JP2009503127A - 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 - Google Patents
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 Download PDFInfo
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- JP2009503127A JP2009503127A JP2008521451A JP2008521451A JP2009503127A JP 2009503127 A JP2009503127 A JP 2009503127A JP 2008521451 A JP2008521451 A JP 2008521451A JP 2008521451 A JP2008521451 A JP 2008521451A JP 2009503127 A JP2009503127 A JP 2009503127A
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Abstract
Description
[表1]
[表2]
本願明細書は本発明に関連する特定のパラメーターを定量化するために数値範囲を用いる。数値範囲が設けられた場合、当該範囲は、範囲の下限値のみを述べる請求項の制限及び範囲の上限のみを述べる請求項の制限のために文字による支援を提供するものとして見なされるべきである。例えば、開示された10乃至100の数値範囲は、「10より大きい」(上限を有さない)を述べる請求項、及び「100より小さい」(下限を有さない)を述べる請求項の文字による支援を提供する。
本願明細書で用いられるように、用語「天然ガス」は、エタン、高級炭化水素、窒素、二酸化炭素、及び/又は水銀、硫化水素、及びメルカプタンのような少量の他の成分と均衡を保っている、少なくとも65モル・パーセントのメタンを有するストリームを意味する。
Claims (62)
- 処理であって、液化天然ガス(LNG)を生成し、前記処理は、
(a)第1のLNG生成物を生成する第1の動作モードでLNG設備を動作する段階、
(b)前記LNG設備が第2の動作モードで動作するように前記LNG設備の少なくとも1つの非供給動作パラメーターを調整する段階、及び
(c)第2のLNG生成物を生成する第2の動作モードで前記LNG設備を動作する段階、を有し、
前記第1及び第2の動作モードは前記LNG設備の始動及び停止の間に実行されず、前記動作段階(a)及び(c)は任意的にそれぞれ第1及び第2の液体天然ガス(NGL)生成物を生成する段階を含み、前記第2のLNG生成物の平均高位発熱量(HHV)は前記第1のLNG生成物の平均HHVより少なくとも約10BTU/SCF異なり、及び/又は前記第2のNGL生成物の平均プロパン含有量は前記第1のNGL生成物の平均プロパン含有量より少なくとも約1モル・パーセント異なる、処理。 - 前記調整する段階(b)は、前記LNG設備を前記第1の動作モードから前記第2の動作モードへLNGの生成を停止することなく遷移する段階を含む、請求項1記載の処理。
- 前記調整する段階(b)は、前記LNG設備の蒸留塔の少なくとも1つの動作パラメーターを調整する段階を含む、請求項1記載の処理。
- 前記蒸留塔の動作パラメーターは、塔の供給成分、塔の供給温度、塔の塔頂圧力、還流ストリームの流速、還流ストリームの組成、還流ストリームの温度、ストリッピング・ガスの流速、ストリッピング・ガスの組成、及びストリッピング・ガスの温度を有するグループから選択された少なくとも1つの動作パラメーターを有する、請求項3記載の処理。
- 前記動作する段階(a)及び(c)は、前記蒸留塔を用いストリームを相対的高揮発性部分と相対的低揮発性部分とに分離する段階を含み、
前記第1及び第2のLNG生成物は前記相対的高揮発性部分の少なくとも一部を有し、及び/又は前記第1及び第2のNGL生成物は前記相対的低揮発性部分の少なくとも一部を有する、請求項3記載の処理。 - 前記第1及び第2のLNG生成物は前記相対的高揮発性部分の少なくとも一部を有し、及び前記第1及び第2のNGL生成物は前記相対的高揮発性部分の少なくとも一部を有する、請求項5記載の処理。
- 前記動作する段階(a)及び(c)は、天然ガス供給ストリームを冷却する段階、前記冷却された天然ガス供給ストリームを第1の相対的高揮発性部分と第1の相対的低揮発性部分とに第1の蒸留塔を用い分離する段階、及び前記第1及び第2のLNG生成物の少なくとも一部を生成するために前記第1の相対的高揮発性部分の少なくとも一部を更に冷却する段階を含む、請求項1記載の処理。
- 前記動作する段階(a)及び(c)は、前記第1の相対的低揮発性部分の少なくとも一部を第2の相対的高揮発性部分と第2の相対的低揮発性部分とに第2の分留塔を用い分離する段階を含む、請求項7記載の処理。
- 前記動作する段階(a)及び(c)は、前記第1及び第2のLNG生成物の少なくとも一部を生成するために、前記第2の相対的高揮発性部分の少なくとも一部を更に冷却する段階を含む、請求項8記載の処理。
- 前記第1及び第2のNGL生成物は、前記第2の相対的低揮発性部分の少なくとも一部を有する、請求項8記載の処理。
- 前記天然ガス供給ストリームの冷却の少なくとも一部は、大気圧で純粋なプロパンの沸点の約20度Fの範囲内の中間沸点を有する第1の冷媒を利用する第1の冷却サイクルを用い実行される、請求項7記載の処理。
- 前記第1の相対的高揮発性部分の更なる冷却の少なくとも一部は、大気圧で純粋なメタンの沸点の約20度Fの範囲内の中間沸点を有する第2の冷媒を利用する第2の冷却サイクルを用い実行される、請求項11記載の処理。
- 前記第1の相対的高揮発性部分の更なる冷却の少なくとも一部は、大気圧で純粋なエチレンの約20度Fの範囲内の中間沸点を有する第3の冷媒を利用する第3の冷却サイクルを用い実行される、請求項12記載の処理。
- 前記第1、第2、及び第3の冷媒は純粋な成分の冷媒である、請求項13記載の処理。
- 前記動作する段階(a)及び(c)は、第1の蒸留塔を用い第1のストリームを第1の相対的高揮発性部分と第1の相対的低揮発性部分とに分離する段階、及び第2の蒸留塔を用い前記第1の相対的低揮発性部分の少なくとも一部を第2の相対的高揮発性部分と第2の相対的低揮発性部分とに分離する段階を含む、請求項1記載の処理。
- 前記第1及び第2のLNG生成物は、前記第1及び第2の相対的高揮発性部分の少なくとも一部を有する、請求項15記載の処理。
- 前記第1及び第2のNGL生成物は、前記第2の相対的低揮発性部分の少なくとも一部を有する、請求項15記載の処理。
- 前記少なくとも1つの非供給動作パラメーターは、前記第1及び/又は第2の蒸留塔の動作パラメーターである、請求項15記載の処理。
- 前記第1の蒸留塔は、前記第2の相対的高揮発性部分の少なくとも一部を還流される、請求項17記載の処理。
- 前記調整する段階(b)は、前記第1の蒸留塔への還流の温度及び/又は流速を調整する段階を含む、請求項19記載の処理。
- 前記第2のLNG生成物の平均HHVは、前記第1のLNG生成物の平均HHVより少なくとも約10BTU/SCF異なる、請求項1記載の処理。
- 前記第2のNGL生成物の平均プロパン含有量は、前記第1のNGL生成物の平均プロパン含有量より少なくとも約1モル・パーセント異なる、請求項1記載の処理。
- 前記第2のLNG生成物の平均HHVは、前記第1のLNG生成物の平均HHVより少なくとも約20BTU/SCF異なる、請求項1記載の処理。
- 前記第2のNGL生成物の平均プロパン含有量は、前記第1のNGL生成物の平均プロパン含有量より少なくとも約2モル・パーセント異なる、請求項1記載の処理。
- 前記第1のLNG生成物は少なくとも1週間の第1の生成時間期間に渡り生成され、前記第2のLNG生成物は少なくとも1週間の第2の生成時間期間に渡り生成され、前記第1及び第2の生成時間期間は1週間より少ない遷移時間期間により分けられる、請求項1記載の処理。
- 前記遷移時間期間は1日より少ない、請求項1記載の処理。
- 方法であって、LNG設備から生成されるLNGの発熱量を変化し、前記方法は、
(a)間接熱交換により天然ガスを冷却し、第1の冷却ストリームを生成する段階、
(b)第1の蒸留塔を用い、前記第1の冷却ストリームの少なくとも一部を第1の相対的高揮発性部分及び第1の相対的低揮発性部分に分離する段階、
(c)前記第1の相対的高揮発性部分の少なくとも一部を冷却し、LNGを生成する段階、並びに
(d)前記第1の蒸留塔の少なくとも1つの動作パラメーターを調整し、前記生成されたLNGの高位発熱量(HHV)を少なくとも約1パーセントだけ約72時間より少ない時間期間に渡り変化する段階、を有する方法。 - 前記第1の蒸留塔の少なくとも1つの動作パラメーターは、前記第1の冷却ストリームの温度、前記第1の冷却ストリームの組成、及び前記第1の蒸留塔の塔頂圧力を有するグループから選択される、請求項27記載の方法。
- 前記第1の蒸留の少なくとも1つの動作パラメーターは、非供給動作パラメーターである、請求項27記載の方法。
- 段階(d)は前記第1の蒸留塔の塔頂圧力を調整する段階を含む、請求項27記載の方法。
- 段階(d)は前記第1の蒸留塔へ導入する前に前記第1の冷却ストリームの温度を調整する段階を含む、請求項27記載の方法。
- 段階(d)は前記第1の冷却ストリームの温度を低下し生成されたLNGのHHVを低下させる段階を含む、請求項31記載の方法。
- 前記第1の冷却ストリームは、前記第1の蒸留塔へ導入される時に約−125乃至約−50度Fの範囲の温度を有し、段階(d)は前記第1の冷却ストリームの温度を少なくとも約1度Fだけ低下する段階を含む、請求項32記載の方法。
- 前記第1の冷却ストリームは、前記第1の蒸留塔へ導入される時に約−115乃至約−65度Fの範囲の温度を有し、段階(d)は前記第1の冷却ストリームの温度を少なくとも約3度Fだけ低下する段階を含む、請求項32記載の方法。
- 段階(b)は主に気体のストリッピング・ガス・ストリームを前記第1の蒸留塔の下側部分へ導入する段階を含む、請求項27記載の方法。
- 前記第1の蒸留塔の少なくとも1つの動作パラメーターは、前記ストリッピング・ガス・ストリームの流速、前記ストリッピング・ガス・ストリームの温度、前記ストリッピング・ガス・ストリームの組成、前記第1の冷却ストリームの温度、前記第1の冷却ストリームの組成、及び前記第1の蒸留塔の塔頂圧力を有するグループから選択される、請求項35記載の方法。
- 段階(d)は前記第1の蒸留塔へのストリッピング・ガス・ストリームの流速を変化する段階を含む、請求項35記載の方法。
- 段階(d)は前記第1の蒸留塔への前記ストリッピング・ガス・ストリームの流速を低下し生成されたLNGのHHVを低下させる段階を含む、請求項35記載の方法。
- 前記第1の冷却ストリームは、前記第1の蒸留塔へ導入される時に約−125乃至約−50度Fの範囲の温度を有し、前記ストリッピング・ガス・ストリームは、前記第1の蒸留塔へ導入される時に約−50乃至約100度Fの範囲の温度を有し、段階(d)は前記ストリッピング・ガス・ストリームの温度を少なくとも5度Fだけ低下し生成されたLNGのHHVを低下する段階を含む、請求項35記載の方法。
- 段階(b)は主に液体の還流ストリームを前記第1の蒸留塔の上側部分へ導入する段階を含む、請求項27記載の方法。
- 前記第1の蒸留塔の少なくとも1つの動作パラメーターは、前記還流ストリームの流速、前記還流ストリームの温度、前記還流ストリームの組成、前記第1の冷却ストリームの温度、前記第1の冷却ストリームの組成、及び前記第1の蒸留塔の塔頂圧力を有するグループから選択される、請求項40記載の方法。
- 段階(d)は前記第1の蒸留塔への還流ストリームの流速を変化する段階を含む、請求項40記載の方法。
- 段階(d)は前記第1の蒸留塔への前記還流ストリームの流速を増加し生成されたLNGのHHVを低下させる段階を含む、請求項40記載の方法。
- 段階(d)は前記還流ストリームのC2+含有量を変化する段階を含む、請求項40記載の方法。
- 段階(d)は前記還流ストリームのC2+含有量を初期C2+含有量から調整されたC2+含有量まで増大し、生成されたLNGのHHVを低下させる段階を含む、請求項40記載の方法。
- 前記調整されたC2+含有量は初期C2+含有量よりモル方式で少なくとも約10パーセント多い、請求項45記載の方法。
- 前記初期C2+含有量は約75モル・パーセントより少なく、前記調整されたC2+含有量は少なくとも約25モル・パーセントである、請求項45記載の方法。
- 段階(d)は前記還流ストリームの温度を変化する段階を含む、請求項40記載の方法。
- 前記第1の冷却ストリームは、前記第1の蒸留塔へ導入される時に約−125乃至約−50度Fの範囲の温度を有し、前記還流ストリームは、前記第1の蒸留塔へ導入される時に約−180乃至約−80度Fの範囲の温度を有し、段階(d)は前記還流ストリームの温度を少なくとも5度Fだけ低下し生成されたLNGのHHVを低下する段階を含む、請求項40記載の方法。
- 段階(d)は前記第1の蒸留塔へのLNGストリームの流速を変化する段階を含む、請求項40記載の方法。
- 段階(d)は前記第1の蒸留塔へのLNGストリームの流速を増加し生成されたLNGのHHVを低下させる段階を有する、請求項40記載の方法。
- (e)第2の蒸留塔を用い、前記第1の相対的低揮発性部分の少なくとも一部を第2の相対的高揮発性部分と第2の相対的低揮発性部分とに分離する段階、を更に有する請求項27記載の方法。
- (f)前記第2の相対的低揮発性部分の少なくとも一部を前記第1の蒸留塔の上側部分に還流ストリームとして導入する段階、を更に有する請求項52記載の方法。
- (g)前記第2の蒸留塔の少なくとも1つの動作パラメーターを調整し、生成されたLNGのHHVを変化する段階、を更に有する請求項52記載の方法。
- 前記第2の蒸留塔の少なくとも1つの動作パラメーターは、前記第2の蒸留塔へ導入される前記第1の相対的低揮発部分の温度、前記第2の蒸留塔へ導入される前記第1の相対的低揮発部分の組成、及び前記第2の蒸留塔の塔頂圧力を有するグループから選択される、請求項54記載の方法。
- (h)前記第2の相対的低揮発性部分の少なくとも一部を前記第1の蒸留塔の上側部分に還流ストリームとして導入する段階、を更に有し、段階(g)は前記還流ストリームのC2+含有量を変化する段階を含む、請求項54記載の方法。
- 段階(a)は、主にプロパンを有する第1の冷媒を利用する第1の冷却サイクルを用い、前記天然ガスの少なくとも一部を冷却する段階を含む、請求項27記載の方法。
- 段階(c)は、主にエタン、エチレン、及び/又はメタンを有する第2の冷媒を利用する第2の冷却サイクルを用い、前記第1の分離されたストリームの少なくとも一部を冷却する段階を含む、請求項57記載の方法。
- 前記第2の冷媒は主にメタンを有する、請求項58記載の方法。
- (i)主にエタン及び/又はエチレンを有する第3の冷媒を利用する第3の冷却サイクルを用い、前記第1の冷却ストリームの少なくとも一部及び/又は前記第1の分離されたストリームの少なくとも一部を冷却する段階、を更に有する請求項59記載の方法。
- 段階(d)は生成されたLNGのHHVを少なくとも約3パーセントだけ約24時間より少ない時間期間に渡り変化する段階を含む、請求項27記載の方法。
- 段階(d)は生成されたLNGのHHVを少なくとも5パーセントだけ約12時間より少ない時間期間に渡り変化する段階を含む、請求項27記載の方法。
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WO2007008638A2 (en) | 2007-01-18 |
JP5256034B2 (ja) | 2013-08-07 |
KR101319793B1 (ko) | 2013-10-22 |
KR101431399B1 (ko) | 2014-08-18 |
EA015525B1 (ru) | 2011-08-30 |
AU2006269366A1 (en) | 2007-01-18 |
WO2007008638A3 (en) | 2009-05-07 |
KR20130036345A (ko) | 2013-04-11 |
MY152617A (en) | 2014-10-31 |
US20120042690A1 (en) | 2012-02-23 |
KR20080033937A (ko) | 2008-04-17 |
JP2012141128A (ja) | 2012-07-26 |
AU2006269366B2 (en) | 2012-03-08 |
US20070012072A1 (en) | 2007-01-18 |
CN101506605B (zh) | 2013-04-24 |
US9841231B2 (en) | 2017-12-12 |
JP5686755B2 (ja) | 2015-03-18 |
PE20100530A1 (es) | 2010-08-20 |
EA200800296A1 (ru) | 2008-06-30 |
PE20070467A1 (es) | 2007-06-14 |
CN101506605A (zh) | 2009-08-12 |
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