JP4763039B2 - Lng再ガス化の精製および発電との統合 - Google Patents
Lng再ガス化の精製および発電との統合 Download PDFInfo
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Description
Claims (21)
- 再沸器および塔頭凝縮器を有するC2またはC3炭化水素分離器と、
液化天然ガス流からの冷熱が、第1の交換流体を介して塔頭凝縮器にもたらされるように、液化天然ガス流および炭化水素分離器に熱的に結合されている第1の熱交換回路と、
熱源からの熱が、第2の交換流体を介して再沸器および液化天然ガス流に送られるように、熱源、炭化水素分離器、および液化天然ガス流に熱的に結合されている第2の熱交換回路とを備える、プラント。 - 熱源が、吸気冷却器、熱回収ユニット、燃焼廃ガス熱交換器、加熱炉、および海水交換器からなる群から選択される、請求項1に記載のプラント。
- 炭化水素分離器が、C2分離器である、請求項1に記載のプラント。
- 炭化水素分離器が、689.5kPaA(100psia)より小さな圧力で作動するように構成されている、請求項1に記載のプラント。
- 炭化水素分離器が、約206.8kPaA(30psi)と約413.7kPaA(60psia)の間の圧力で作動するように構成されている、請求項1に記載のプラント。
- 第1の熱交換回路が、液化天然ガス流が約−156.7℃(−250°F)の温度から約−73.3℃(−100°F)と−51.1℃(−60°F)の間の温度に加熱されるように構成され、液化天然ガス流に結合されている、請求項1に記載のプラント。
- 第2の熱交換回路が、液化天然ガス流が約−73.3℃(−100°F)と−51.1℃(−60°F)の間の温度から約4.4℃(40°F)の温度に加熱されるように構成され、液化天然ガス流に結合されている、請求項1に記載のプラント。
- 底部生成物をC2またはC3炭化水素分離器にもたらすようにC2またはC3炭化水素分離器に流体的に結合された分割カラムをさらに備える、請求項1に記載のプラント。
- 分割カラムが、第1の熱交換回路に熱的に結合された還流凝縮器をさらに含む、請求項8に記載のプラント。
- 炭化水素分離器がC3分離器であり、分割カラムが脱エタン装置である、請求項8に記載のプラント。
- C2またはC3炭化水素分離器を運転する方法であって、
液化天然ガスによって冷却される第1の熱交換流体を使用して冷熱をC2またはC3炭化水素分離器の塔頭凝縮器にもたらすステップと、
熱源によって加熱される第2の熱交換流体を使用してC2またはC3炭化水素分離器の再沸器および液化天然ガスに熱をもたらすステップとを含む、方法。 - 熱源が、吸気冷却器、熱回収ユニット、燃焼廃ガス熱交換器、加熱炉、および海水交換器からなる群から選択される、請求項11に記載の方法。
- 炭化水素分離器が、C2分離器である、請求項11に記載の方法。
- 炭化水素分離器が、689.5kPaA(100psia)より小さな圧力で作動される、請求項11に記載の方法。
- 炭化水素分離器が、約206.8lPaA(30psia)と約413.7kPaA(60psia)の間の圧力で作動される、請求項11に記載の方法。
- 第1の熱交換流体が、液化天然ガス流を−156.7℃(−250°F)の温度から約−73.3℃(−100°F)と−51.1℃(−60°F)の間の温度に加熱する、請求項11に記載の方法。
- 第2の熱交換流体が、液化天然ガス流を約−73.3℃(−100°F)と−51.1℃(−60°F)の間の温度から4.4℃(40°F)の温度に加熱する、請求項11に記載の方法。
- 分割カラムが流体的にC2またはC3炭化水素分離器に結合され、それによって底部生成物がC2またはC3炭化水素分離器にもたらされる、請求項11に記載の方法。
- 分割カラムが、第1の熱交換流体に熱的に結合されている還流凝縮器をさらに含む、請求項18に記載の方法。
- 炭化水素分離器がC3分離器であり、分割カラムが脱エタン装置である、請求項18に記載の方法。
- 発電部分および液化天然ガス再ガス化部分を備えるプラントを運転する方法であって、
第1の熱交換流体を使用してカラムの塔頭凝縮能力をもたらすために液化天然ガスの冷熱を使用するステップと、
第2の熱交換流体を使用して該カラムの再沸能力をもたらすために発電部分からの熱を使用するステップとを含み、
第1および第2の熱交換流体が液化天然ガスを再ガス化するのに使用される、方法。
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Application Number | Priority Date | Filing Date | Title |
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US66700205P | 2005-03-30 | 2005-03-30 | |
US60/667,002 | 2005-03-30 | ||
PCT/US2006/010368 WO2006104799A2 (en) | 2005-03-30 | 2006-03-21 | Integrated of lng regasification with refinery and power generation |
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JP2008534741A JP2008534741A (ja) | 2008-08-28 |
JP4763039B2 true JP4763039B2 (ja) | 2011-08-31 |
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JP2008504156A Expired - Fee Related JP4763039B2 (ja) | 2005-03-30 | 2006-03-21 | Lng再ガス化の精製および発電との統合 |
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US (1) | US8316665B2 (ja) |
EP (1) | EP1864065A4 (ja) |
JP (1) | JP4763039B2 (ja) |
AU (1) | AU2006229877B2 (ja) |
CA (1) | CA2600155C (ja) |
EA (1) | EA011918B1 (ja) |
MX (1) | MX2007011839A (ja) |
NO (1) | NO20074396L (ja) |
WO (1) | WO2006104799A2 (ja) |
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EP1734027B1 (en) * | 2005-06-14 | 2012-08-15 | Toyo Engineering Corporation | Process and Apparatus for Separation of Hydrocarbons from Liquefied Natural Gas |
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AU2006229877B2 (en) | 2009-04-23 |
US20080307789A1 (en) | 2008-12-18 |
WO2006104799A2 (en) | 2006-10-05 |
EA200702111A1 (ru) | 2008-02-28 |
JP2008534741A (ja) | 2008-08-28 |
NO20074396L (no) | 2007-10-29 |
CA2600155C (en) | 2010-04-27 |
AU2006229877A1 (en) | 2006-10-05 |
EP1864065A4 (en) | 2017-12-20 |
WO2006104799B1 (en) | 2007-02-22 |
EA011918B1 (ru) | 2009-06-30 |
MX2007011839A (es) | 2007-11-22 |
WO2006104799A3 (en) | 2006-12-21 |
US8316665B2 (en) | 2012-11-27 |
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