JP2014522477A - 天然ガスの液化プロセス - Google Patents
天然ガスの液化プロセス Download PDFInfo
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- JP2014522477A JP2014522477A JP2014515273A JP2014515273A JP2014522477A JP 2014522477 A JP2014522477 A JP 2014522477A JP 2014515273 A JP2014515273 A JP 2014515273A JP 2014515273 A JP2014515273 A JP 2014515273A JP 2014522477 A JP2014522477 A JP 2014522477A
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 42
- 239000003345 natural gas Substances 0.000 title claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 238000003303 reheating Methods 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims abstract description 4
- 238000004064 recycling Methods 0.000 claims abstract 4
- 239000007789 gas Substances 0.000 claims description 51
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 4
- 238000005057 refrigeration Methods 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims 2
- 229910002092 carbon dioxide Inorganic materials 0.000 claims 1
- 239000001569 carbon dioxide Substances 0.000 claims 1
- 238000010438 heat treatment Methods 0.000 claims 1
- 239000012535 impurity Substances 0.000 claims 1
- 239000002994 raw material Substances 0.000 abstract description 4
- 239000003949 liquefied natural gas Substances 0.000 description 20
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 239000003507 refrigerant Substances 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
【選択図】図1
Description
−液体冷媒の蒸発
−膨張機(エキスパンダー)におけるガスの仕事膨張
によって行うことができる。
−近年までエキスパンダーの容量に制限があり、かつ経験が限られていること、
−動力要求量が高いこと、
−内部のガス流量が高いので、ラインの必要直径が大きくなること、
などである。
−国際公開第01/44735号パンフレット(Mintaその他)は、「1600psiaより高い」圧力に圧縮された原料ガスからの−112℃の加圧液化天然ガス(PLNG)の製造を記載しており、
−米国特許出願公開第2006/0213222号明細書(Whitesell)は、「約1500psig〜約3500psig」の圧力でプロセスに流入するか、あるいはプロセス内でその圧力に圧縮される原料ガスからのLNGの製造を記載している。
−最初のステップにおいて、第1熱交換器によって、かつ第1仕事エキスパンダー内において、原料ガス及びリサイクルガス(以下に述べる)を冷却する工程であって、その熱交換器は、−50℃〜−80℃、好ましくは−60℃〜−70℃の流出温度を有し、そのエキスパンダーは、前記熱交換器の流出温度より低い流出温度を有し、かつ、そのエキスパンダーの流出ストリームは、前記熱交換器の低温側流路において再加熱され、続いて、上記のリサイクルガスの一部を形成するために再圧縮される、工程と、
−前記第1熱交換器からの前記冷却された流出ストリームを、部分的に、その流出ストリームが本質的に凝縮される第2熱交換器の高温側流路内に通し、かつ部分的に、第2仕事エキスパンダー内に通す工程であって、その第2エキスパンダーは第2熱交換器の低温流出流体より低い流出温度を有し、その第2エキスパンダーの流出ストリームはかなりの量の液体(通常10〜15重量%)を含み、そのエキスパンダーの流出流体は蒸気留分と液体留分とに分離され、蒸気留分は前記第2及び第1熱交換器の低温側流路において再加熱され、続いて、再圧縮され、上記のリサイクルガスの一部としてプロセスの流入側に戻される、工程と、
−上記の分離された液体及び第2熱交換器の高温側流路から凝縮された液体(両者共通常約−120℃)の圧力をほぼ大気圧に低下させ、放出されたフラッシュガスを上記の熱交換器における別の低温側流路内において再加熱し、かつ、液体をLNG製品として使用するために取り出す工程と、
を含む。
Claims (8)
- 天然ガスまたは他のメタンリッチガスの液化プロセスにおいて、
−原料天然ガスを、熱交換器及び第1ガスエキスパンダーによって、−50℃〜−80℃の温度に冷却する工程であって、前記熱交換器は、前記原料天然ガスを受け入れると共に、前記エキスパンダーの流出温度より高い流出温度を有する、工程と、
−前記エキスパンダーの流出ストリームを、前記熱交換器の第1低温側流路において、前記原料天然ガスの前記熱交換器への流入温度のすぐ下の温度に再加熱し、圧縮し、かつリサイクルする工程と、
−前記熱交換器からの低温流出ストリームの一部またはすべてを、それが部分的に液化される第2エキスパンダー内に通す工程と、
−前記第2エキスパンダーの流出ストリームを蒸気留分及び液体留分に分離する工程と、
−前記液体留分をLNG製品として使用するために捕集する工程と、
−前記蒸気留分を、前記熱交換器の第2低温側流路において、前記原料天然ガスの前記熱交換器への流入温度のすぐ下の温度に再加熱する工程と、
−前記再加熱された蒸気留分を、圧縮後、一部は前記第1エキスパンダーに、一部は前記熱交換器にリサイクルする工程と、
を含むことを特徴とするプロセス。 - 請求項1に記載のプロセスにおいて、前記熱交換器が前記原料天然ガスのすべてを受け入れる、ことを特徴とするプロセス。
- 請求項1に記載のプロセスにおいて、前記熱交換器が、前記原料天然ガスのかなりの部分、少なくとも30%を受け入れる、ことを特徴とするプロセス。
- 請求項1乃至3の何れか一項に記載のプロセスにおいて、前記原料天然ガスが−60℃〜−70℃の温度に冷却される、ことを特徴とするプロセス。
- 請求項1乃至4の何れか一項に記載のプロセスにおいて、前記第1及び第2ガスエキスパンダーが、3bar(0.3MPa)〜20bar(2MPa)、好ましくは5bar(0.5MPa)〜15bar(1.5MPa)の基本的に同じ流出圧力を有し、その両エキスパンダーからの流出ストリームが、最終的な再加熱、圧縮及びリサイクルに先立って結合される、ことを特徴とするプロセス。
- 請求項1乃至5の何れか一項に記載のプロセスにおいて、前記原料ストリーム及び/または圧縮機排出ストリーム及び/またはリサイクルストリームの任意の一部分またはすべてが、通常、例えば臭化リチウム(LiBr)のような吸収式冷凍サイクルを用いて冷却される、ことを特徴とするプロセス。
- 請求項1乃至6の何れか一項に記載のプロセスにおいて、吸収式冷凍システムに必要な熱が、プロセスの圧縮機への動力供給用として用いることができるガスエンジンまたはタービンの排熱によって供給される、ことを特徴とするプロセス。
- 請求項1乃至7の何れか一項に記載のプロセスにおいて、原料ストリーム及び/またはリサイクルストリームの何れかの前記のような冷却が、原料ガスからの二酸化炭素及び/または他の不純物の除去と組み合わされる、ことを特徴とするプロセス。
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PCT/GB2012/000502 WO2012172281A2 (en) | 2011-06-15 | 2012-06-11 | Process for liquefaction of natural gas |
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