JP2016513867A - 製油所配置における溶融炭酸塩形燃料電池の集積化 - Google Patents
製油所配置における溶融炭酸塩形燃料電池の集積化 Download PDFInfo
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- JP2016513867A JP2016513867A JP2016501788A JP2016501788A JP2016513867A JP 2016513867 A JP2016513867 A JP 2016513867A JP 2016501788 A JP2016501788 A JP 2016501788A JP 2016501788 A JP2016501788 A JP 2016501788A JP 2016513867 A JP2016513867 A JP 2016513867A
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Abstract
Description
様々な態様において、溶融炭酸塩形燃料電池の作動は、様々な化学および/または材料製造プロセスと集積化することができる。製造プロセスは、溶融炭酸塩形燃料電池からのアウトプットの生成に相当することができ、あるいは製造プロセスは、1つ以上の燃料電池流を消費または提供することができる。
水素は、様々なプロセスのために製油所内で使用することができる。ほとんどの製油所は、いくつかのプロセス(例えば、芳香族化合物を製造するためのガソリン改質)において水素を発生し、かつ他のプロセス(例えば、ガソリンおよびディーゼルブレンド流からの硫黄除去)のために水素を使用する。追加的に、製油所はエネルギーを必要とする反応器を加熱するために、多数の煮沸器(又はボイラー)、炉および/または他のシステムを有することができる。水素は典型的に、他の燃料供給源よりも有用である可能性があるため、かつほとんどの製油所が、全体的な基準で、水素の正味の導入物であるため、これらの加熱および/またはエネルギー発生システムは一般に水素を利用しない。一般に、水素導入は、その場で構築することによって、および/または全体的な製油所に釣り合いをもたらすために、水素の付近の供給源/パイプライン供給源に接近することによって実行されることができる。
本明細書に記載される燃料電池作動戦略の追加、補足、および/または代替として、燃料電池のために所望の熱比率を達成するために、酸化の量と比較して改質の量を選択することができるように、溶融炭酸塩形燃料電池を作動させることができる。本明細書で使用される場合、「熱比率」は、燃料電池アセンブリで生じる改質反応の吸熱性熱需要で割られた燃料電池アセンブリでの発熱性反応によって発生した熱として定義される。数学的に表すと、熱比率(TH)=QEX/QENであり、QEXは発熱性反応によって発生する熱の合計であり、そしてQENは、燃料電池内で生じる吸熱性反応によって消費される熱の合計である。なお、発熱性反応によって発生する熱は、改質反応、水性ガスシフト反応および電池内での電気化学反応によるいずれかの熱に相当する。電気化学反応によって発生する熱は、燃料電池の実際の出力電圧を差し引いた、電解質全体での燃料電池反応の理想電気化学ポテンシャルをベースとして算出することができる。例えば、MCFCの反応の理想電気化学ポテンシャルは、電池で生じる正味の反応をベースとし、約1.04Vであると考えられている。MCFCの作動の間、電池は様々な損失のため、1.04V未満の出力電圧を典型的に有する。例えば、共通の出力/作動電圧は、約0.7Vであることができる。発生する熱は、電池の電気化学ポテンシャル(すなわち約1.04V)から作動電圧を引いたものに等しい。例えば、電池において電気化学反応によって発生する熱は、約0.7Vの出力電圧の場合、約0.34Vである。したがって、このシナリオで、電気化学反応は、約0.7Vの電気および約0.34Vの熱エネルギーを生じる。そのような実施例において、約0.7Vの電気エネルギーは、QEXの一部として含まれない。言い換えると、熱エネルギーは電気エネルギーではない。
アノード排出物中の正味の合成ガスとカソードCO2との比率=(H2+CO)ANODEの正味のモル/(CO2)CATHODEのモル
合成ガス:本記載において、合成ガスは、いずれかの比率でのH2とCOとの混合物として定義される。任意に、H2Oおよび/またはCO2が合成ガスに存在してもよい。任意に、不活性化合物(例えば、窒素)および残留する改質可能燃料化合物が合成ガスに存在してもよい。H2およびCO以外の成分が合成ガスに存在する場合、合成ガス中のH2およびCOの組み合わせられた体積パーセントは、合成ガスの全体積と比較して、少なくとも25体積%、例えば、少なくとも40体積%、または少なくとも50体積%、または少なくとも60体積%であることができる。追加的に、または代わりとして、合成ガス中のH2およびCOの組み合わせられた体積パーセントは、100体積%以下、例えば、95体積%以下、または90体積%以下であることができる。
本発明の様々な態様において、MCFCアレイには、例えば、水素および炭化水素、例えば、メタン(または代わりに、CおよびHとは異なるヘテロ原子を含有してもよい炭化水素もしくは炭化水素様化合物)を含んでなる、アノードインレットで受け取られる燃料が供給されることができる。アノードに供給される大部分のメタン(または他の炭化水素もしくは炭化水素様化合物)は、典型的に新しいメタンであることができる。本記載において、新しいメタンなどの新しい燃料は、別の燃料電池プロセスからリサイクルされない燃料を指す。例えば、アノードアウトレット流からアノードインレットにリサイクルされるメタンは、「新しい」メタンとは考えられず、その代わりに、回収されたメタンと記載することができる。使用された燃料供給源は、CO2含有流をカソードインプットに提供するために燃料供給源の一部分を使用するタービンなどの他の構成要素と共有されることができる。燃料供給源インプットは、水素を発生させる改質部分において炭化水素(または炭化水素様)化合物を改質するために、燃料に対して適切な割合で、水を含むことができる。例えば、メタンがH2を発生させるために改質するための燃料インプットである場合、水と燃料とのモル比(又は燃料に対する水のモル比)は、約1:1〜約10:1、例えば少なくとも約2:1であることができる。4:1以上の比率は外部改質に関して典型的であるが、内部改質に関してはより低い値が典型的であることができる。H2が燃料供給源の一部分である範囲まで、いくつかの任意の態様において、アノードにおけるH2の酸化が、燃料を改質するために使用することができるH2Oを生じる傾向があることが可能であるため、追加的な水は燃料に必要とされなくてもよい。燃料供給源は、燃料供給源に重要ではない成分を任意に含有することもできる(例えば、天然ガス供給は、追加的な成分としてCO2のいくらかの含有量を含有することができる)。例えば、天然ガス供給は、追加的な成分として、CO2、N2および/または他の不活性(不活性)ガスを含有することができる。任意に、いくつかの態様において、燃料供給源は、アノード排出物のリサイクルされた部分からのCOなどのCOを含有してもよい。燃料電池アセンブリへの燃料におけるCOのための追加的、または代わりの潜在的供給源は、燃料電池アセンブリに入る前に燃料において実行される炭化水素燃料の蒸気改質によって発生するCOであることができる。
Keq=[CO2][H2]/[CO][H2O]
従来、溶融炭酸塩形燃料電池は、アノードに送られる燃料流における燃料のいくらかの部分を消費しながら、所望の負荷を引き出すことをベースとして作動されることができる。次いで、燃料電池の電圧は、負荷、アノードへの燃料インプット、カソードに提供される空気およびCO2、ならびに燃料電池の内部抵抗によって決定することができる。カソードへのCO2は、従来、カソードインプット流の少なくとも一部分としてアノード排出物を使用することによって、部分的に提供されることができる。対照的に、本発明はアノードインプットおよびカソードインプットのための別々の/異なる供給源を使用することができる。アノードインプットフローおよびカソードインプットフローの組成物のいずれの直接的な関連も除去することによって、追加的な選択肢は、燃料電池を作動するために利用可能になり、例えば、過剰量の合成ガスを発生させ、二酸化炭素の捕捉を改善し、および/または特に、燃料電池の全体効率(電気および化学動力)を改善する。
様々な態様において、燃料電池(例えば、複数の燃料電池積層を含有する燃料電池アレイ)のための構成選択肢は、複数の燃料電池間でCO2含有流を分割することであることができる。CO2含有流のいくつかの種類の供給源は、個々の燃料電池の能力と比較して、大きい体積フローレートを発生させることができる。例えば、工業用の燃焼供給源からのCO2含有アウトプット流は、典型的に、適切な径の単一MCFCのために望ましい作動条件と比較して大きいフロー体積に相当することができる。単一MCFCで全フローを処理する代わりに、それぞれのユニットのフローレートが所望のフロー範囲内にあることができるように、通常そのなかの少なくともいくつかが並列であることができる複数のMCFCユニットの間にフローを分割することができる。
いくつかの態様において、燃料電池は、単回通過または貫流モードで作動されてよい。単回通過モードにおいては、アノード排出物の改質された生成物はアノードインレットに戻されない。したがって、アノードアウトプットから直接、アノードインレットに合成ガス、水素またはいくつかの他の生成物をリサイクルすることは、単回通過作動では行われない。より一般に、単回通過作動において、アノード排出物の改質された生成物は、例えば、その後アノードインレットに導入された燃料流を処理するために改質された生成物を用いることによって、アノードインレットに間接的にも戻されない。任意に、アノードアウトレットからのCO2は、単回通過モードのMCFCの作動の間、カソードインレットにリサイクルされることができる。より一般に、いくつかの別の態様において、アノードアウトレットからカソードインレットへのリサイクルは、単回通過モードで作動するMCFCに関して生じてもよい。アノード排出物またはアウトプットからの熱は、単回通過モードにおいて追加的に、または代わりとしてリサイクルされてもよい。例えば、アノードアウトプットフローは熱交換器を通過してもよく、そこでは、アノードアウトプットは冷却されて、そして別の流れ、例えばアノードおよび/またはカソードのためのインプット流が加温される。アノードから燃料電池まで熱をリサイクルすることは、単回通過または貫流モード作動における使用と調和する。任意に、しかし好ましくはないが、アノードアウトプットの成分は、単回通過モードの間、燃料電池に熱を提供するために燃焼されてもよい。
本発明の様々な態様において、上記のシステムおよび方法によって、加圧流体としての二酸化炭素の生成を可能にすることができる。例えば、低温分離段階から発生するCO2は、最初、少なくとも約90%、例えば、少なくとも約95%、少なくとも約97%、少なくとも約98%、または少なくとも約99%の純度を有する加圧されたCO2液体に相当することができる。この加圧されたCO2流は、例えば、二次石油採集においてなど、さらに油またはガス回収を向上させるためのウェルへの注入に使用されることができる。ガスタービンを包含する設備の付近で実行される場合、全体的なシステムは、電気/機械的動力の使用における追加的な相乗効果から、および/または全体システムとの熱集積化を通して利益を得てもよい。
本発明のいくつかの態様において、動力を発生させるため、およびCO2含有排気物を排気するための燃焼供給源は、溶融炭酸塩形燃料電池の作動と集積化させることができる。適切な燃焼供給源の一例は、ガスタービンである。好ましくは、ガスタービンは、追加的な効率のために蒸気発生および熱回収と集積化された複合サイクルモードにおいて、天然ガス、メタンガスまたは他の炭化水素ガスを燃焼させることができる。現代の天然ガス複合サイクル効率は、最大および最新のデザインに関して、約60%である。得られるCO2含有排出物ガス流は、MCFC作動との適合性を有する高温、例えば、300℃〜700℃、好ましくは500℃〜650℃で生成することができる。ガス供給源は、任意であるが、好ましくは、タービンに入る前に、MCFCに悪影響を及ぼす可能性のある硫黄などの汚染物質をクリーニングすることができる。あるいは、ガス供給源は、排出物ガスが典型的に、排出物ガスの汚染物質のより高い濃度のため、燃焼後にクリーニングされる発電機であることができる。そのような代替案において、ガスへの/ガスからのいくらかの熱交換は、より低い温度でのクリーンアップを可能にするために必要とされてもよい。追加的または代わりの実施形態において、CO2含有排出物ガスの供給源は、煮沸器、燃焼室、または炭素の豊富な燃料を燃焼させる熱供給源からのアウトプットであることができる。他の追加的または代わりの実施形態において、CO2含有排出物ガスの供給源は、他の供給源と組み合わせた生物学的に生成されたCO2であることができる。
CO2の捕獲および最終的な分離のために燃料電池アレイに排出物ガスを提供することを除き、排出物ガスの追加的または代わりの潜在的用途は、CO2含有量を増加させるための燃焼反応へのリサイクルを含むことができる。燃焼電池アレイのアノード排出物からの水素などの水素が燃焼反応への添加のために利用可能である場合、燃焼反応の範囲内でCO2含有量を増加させるためにリサイクルされた排出物ガスを使用することから、さらなる利点を得ることができる。
図4は、タービンに動力を供給するために、CO2を含有するリサイクルされた排出物ガスおよび燃料電池アノード排出物からのH2またはCOの両方の燃焼反応への導入を含む、集積化されたシステムの実施例を概略的に示す。図4中、タービンは、圧縮器402、シャフト404、膨張器406および燃焼領域415を含むことができる。酸素供給源411(例えば、空気および/または酸素富化空気)を、リサイクルされた排出物ガス498と組み合わせ、そして燃焼領域415に入る前に圧縮器402において圧縮することができる。CH4などの燃料412、および任意にH2またはCO187を含有する流れを、燃焼領域まで送ることができる。燃料および酸化剤は、領域415において反応することができ、そして任意であるが、好ましくは、電力を発生させるために、膨張器406に通過させることができる。膨張器106からの排出物ガスは、2つの流れ、例えば、CO2含有流422(燃料電池アレイ425のためのインプット供給として使用することができる)および別のCO2含有流492(例えば、蒸気タービン494を使用して、追加的な電気の発生を可能にすることができる、熱回収および蒸気発生器システム490のためのインプットとして使用することができる)を形成するために使用することができる。CO2含有流からのH2Oの一部分の任意の除去を含む、熱回収システム490を通過した後、アウトプット流498は、圧縮器402または図示されない第2の圧縮器における圧縮のためにリサイクルすることができる。CO2含有流492のために使用される膨張器406からの排出物の割合は、燃焼領域415への添加のためのCO2の所望の量をベースとして決定することができる。
ガスタービンは、いくつかの因子によってそれらの作動で制限されることができる。1つの典型的な制限は、規制排出限界を満たすために、酸化窒素(NOx)の十分に低い濃度を達成するため、燃焼領域における最大温度が特定の限界より低く制御されることができるということであることができる。規制排出限界は、燃焼排出物を環境に出す時に、燃焼排出物が約20vppm以下、可能であれば10vppm以下のNOx含有量を有することを必要とすることができる。
実施形態1.改質可能燃料を含んでなる燃料流を、溶融炭酸塩形燃料電池のアノード、アノードと関連する内部改質要素、またはそれらの組み合わせに導入する(又は引き合わせる)ステップと;CO2およびO2を含んでなるカソードインレット流を、溶融炭酸塩形燃料電池のカソードに導入するステップと;溶融炭酸塩形燃料電池内で電気を発生させるステップと;H2およびCO2を含んでなるアノード排出物を生成させるステップと;アノード排出物において分離(例えば、膜を使用して)を実行し、アノード排出物のCO2含有量より高いCO2含有量を有するCO2豊富ガス流(又はCO2に富むガス流)、ならびにアノード排出物のCO2含有量より低いCO2含有量を有し、任意にH2豊富ガス流(又はH2に富むガス流)および合成ガス流を含んでなるCO2欠乏(又は減少)ガス流を形成するステップと;CO2欠乏ガス流を、1つ以上の第2の精製プロセスに送るステップとを含んでなる、製油所において水素を発生させる方法。
下記の実施例では、エネルギー供給源として燃料の燃焼を使用する、様々なバーナー、煮沸器および/または他のユニットに供給するための水素供給源としてMCFCシステムが使用された構成に関して、計算を実行した。以下の実施例は、燃焼反応に水素を供給することに焦点を合わせたが、MCFCによって発生する水素は、追加的に、または代わりとして、燃焼以外の目的のために水素を使用することができる1つ以上のプロセス(例えば、複数のプロセス)に供給するために使用されることができるであろう。例えば、MCFCによって発生する水素は、製油所内の1つ以上の水素化反応器において使用することができる。
Claims (15)
- 改質可能燃料を含む燃料流を、溶融炭酸塩形燃料電池のアノード、前記アノードと関連する内部改質要素、またはそれらの組み合わせに導入するステップ;CO2およびO2を含むカソードインレット流を、前記溶融炭酸塩形燃料電池のカソードに導入するステップ;前記溶融炭酸塩形燃料電池内で電気を発生させるステップ;H2およびCO2を含むアノード排出物を生成させるステップ;前記アノード排出物において分離(例えば、膜を使用して)を行い、前記アノード排出物のCO2含有量より高いCO2含有量を有するCO2豊富ガス流、ならびに前記アノード排出物の前記CO2含有量より低いCO2含有量を有し、任意にH2豊富ガス流および合成ガス流を含むCO2欠乏ガス流を形成するステップ;及びCO2欠乏ガス流を、1つ以上の第2の精製プロセスに送るステップを含む、製油所で水素を発生させる方法。
- 前記カソードインレット流が、1つ以上の第1の精製プロセスから直接または間接的に誘導される1つ以上のCO2含有流を含む、請求項1に記載の方法。
- 前記溶融炭酸塩形燃料電池が、約0.25〜約1.5(例えば、約0.25〜約1.3、約0.25〜約1.15、約0.25〜約1.0、約0.25〜約0.85、または約0.25〜約0.75)の熱比率で作動される、請求項1または2に記載の方法。
- 1つ以上の分離段階において、前記アノード排出物、前記CO2欠乏流、および前記CO2豊富流の少なくとも1つからH2Oを分離するステップをさらに含む、請求項1〜3のいずれかに記載の方法。
- 前記アノード、前記アノードと関連する前記内部改質要素、または前記それらの組み合わせに導入される前記改質可能燃料の量が、少なくとも約1.5(例えば、少なくとも約2.0、少なくとも約2.5、または少なくとも約3.0)の改質可能燃料過剰比率を与える、請求項1〜4のいずれかに記載の方法。
- 前記アノード排出物における合成ガスの正味のモルとカソード排出物におけるCO2のモルとの比率が、少なくとも約2.0(例えば、少なくとも約3.0、少なくとも約4.0、少なくとも約5.0、少なくとも約10.0、または少なくとも約20.0)であり、かつ任意に約40.0以下(例えば、約30.0以下、または約20.0以下)である、請求項1〜5のいずれかに記載の方法。
- 前記アノードにおける燃料利用が、約50%以下(例えば、約45%以下、約40%以下、約35%以下、約30%以下、約25%以下、または約20%以下)であり、かつ前記カソードにおけるCO2利用が、少なくとも約60%(例えば、少なくとも約65%、少なくとも約70%、または少なくとも約75%)である、請求項1〜6のいずれかに記載の方法。
- 少なくとも約150mA/cm2の電流密度を提供する第1の作動条件で、前記溶融炭酸塩形燃料電池を作動して、電力および少なくとも約50mW/cm2(例えば、少なくとも約80mW/cm2、または少なくとも100mW/cm2)の廃熱が発生し、かつ吸熱性反応の有効な量を、約100℃以下(例えば、約80℃以下または約60℃以下)のアノードインレットとアノードアウトレットとの間の温度差を維持するために行う、請求項1〜7のいずれかに記載の方法。
- 前記吸熱性反応を行うことによって、前記廃熱の少なくとも約40%(例えば、少なくとも約50%、少なくとも約60%、または少なくとも約75%)を消費する、請求項8に記載の方法。
- 前記溶融炭酸塩形燃料電池の電気効率が、約10%〜約40%(例えば、約10%〜約35%、約10%〜約30%、約10%〜約25%、または約10%〜約20%)であり、かつ前記溶融炭酸塩形燃料電池の全燃料電池効率が、少なくとも約55%(例えば、少なくとも約60%、少なくとも約65%、少なくとも約70%、少なくとも約75%、または少なくとも約80%)である、請求項1〜9のいずれかに記載の方法。
- 前記1つ以上の第1の製油所プロセスの少なくとも1つのプロセスが、前記1つ以上の第2の製油所プロセスのプロセスであること;前記燃料流が、1つ以上の第3の製油所プロセスから誘導されること;および前記アノード排出物が、少なくとも約3.0:1のH2とCOとのモル比を有し、かつ少なくとも約10体積%のCO2含有量を有すること:の1つ以上を満たす、請求項1〜10のいずれかに記載の方法。
- 前記燃料流の少なくとも一部分が、前記アノードに導入される前に、予備改質段階を通る、請求項1〜11のいずれかに記載の方法。
- 前記燃料流の少なくとも一部分が、前記アノードに導入される前に、脱硫段階を通る、請求項1〜12のいずれかに記載の方法。
- 水性ガスシフトプロセスを使用して、前記アノード排出物、前記CO2豊富ガス流、および前記CO2欠乏ガス流の1つ以上のH2含有量を変更するステップをさらに含む、請求項1〜13のいずれかに記載の方法。
- 前記CO2欠乏ガス流が、第1のH2純度を有する第1のH2豊富流および第2のH2純度を有する第2のH2豊富流にさらに分離され、前記第2のH2豊富流が、前記第1のH2豊富流より高い圧力に圧縮される、請求項1〜14のいずれかに記載の方法。
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