JP6561196B2 - 天然ガス給送ストリームを予冷することによるlng生産システムにおける効率増大 - Google Patents
天然ガス給送ストリームを予冷することによるlng生産システムにおける効率増大 Download PDFInfo
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- JP6561196B2 JP6561196B2 JP2018501312A JP2018501312A JP6561196B2 JP 6561196 B2 JP6561196 B2 JP 6561196B2 JP 2018501312 A JP2018501312 A JP 2018501312A JP 2018501312 A JP2018501312 A JP 2018501312A JP 6561196 B2 JP6561196 B2 JP 6561196B2
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- natural gas
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- compressed
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 660
- 239000003345 natural gas Substances 0.000 title claims description 325
- 238000004519 manufacturing process Methods 0.000 title claims description 68
- 238000001816 cooling Methods 0.000 title claims description 36
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 180
- 239000003949 liquefied natural gas Substances 0.000 claims description 125
- 229910052757 nitrogen Inorganic materials 0.000 claims description 89
- 239000005431 greenhouse gas Substances 0.000 claims description 84
- 239000003507 refrigerant Substances 0.000 claims description 60
- 238000000034 method Methods 0.000 claims description 56
- 238000004821 distillation Methods 0.000 claims description 49
- 238000005292 vacuum distillation Methods 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000000047 product Substances 0.000 description 43
- 239000007788 liquid Substances 0.000 description 27
- 238000005057 refrigeration Methods 0.000 description 21
- 239000007789 gas Substances 0.000 description 17
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 14
- 230000000153 supplemental effect Effects 0.000 description 14
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 10
- 229910052799 carbon Inorganic materials 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 238000010586 diagram Methods 0.000 description 9
- 229910001868 water Inorganic materials 0.000 description 9
- 238000003860 storage Methods 0.000 description 8
- 229910052786 argon Inorganic materials 0.000 description 7
- 239000000356 contaminant Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 239000012530 fluid Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 5
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- 239000000498 cooling water Substances 0.000 description 4
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
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- 239000007787 solid Substances 0.000 description 2
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- 239000012808 vapor phase Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
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- 239000001273 butane Substances 0.000 description 1
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- 230000001276 controlling effect Effects 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
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- 239000000945 filler Substances 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000013529 heat transfer fluid Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000011221 initial treatment Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
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- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
Images
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- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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- F25J2270/00—Refrigeration techniques used
- F25J2270/58—Quasi-closed internal or closed external argon refrigeration cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
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Description
この出願は、本明細書に引用によりその全体が組み込まれている「天然ガス給送ストリームを予冷することによるLNG生産システムおける効率増大」という名称の2015年7月15日出願の米国特許出願第62/192,657号の優先権利益を主張するものである。
1.天然ガスのサプライからの天然ガスストリームと、冷媒サプライからの冷媒ストリームと、冷媒ストリームと天然ガスストリームの間で熱を交換し、冷媒ストリームを少なくとも部分的に気化させて天然ガスストリームを少なくとも部分的に凝結させる少なくとも1つの熱交換器と、天然ガスストリームを少なくとも135baraの圧力まで圧縮して圧縮天然ガスストリームを形成する天然ガス圧縮機と、天然ガス圧縮機によって圧縮された後で圧縮天然ガスストリームを冷却する天然ガス冷却機と、天然ガス冷却機によって冷却された後に、200bara未満の圧力であるが天然ガス圧縮機が天然ガスストリームを圧縮する圧力よりも高くない圧力まで圧縮天然ガスを膨脹させる天然ガス膨脹器とを含み、天然ガス膨脹器が、少なくとも1つの熱交換器にそこに天然ガスを供給するために接続された液化天然ガス生産システム。
2.天然ガス圧縮機が、200baraよりも高い圧力まで天然ガスストリームを圧縮する段落1による液化天然ガス生産システム。
3.天然ガス膨脹器が、135bara未満の圧力まで圧縮天然ガスストリームを膨脹させる段落1又は2による液化天然ガス生産システム。
4.少なくとも1つの熱交換器が、第1の熱交換器を含み、天然ガスストリームが天然ガス圧縮機内で圧縮される前に天然ガスストリームを冷却する第2の熱交換器を更に含む段落1〜3のいずれかによる液化天然ガス生産システム。
5.冷媒ストリームが、第2の熱交換器内で天然ガスストリームを冷却するのに使用される段落4による液化天然ガス生産システム。
6.少なくとも1つの熱交換器が、第1の熱交換器を含み、システムが、圧縮天然ガスストリームが天然ガス冷却機内で冷却される前に圧縮天然ガスストリームを冷却する第2の熱交換器を更に含む段落1〜5のいずれかによる液化天然ガス生産システム。
7.冷媒ストリームが、液化窒素ストリームを含み、少なくとも1つの熱交換器が、窒素ストリームを少なくとも部分的に気化させる段落1〜6のいずれかによる液化天然ガス生産システム。
8.少なくとも部分的に気化した窒素ストリームから温室効果ガスを除去するように構成された温室効果ガス除去ユニットを更に含む段落7による液化天然ガス生産システム。
9.温室効果ガス除去ユニットが、熱ポンプ凝縮器と再沸騰器システムとを有する蒸留塔を含み、システムが、少なくとも部分的に気化した窒素ストリームの圧力を低減する少なくとも1つの膨脹器サービスを更に含み、蒸留塔の入口ストリームが、少なくとも1つの膨脹器サービスのうちの第1のものの出口ストリームである段落8による液化天然ガス生産システム。
10.少なくとも部分的に気化した窒素ストリームが少なくとも1つの膨脹器サービスのうちの第1のものを通って流れた後でそれを通って流れる熱ポンプシステムを更に含む段落9による液化天然ガス生産システム。
11.熱ポンプシステムが、熱ポンプ圧縮機、熱ポンプ冷却機、及び給送−排出熱交換器を含む段落10による液化天然ガス生産システム。
12.天然ガスストリームが少なくとも1つの熱交換器に入る前に少なくとも部分的に気化した窒素ストリームを使用して天然ガスストリームを予冷する乾湿熱交換器を更に含む段落1〜9のいずれかによる液化天然ガス生産システム。
13.天然ガス冷却機が、天然ガス圧縮機によって圧縮された後で圧縮天然ガスストリームを周囲温度の近くまで冷却するように構成される段落1〜12のいずれかによる液化天然ガス生産システム。
14.天然ガスのサプライから天然ガスストリームを与える段階と、冷媒サプライから冷媒ストリームを与える段階と、冷媒ストリームと天然ガスストリームの間で熱を交換し、冷媒ストリームを少なくとも部分的に気化させて天然ガスストリームを少なくとも部分的に凝結させる第1の熱交換器に天然ガスストリーム及び液化窒素ストリームを通す段階と、少なくとも135baraの圧力まで天然ガス圧縮機内で天然ガスストリームを圧縮して圧縮天然ガスストリームを形成する段階と、天然ガス圧縮機によって圧縮された後で圧縮天然ガスストリームを天然ガス冷却機内で冷却する段階と、天然ガス冷却機によって冷却された後に200bara未満の圧力であるが天然ガス圧縮機が天然ガスストリームを圧縮する圧力よりも高くない圧力まで天然ガス膨脹器内で圧縮天然ガスを膨脹させる段階と、天然ガスを天然ガス冷却機から少なくとも1つの熱交換器にそこで少なくとも部分的に凝結されるように供給する段階とを含む液化天然ガス(LNG)を生産する方法。
15.天然ガス圧縮機が、200baraよりも高い圧力まで天然ガスストリームを圧縮する段落14による方法。
16.天然ガス膨脹器が、135bara未満の圧力まで圧縮天然ガスストリームを膨脹させる段落14又は15による方法。
17.少なくとも1つの熱交換器が、第1の熱交換器を含み、方法が、天然ガス圧縮機内で天然ガスストリームを圧縮する前に第2の熱交換器内で天然ガスストリームを冷却する段階を更に含む段落14〜16のいずれかによる方法。
18.冷媒ストリームを使用して第2の熱交換器内で天然ガスストリームを冷却する段落17による方法。
19.少なくとも1つの熱交換器が、第1の熱交換器を含み、方法が、天然ガス冷却機内で冷却される圧縮天然ガスストリームを冷却する前に第2の熱交換器内で圧縮天然ガスストリームを冷却する段階を更に含む段落14〜18のいずれかによる方法。
20.冷媒ストリームが、液化窒素ストリームを含み、少なくとも1つの熱交換器が、窒素ストリームを少なくとも部分的に気化させる段落14〜19のいずれかによる方法。
21.温室効果ガス除去ユニットを使用して少なくとも部分的に気化した窒素ストリームから温室効果ガスを除去する段階を更に含む段落20による方法。
22.温室効果ガス除去ユニットが、蒸留塔及び熱ポンプ凝縮器及び再沸騰器システムを含み、方法が、蒸留塔のオーバーヘッドストリームの圧力及び凝結温度を上昇させる段階と、蒸留塔のオーバーヘッドストリーム及び蒸留塔のボトムストリームを交差交換して蒸留塔のオーバーヘッド凝縮器デューティ及びボトム再沸騰器デューティの両方に影響を与える段階と、交差交換段階後に蒸留塔オーバーヘッドストリームの圧力を低減して減圧蒸留塔オーバーヘッドストリームを生成する段階と、減圧蒸留塔オーバーヘッドストリームを分離して、温室効果ガスがそこから除去された温室効果ガス除去ユニットを出るガス状窒素である第1の分離器オーバーヘッドストリームを生成する段階とを更に含む段落21による方法。
23.少なくとも1つの膨脹器サービスのうちの第1のものを通って流れた後に熱ポンプシステムを通して少なくとも部分的に気化した窒素ストリームを流す段階を更に含む段落22による方法。
24.天然ガス冷却機が、天然ガス圧縮機によって圧縮された後で圧縮天然ガスストリームが周囲温度の近くになるように冷却する段落14〜23のいずれかによる方法。
25.少なくとも135baraの圧力まで天然ガスストリームを天然ガス圧縮機内で圧縮して圧縮天然ガスストリームを形成する段階と、天然ガス圧縮機によって圧縮された後で圧縮天然ガスストリームを周囲温度の近くまで天然ガス冷却機内で冷却する段階と、天然ガス冷却機によって冷却された後に200bara未満の圧力であるが天然ガス圧縮機が天然ガスストリームを圧縮する圧力よりも高くない圧力まで圧縮天然ガスを膨脹させる段階と、液化窒素ストリームと天然ガスストリームの間で熱を交換して液化窒素ストリームを少なくとも部分的に気化させて天然ガスストリームを少なくとも部分的に凝結させる第1の熱交換器に天然ガスストリーム及び液化窒素ストリームを通す段階であって、液化窒素ストリームが第1の熱交換器を通して少なくとも3回循環される上記通す段階と、少なくとも1つの膨脹器サービスを使用して少なくとも部分的に気化した窒素ストリームの圧力を低減する段階と、蒸留塔と熱ポンプ凝縮器と再沸騰器システムとを含む温室効果ガス除去ユニットを与える段階と、蒸留塔のオーバーヘッドストリームの圧力及び凝結温度を上昇させる段階と、蒸留塔オーバーヘッドストリームのオーバーヘッドストリーム及び蒸留塔のボトムストリームを交差交換して蒸留塔のオーバーヘッド凝縮器デューティ及びボトム再沸騰器デューティの両方に影響を与える段階と、交差交換段階後に蒸留塔オーバーヘッドストリームの圧力を低減して減圧蒸留塔オーバーヘッドストリームを生成する段階と、減圧蒸留塔オーバーヘッドストリームを分離して、温室効果ガスがそこから除去された温室効果ガス除去ユニットを出るガス状窒素である第1の分離器オーバーヘッドストリームを生成する段階と、第1の分離器オーバーヘッドストリームを大気に放出する段階とを含む、天然ガスストリームを液化するのに使用される液体窒素ストリーム内の温室効果ガス汚染物質を除去する方法。
Claims (18)
- 液化天然ガス生産システムであって、
天然ガスのサプライからの天然ガスストリームと、
冷媒サプライからの冷媒ストリームと、
前記冷媒ストリームと前記天然ガスストリームの間で熱を交換し、該冷媒ストリームを少なくとも部分的に気化させて該天然ガスストリームを少なくとも部分的に凝結させる少なくとも1つの熱交換器と、
前記天然ガスストリームを少なくとも135baraの圧力まで圧縮して圧縮天然ガスストリームを形成する天然ガス圧縮機と、
前記天然ガス圧縮機によって圧縮された後で前記圧縮天然ガスストリームを冷却する天然ガス冷却機であって、前記圧縮天然ガスストリームを周囲温度の近くまで冷却するように構成されている天然ガス冷却機と、
前記天然ガス冷却機によって冷却された後で、200bara未満の圧力であるが前記天然ガス圧縮機が前記天然ガスストリームを圧縮する前記圧力よりも高くない圧力まで該圧縮天然ガスを膨脹させる天然ガス膨脹器と、を備え、
前記天然ガス膨脹器が、前記少なくとも1つの熱交換器に天然ガスを供給するために前記少なくとも1つの熱交換器に接続されており、
前記少なくとも1つの熱交換器は、第1の熱交換器と、第2の熱交換器を備え、
前記第2の熱交換器は、前記天然ガスストリームを該天然ガスストリームが前記天然ガス圧縮機内で圧縮される前に冷却する、又は、前記圧縮天然ガスストリームを該圧縮天然ガスストリームが前記天然ガス冷却機内で冷却される前に冷却する、
ことを特徴とする液化天然ガス生産システム。 - 前記天然ガス圧縮機は、前記天然ガスストリームを200baraよりも高い圧力まで圧縮する、
請求項1に記載の液化天然ガス生産システム。 - 前記天然ガス膨脹器は、前記圧縮天然ガスストリームを135bara未満の圧力まで膨脹させる、
請求項1又は2に記載の液化天然ガス生産システム。 - 前記冷媒ストリームは、前記第2の熱交換器内で前記天然ガスストリームを冷却するために使用される、
請求項1に記載の液化天然ガス生産システム。 - 前記冷媒ストリームは、液化窒素ストリームを備え、
前記少なくとも1つの熱交換器は、前記窒素ストリームを少なくとも部分的に気化させ、少なくとも部分的に気化した窒素ストリームを生成する、
請求項1に記載の液化天然ガス生産システム。 - 前記少なくとも部分的に気化した窒素ストリームから温室効果ガスを除去するように構成された温室効果ガス除去ユニットを更に備えている、
請求項5に記載の液化天然ガス生産システム。 - 前記温室効果ガス除去ユニットは、熱ポンプ凝縮器と再沸騰器システムとを有する蒸留塔を備え、
システムが、
前記少なくとも部分的に気化した窒素ストリームの圧力を低減する少なくとも1つの膨脹器サービスを更に備え、
前記蒸留塔の入口ストリームが、前記少なくとも1つの膨脹器サービスのうちの第1のものの出口ストリームである、
請求項6に記載の液化天然ガス生産システム。 - 前記少なくとも部分的に気化した窒素ストリームが前記少なくとも1つの膨脹器サービスのうちの第1のものを通って流れた後でそこを通って流れる熱ポンプシステムを更に備えている、
請求項7に記載の液化天然ガス生産システム。 - 前記熱ポンプシステムは、熱ポンプ圧縮機、熱ポンプ冷却機、及び給送−排出熱交換器を備えている、
請求項8に記載の液化天然ガス生産システム。 - 前記天然ガスストリームが前記少なくとも1つの熱交換器に入る前に前記少なくとも部分的に気化した窒素ストリームを使用して該天然ガスストリームを予冷する乾湿熱交換器を更に備えている、
請求項7に記載の液化天然ガス生産システム。 - 液化天然ガス(LNG)を生産する方法であって、
天然ガスのサプライから天然ガスストリームを与える段階と、
冷媒サプライから冷媒ストリームを与える段階と、
前記冷媒ストリームと前記天然ガスストリームの間で熱を交換し、該冷媒ストリームを少なくとも部分的に気化させて該天然ガスストリームを少なくとも部分的に凝結させる第1の熱交換器に該天然ガスストリーム及び該冷媒ストリームを通す段階と、
前記天然ガスストリームを少なくとも135baraの圧力まで天然ガス圧縮機内で圧縮して圧縮天然ガスストリームを形成する段階と、
前記天然ガス圧縮機によって圧縮された後で前記圧縮天然ガスストリームを前記天然ガス冷却機内で冷却する段階であって、前記天然ガス冷却機が、前記圧縮天然ガスストリームを周囲温度の近くまで冷却する段階と、
前記天然ガス冷却機によって冷却された後で、前記圧縮天然ガスストリームを200bara未満の圧力であるが前記天然ガス圧縮機が前記天然ガスストリームを圧縮する前記圧力よりも高くない圧力まで天然ガス膨脹器内で膨脹させる段階と、
天然ガスを前記天然ガス冷却機から前記少なくとも1つの熱交換器にそこで少なくとも部分的に凝結されるように供給する段階と、を含み、
前記少なくとも1つの熱交換器は、第1の熱交換器と、第2の熱交換器を備え、
前記第2の熱交換器は、前記天然ガスストリームを該天然ガスストリームが前記天然ガス圧縮機内で圧縮される前に冷却する、又は、前記圧縮天然ガスストリームを該圧縮天然ガスストリームが前記天然ガス冷却機内で冷却される前に冷却する、
ことを特徴とする方法。 - 前記天然ガス圧縮機は、前記天然ガスストリームを200baraよりも高い圧力まで圧縮する、
請求項11に記載の方法。 - 前記天然ガス膨脹器は、前記圧縮天然ガスストリームを135bara未満の圧力まで膨脹させる、
請求項11に記載の方法。 - 前記冷媒ストリームは、前記第2の熱交換器内で前記天然ガスストリームを冷却するのに使用される、
請求項11に記載の方法。 - 前記冷媒ストリームは、液化窒素ストリームを含み、
前記少なくとも1つの熱交換器は、前記窒素ストリームを少なくとも部分的に気化させ、少なくとも部分的に気化した窒素ストリームを生成する、
請求項11に記載の方法。 - 温室効果ガス除去ユニットを使用して前記少なくとも部分的に気化した窒素ストリームから温室効果ガスを除去する段階を更に含む、
請求項15に記載の方法。 - 前記温室効果ガス除去ユニットは、蒸留塔及び熱ポンプ凝縮器及び再沸騰器システムを含み、
方法が、
前記蒸留塔のオーバーヘッドストリームの圧力及び凝結温度を上昇させる段階と、
前記圧力及び凝結温度を上昇させる段階の後に、前記蒸留塔のオーバーヘッド凝縮器デューティ及びボトム再沸騰器デューティの両方に影響を与えるために該蒸留塔の前記オーバーヘッドストリーム及び該蒸留塔のボトムストリームを交差交換する段階と、
前記交差交換する段階の後で前記蒸留塔オーバーヘッドストリームの圧力を低減して減圧蒸留塔オーバーヘッドストリームを生成する段階と、
前記減圧蒸留塔オーバーヘッドストリームを分離して、温室効果ガスがそこから除去された前記温室効果ガス除去ユニットを出るガス状窒素である第1の分離器オーバーヘッドストリームを生成する段階と、を更に含む、
請求項16に記載の方法。 - 少なくとも1つの膨脹器サービスのうちの第1のものを通って流れた後に熱ポンプシステムを通して前記少なくとも部分的に気化した窒素ストリームを流す段階を更に含む、
請求項17に記載の方法。
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AU2016292348B2 (en) | 2019-04-04 |
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TW201715189A (zh) | 2017-05-01 |
KR20180030643A (ko) | 2018-03-23 |
KR102064168B1 (ko) | 2020-02-11 |
TWI608206B (zh) | 2017-12-11 |
US11060791B2 (en) | 2021-07-13 |
EP3322946A1 (en) | 2018-05-23 |
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