JP2012519649A5 - - Google Patents

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JP2012519649A5
JP2012519649A5 JP2011553503A JP2011553503A JP2012519649A5 JP 2012519649 A5 JP2012519649 A5 JP 2012519649A5 JP 2011553503 A JP2011553503 A JP 2011553503A JP 2011553503 A JP2011553503 A JP 2011553503A JP 2012519649 A5 JP2012519649 A5 JP 2012519649A5
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hydrogen
rich
vapor stream
rich vapor
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JP2012519649A (en
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Priority claimed from EP09250654A external-priority patent/EP2233870A1/en
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Priority claimed from PCT/GB2010/000405 external-priority patent/WO2010103259A2/en
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Claims (15)

ガス流を水素リッチ蒸気流及び二酸化炭素リッチ流に分離する製造方法において、
（ａ）二相混合物が形成される温度に二酸化炭素と４０乃至６５モル％の水素とを含む合成ガス流を冷却するステップと、
（ｂ）ステップ（ａ）で形成された冷却された流を直接又は間接的に第一気液セパレータ容器を通過するステップであって、１５０バージ未満の圧力を有する気液セパレータ容器への供給と、
（ｃ）セパレータ容器から水素リッチ蒸気流を及びセパレータ容器からの液体ＣＯ２流を引き抜くステップと、
（ｄ）少なくとも一つの膨張機を含む膨張システムに分離された水素リッチ蒸気流を供給し、水素リッチ蒸気流をシステムの膨張機において膨張させ、水素リッチ蒸気流を低下させた温度と圧力で膨張機から引き抜き、
（ｅ）膨張された水素リッチ蒸気流を冷却材として使用するステップ、を含む製造方法。 In a production process for separating a gas stream into a hydrogen rich vapor stream and a carbon dioxide rich stream,
(A) cooling a synthesis gas stream comprising carbon dioxide and 40 to 65 mol% hydrogen to a temperature at which a two-phase mixture is formed;
(B) passing the cooled stream formed in step (a) directly or indirectly through the first gas-liquid separator container, the supply to the gas-liquid separator container having a pressure of less than 150 barge; ,
(C) drawing a hydrogen rich vapor stream from the separator vessel and a liquid CO 2 stream from the separator vessel;
(D) feeding at least one expander hydrogen-rich vapor stream that is separated in the expansion system comprising, expanding the hydrogen-rich vapor stream in the expander system, the expansion at a temperature and pressure with a reduced hydrogen-rich vapor stream Pulled out of the machine ,
(E) manufacturing method comprising steps, a to use expanded hydrogen-rich vapor stream as a coolant. 合成ガス供給流の二酸化炭素の総モルの７５乃至８５％が、プロセスで合成ガス供給流から分離されることを特徴とする請求項１に記載の製造方法。 The process according to claim 1, characterized in that 75 to 85% of the total moles of carbon dioxide in the synthesis gas feed stream is separated from the synthesis gas feed stream in the process . 合成ガス供給流の二酸化炭素の総モルの６５乃至８０％が、プロセスで合成ガス供給流から分離されることを特徴とする請求項１に記載の製造方法。 The process according to claim 1, characterized in that 65 to 80% of the total moles of carbon dioxide in the synthesis gas feed stream is separated from the synthesis gas feed stream in the process . 気液セパレータ容器への流が８０バール未満の圧力を有することを特徴とする請求項１乃至３のいずれかに記載の製造方法。 4. A method according to claim 1, wherein the flow to the gas-liquid separator container has a pressure of less than 80 bar . 冷却するステップは、プロセスで順次生産される内部冷却材流との熱交換器関係で、合成ガスを熱交換器システムに供給することを含み、内部冷却材流が水素リッチ蒸気流及び濃厚二酸化炭素流から成る群から選択されることを特徴とする請求項１乃至４のいずれかに記載の製造方法。 The cooling step includes supplying synthesis gas to the heat exchanger system in a heat exchanger relationship with an internal coolant stream produced sequentially in the process, the internal coolant stream being a hydrogen rich vapor stream and a rich carbon dioxide. The method according to any one of claims 1 to 4, wherein the method is selected from the group consisting of streams . 直列に配置された複数の膨張機を含む膨張システムに分離された水素リッチ蒸気流を供給し、連続する膨張機それぞれで水素リッチ蒸気流を膨張させ、膨張された水素リッチ蒸気流を各膨張機から低下された温度と続いて低下された圧力で引き抜かれるステップ、および少なくとも一つの膨張水素リッチ蒸気を冷却材として使用するステップを含むことを特徴とする請求項１乃至５のいずれかに記載の製造方法。 The separated hydrogen-rich vapor stream is supplied to an expansion system including a plurality of expanders arranged in series, and the hydrogen-rich vapor stream is expanded in each successive expander. 6. The method of any one of claims 1 to 5, comprising the step of withdrawing at a reduced temperature and subsequently at a reduced pressure, and using at least one expanded hydrogen rich steam as a coolant . Manufacturing method . 膨張された水素リッチ蒸気流は、水素リッチガス流、二酸化炭素流、及び合成ガス流から選択された一つ以上の流を冷却するために使用されることを特徴とする請求項１乃至６のいずれかに記載の方法。 Expanded hydrogen-rich vapor stream, hydrogen-rich gas stream, the carbon dioxide stream, and any of claims 1 to 6 that, wherein for use of one or more flow selected from the syngas stream to cool The method of crab . 膨張機は、連続する膨張機それぞれの水素リッチ蒸気に対し等エントロピー膨張をもたらし、原動力を生み出すことを特徴とする請求項６に記載の方法。 The method of claim 6 , wherein the expander provides isentropic expansion for the hydrogen-rich steam of each successive expander to generate a motive force. 分離された二酸化炭素流の圧力を増加させることを更に含む請求項１乃至８のいずれかに記載の方法。 The method according to any one of claims 1 to 8 further comprising increasing the pressure of the separated carbon dioxide stream. 分離された水素リッチ流を直接的に又は間接的に別のガス液体セパレータ容器を通過させ、第二分離された水素リッチ蒸気流をセパレータ容器から第二液体ＣＯ２流をセパレータ容器から引き抜くことを更に含む請求項１乃至９のいずれかに記載の方法。 Passing the separated hydrogen-rich stream directly or indirectly through another gas-liquid separator container and drawing the second separated hydrogen-rich vapor stream from the separator container and the second liquid CO 2 stream from the separator container. the method according to any one of claims 1 to 9 further comprising. 第二セパレータ容器の上流の分離された水素リッチ流を冷却することを更に含む請求項１０の製造方法。 The method of claim 10 , further comprising cooling the separated hydrogen rich stream upstream of the second separator vessel. 合成ガス供給流は、合成ガス供給流を多チャネル熱交換器の少なくとも一つのチャネルを介して及び複数の低温のプロセス流を多チャネル熱交換器の別のチャネルを介して通過することによって、冷却されることを特徴とする請求項１乃至１１のいずれかに記載の製造方法。 The syngas feed stream is cooled by passing the syngas feed stream through at least one channel of the multi-channel heat exchanger and a plurality of cold process streams through another channel of the multi-channel heat exchanger. the process according to any one of claims 1 to 11, characterized in that it is. セパレータを出る水素リッチガス蒸気流は、多チャネル熱交換器のチャネルを介して、合成ガス供給流との熱交換器関係で通過させ膨張により冷却され、多チャネル熱交換器の別のチャネルに供給される前に第一ターボ膨張機の圧力を下げることを特徴とする請求項１２に記載の製造方法。 The hydrogen rich gas vapor stream exiting the separator is passed through the channel of the multi-channel heat exchanger in a heat exchanger relationship with the synthesis gas feed stream, cooled by expansion, and fed to another channel of the multi-channel heat exchanger. the method according to claim 12, the pressure in the first turboexpander, wherein the lower Geruko before. ステップ（ａ）の合成ガスの冷却の全て又は略全てが一つ以上の内部冷却流を用いて実行されることを特徴とする請求項１乃至１３のいずれかに記載の製造方法。 The process according to any one of claims 1 to 13, all or substantially all of the cooling of the synthesis gas in step (a) is characterized in that it is performed using one or more internal cooling flow. 合成ガス流を水素リッチ蒸気流及び二酸化炭素リッチ流に分離するシステムにおいて、
（ａ）二相混合物が形成される温度に二酸化炭素と４０乃至６５モル％の水素とを含む合成ガス流を冷却する冷却システムと、
（ｂ）配置された第一気液セパレータ容器であって、直接又は間接的に冷却流を受け、１５０バージ未満の圧力を有する気液セパレータ容器への供給と、第一水素リッチ蒸気流及び液体ＣＯ２流を出力し、
（ｃ）少なくとも一つの膨張機を含む膨張システムであって、水素リッチ蒸気流を受け、システムの膨張機において膨張させ、膨張された水素リッチ蒸気流が膨張機から低下した温度と圧力とで引き抜かれ、
（ｄ）膨張された水素リッチ蒸気流を冷却システムに供給する流路と、を含むシステム。 In a system for separating a synthesis gas stream into a hydrogen rich vapor stream and a carbon dioxide rich stream,
(A) a cooling system for cooling a synthesis gas stream comprising carbon dioxide and 40 to 65 mol% hydrogen to a temperature at which a two-phase mixture is formed;
(B) the first gas-liquid separator container arranged, which receives the cooling flow directly or indirectly and has a pressure of less than 150 barge, supply to the gas-liquid separator container and the first hydrogen-rich vapor stream and liquid Output CO 2 flow,
(C) A inflation system including even without least one expander receives the hydrogen-rich vapor stream, is expanded in expander system, expanded hydrogen-rich vapor stream and a temperature and pressure drops from the expander Pulled out
(D) a system including a flow path for supplying the expanded hydrogen-rich vapor stream to the cooling system.
JP2011553503A 2009-03-09 2010-03-05 Separation of carbon dioxide and hydrogen Pending JP2012519649A (en)

Applications Claiming Priority (9)

Application Number Priority Date Filing Date Title
EP09250654.2 2009-03-09
EP09250654A EP2233870A1 (en) 2009-03-09 2009-03-09 Separation of carbon dioxide and hydrogen
GB2009002895 2009-12-16
GBPCT/GB2009/002895 2009-12-16
EP10250045 2010-01-12
EP10250045.1 2010-01-12
EP10250096 2010-01-21
EP10250096.4 2010-01-21
PCT/GB2010/000405 WO2010103259A2 (en) 2009-03-09 2010-03-05 Separation of carbon dioxide and hydrogen

Publications (2)

Publication Number Publication Date
JP2012519649A JP2012519649A (en) 2012-08-30
JP2012519649A5 true JP2012519649A5 (en) 2013-04-18

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US (1) US20120000243A1 (en)
EP (1) EP2406566A2 (en)
JP (1) JP2012519649A (en)
CN (1) CN102422108A (en)
AU (1) AU2010222763A1 (en)
BR (1) BRPI1009260A2 (en)
CA (1) CA2754135A1 (en)
RU (1) RU2011140704A (en)
WO (1) WO2010103259A2 (en)
ZA (1) ZA201106560B (en)

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