリームをレベルN3の下のレベルN2で主塔(49)に導入する手段
を有し、及び
液化天然ガス(161)を製造する手段は、前処理ユニット(17)に直接由来する前処理天然ガス(111)の調整可能な部分(115)を液化天然ガス(161)のラインに選択的に導入する手段を有する
ことを特徴とする設備。 - 液化天然ガス(161)を製造する手段(53,55,41)は、
(d1)主塔(49)の塔頂から抽出された精製天然ガス(151)を液化圧力に圧縮し、少なくとも第1圧縮機(53)を有する手段(53,55)、及び
(d2)圧縮手段(53,55)由来の圧縮された精製天然ガス(155)を主塔(49)の塔頂から抽出された精製天然ガス(151)と熱交換させる第1熱交換器(41)であって、液化天然ガス(161)を製造するために、圧縮された精製天然ガス(155)を冷却する第1熱交換器(41)
を備えることを特徴とする請求項10に記載の設備。 - 前処理天然ガス(111)を冷却する手段(43)は、ガス(111)を主塔(49)から抽出された精製天然ガス(151)と熱交換させる第2熱交換器(43)を有することを特徴とする請求項11に記載の設備。
- 主塔(49)の塔頂から抽出された精製天然ガス(151)を圧縮する手段(53,55)は更に、外部エネルギー源で駆動される第2圧縮機(55)を有し、圧縮された精製天然ガス(155)の圧力を前記液化圧力に達するよう増加するべくなされていることを特徴とする請求項11又は12に記載の方法。
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Application Number | Priority Date | Filing Date | Title |
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FR0306632A FR2855526B1 (fr) | 2003-06-02 | 2003-06-02 | Procede et installation de production simultanee d'un gaz naturel apte a etre liquefie et d'une coupe de liquides du gaz naturel |
PCT/FR2004/001334 WO2004108865A2 (fr) | 2003-06-02 | 2004-05-28 | Procede et installation de production simultanee d'un gaz naturel apte a etre liquefie et d'une coupe de liquides du gaz naturel. |
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JP2007526924A true JP2007526924A (ja) | 2007-09-20 |
JP4669473B2 JP4669473B2 (ja) | 2011-04-13 |
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JP2010523924A (ja) * | 2006-03-31 | 2010-07-15 | ハネウェル・インターナショナル・インコーポレーテッド | 液化天然ガス(lng)プロセスの調整および最適化のためのシステムおよび方法 |
JP2012141128A (ja) * | 2005-07-12 | 2012-07-26 | Conocophillips Co | 液体復元及び生成の汎用性を拡張する統合nglを有するlng設備 |
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Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2012141128A (ja) * | 2005-07-12 | 2012-07-26 | Conocophillips Co | 液体復元及び生成の汎用性を拡張する統合nglを有するlng設備 |
JP2010523924A (ja) * | 2006-03-31 | 2010-07-15 | ハネウェル・インターナショナル・インコーポレーテッド | 液化天然ガス(lng)プロセスの調整および最適化のためのシステムおよび方法 |
JP2009533644A (ja) * | 2006-04-12 | 2009-09-17 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ | 天然ガス流の液化方法及び装置 |
KR101561385B1 (ko) * | 2014-03-28 | 2015-10-27 | 영남대학교 산학협력단 | 천연가스의 예비 분리를 통한 천연가스오일 회수방법 |
Also Published As
Publication number | Publication date |
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CA2527381C (fr) | 2012-03-13 |
WO2004108865A3 (fr) | 2005-02-17 |
CA2527381A1 (fr) | 2004-12-16 |
KR20060021869A (ko) | 2006-03-08 |
US7237407B2 (en) | 2007-07-03 |
FR2855526B1 (fr) | 2007-01-26 |
CN100588702C (zh) | 2010-02-10 |
WO2004108865A2 (fr) | 2004-12-16 |
PT1639062E (pt) | 2007-08-09 |
US20040244415A1 (en) | 2004-12-09 |
DE602004006266D1 (de) | 2007-06-14 |
ATE361352T1 (de) | 2007-05-15 |
PL1639062T3 (pl) | 2007-11-30 |
TW200503815A (en) | 2005-02-01 |
KR101062153B1 (ko) | 2011-09-05 |
FR2855526A1 (fr) | 2004-12-03 |
DE602004006266T2 (de) | 2008-01-10 |
JP4669473B2 (ja) | 2011-04-13 |
EP1639062A2 (fr) | 2006-03-29 |
CY1106780T1 (el) | 2012-05-23 |
MXPA05012952A (es) | 2006-02-28 |
CN1813046A (zh) | 2006-08-02 |
EP1639062B1 (fr) | 2007-05-02 |
ES2286670T3 (es) | 2007-12-01 |
TWI352614B (en) | 2011-11-21 |
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