JP4673406B2 - 液化天然ガスからの二段式の窒素除去 - Google Patents
液化天然ガスからの二段式の窒素除去 Download PDFInfo
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- JP4673406B2 JP4673406B2 JP2008507153A JP2008507153A JP4673406B2 JP 4673406 B2 JP4673406 B2 JP 4673406B2 JP 2008507153 A JP2008507153 A JP 2008507153A JP 2008507153 A JP2008507153 A JP 2008507153A JP 4673406 B2 JP4673406 B2 JP 4673406B2
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- nitrogen
- stream
- natural gas
- overhead vapor
- enriched overhead
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims description 333
- 229910052757 nitrogen Inorganic materials 0.000 title claims description 166
- 239000003949 liquefied natural gas Substances 0.000 title claims description 113
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 85
- 239000007788 liquid Substances 0.000 claims description 77
- 239000007789 gas Substances 0.000 claims description 39
- 238000000034 method Methods 0.000 claims description 39
- 239000003345 natural gas Substances 0.000 claims description 37
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 28
- 238000001816 cooling Methods 0.000 claims description 27
- 238000010992 reflux Methods 0.000 claims description 27
- 239000003507 refrigerant Substances 0.000 claims description 23
- 238000005194 fractionation Methods 0.000 claims description 21
- 238000004821 distillation Methods 0.000 claims description 20
- 239000002737 fuel gas Substances 0.000 claims description 19
- 238000004781 supercooling Methods 0.000 claims description 11
- 239000012530 fluid Substances 0.000 claims description 4
- 239000002826 coolant Substances 0.000 claims description 2
- 239000001307 helium Substances 0.000 description 26
- 229910052734 helium Inorganic materials 0.000 description 26
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 26
- 239000000047 product Substances 0.000 description 20
- 238000000926 separation method Methods 0.000 description 16
- 238000009833 condensation Methods 0.000 description 9
- 230000005494 condensation Effects 0.000 description 9
- 239000000446 fuel Substances 0.000 description 7
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Description
燃料ガスにより動力が与えられるガスタービンによって仕事が供給される循環冷媒システムによって熱交換器冷却負荷が提供される、液化部と過冷却部とを有するスパイラル式(spiral−wound)熱交換器に、窒素含有天然ガス流を供給すること、
前記液化部の後で液化ガス流を抜き出すこと、
前記液化ガス流に蒸留塔での第1の分別を受けさせて第1の窒素富化オーバーヘッド蒸気流と窒素含有ボトム液体流とを提供すること、
前記ボトム液体流の少なくとも一部分を前記過冷却部で過冷却し、そして当該部分を減圧すること、
当該減圧した部分にフラッシュドラムで第2の分別を受けさせて、前記第1のオーバーヘッド蒸気流よりも低い純度の第2の窒素富化オーバーヘッド蒸気流と、精製液化天然ガス流とを提供すること、
第1の窒素富化オーバーヘッド蒸気流の一部分を前記フラッシュドラムで凝縮させてそこでの熱負荷を提供し、そして凝縮された窒素富化オーバーヘッド流を生じさせること、
当該凝縮された窒素富化オーバーヘッド流の少なくとも一部分を蒸留塔に還流として戻すこと、及び、
前記第2の窒素富化オーバーヘッド蒸気流を燃料ガスの少なくとも成分として使用すること、
を含む。
窒素含有天然ガス原料を液化するための冷却システム、
第1の分別装置、
第2の分別装置、
冷却システムから第1の分別装置へ窒素含有液化天然ガスを供給するための導管、
第1の分別装置から第1の窒素富化オーバーヘッド蒸気流を取り出すための導管、
第1の分別装置から窒素含有ボトム液体流を第2の分別装置に送るための導管、
第2の分別装置から第2の窒素富化オーバーヘッド蒸気流を取り出すための導管、及び、
第2の分別装置から精製液化天然ガス流を取り出すための導管、
を含む装置も提供する。
この例は、図1の態様に基づくものである。このLNGプロセスには、4.8mol%の窒素を含有し、残りは主にメタンである周囲温度及び900psia(6.2MPa)の圧力の88,000ポンドモル/h(40,000kgmol/h)の原料天然ガスが供給される。原料ガスを乾燥させ、予冷し、そして分離塔7において、−38°F(−39℃)の温度及び約850psia(5.8MPa)の圧力で熱交換器16に入るように前処理する。流れ17は、−178°F(−116.5℃)の温度で熱交換器16を出て、220psia(1.5MPa)に減圧してから、220psia(1.5MPa)で運転する窒素除去塔23へ供給される。塔23の底部から流れ19を抜き出し、熱交換器16で−247°F(−155℃)まで更に冷却する。次に、熱交換器16を出た流れ20を低圧にしてフラッシュドラム25に送る。フラッシュドラム25から、−261°F(−163℃)の温度で窒素含有量1.5mol%未満の製品LNG流50を抜き出す。燃料流36をフラッシュドラム25から、流量7,900ポンドモル/h(3,600kgmol/h)、窒素含有量30mol%で抜き出す。窒素放出流26を塔23の頂部から、流量600ポンドモル/h(272kgmol/h)、窒素含有量98.0mol%、そして温度−257°F(−160.5℃)で抜き出す。
この例は、図5の粗ヘリウム抽出の増強を伴う図1の態様に基づくものである。このLNGプロセスには、4.8mol%の窒素及び600ppmvのヘリウムを含有し、残りは主にメタンである、周囲温度及び900psia(6.2MPa)の圧力の88,000ポンドモル/h(40,000kgmol/h)の原料天然ガスが供給される。原料ガスを乾燥させ、予冷し、そして分離塔7において、−38°F(−39℃)の温度及び約850psia(5.9MPa)の圧力で熱交換器16に入るように前処理する。流れ17は、−178°F(−116.5℃)の温度で熱交換器16を出て、220psia(1.5MPa)に減圧してから、220psia(1.5MPa)で運転する窒素塔23へ供給される。塔23の底部から流れ19を抜き出し、熱交換器16で−247°F(−155℃)まで更に冷却する。次に、熱交換器16を出た流れ20を低圧にしてフラッシュドラム25に送る。フラッシュドラム25から、−261°F(−163℃)の温度で窒素含有量1.5mol%未満の製品LNG流50を抜き出す。流量7,900ポンドモル/h(3,600kgmol/h)、窒素含有量30mol%で、フラッシュドラム25から燃料流36を抜き出す。流量710ポンドモル/h(322kgmol/h)、窒素含有量98.0mol%、温度−259°F(−161.5℃)、そして圧力220psia(1.5MPa)で、塔23の頂部から窒素放出流26を抜き出す。図5を参照すると、流れ26を熱交換器70において、戻り流73及び76との熱交換で−298°F(−183.5℃)の温度まで冷却し、そして分離器72で液体流と蒸気流とに分離する。液体流を、流れ76が−310°F(−190℃)の温度に達するジュール−トムソン冷却をもたらす低圧にする。液体流76及び蒸気流73の両方を交換器70で再加温する。流れ77は、流量が656ポンドモル/h(297.5kgmol/h)、窒素含有量が97.5%の窒素放出流である。流れ78は、流量が54ポンドモル/h(24.5kgmol/h)、ヘリウム濃度が74mol%の粗ヘリウム製品流である。
Claims (10)
- 窒素を含まなくした液化天然ガス流(50)を製造する方法であって、
ガスタービンにより提供される仕事を利用して、窒素を含有する天然ガス(15)を液化(16)して窒素含有液化天然ガス流(41)を提供すること、
この液化天然ガス流に蒸留塔(23)での第1の分別を受けさせて第1の窒素富化オーバーヘッド蒸気流(46)と窒素含有ボトム液体流(19)とを提供すること、
前記ボトム液体流(19)の少なくとも一部分(20)を、前記液化天然ガス流に由来しない冷媒流体(39)により供給される寒冷を利用して過冷却(16)し、減圧(21)すること、
前記過冷却し減圧した部分(42)に、前記第1の窒素富化オーバーヘッド蒸気流(46)の一部分を凝縮させることにより提供される熱交換負荷を利用して、フラッシュドラム(25)における第2の分別(25)を受けさせて、前記第1のオーバーヘッド蒸気流(46)よりも低い純度の第2の窒素富化オーバーヘッド蒸気流(36)と、精製液化天然ガス流とを提供すること、
前記蒸留塔(23)に凝縮された第1の窒素富化オーバーヘッド蒸気(45)を還流させ、そして
前記窒素富化オーバーヘッド蒸気流(46、36)のうちの、第1のもの(46)でなく、第2のもの(36)を、前記ガスタービンで使用される燃料ガスとして使用し、あるいはそれに加えること、
を含む、窒素を含まなくした液化天然ガス流の製造方法。 - 前記窒素含有ボトム液体流(19)の全体を前記フラッシュドラム(25)に供給する、請求項1に記載の方法。
- 前記過冷却された窒素含有ボトム液体流(20)の一部分(54)だけを前記フラッシュドラム(25)に供給し、そして残り(53)は、前記第1のオーバーヘッド蒸気流(46)よりも低い純度の第3の窒素富化オーバーヘッド蒸気流(55)と第2の精製液化天然ガス流(51)とに分離するための第2のフラッシュドラム(52)に供給する、請求項1に記載の方法。
- 前記第1の窒素富化オーバーヘッド蒸気流(46)の窒素濃度が80mol%を超える、請求項1から3までのいずれか1項に記載の方法。
- 前記第1の窒素富化オーバーヘッド蒸気流(46)の窒素濃度が90mol%を超える、請求項4に記載の方法。
- 前記第1の窒素富化オーバーヘッド蒸気流(46)の窒素濃度が95mol%を超える、請求項5に記載の方法。
- 前記窒素含有天然ガス(15)を液化部と過冷却部とを有するスパイラル式熱交換器(16)で液化させ、前記窒素含有液化天然ガス流を該液化部の後で抜き出し、そして前記蒸留塔(23)からの前記ボトム液体流を該過冷却部で過冷却する、請求項1から6までのいずれか1項に記載の方法。
- 燃料ガスにより動力が与えられる前記ガスタービンによって仕事が供給される循環冷媒システム(27〜89)によって熱交換器冷却負荷が提供される、液化部と過冷却部とを有するスパイラル式熱交換器(16)に、前記窒素含有天然ガス流(15)を供給すること、
前記液化部の後で液化ガス流(17)を抜き出すこと、
前記液化ガス流に前記蒸留塔(23)での第1の分別を受けさせて前記第1の窒素富化オーバーヘッド蒸気流(46)と前記窒素含有ボトム液体流(19)とを提供すること、
前記ボトム液体流の少なくとも一部分(19)を前記熱交換器(16)の前記過冷却部で過冷却し、そして当該一部分を減圧(21)すること、
当該減圧した一部分に前記フラッシュドラム(25)での第2の分別を受けさせて、前記第1のオーバーヘッド蒸気流(46)よりも低い純度の前記第2の窒素富化オーバーヘッド蒸気流と、前記精製液化天然ガス流(50)とを提供すること、
前記第1の窒素富化オーバーヘッド蒸気流の一部分を前記フラッシュドラムで凝縮させてそこでの熱負荷を提供し、そして前記凝縮された窒素富化オーバーヘッド流(44)を生じさせること、
当該凝縮された窒素富化オーバーヘッド流の少なくとも一部分(45)を前記蒸留塔(23)に還流として戻すこと、及び、
前記第2の窒素富化オーバーヘッド蒸気流(36)を燃料ガスの少なくとも成分として使用すること、
を含む、請求項7に記載の方法。 - 請求項1に記載の方法によって、窒素を含まなくした液化天然ガス流を製造するための装置であって、
窒素含有天然ガス原料(15)を液化するための冷却システム(16)、
前記冷却システム(16)に関連して用いるための仕事を提供するガスタービン、
蒸留塔(23)、
フラッシュドラム(25)、
前記フラッシュドラム内のコンデンサー(24)、
冷媒流体(39)から冷却負荷を受け取るための熱交換器(16)、
前記冷却システム(16)から前記蒸留塔(23)へ窒素含有液化天然ガスを供給するための導管手段(17、41)、
前記蒸留塔(23)から第1の窒素富化オーバーヘッド蒸気流を取り出すための導管手段(46)、
前記第1の窒素富化オーバーヘッド蒸気流の一部分を前記コンデンサー(25)に送るための導管手段(43)、
凝縮された第1の窒素富化オーバーヘッド蒸気流を前記コンデンサー(25)から前記蒸留塔(23)に還流として戻すための導管手段(44、45)、
前記窒素含有ボトム液体流を前記蒸留塔(23)から前記熱交換器(24)に送るための導管手段(19)、
過冷却された窒素含有ボトム液体流を前記熱交換器から低下した圧力の前記フラッシュドラム(25)に送るための導管手段(20)、
前記第2の窒素富化オーバーヘッド蒸気流を前記フラッシュドラム(25)から取り出すための導管手段(36)、
前記精製液化天然ガス流を前記フラッシュドラムから取り出すための導管手段(50)、及び、
前記ガスタービンに前記第2の窒素富化オーバーヘッド蒸気流を燃料ガス供給物として供給するための導管手段(36)、
を含む、窒素を含まなくした液化天然ガス流の製造装置。 - 前記冷却システムが、液化部と過冷却部とを有するスパイラル式熱交換器(16)を含み、前記蒸留塔(23)に窒素含有液化天然ガスを供給するための前記導管手段(17、41)が、前記液化部の後で前記熱交換器から前記流れを抜き出し、そして前記過冷却部が、前記蒸留塔(23)からの窒素含有ボトム液体流を過冷却する熱交換器(16)を構成する、請求項9に記載の装置。
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EP05252524A EP1715267A1 (en) | 2005-04-22 | 2005-04-22 | Dual stage nitrogen rejection from liquefied natural gas |
PCT/GB2006/001390 WO2006111721A1 (en) | 2005-04-22 | 2006-04-18 | Dual stage nitrogen rejection from liquefied natural gas |
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EP (2) | EP1715267A1 (ja) |
JP (1) | JP4673406B2 (ja) |
KR (1) | KR100939515B1 (ja) |
CN (1) | CN101163934B (ja) |
AU (1) | AU2006238748B2 (ja) |
CA (1) | CA2605545C (ja) |
EG (1) | EG25070A (ja) |
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RU (1) | RU2355960C1 (ja) |
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MX2007013033A (es) | 2008-01-11 |
EP1872072B1 (en) | 2018-08-01 |
EG25070A (en) | 2011-07-27 |
AU2006238748A1 (en) | 2006-10-26 |
NO343069B1 (no) | 2018-10-22 |
JP2008537089A (ja) | 2008-09-11 |
RU2355960C1 (ru) | 2009-05-20 |
EP1715267A1 (en) | 2006-10-25 |
EP1872072A1 (en) | 2008-01-02 |
TWI273207B (en) | 2007-02-11 |
KR20080010417A (ko) | 2008-01-30 |
WO2006111721A1 (en) | 2006-10-26 |
CN101163934A (zh) | 2008-04-16 |
US20070245771A1 (en) | 2007-10-25 |
NO20075947L (no) | 2007-11-19 |
CA2605545C (en) | 2010-11-02 |
AU2006238748B2 (en) | 2010-04-01 |
CA2605545A1 (en) | 2006-10-26 |
US7520143B2 (en) | 2009-04-21 |
TW200638013A (en) | 2006-11-01 |
CN101163934B (zh) | 2012-03-14 |
KR100939515B1 (ko) | 2010-02-03 |
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