JP2022528126A - 集積化co2回収による水素生成 - Google Patents
集積化co2回収による水素生成 Download PDFInfo
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- JP2022528126A JP2022528126A JP2021559074A JP2021559074A JP2022528126A JP 2022528126 A JP2022528126 A JP 2022528126A JP 2021559074 A JP2021559074 A JP 2021559074A JP 2021559074 A JP2021559074 A JP 2021559074A JP 2022528126 A JP2022528126 A JP 2022528126A
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Abstract
Description
種々の態様において、反応器の作動の間に生じるCO2の管理を改善しながら、逆流反応器環境(又はフローが反対方向である別の反応器環境)内で炭化水素の改質を実行するためのシステム及び方法が提供される。改善されたCO2の管理は、逆流反応器の作動の1つ又はそれ以上に変更を行うことによって達成される。1つの変化は、減少又は最小化された窒素含有量を有する酸素源を提供するために、空気分離ユニットを使用することであることが可能である。これによって、燃焼ガス中に存在する希釈ガスの量を減少又は最小化させながら、反応器の再生の間に生じる燃焼ガス中のCO2の濃度を増加させることが可能である。別の変化は、再生段階の間に高圧で反応器を作動させることであることが可能である。高圧で再生を作動させることによって、高圧においてCO2がリッチな再生燃焼ガスを生じることが可能である。CO2エンリッチド流は、汚染物質として主に水を含むことが可能であり、そしてこれは、流れの圧力を実質的に維持しながら、冷却によって除去されることが可能である。これはその後のCO2の回収及び使用を促進することが可能である。さらに別の変化は、改質の間に生じる酸化炭素も高圧、CO2エンリッチド燃焼ガス流中に組み込まれるように、再生のために燃料の一部として改質生成物から分離されるテールガスを使用することを含むことが可能である。さらに別の変化は、COの追加的な生成の利益となるように、生成される水素の量を減少するように水性ガスシフト段階の作動を変性することであることが可能である。燃焼する酸素あたり生じる熱に関して、COの燃焼は、CH4又はH2の燃焼より多くの熱を生じる。これによって、空気分離ユニットのサイズの減少を可能にすることが可能である。
逆流反応器、及び/又は反応サイクルの異なる段階において反対方向の流れを有する他の反応器は、600℃以上又は800℃以上などの高温において吸熱反応を実行する場合に有用となることが可能である。燃焼流、再生流、又は燃料混合物と記載されることのある第1の方向からの流れを使用して、反応器内の反応領域の1つ又はそれ以上の表面を所望の温度に加熱することが可能である。次いで、反対方向の流れを使用して、所望の吸熱反応のための試薬を届けることが可能である。再生ステップの間に反応器内に貯蔵される熱は、所望の吸熱反応に熱を提供するために使用される。
いくつかの態様において、再生ステップのための燃料混合物への変更の1つは、改質流出物の分離からのテールガスを添加することによって燃料を変性することであることが可能である。そのような態様において、改質流出物の加工及び分離を、CO含有が増加したテールガスを提供するように変更することも可能である。
(1)H2O+CO⇔H2+CO2
図1は、逆流反応器を含む反応システム中での炭化水素改質による集積化炭素回収のために適切な反応システムの例を示す。図1に示される例において、反応システムは複数の逆流反応器を含む。合計5つの反応器が図1に示されるが、いずれかの都合のよい数の反応器が使用可能であることは理解される。複数の反応器を使用することにより、反応生成物の連続又は実質的に連続な流れを、精製所、化学工場又は他の施設の下流部分へのインプットとして提供することが可能である。
炭化水素改質などの高温で作動される吸熱反応に関して、逆流反応器は、吸熱反応に熱を提供するために適切な反応環境を提供することが可能である。
逆流反応器システム中で実行可能な反応の例は、H2Oの存在下の蒸気改質条件下、CO2の存在下の乾燥改質条件下、又は反応環境中にH2O及びCO2の両方が存在する条件下での炭化水素の改質である。逆流反応器などのスイング反応器中での改質の間の作動の一般概要として、反応サイクルの再生ステップ又は部分を使用して反応器のための熱を提供することができる。次いで、改質はサイクルの改質ステップ又は部分の間に生じることが可能であり、改質反応によって、反応器再生ステップの間に提供された熱が消費される。反応器再生の間、燃料、酸化体及び希釈剤は、反応器の再生端部から反応器中に導入される。反応器の再生部分中の層及び/又はモノリスは熱を吸収することができるが、再生部分の少なくとも一部分は典型的に改質のための触媒を含まない。燃料及び酸化体が再生部分を通過すると、熱は再生部分から燃料及び酸化体へ伝達する。燃焼はすぐに生じないが、その代わりに、燃焼の位置が反応器の中央部分で生じるように制御される。燃料、酸化体及び希釈剤のフローは再生ステップの間に継続し、そして反応器の反応領域/改質端部中への燃焼から生じる熱の追加的な伝達が導かれる。
(2)乾燥改質:CH4+CO2=2CO+2H2
(3)蒸気改質:CH4+H2O=CO+3H2
(4)バイ改質:3CH4+2H2O+CO2=4CO+8H2。
燃焼モデルを使用して、燃焼の間の希釈剤ガスの組成の変化に基づき、層流火炎変速を決定した。モデル化された燃焼反応において、H2、O2及び希釈剤のガスフローを燃焼した。燃料の量は、全ガスフローの約10%に相当する。試験の第1の組合せにおいて、種々の量のCO2を有する希釈剤を使用して、400℃、500℃、600℃及び700℃の温度で燃焼をモデル化した。図2に、モデル化された燃焼反応からの火炎速度を示す。図2に示すように、500℃以下の温度において、希釈剤ガスの性質は火炎速度に対して影響をほとんど有さないか、又は有さなかった。しかしながら、600℃以上の温度において、100体積%のN2に相当する希釈剤ガスは、火炎速度の実質的な増大を示す。CO2が希釈剤中にブレンドされると、火炎速度の増加は減少し、希釈剤中10体積%以上のCO2量に関して、火炎速度の予想外に大きい減少が生じる。25体積%又は30体積%のCO2において、600℃以上の火炎速度は、ほぼ500℃以下の火炎速度値まで減少する。
パイロットスケール反応器(約12インチ/約30cmの長さ)を使用して、逆流反応器システムの作動に及ぼす燃焼ガス出口温度の変更の影響及び利益を調査した。本明細書に提供される例は単一反応器からの結果に相当するが、当業者は複数の逆流反応器を含む反応システムへの以下の結果の適用を容易に理解するであろう。
作業流体の体積を減少させた状態で高圧で逆流反応器を作動することの利点を示すために、熱効率の計算を実行し、炭素分離によるメタン改質を実行することに関する熱効率を決定した。第1の構成は、図1に示される構成と類似の、高熱容量作業流体を用いて高い再生圧力で逆流反応器を作動することに相当した。これによって、高圧、高純度CO2生成物を生成するために最小量の追加的なプロセシングのみを必要とする高圧CO2含有流が得られた。第2の構成は、熱を改質反応に提供するために使用される燃料からCO2を90%回収するための従来のアミンプラントで、従来の蒸気メタン改質を実行することに相当した。次いで、回収されたCO2は、図1に示される構成によって生成された高圧CO2含有流に匹敵する流れを生じるために圧縮された。
実施形態1.燃焼ガスを形成するため、そして触媒組成物を含む反応領域中の1つ又はそれ以上の表面を600℃以上の再生表面温度まで加熱するために、反応器内の燃焼領域中で0.7MPa-g以上の燃焼圧力を含む燃焼条件下で、燃料流、酸素含有流の体積に対して15体積%以下のN2を含む酸素含有流、及びリサイクル流を含む、燃料混合物の体積に対して0.1体積%以上のO2及び20体積%以上のCO2を含む燃料混合物を反応させること;燃焼ガスを分離して、少なくとも0.7MPa-g以上の第2の圧力を含むCO2含有流とリサイクル流とを形成すること;並びに改質条件下、再生表面温度において反応領域中で触媒組成物に炭化水素含有流を暴露して、H2及びCOを含む改質生成物流を形成することを含む、改質を実行する方法であって、反応領域中の炭化水素含有流の流れ方向が、燃料混合物の流れの方向に対して逆になる方法。
Claims (15)
- 燃焼ガスを形成するため、及び触媒組成物を含む反応領域中の1つ又はそれ以上の表面を600℃以上の再生表面温度まで加熱するために、反応器内の燃焼領域中で0.7MPa-g以上の燃焼圧力を含む燃焼条件下で、燃料流、酸素含有流の体積に対して15体積%以下のN2を含む酸素含有流、及びリサイクル流を含む、燃料混合物の体積に対して0.1体積%以上のO2及び20体積%以上のCO2を含む燃料混合物を反応させること;前記燃焼ガスを分離して、少なくとも0.7MPa-g以上の第2の圧力を含むCO2含有流と前記リサイクル流とを形成すること;並びに改質条件下、前記再生表面温度において前記反応領域中で前記触媒組成物に炭化水素含有流を暴露して、H2及びCOを含む改質生成物流を形成することを含む、改質を実行する方法であって、前記反応領域中の前記炭化水素含有流の流れ方向が、前記燃料混合物の流れの方向に対して逆になる方法。
- 前記燃焼条件が1.4MPa-g以上の燃焼圧力を含むか;又は前記第2の圧力が1.4MPa-g以上であるか;又はそれらの組合せである、請求項1に記載の方法。
- 前記燃焼条件が3.4MPa-g以上の燃焼圧力を含むか;又は前記第2の圧力が3.4MPa-g以上であるか;又はそれらの組合せである、請求項1又は2に記載の方法。
- 少なくとも前記CO2含有流及び前記リサイクル流を形成するために前記燃焼ガスを分離する前に、前記燃焼ガスを圧縮することをさらに含む、請求項1~3のいずれか一項に記載の方法。
- 前記改質生成物流を水性ガスシフト反応条件に暴露して、シフトされた合成ガス生成物流を形成すること;及び前記シフトされた合成ガス生成物流を分離して、H2含有流及びCO2を含む流れを形成することをさらに含み、前記シフトされた合成ガス流が、任意選択的に、10未満のCOに対するH2のモル比を含む、請求項1~4のいずれか一項に記載の方法。
- 前記シフトされた合成ガス生成物流が圧力スイング吸着によって分離され、前記CO2を含む流れが、前記CO2を含む流れの体積に対して5.0体積%以上のCOを含むテールガスを含み、且つ前記燃料混合物が、前記CO2を含む流れの少なくとも一部分を含む、請求項5に記載の方法。
- a)前記リサイクル流及び前記燃料流の少なくとも1つが15体積%以下のN2を含むか;又はb)前記方法が、前記酸素含有流を形成するために空気分離ユニット中で空気を分離することをさらに含むか;又はc)a)及びb)の組合せである、請求項1~6のいずれか一項に記載の方法。
- 前記反応器に入る前に、前記燃料流、前記酸素含有流及び前記リサイクル流を組み合わせて、前記燃料混合物が形成されるか、又は前記燃焼領域に入る前に、前記燃料流、前記酸素含有流及び前記リサイクル流を組み合わせて、前記燃料混合物が形成されるか、又はその組合せである、請求項1~7のいずれか一項に記載の方法。
- 前記リサイクル流が25体積%以上のCO2を含む、請求項1~8のいずれか一項に記載の方法。
- 前記燃料混合物が2.0体積%以上のCOを含む、請求項1~9のいずれか一項に記載の方法。
- 前記再生表面温度が800℃以上である、請求項1~10のいずれか一項に記載の方法。
- 前記CO2含有流を分離して、水を含有する流れ、及び80体積%以上のCO2含有量を含むCO2エンリッチド流を形成すること;並びに前記CO2エンリッチド流の圧力に対して7.0MPa-g以上の圧力まで前記CO2エンリッチド流を圧縮することをさらに含む、請求項1~11のいずれか一項に記載の方法。
- 前記燃焼条件が100cm/秒以下の層流火炎速度を含む、請求項1~12のいずれか一項に記載の方法。
- 反応器入口端部、再生器入口端部、及び改質触媒を含む反応領域を含む反応器;前記反応器入口端部と前記再生器入口との間で断続的な流体連通を提供する、リサイクルループであって、リサイクル圧縮器、燃料源入口、酸素含有ガス入口及びCO含有ガス出口を含むリサイクルループ;前記酸素含有ガス入口と流体連通する空気分離ユニット;並びにCO2含有ガス出口と流体連通する水分離段階を含む、逆流反応器システム。
- 吸着器入口、生成物出口及びテールガス出口を含む圧力スイング吸着セパレーターをさらに含み、前記再生器入口端部が、前記吸着器入口と断続的に流体連通であり、前記テールガス出口が、前記リサイクルループと断続的に流体連通である、請求項14に記載の逆流反応器システム。
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