JP5869143B2 - 発電および石油増進回収のためのシステムおよび方法 - Google Patents
発電および石油増進回収のためのシステムおよび方法 Download PDFInfo
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- JP5869143B2 JP5869143B2 JP2014542478A JP2014542478A JP5869143B2 JP 5869143 B2 JP5869143 B2 JP 5869143B2 JP 2014542478 A JP2014542478 A JP 2014542478A JP 2014542478 A JP2014542478 A JP 2014542478A JP 5869143 B2 JP5869143 B2 JP 5869143B2
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- gas
- carbon dioxide
- process gas
- methane
- hydrocarbon
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Classifications
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- H—ELECTRICITY
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- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
- H01M8/0675—Removal of sulfur
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- C—CHEMISTRY; METALLURGY
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- E—FIXED CONSTRUCTIONS
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- E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/164—Injecting CO2 or carbonated water
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- E—FIXED CONSTRUCTIONS
- E21—EARTH DRILLING; MINING
- E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/34—Arrangements for separating materials produced by the well
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- E—FIXED CONSTRUCTIONS
- E21—EARTH DRILLING; MINING
- E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/34—Arrangements for separating materials produced by the well
- E21B43/40—Separation associated with re-injection of separated materials
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Description
[図1]
[蒸気質の炭化水素]
[コンデンセート除去システム]
[酸ガス除去システム]
[水素化脱硫および吸着ベッドシステム]
[予備改質器]
SCR=H2Oのモル流量/(H2+CO+C1−5アルカンのモル流量)(式1)
MSR=CH4モル%/(CH4モル%+H2モル%+COモル%)(式6)
[固体酸化物形燃料電池]
[水性ガスシフト反応炉システム]
[CO2分離および脱水のシステム]
[SOFCシステムを用いての炭化水素含有地層からの炭化水素流体の回収を増進する方法]
[支持装置]
Claims (33)
- 固体酸化物形燃料電池(SOFC)システムを用いて蒸気質炭化水素供給原料から石油増進回収(EOR)に適した精製された二酸化炭素生成物および余剰電気を生産する方法であって、
生産井を用いて炭化水素含有地層から炭化水素流体を生成するステップと、
生成された前記炭化水素流体から随伴ガスを分離することにより、前記蒸気質炭化水素供給原料を生成するステップと、
前記蒸気質炭化水素供給原料を前記SOFCシステム中に導入するステップと、
蒸気を前記SOFCシステムの予備改質器中に導入するステップと、
脱硫済みプロセスガスが生成され、予備改質器中に入り;改質されたプロセスガスが、前記脱硫済みプロセスガス中の非メタンアルカンを予備改質触媒の存在下でメタンおよび炭素酸化物に転化させることによって、前記予備改質器中で生成され;前記改質されたプロセスガスが、前記予備改質器から固体酸化物形燃料電池中に入り;そして精製された二酸化炭素生成物および余剰電気が生産されるように、前記SOFCシステムを作動させるステップと、を含み、
ここで、前記SOFCシステムが、前記蒸気質炭化水素供給原料の受容と、前記脱硫済みプロセスガス、石油増進回収のための前記精製された二酸化炭素生成物、および余剰電気の生産との双方を実行するように作動可能であり、前記SOFCシステムが、前記固体酸化物形燃料電池の上流側に流体連結し、かつ前記脱硫済みプロセスガスを受容することと、活性金属予備改質触媒の存在下で蒸気を用いて前記非メタンアルカンをメタンおよび炭素酸化物に転化することとの双方を実行するように作動可能である前記予備改質器と、電気を生産するように作動可能な前記固体酸化物形燃料電池と、を含み、
さらに、前記精製された二酸化炭素生成物を、注入井を用いて前記炭化水素含有地層中に導入するステップ、を含み、
前記炭化水素含有地層が前記炭化水素流体を含有し、かつ前記生産井および前記注入井を通じて別々に到達可能であり、前記炭化水素流体の一部に前記蒸気質炭化水素供給原料が含まれる、方法。 - 前記導入された蒸気が過熱蒸気であり、かつ250℃〜500℃の範囲の温度および8バール〜12バールの範囲の圧力を有する、請求項1に記載の方法。
- 前記脱硫済みプロセスガスが、200℃〜450℃の範囲の温度を有する、請求項1または2に記載の方法。
- 前記導入された脱硫済みプロセスガスに対する前記導入された蒸気の蒸気/炭素比(SCR)が、1.5〜3.0の範囲にある、請求項1〜3のいずれか1項に記載の方法。
- 前記改質されたプロセスガスのメタン選択比(MSR)が、0.90〜0.99の範囲にある、請求項1〜4のいずれか1項に記載の方法。
- 前記脱硫済みプロセスガスが、各々前記脱硫済みプロセスガスの乾量基準で、51〜66組成モルパーセントの範囲のメタンと、33〜45組成モルパーセントの範囲の非メタンアルカンとを含む、請求項1〜5のいずれか1項に記載の方法。
- 前記脱硫済みプロセスガスが、1.0〜2.0の範囲の、メタン/非メタンアルカンモルパーセント比を有する、請求項1〜6のいずれか1項に記載の方法。
- 前記改質されたプロセスガスが、各々が前記改質されたプロセスガスの乾量基準で、78〜88組成モルパーセントの範囲のメタンと、9〜12組成モルパーセントの範囲の炭素酸化物と、0.5〜10組成モルパーセントの範囲の水素とを含む、請求項1〜7のいずれか1項に記載の方法。
- 前記改質されたプロセスガスが、モル基準で、実質的に非メタンアルカンを含まない、請求項1〜8のいずれか1項に記載の方法。
- 前記改質されたプロセスガスが、モル基準で、硫黄および硫黄含有化合物を実質的に含まない、請求項1〜9のいずれか1項に記載の方法。
- 前記精製された二酸化炭素生成物が、モル基準で、実質的に非二酸化炭素成分を含まない、請求項1〜10のいずれか1項に記載の方法。
- 二酸化炭素リッチガスが酸ガス除去システム中で生成されて、CO2脱水システム中に入るように前記SOFCシステムを作動させるステップを更に含み、前記SOFCシステムが、前記予備改質器の上流側に流体連結し、かつ二酸化炭素リッチガスを生成するように作動可能な前記酸ガス除去システムと、前記予備改質器の下流側および前記酸ガス除去システムの双方に流体連結する前記CO2脱水システムとを更に含む、請求項1〜11のいずれか1項に記載の方法。
- 水素リッチガスがCO2分離システム中で生成されるように前記SOFCシステムを作動させ、かつ前記水素リッチガスの一部を水素化脱硫システムに送るステップを更に含み、前記SOFCシステムが、前記予備改質器の下流側に流体連結し、かつ水素リッチガスを生成するように作動可能な前記CO2分離システムと、前記予備改質器の上流側および前記CO2分離システムの双方に流体連結する前記水素化脱硫システムとを更に含む、請求項1〜12のいずれか1項に記載の方法。
- SOFCシステムを用いて、炭化水素含有地層からの炭化水素流体の回収を増進させる方法であって、
生産井を用いて前記炭化水素含有地層から炭化水素流体を生成するステップと、
前記生成された炭化水素流体から随伴ガスを分離するステップと、
前記随伴ガスを前記SOFCシステム中に導入するステップと、
前記SOFCシステムを作動させて、精製された二酸化炭素生成物を石油増進回収および余剰電気を生産するステップと、
前記精製された二酸化炭素生成物を、注入井を用いて前記炭化水素含有地層中に導入するステップと、
を含み、
前記炭化水素含有地層が前記炭化水素流体を含有し、かつ前記生産井および前記注入井を通じて別々に到達可能であり、前記SOFCシステムが、随伴ガスを受容し、かつ前記随伴ガスから、石油増進回収に適した精製された二酸化炭素生成物および余剰電気を生産するように作動可能であり、前記炭化水素流体の一部に前記随伴ガスが含まれる、
方法。 - 蒸気質炭化水素供給原料から、EORに適した精製された二酸化炭素生成物および余剰電気を生成するためのSOFCシステムであって、
前記蒸気質炭化水素供給原料を受容し、かつ前記蒸気質炭化水素供給原料から高炭素化合物を分離して乾燥サワーガスを生成するように作動可能なコンデンセート除去システムと、
前記コンデンセート除去システムに流体連結し、かつ前記乾燥サワーガスから硫化水素を抽出して乾燥スイートガスを生成するように作動可能な酸ガス除去システムと、
前記酸ガス除去システムに流体連結し、かつ水素化処理触媒の存在下で水素を用いて、前記乾燥スイートガス中のヘテロ有機化合物を吸着ベッド材料に吸収される化合物に転化して処理済みプロセスガスを生成するように作動可能な水素化脱硫システムと、
前記水素化脱硫システムに流体連結し、かつ前記吸着ベッド材料に吸収される化合物を前記処理済みプロセスガスから抽出して脱硫済みプロセスガスを生成するように作動可能な吸着ベッドシステムと、
前記吸着ベッドシステムに流体連結し、かつ活性予備改質触媒の存在下で蒸気を用いて前記脱硫済みプロセスガス中の非メタンアルカンをメタンおよび炭素酸化物に転化して改質済みのプロセスガスを生成するように作動可能な予備改質器と、
前記予備改質器に流体連結し、かつ改質触媒および電気化学転化触媒の存在下で酸素を用いて前記改質済みプロセスガス中のメタンを二酸化炭素および水に転化して陽極排ガスを生成し、かつ電気を生成するように作動可能な固体酸化物形燃料電池と、
前記固体酸化物形燃料電池に流動連結し、かつ前記陽極排ガスから二酸化炭素を抽出して二酸化炭素リッチガスを生成するように作動可能なCO2分離システムと、
前記CO2分離システムに流動連結し、かつ前記二酸化炭素リッチガスから水を抽出して前記精製された二酸化炭素生成物を生成するように作動可能なCO2脱水システムと、
を備え、
前記SOFCシステムが、前記固体酸化物形燃料電池によって生成された電気から余剰電気を生産するように作動可能である、
SOFCシステム。 - 下流側において前記固体酸化物形燃料電池に流動連結し、かつ水性ガスシフト触媒の存在下で水を用いて前記陽極排ガス中の一酸化炭素を二酸化炭素および水素に転化してシフト済み陽極排ガスを生成するように作動可能な水性ガスシフト反応炉システムを更に備え、前記CO2分離システムが、前記固体酸化物形燃料電池の代わりに前記水性ガスシフト反応炉システムに流体連結し、かつ前記固体酸化物形燃料電池の前記陽極排ガスの代わりに前記水性ガスシフト反応炉システムの前記シフト済み陽極排ガスから二酸化炭素を抽出して前記二酸化炭素リッチガスを生成するように作動可能な、請求項15に記載のSOFCシステム。
- 前記酸ガス除去システムが、前記乾燥サワーガスから二酸化炭素を抽出して二酸化炭素リッチガスを生成するように更に作動可能であり、前記CO2脱水システムが、前記酸ガス除去システムに更に流体連結し、かつ前記酸ガス除去システムからの前記二酸化炭素リッチガスから二酸化炭素を抽出するように作動可能である、請求項15または16に記載のSOFCシステム。
- 前記CO2分離システムが、水素リッチガスを生成するように更に作動可能であり、前記水素化脱硫システムが、前記CO2分離システムに更に流体連結し、かつ前記CO2分離システムからの水素リッチガスを水素の源として用いるように作動可能である、請求項15〜17のいずれか1項に記載のSOFCシステム。
- 前記コンデンセート除去システムが、低温冷却された液体を利用して、前記蒸気質炭化水素供給原料から高炭素化合物を分離する、請求項15〜18のいずれか1項に記載のSOFCシステム。
- 前記コンデンセート除去システムが、吸収抽出プロセスを利用して、前記蒸気質炭化水素供給原料から高炭素化合物を分離する、請求項15〜19のいずれか1項に記載のSOFCシステム。
- 前記酸ガス除去システムが、反応性液体を利用して、硫化水素を抽出する、請求項15〜20のいずれか1項に記載のSOFCシステム。
- 前記固体酸化物形燃料電池の陽極側が、メタンを間接的に内部改質するように作動可能である、請求項15〜21のいずれか1項に記載のSOFCシステム。
- 前記固体酸化物形燃料電池の陽極側が、メタンを直接的に内部改質するように作動可能である、請求項15〜22のいずれか1項に記載のSOFCシステム。
- 前記CO2分離システムが、圧力スイング吸着法を利用して、二酸化炭素を分離する、請求項15〜23のいずれか1項に記載のSOFCシステム。
- 前記CO2脱水システムが、前記精製された二酸化炭素生成物を液化するようにさらに作動可能である、請求項15〜24のいずれか1項に記載のSOFCシステム。
- 前記蒸気質炭化水素供給原料が、随伴ガスである、請求項15〜25のいずれか1項に記載のSOFCシステム。
- 下流の固体酸化物形燃料電池の内部改質能力を最大化するために予備改質器を作動させる方法であって、
生産井を用いて炭化水素含有地層から炭化水素流体を生成するステップと、
生成された前記炭化水素流体から随伴ガスを分離することにより、プロセスガスを生成するステップと、
水素化脱硫システムにより、前記プロセスガスを脱硫するステップと、
脱硫済みプロセスガスを前記予備改質器中に導入するステップであって、前記脱硫済みプロセスガスが、200℃〜450℃の範囲の温度を有し、かつ各々が前記脱硫済みプロセスガスの乾量規準で、51〜66組成モルパーセントの範囲のメタンおよび33〜45組成モルパーセントの範囲の非メタンアルカンを含むステップと、
過熱蒸気を前記予備改質器中に導入するステップであって、前記過熱蒸気は、250℃〜500℃の範囲の温度および8バール〜12バールの範囲の圧力を有し、これにより前記導入された脱硫済みプロセスガスに対する前記導入された過熱蒸気の蒸気/炭素比(SCR)が0.5〜1.5の範囲にあるステップと、
改質済みプロセスガスが、前記脱硫済みプロセスガスおよび前記過熱蒸気から生成されるように前記予備改質器を作動させるステップであって、前記改質済みプロセスガスが、各々が前記改質済みプロセスガスの乾量規準で、78〜88組成モルパーセントの範囲のメタン、9〜12組成モルパーセントの範囲の炭素酸化物、および0.5〜10組成モルパーセントの範囲の水素を含むステップと、
を含み、
前記改質済みプロセスガスが、0.90〜0.99の範囲のメタン選択度を有し、前記予備改質器が、固体酸化物形燃料電池の上流側に流体連結し、かつ前記脱硫済みプロセスガスを受容することと、活性金属予備改質触媒の存在下で蒸気を用いて前記非メタンアルカンをメタンおよび炭素酸化物に転化することとの双方を実行するように作動可能であり、
さらに、前記炭素酸化物から生成された精製された二酸化炭素生成物を、注入井を用いて前記炭化水素含有地層中に導入するステップ、を含み、
前記炭化水素含有地層が前記炭化水素流体を含有し、かつ前記生産井および前記注入井を通じて別々に到達可能であり、前記炭化水素流体の一部に前記プロセスガスが含まれる、方法。 - 前記予備改質器を作動させることが、前記予備改質器を断熱的に作動させるステップを更に含む、請求項27に記載の方法。
- 前記生成された改質済みプロセスガスの温度が、前記導入された脱硫済みプロセスガスの温度より低い55℃〜80℃の範囲にある、請求項27または28に記載の方法。
- 前記脱硫済みプロセスガスの中のメタン/非メタンアルカンモルパーセント比が、1.0〜2.0の範囲にある、請求項27〜29のいずれか1項に記載の方法。
- 前記改質済みプロセスガスが、乾量規準で少なくとも10組成モルパーセントの二酸化炭素を含む、請求項27〜30のいずれか1項に記載の方法。
- 前記改質済みプロセスガスが、モル規準で非メタンアルカンを実質的に含まない、請求項27〜31のいずれか1項に記載の方法。
- 前記改質済みプロセスガスが、モル規準で硫黄および硫黄含有化合物を実質的に含まない、請求項27〜32のいずれか1項に記載の方法。
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