JP4885734B2 - 極低温の空気分離法および装置 - Google Patents
極低温の空気分離法および装置 Download PDFInfo
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- JP4885734B2 JP4885734B2 JP2006546347A JP2006546347A JP4885734B2 JP 4885734 B2 JP4885734 B2 JP 4885734B2 JP 2006546347 A JP2006546347 A JP 2006546347A JP 2006546347 A JP2006546347 A JP 2006546347A JP 4885734 B2 JP4885734 B2 JP 4885734B2
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- air
- gas
- oxygen
- air separation
- product
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- 239000007789 gas Substances 0.000 claims description 187
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 90
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 83
- 239000001301 oxygen Substances 0.000 claims description 80
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- GNFTZDOKVXKIBK-UHFFFAOYSA-N 3-(2-methoxyethoxy)benzohydrazide Chemical compound COCCOC1=CC=CC(C(=O)NN)=C1 GNFTZDOKVXKIBK-UHFFFAOYSA-N 0.000 claims description 16
- 238000007906 compression Methods 0.000 claims description 15
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- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 description 1
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Description
本発明は、空気分離方法および関連する装置に関する。
空気分離は、非常に電力の高い技術であり、化学薬品工場、精錬所、製鋼所等のようなトン単位での用途のための大量の工業用ガスを製造するためには、何千ものキロワット、または数メガワットの電力を消費する。
本発明は、ピーク時の電力消費の低減に伴う問題を解決すると同時に、同様の製品生産高を維持することができる技術を提供し、従って、電力コスト節約を達成することができる。
a)オフピーク時においてプロセス流を液化して、第1の液体生成物を製造すること、
b)ピーク時において、空気分離ユニットに、製造した第1の液体生成物を供給すること、
c)空気圧縮機により供給される空気供給物を低減させ、供給流中に含まれる酸素の総量を本質的に同一に保つこと、
d)カラムシステムから少なくとも1種の生成物を回収し、およびその圧力をポンプで送り込むことにより上昇させた後、ガス状生成物を生成するために、熱交換器内で気化させること、
e)低温で、系から冷却ガスを回収すること、および
f)低温ガス圧縮機で、生成した低温ガスをより高い圧力に低温で圧縮すること
を含む。
本発明によれば、蒸留カラムのシステムを用いる、空気分離ユニットにおける加圧ガス生成物を製造するための低温空気分離方法を提供し、これは以下の工程:
i)熱交換ライン中の圧縮空気流を冷却し、圧縮冷却空気流を生成する工程、
ii)上記圧縮冷却空気中の少なくとも一部を、システムの1つのカラムに送る工程、
iii)第1の時間帯において、プロセス流を液化して第1の液体生成物を生成し、およびこの第1の液体生成物の少なくとも一部を貯蔵する工程、
iv)第2の時間帯において、上記の貯蔵された第1の液体生成物を、供給物の1つとして空気分離ユニットに送給する工程、
v)少なくとも1つの第2の液体生成物流を加圧する工程、
vi)熱交換ライン中で、上記の加圧された第2の液体生成物流を気化させ、加圧されたガス生成物を生成する工程、および
vii)上記第2の時間帯の間中、 の間の温度で、空気分離ユニットから低温ガスを抽出する工程
を含む。
加圧されたガス生成物は、酸素生成物であり、
加圧されたガス生成物は、窒素生成生物であり、
低温ガスは、−195℃〜−20℃、好ましくは−180℃〜−50℃の温度で、空気分離ユニットのコールドボックスから抽出され、
工程c)のプロセス流は、いずれもの割合の酸素、窒素およびアルゴンを含み、
工程c)のプロセス流は、純粋窒素、空気、少なくとも37モル%の酸素を含む酸素、少なくとも65モル%の酸素を含む酸素、少なくとも85モル%の酸素を含む酸素、少なくとも99.5モル%を含む酸素のうちの少なくとも1つであり、
工程g)の低温ガスが、窒素リッチなガス、純粋窒素ガス、空気、空気と同様の組成を有するガス、酸素リッチなガス、および純粋酸素生成物を含む群から選択され、
工程e)の第2の液体生成物は、工程c)の貯蔵された第1の液体生成物と同一であり、
工程c)を、電気料金が、予め決められた基準以下の場合に行い、
工程c)を、電気料金が、予め決められた基準以下の場合に限り行い、
工程d)を、電気料金が、予め決められた基準を上回る場合に行い、
工程d)を、電気料金が、予め決められた基準を上回る場合に限り行い、
工程g)を、電気料金が、予め決められた基準を上回る場合に行い、
工程g)を、電気料金が、予め決められた基準を上回る場合に限り行い、
工程g)の低温ガスの少なくとも一部を加熱し、エネルギーを回収するために熱膨張機(hot expander)内で膨張させ、
工程g)の低温ガスの少なくとも一部を、エネルギー回収のために、ガスタービン中に注入し、
工程g)の低温ガスの少なくとも一部を、空気分離ユニットに再循環し、
空気分離ユニットは、IGCC設備に加圧されたガス状酸素生成物を供給し、
IGCC設備は、ガスタービンを備え、以下の工程:
a)電力の料金が、予め決められた基準以下の場合に、ガスタービンから空気を抽出する工程、および
b)上記抽出した空気を、空気分離ユニットに供給する工程
をさらに包含し、
電気料金が、予め決められた基準よりも高い場合に、ガスタービンに加圧された低温ガスを注入し、
LNGを気化させることによる冷却を、第1の液体生成物の液化コストを低下させるために回収し、
電気料金が、予め決められた基準以下の場合の熱交換器内で冷却された空気の量と比較して、電気料金が予め決められた基準を上回る場合の、熱交換器中の圧縮された空気の流量を低減し、
熱交換ライン中で昇温させることなく空気分離ユニットから低温ガスを取り出し、
熱交換ライン中で部分的に昇温させた後に、空気分離ユニットから低温ガスを取り出し、
低温ガスを、熱交換ラインの温末端(warm end)のみを横断することにより冷却した後に、空気分離ユニットから取り出す。
i)熱交換ライン中の圧縮空気流を冷却し、圧縮冷却空気流を生成する工程、
ii)圧縮冷却空気流の少なくとも一部を、システムの1つのカラムに送る工程、
iii)第1の時間帯において、プロセス流を液化して第1の液体生成物を生成し、およびこの第1の液体生成物の少なくとも一部を貯蔵する工程、
iv)第2の時間帯において、上記の貯蔵した第1の液体生成物を、供給物の1つとして空気分離ユニットに送る工程、
v)少なくとも1つの第2の液体生成物流を加圧する工程、
vi)熱交換ライン中で、上記の加圧された第2の液体生成物流を気化させ、加圧されたガス生成物を生成する工程、および
vii)上記の第2の時間帯の間、空気分離ユニットから低温ガスを抽出し、−180℃〜−50℃の入口温度および高くとも−20℃の出口温度を有する圧縮機中で、上記低温ガスを圧縮し、加圧ガスを生成する工程
を含む。
加圧されたガス生成物は、酸素生成物であり、
加圧されたガス生成物は、窒素生成物であり、
工程c)のプロセス流は、いずれもの割合の酸素、窒素およびアルゴンを含み、
工程c)のプロセス流は、純粋窒素、空気、少なくとも37モル%の酸素を含む酸素、少なくとも65モル%の酸素を含む酸素、少なくとも85モル%の酸素を含む酸素、および少なくとも99.5モル%を含む酸素のうちの少なくとも1つであり、
工程g)の低温ガスが、窒素リッチなガス、純粋窒素、空気、空気と同様の組成を有するガス、酸素リッチなガス、および純粋酸素生成物を含む群から選択され、
工程c)を、電気料金が、予め決められた基準以下の場合に行い、
工程c)を、電気料金が、予め決められた基準以下の場合に限り行い、
工程d)を、電気料金が、予め決められた基準を上回る場合に行い、
工程d)を、電気料金が、予め決められた基準を上回る場合に限り行い、
工程g)を、電気料金が、予め決められた基準を上回る場合に行い、
工程g)を、電気料金が、予め決められた基準を上回る場合に限り行い、
圧縮機中で、35〜80bar絶対圧の圧力まで、低温ガスを圧縮し、
加圧されたガスの少なくとも一部を加熱し、および熱膨張機中で膨張させてエネルギーを回収し、
加圧されたガスの少なくとも一部を、エネルギー回収のために、ガスタービン中に注入し、
加圧されたガスの少なくとも一部を、空気分離ユニットのカラムシステムに再循環し、
空気分離ユニットが、IGCC設備に、加圧されたガス状酸素生成物を供給し、
IGCC設備は、ガスタービンを備え、以下の工程:
a)電気料金が、予め決められた基準以下の場合に、ガスタービンから空気を抽出する工程、および
b)上記抽出された空気を、空気分離ユニットに供給する工程
をさらに包含し、
プロセスは、電気料金が予め決められた基準よりも高い場合に、加圧された低温ガスを、ガスタービンに注入する工程を含み、
プロセスは、
a)熱交換ライン中で加圧されたガスを昇温させる工程、
b)熱交換ライン中で追加のガスを冷却し、低温追加ガスを精製する工程、および
c)低温追加ガスを、高圧にまで低温で圧縮する工程
を含み、
双方のガスを、10〜20bar絶対圧まで圧縮し、
LNGを気化させることによる冷却を、第1の液体生成物の液化コストを低下させるために回収し、
プロセスは、電気料金が予め決められた基準以下の場合の熱交換器中で冷却された空気の量と比較して、電気料金が予め決められた基準を上回る場合の、熱交換ライン中の圧縮された空気の流量を低減させることを含み、
低温ガスを、熱交換ライン中で昇温させることなく、空気分離ユニットのコールドボックスから取り出し、
低温ガスを、熱交換ライン中で部分的に昇温した後に、空気分離ユニットのコールドボックスから取り出し、
低温ガスを、熱交換ラインの温かい末端のみを横切ることにより冷却した後に、空気分離ユニットのコールドボックスから取り出し、
プロセスは、熱交換ライン中で加圧されたガスを昇温させる工程を含み、
空気分離ユニットは、コールドボックス内に含まれ、−195℃〜−20℃の温度で、コールドボックスから低温ガスを抽出する。
a)蒸留カラムのシステム、
b)熱交換ライン、
c)少なくとも蒸留カラムのシステムと熱交換ラインを収容するコールドボックス、
d)供給空気を、熱交換ラインに送るための導管、
e)熱交換ラインからの低温供給空気を、カラムシステムに送るための導管、
f)カラムシステムに第1の液体生成物を送るための手段、
g)カラムシステムの1つのカラムから、液体を取り出すための導管、
h)液体を、熱交換ラインに送るための導管、
i)熱交換ラインから気化された液体を取り出すための導管、および
j)システムのカラムからガスを抽出するための、および熱交換ライン全体を横切ることによりガスを昇温させることを伴わずに、空気分離装置からガスを取り出すための導管
を含む空気分離装置を提供する。
カラムシステムのいずれかのカラムの外部で、第1の液体生成物を貯蔵するための手段、
ガスを抽出するための導管に接続されたガス圧縮機、
入口と出口を有する空気圧縮機であって、空気圧縮機の入口が、熱交換器の中間地点において、圧縮ガス導管に接続されている空気圧縮機、
膨張機、および低温ガス圧縮機中で圧縮されたガスを、膨張機の上流地点に送るための導管を有するガスタービン、
熱交換ライン中でガスを昇温させることなく、空気分離装置からガスを取り出すための導管、
第1の液体生成物を生成するためにガスを液化するための手段
を含む。
低温ガスの流量=k[全気化液体−全流入液体]、ここで、k=1.6〜2.6。
1.図2Aにおいて上記した通り、低温ガスの低温圧縮を、単一工程で行うことができる。圧縮される低温ガスの最終圧力は、比較的低く、すなわち、圧縮ガス温度は、引き続き低いレベルであり、その後、図7に示すように、主空気圧縮機1からの追加の空気85(または窒素ガス)を、交換ライン30内で、低温圧縮機70からの圧縮低温ガスを用いて冷却した後、この追加ガスを、低温圧縮機75内でより高い圧力にまで圧縮することにより、圧縮ガス流量を増加させることができる。その後、2つの低温圧縮流を熱交換ライン30の上流で混合して、流95を生成する。この交換器を、図2Aの主交換器30と兼ねてもよい。図8も、この態様を記載する。
(付記)
なお、当初の特許請求の範囲に記載された請求項26乃至60を削除したが、これら請求項に記載の発明もまた、本明細書に記載された発明である。これらの発明は以下の通りである。
[請求項26]
蒸留カラムシステムを用いる空気分離ユニットにおいて、加圧されたガス状生成物を製造するための低温空気分離方法であって、以下の工程:
a)熱交換ライン中で圧縮空気流を冷却し、圧縮冷却空気流を生成する工程、
b)前記圧縮冷却空気流の少なくとも一部を、前記システムの1つのカラムに送る工程、
c)第1の時間帯において、プロセス流を液化して、第1の液体生成物を生成し、および前記第1の液体生成物の少なくとも一部を貯蔵する工程、
d)第2の時間帯において、上記貯蔵された第1の液体生成物を、供給物の1つとして、前記空気分離ユニットに送る工程、
e)少なくとも1つの第2の液体生成物流を加圧する工程、
f)前記熱交換ラインにおいて、上記加圧された第2の液体生成物流を気化させ、加圧されたガス状生成物を生成する工程、
g)上記第2の時間帯の間に、前記空気分離ユニットから低温ガスを抽出し、約−180℃〜−50℃の入口温度および高くとも−20℃の出口温度を有する圧縮機内で、前記低温ガスを圧縮し、加圧されたガスを生成する工程
を含む低温空気分離方法。
[請求項27]
前記加圧されたガス状生成物が、酸素生成物である請求項26に記載の方法。
[請求項28]
前記加圧されたガス状生成物が、窒素生成物である請求項26に記載の方法。
[請求項29]
工程c)の前記プロセス流が、いずれもの割合の酸素、窒素およびアルゴンを含有する請求項26に記載の方法。
[請求項30]
工程c)の前記プロセス流が、純粋窒素、空気、少なくとも37モル%の酸素を含む酸素、少なくとも65モル%の酸素を含む酸素、少なくとも85モル%の酸素を含む酸素、および少なくとも99.5モル%を含む酸素のうちの少なくとも1つである請求項26に記載の方法。
[請求項31]
工程g)の前記低温ガスが、窒素リッチなガス、純粋窒素、空気、空気と同様の組成を有するガス、酸素リッチなガスおよび純粋酸素生成物を含む群から選択される請求項26に記載の方法。
[請求項32]
工程c)を、電気料金が、予め決められた基準以下である場合に行う請求項26に記載の方法。
[請求項33]
工程c)を、電気料金が、予め決められた基準以下である場合に限り行う請求項32に記載の方法。
[請求項34]
工程d)を、電気料金が、予め決められた基準を上回る場合に行う請求項26に記載の方法。
[請求項35]
工程d)を、電気料金が、予め決められた基準を上回る場合に限り行う請求項34に記載の方法。
[請求項36]
工程g)を、電気料金が、予め決められた基準を上回る場合に行う請求項26に記載の方法。
[請求項37]
工程g)を、電気料金が、予め決められた基準を上回る場合に限り行う請求項36に記載の方法。
[請求項38]
前記低温ガスを、前記圧縮機内で、35〜80bar絶対圧の圧力まで圧縮する請求項26に記載の方法。
[請求項39]
前記加圧されたガスの少なくとも一部を加熱し、エネルギー回収のために熱膨張機内で膨張させる請求項26に記載の方法。
[請求項40]
前記加圧されたガスの少なくとも一部を、エネルギー回収のために、ガスタービン中に注入する請求項26に記載の方法。
[請求項41]
前記加圧されたガスの少なくとも一部を、前記空気分離ユニットのカラムシステムに再循環させる請求項26に記載の方法。
[請求項42]
前記空気分離ユニットが、IGCC設備に、加圧されたガス状酸素生成物を供給する請求項26に記載の方法。
[請求項43]
前記IGCC設備が、ガスタービンを備え、以下の工程:
a)電気料金が、予め決められた基準以下である場合に、前記ガスタービンから空気を抽出する工程、
b)上記抽出した空気を、前記空気分離ユニットに送る工程
をさらに包含する請求項42に記載の方法。
[請求項44]
電気料金が、予め決められた基準よりも高い場合に、前記加圧された低温ガスを、前記ガスタービンに注入する工程を含む請求項26に記載の方法。
[請求項45]
以下の工程:
a)前記熱交換ライン中で、前記加圧されたガスを昇温させる工程、
b)前記熱交換ライン中で追加のガスを冷却し、低温追加ガスを生成する工程、および
c)低温追加ガスを、より高い圧力にまで低温圧縮する工程
をさらに包含する請求項26に記載の方法。
[請求項46]
双方のガスを、約10〜約20bar絶対圧まで圧縮する請求項45に記載の方法。
[請求項47]
LNGを気化させることによる冷却を、前記第1の液体生成物の液化コストを下げるために回収する請求項26に記載の方法。
[請求項48]
電気料金が予め決められた基準以下である場合の、前記熱交換ラインにおいて冷却される空気の量と比較して、電気料金が予め決められた基準を上回る場合の、前記熱交換ラインにおける圧縮空気の流量を低下せることを含む請求項26に記載の方法。
[請求項49]
前記低温ガスを、前記熱交換ライン中で昇温させることなく、前記空気分離ユニットのコールドボックスから取り出す請求項26に記載の方法。
[請求項50]
前記低温ガスを、前記熱交換ライン中で部分的に昇温させた後に、前記空気分離ユニットのコールドボックスから取り出す請求項26に記載の方法。
[請求項51]
前記低温ガスを、前記熱交換ラインの温末端のみを横切ることにより冷却した後に、前記空気分離ユニットのコールドボックスから取り出す請求項50に記載の方法。
[請求項52]
前記熱交換ラインにおいて、前記加圧されたガスを昇温させる工程を含む請求項26に記載の方法。
[請求項53]
前記空気分離ユニットが、コールドボックス内に収容され、および約−195℃〜約−20℃の温度で、前記コールドボックスから低温ガスを抽出する請求項1に記載の方法。
[請求項54]
a)蒸留カラムシステム、
b)熱交換ライン、
c)少なくとも前記蒸留カラムシステムと前記熱交換ラインを収容するコールドボックス、
d)前記熱交換ラインに供給空気を送るための導管、
e)前記熱交換ラインから前記カラムシステムに、冷却された供給空気を送るための導管、
f)第1の液体生成物を、前記カラムシステムに送るための手段、
g)前記カラムシステムの1つのカラムから、液体を取り出すための導管、
h)前記液体を、前記熱交換ラインへ送るための導管、
i)前記熱交換ラインから、気化された液体を取り出すための導管、および
j)前記システムの1つのカラムからガスを抽出し、および前記空気分離装置からガスを、熱交換ライン全体に渡って横切ることによりガスを昇温させることを伴わずに取り出すための導管
を含む空気分離装置。
[請求項55]
前記カラムシステムのいずれかのカラムの外部に、前記第1の液体生成物を貯蔵するための手段を含む請求項54に記載の装置。
[請求項56]
ガスを抽出するための前記導管に接続されたガス圧縮機を含む請求項54に記載の装置。
[請求項57]
入口と出口を有し、前記入口が、前記熱交換器の中間地点において、圧縮空気の導管に接続された空気圧縮機を含む請求項54に記載の装置。
[請求項58]
膨張機と、前記低温ガス圧縮機において圧縮されたガスを、前記膨張機の上流地点に送るための導管を有するガスタービンを含む請求項54に記載の装置。
[請求項59]
前記空気分離装置から前記ガスを、前記熱交換ライン中で前記ガスを昇温させることなく取り出すための導管を含む請求項54に記載の装置。
[請求項60]
前記第1の液体生成物を生成するために、ガスを液化させるための手段を含む請求項54に記載の装置。
Claims (17)
- 蒸留カラムシステムを用いる空気分離ユニットにおいて、加圧されたガス生成物を製造するための、低温空気分離方法であって、以下の工程:
a)熱交換ライン内で圧縮空気流を冷却し、圧縮冷却空気流を生成する工程、
b)前記圧縮冷却空気流の少なくとも一部を、前記システムの1つのカラムに送る工程、
c)第1の時間帯において、蒸留カラムシステムから発生するプロセス流を液化して第1の液体生成物を生成し、およびこの第1の液体生成物の少なくとも一部を貯蔵する工程であって、この工程を、電気料金が、予め決められた基準以下の場合に限り行う工程、
d)第2の時間帯において、前記貯蔵された第1の液体生成物を、供給物の1つとして、前記空気分離ユニットに送る工程であって、この工程を、電気料金が、予め決められた基準を上回る場合に限り行う工程、
e)蒸留カラムシステムから発生する少なくとも1つの第2の液体生成物流を加圧する工程、
f)前記熱交換ライン内で、前記加圧された第2の液体生成物流を気化させ、加圧されたガス状生成物を生成する工程、および
g)前記第2の時間帯の間のみに、−195℃〜−20℃の温度で、前記空気分離ユニットから低温ガスを抽出する工程であって、この工程を、電気料金が、予め決められた基準を上回る場合に限り行う工程、
を含み、
前記空気分離ユニットは、コールドボックスの内部にあり、および前記低温ガスを、−195℃〜−20℃の温度において、前記空気分離ユニットのコールドボックスから抽出するものであり、かつ、
電気料金が予め決められた基準以下である場合の、前記熱交換器において冷却される空気の量と比較して、電気料金が予め決められた基準を上回る場合の、前記熱交換器内の圧縮された空気の流量を低下させる、
低温空気分離方法。 - 前記加圧されたガス状生成物が、酸素生成物である請求項1に記載の方法。
- 前記加圧されたガス状生成物が、窒素生成物である請求項1に記載の方法。
- 工程c)の前記プロセス流は、いずれもの割合の酸素、窒素およびアルゴンを含有する請求項1に記載の方法。
- 工程c)の前記プロセス流は、純粋窒素、空気、少なくとも37モル%の酸素を含む酸素、少なくとも65モル%の酸素を含む酸素、少なくとも85モル%の酸素を含む酸素、および少なくとも99.5モル%を含む酸素のうちの少なくとも1つである請求項1に記載の方法。
- 工程g)の前記低温ガスが、窒素リッチなガス、純粋窒素ガス、空気、空気と同様の組成を有するガス、酸素リッチなガス、および純粋酸素生成物を含む群から選択される請求項1に記載の方法。
- 工程e)の前記第2の液体生成物が、工程c)の前記貯蔵された第1の液体生成物と同じである請求項1に記載の方法。
- 工程g)の前記低温ガスの少なくとも一部を加熱し、エネルギーを回収するために熱膨
張機(hot expander)内で膨張させる請求項1に記載の方法。 - 工程g)の前記低温ガスの少なくとも一部を、エネルギー回収のためにガスタービン中に注入する請求項1に記載の方法。
- 工程g)の前記低温ガスの少なくとも一部を、空気分離ユニットに再循環させる請求項1に記載の方法。
- 前記空気分離ユニットが、IGCC設備に、加圧されたガス状酸素生成物を供給する請求項1に記載の方法。
- IGCC設備が、ガスタービンを備え、以下の工程:
a)電気料金が、予め決められた基準以下の場合に、前記ガスタービンから空気を抽出する工程、および
b)上記抽出された空気を、前記空気分離ユニットに供給する工程
をさらに包含する請求項11に記載の方法。 - 電気料金が、予め決められた基準よりも高い場合に、加圧された低温ガスを、前記ガスタービンに注入する工程を含む請求項11に記載の方法。
- LNGを気化させることによる冷却を、前記第1の液体生成物の液化コストを下げるために回収する請求項1に記載の方法。
- 前記低温ガスを、前記熱交換ライン中で昇温させることなく、前記空気分離ユニットから取り出す請求項1に記載の方法。
- 前記低温ガスを、前記熱交換ライン中で部分的に昇温させた後に、前記空気分離ユニットから取り出す請求項1に記載の方法。
- 前記低温ガスを、前記熱交換ラインの温末端(warm end)のみを横切ることにより加熱した後に、前記空気分離ユニットから取り出す請求項16に記載の方法。
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US53221903P | 2003-12-23 | 2003-12-23 | |
US60/532,219 | 2003-12-23 | ||
US79806804A | 2004-03-11 | 2004-03-11 | |
US10/798,068 | 2004-03-11 | ||
US10/899,688 US7228715B2 (en) | 2003-12-23 | 2004-07-27 | Cryogenic air separation process and apparatus |
US10/899,688 | 2004-07-27 | ||
PCT/IB2004/003405 WO2005064252A1 (en) | 2003-12-23 | 2004-10-18 | Cryogenic air separation process and apparatus |
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JP2007516407A JP2007516407A (ja) | 2007-06-21 |
JP4885734B2 true JP4885734B2 (ja) | 2012-02-29 |
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US (2) | US7228715B2 (ja) |
EP (2) | EP1706692B1 (ja) |
JP (1) | JP4885734B2 (ja) |
CN (1) | CN1918444B (ja) |
BR (1) | BRPI0417269A (ja) |
CA (1) | CA2550947C (ja) |
WO (1) | WO2005064252A1 (ja) |
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US20050132746A1 (en) | 2005-06-23 |
CN1918444A (zh) | 2007-02-21 |
EP1706692B1 (en) | 2018-05-30 |
BRPI0417269A (pt) | 2007-03-13 |
JP2007516407A (ja) | 2007-06-21 |
US20070130992A1 (en) | 2007-06-14 |
EP2031329A1 (en) | 2009-03-04 |
CN1918444B (zh) | 2010-06-09 |
CA2550947A1 (en) | 2005-07-14 |
EP2031329B1 (en) | 2017-12-06 |
EP1706692A1 (en) | 2006-10-04 |
US7228715B2 (en) | 2007-06-12 |
WO2005064252A1 (en) | 2005-07-14 |
CA2550947C (en) | 2011-05-03 |
WO2005064252A8 (en) | 2006-08-03 |
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