JP2022522968A - オレフィン合成における再生可能エネルギーの使用 - Google Patents
オレフィン合成における再生可能エネルギーの使用 Download PDFInfo
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- JP2022522968A JP2022522968A JP2021540821A JP2021540821A JP2022522968A JP 2022522968 A JP2022522968 A JP 2022522968A JP 2021540821 A JP2021540821 A JP 2021540821A JP 2021540821 A JP2021540821 A JP 2021540821A JP 2022522968 A JP2022522968 A JP 2022522968A
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- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
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- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
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- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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Abstract
Description
本開示は、オレフィンの合成における再生可能エネルギーの使用に関する。さらに詳細には、本開示は、オレフィン合成プラントの電化に関する。さらになお詳細には、本開示は、オレフィン合成プラントにおける燃料のための炭化水素(例えば、天然ガス/化石燃料)の燃焼を低減することによる環境排出物、例えば、二酸化炭素の低減に関する。
化学合成プラントは、様々な化学物質を提供するために利用される。多くの場合、専用の燃料が燃やされるか「燃焼」されて、化学合成のための反応熱、1つもしくは複数のプロセス流を加熱するためのエネルギー、液体を気化させるためのエネルギー(例えば、希釈剤として使用される水を沸騰させる)、作業をするためのエネルギー(例えば、圧縮機またはポンプを駆動する)、または化学合成プラント全体の他のプロセス動作のためのエネルギーが供給される。燃料をこのように燃やすか燃焼させると、環境に有害であり得る排煙が生成され、プロセスのエネルギー効率も低下する。同様に、水蒸気は、化学合成プラント内のプラント全体の熱および/またはエネルギー伝達流体として従来から利用されることが多い。熱および/またはエネルギー伝達に利用される水蒸気は、多くの場合、燃料の燃焼によって生成され、その結果、追加の排煙が生成され、化学合成中にエネルギー効率がさらに低下する。さらに、燃料として燃焼させるための反応物として他の方法で利用され得る材料の使用はまた、所与の量の材料から化学合成プラントで生成される所望の化学生成物の量を減少させる。したがって、エネルギーを供給するために燃やされる燃料、特に化石燃料の量を低減または排除する、化学合成の増強されたシステムおよび方法が必要とされている。望ましくは、そのようなシステムおよび方法はまた、化学合成プラントによるエネルギー効率の増加および/または温室効果ガス(GHG)の排出量などの排出量の減少をもたらす。
本明細書において、供給流を前処理するように構成された供給物前処理セクション;希釈剤の存在下で供給流中の炭化水素を分解して分解ガス流を生成するように構成された1つまたは複数の熱分解反応器を備える熱分解セクション;分解ガス流からの熱回収と、分解ガス流のクエンチとを提供し、分解ガス流から燃料油、硫化水素、二酸化炭素、水、熱分解ガソリンまたはそれらの組合せを除去し、分解ガス流を圧縮し、それにより圧縮された分解ガス流を提供するように構成された一次分留および圧縮セクション;および/または圧縮された分解ガス流から生成物オレフィン流を分離するように構成された生成物分離セクションを備える、軽質オレフィンを生成するためのオレフィン合成プラントであって、従来のオレフィン合成プラントと比較して、オレフィン合成プラント、供給物前処理セクション、熱分解セクション、一次分留および圧縮セクション、生成物分離セクションまたはそれらの組合せによって必要とされるエネルギーおよび/または正味エネルギーのさらに多くが、非炭素系エネルギー源、再生可能エネルギー源および/または電気によって供給されるようにオレフィン合成プラントが構成されている、オレフィン合成プラントが開示される。
最初に、1つまたは複数の態様の例示的な実装形態が以下に提供されるが、開示される組成物、方法および/または生成物は、現在知られているか、未だ存在していないかにかかわらず、任意の数の技術を使用して実装され得ることを理解されたい。本開示は、本明細書において図示および説明される例示的な設計および実装形態を含む、以下に図示される例示的な実装形態、図面および技術に決して限定されるべきではなく、それらの均等物の全範囲とともに添付の特許請求の範囲内で変更され得る。
エタンの水蒸気分解によるエチレンの生成のための典型的なプロセスIIIの熱および質量流量を決定するために、プロセスシミュレーションを行った。この比較例1で利用したプロセスシミュレーションは、Aspen Plus(登録商標)を使用して行った。これは特定の動作プラントを表すものではないが、図5を参照して以下に説明する典型的なプラントを表す。設計パラメータは、特定のプラントの知識、および典型的なプロセス動作に関する文献情報から得た。変形例は当業者には明らかであるが、この比較例1は、本開示の態様による電化変更の効果を比較するための基礎として使用することができる典型的なプロセスを表す。
実施例1は、比較例1に記載される水蒸気分解プロセスの本開示の一態様による部分電化である。実施例1では、補助ボイラが取り外され、天然ガスの燃焼によってそのボイラに供給されていたエネルギーが、それよりも少量の再生可能電気に置き換えられる。外部エネルギーのこの置き換えは、プロセスのエネルギー統合のいくらかの再構成を必要とする。実施例1では、最も重要な差は、(1)極低温冷凍システムおよびいくつかのポンプがここでは電気モータによって駆動されること、(2)希釈水蒸気を作るための再循環水の気化に必要なエネルギーの一部が電気加熱によって供給されること、ならびに(3)高温生成物ガスの冷却から回収された熱の多くが供給ガスを予熱するために使用されるように、TLEが熱交換器システムに置き換えられていることである。
実施例2は、比較例1に記載される水蒸気分解プロセスの本開示の一態様による完全電化である。実施例2では、比較例1では天然ガス燃焼補助ボイラおよび分解炉によって供給されるエネルギーは再生可能電気に置き換えられ、再生可能電気は、あらゆる圧縮機およびポンプに動力供給し、分解のためのエネルギーを供給し、再循環水および補給水の気化のための熱を提供する。また、比較例1のTLEは、高温の生成物ガスの冷却から回収された熱の多くが供給ガスを予熱するために使用されるように、熱交換器システムに置き換えられている。これらの変化は、プロセス水蒸気システムの排除と、排煙損失の完全な回避とを可能にする。
実施例3は、比較例1に記載される水蒸気分解プロセスの本開示の一態様による完全電化である。この例では、実施例1とは対照的に、伝達ライン交換器223は保持され、それによって捕捉されたエネルギーは水蒸気に変換され、様々な目的に使用されるが、供給物予熱、熱分解反応セクション220の熱分解反応器、および233の分解ガス圧縮機を含むプロセスの他の部分は電化されている。
一態様では、図9に示すように、プロセスVIIは、実施例2に記載のプロセスVに追加されたガス分離ユニット260を備える。ガス分離ユニット260は、圧力スイング吸着(PSA)ユニットを備えることができる。ガス分離ユニット260は、水素およびメタン含有流244を精製するように構成される。上記の実施例2によれば、流れ244は、30.1t/hrの流量を有し、48重量%(88mol%)の水素および52重量%(12mol%)のメタンを含む。ガス分離ユニット260(例えば、PSAガス分離ユニット260)は、3MWの電気を消費し、純粋なメタンから本質的になるメタン流247および純粋な水素から本質的になる水素流248の2つの生成物流を生じる。このプロセスVIIを介して、PSA260内で生成された14.3t/hrの量の精製水素を燃料電池270に供給することができ、そこで水素は水流249中の水に、および電気効率45%で電気Eに変換され、253MWの電気の連続生成をもたらす。正味の電気(250MW)は、プロセスに必要な603MWの電気の41%を供給するために使用される(実施例2のプロセスVについて上述されるように;表2を参照されたい。)
態様では、実施例4に記載のプロセスVIIは、水素圧縮貯蔵装置280をさらに備え、この装置は、少なくとも1つの圧縮機および貯蔵容器を備え、再生可能電気の利用可能性が比較的低い場合または比較的高価である場合に使用するために、得られた14.3t/hrの精製水素(ライン248Aを介してそこに導入され得る)を圧縮し貯蔵するように構成される。必要に応じて、圧縮および貯蔵された水素は、プロセスVIIによってその時点で生成されている水素(例えば、ライン248内の水素)と組み合わされ得(例えば、ライン248Bを介して)、その両方を燃料電池270を使用して電気に変換することができる。電気生成のために貯蔵された水素を使用する時期は、様々な要因に従って当業者によって決定され得る。1つの可能性として、一部の再生可能電気が日中ベースで利用可能である場合、172トンの水素を収集し、12時間にわたって貯蔵することができる。次の12時間にわたって放出し、プロセスによってなおも生成されている14.3t/hrの水素と組み合わせると、約503MWの電気が12時間連続して利用可能になる。これにより、プロセスの動作に必要な603MWの電気の80%を供給することができる。
本開示は、本明細書における教示の利益を有する当業者に明らかな、異なるが同等の方法で変更および実施され得るため、上記で開示された特定の態様は例示に過ぎない。さらに、添付の特許請求の範囲に記載されているもの以外は、本明細書において示されている構造または設計の詳細を限定することを意図するものではない。したがって、上記で開示された特定の例示的な態様は改変または変更されてもよく、そのような変形例はいずれも本開示の範囲および趣旨内にあると考えられることは明らかである。態様の特徴を組み合わせ、統合し、および/または省略することから生じる代替的な態様も、本開示の範囲内である。組成物および方法は、様々な構成要素または工程を「有する(having)」、「含む(comprising)」、「含む(containing)」または「含む(including)」という広範囲な用語で記載されているが、組成物および方法は、様々な構成要素および工程「から本質的になる(consist essentially of)」または「からなる(consist of)」こともできる。請求項の任意の要素に関する用語「任意で」の使用は、その要素が必要とされるか、あるいはその要素が必要とされず、両選択肢が特許請求の範囲内にあることを意味している。
以下は、本開示による非限定的な特定の態様である。
以下は、本開示による非限定的な特定の態様である。
以下は、本開示による非限定的な特定の態様である。
以下は、本開示による非限定的な特定の態様である。
Claims (22)
- 供給流を前処理するように構成された、供給物前処理セクション;
1つまたは複数の炉であって、該1つまたは複数の炉のうちの少なくとも1つが、電化された炉であるように構成されており、各電化された炉が、希釈剤の存在下で該供給流中の炭化水素を分解して分解ガス流を生成するように構成された1つまたは複数の熱分解反応器を備える熱分解セクションをさらに備える、1つまたは複数の炉;
(a)該分解ガス流からの熱回収と該分解ガス流のクエンチとを提供し、
(b)該分解ガス流から燃料油、硫化水素、二酸化炭素、水、熱分解ガソリンまたはそれらの組合せを除去し、
(c)該分解ガス流を圧縮し、それにより圧縮された分解ガス流を提供する
ように構成された、一次分留および圧縮セクション;ならびに
少なくともエチレンを含む生成物オレフィン流を該圧縮された分解ガス流から分離するように構成された、生成物分離セクション
を備える、軽質オレフィンを生成するためのオレフィン合成プラントであって、
燃料も炭素系燃料も化石燃料もそれらの組合せも燃焼させることなく、各電化された炉全体の加熱の少なくとも90%が引き起こされるように、各電化された炉が構成されており、
該オレフィン合成プラントが、10MW以上の電力を消費するように構成されている、
該オレフィン合成プラント。 - 各電化された炉が、排煙熱回収セクションを有しない、請求項1記載のオレフィン合成プラント。
- オレフィン合成プラントにおける機械的仕事の少なくとも10%が、水蒸気を使用せずに引き起こされる、請求項1記載のオレフィン合成プラント。
- 生成されるエチレン1トン当たりの生成されるCO2の量が、オレフィン合成プラントで生成されるエチレン1トン当たりCO2 0.5トン未満に低減される、請求項1記載のオレフィン合成プラント。
- 各電化された炉における正味エネルギー入力から計算される比エネルギー消費量が17GJ/トン未満である、請求項1記載のオレフィン合成プラント。
- 1つまたは複数の熱分解反応器が、抵抗加熱によって所定の分解温度まで加熱される、請求項1記載のオレフィン合成プラント。
- 1つまたは複数の熱分解反応器が、誘導加熱によって所定の分解温度まで加熱される、請求項1記載のオレフィン合成プラント。
- 1つまたは複数の熱分解反応器が、放射セクションを介して所定の分解温度まで加熱され、該放射セクションにおいて、電気的に生成された熱が、放射によって1つまたは複数の熱分解反応器に熱を直接伝達するために使用されるか、放射によって該1つまたは複数の熱分解反応器に熱を伝達する放射パネルを加熱するために使用されるか、これらの方法の組合せによって使用される、請求項1記載のオレフィン合成プラント。
- 1つもしくは複数の熱分解反応器内で希釈剤として使用するための水蒸気の生成以外に、または分解ガス流との熱伝達を促進するために使用するための水蒸気の生成以外に、一次エネルギー伝達媒体として使用するための水蒸気が生成されない、請求項1記載のオレフィン合成プラント。
- 再生可能電気が利用可能でない場合に貯蔵エネルギーを利用することができるように、圧縮水素、供給物の圧縮炭化水素、生成物の圧縮炭化水素、極低温液体、熱電池、電気電池、またはそれらの組合せの形態のエネルギーを貯蔵することをさらに含む、請求項1記載のオレフィン合成プラント。
- (a)高圧の圧縮エタンもしくはLPG供給物のための貯蔵部であって、貯蔵された圧縮エタンもしくはLPG供給物が、電気を生成するために後に膨張され、続いて供給物として使用され得る、貯蔵部;
(b)低温の圧縮エタンもしくはプロパン供給物のための貯蔵部であって、貯蔵された圧縮エタンもしくはLPG供給物が、冷媒として後に使用され、続いて供給物として利用され得る、貯蔵部;または
(c)それらの組合せ
を備える、請求項9記載のオレフィン合成プラント。 - (a)高圧の圧縮エテンおよび/もしくはプロペンまたはそれらの組合せの中間生成物のための貯蔵部であって、貯蔵された圧縮エテンおよび/もしくはプロペン中間生成物が、電気を生成するために後に膨張され、続いて最終生成物として使用され得る、貯蔵部;
(b)低温の圧縮エテンもしくはプロペン中間生成物のための貯蔵部であって、貯蔵された圧縮エテンおよび/もしくはプロペン中間生成物が、冷媒として後に使用され、続いて最終生成物として利用され得る、貯蔵部;または
(c)それらの組合せ
を備える、請求項9記載のオレフィン合成プラント。 - (a)炭化水素を含む供給流を分解して、オレフィンを含む分解ガスを生成する工程であって、該供給流を分解することが、該供給流の温度を分解温度まで上昇させることを含む、工程;
(b)オレフィンを含む該分解ガスから熱を回収する工程;
(c)該分解ガスを圧縮して、圧縮された分解ガスを提供する工程;
(d)該圧縮された分解ガスから酸性ガスを除去する工程;
(e)該酸性ガス低減分解ガスを乾燥させて、乾燥させた分解ガスを生成する工程;
(f)該乾燥させた分解ガスを冷却して、冷却された分解ガスを提供する工程;および
(g)該冷却された分解ガスから、少なくともエチレンを含む1つまたは複数のオレフィンを分離する工程
を含む、オレフィンを生成する方法であって、
生成されるエチレン1トン当たりの生成されるCO2の量が、エチレン1トン当たりCO2 0.5トン未満に低減され、
該方法中の加熱の少なくとも50%が、燃料も炭素系燃料も化石燃料もそれらの組合せも燃焼させることなく引き起こされ、
該方法が、10MW以上の電力を消費する、
該方法。 - 供給流の温度を分解温度まで上昇させるための所要熱量の少なくとも90%が、燃料も炭素系燃料も化石燃料もそれらの組合せも燃焼させることなくもたらされる、請求項13記載の方法。
- 前記方法中の加熱の少なくとも90%が、燃料も炭素系燃料も化石燃料もそれらの組合せも燃焼させることなく達成される、請求項13記載の方法。
- (b)分解ガスから熱を回収する工程が、水蒸気を生成することを含み、(b)における水蒸気の生成以外に、水蒸気が一次エネルギー伝達媒体として利用されない、請求項13記載の方法。
- (i)水蒸気が生成されない;
(ii)水蒸気が、(a)における希釈剤として以外には生成および利用されない;または
(iii)(b)分解ガスから熱を回収する工程が、供給流を予熱するためにのみ利用される水蒸気を生成することを含むが、(a)における希釈剤として以外には他の水蒸気が生成および利用されない、
請求項13記載の方法。 - (b)分解ガスから熱を回収する工程が、
該分解ガスと供給流との間の直接熱交換;
1つもしくは複数の温度での1つもしくは複数の熱交換を介した該分解ガスと該供給流との間の間接熱交換であって、熱伝達流体が該分解ガスから該供給流に熱を移動させるためにのみ使用される、間接熱交換;
電気を生成するための熱電装置と結合された分解ガス冷却器を介して熱を抽出すること;または
それらの組合せ
を含む、請求項13記載の方法。 - 電気ヒータを利用して、プロセス水ストリッパリボイラを加熱する;
電気ボイラを利用して、再循環されたプロセス水を気化させ、(a)で希釈剤として利用される水蒸気を生成する;
電気ヒータを利用して、水蒸気もしくは過熱水蒸気を生成する;または
それらの組合せを行う、
請求項13記載の方法。 - (a)で利用される希釈水蒸気が、電気的に生成および加熱される、請求項13記載の方法。
- (a)の温度を超えるまで希釈剤流を過熱して過熱希釈剤流を提供すること、および該過熱希釈剤流と供給流とを組み合わせることによって、(a)に必要なエネルギーの一部が得られる、請求項13記載の方法。
- (a)で利用される1つまたは複数の分解反応器に温度プロファイルを課すために電気加熱が使用される、請求項13記載の方法。
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