JP6105630B2 - 超低レベルの有機硫黄化合物を有する燃料を生成するための、穏やかな水素化脱硫の統合気相接触酸化 - Google Patents
超低レベルの有機硫黄化合物を有する燃料を生成するための、穏やかな水素化脱硫の統合気相接触酸化 Download PDFInfo
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- JP6105630B2 JP6105630B2 JP2014555671A JP2014555671A JP6105630B2 JP 6105630 B2 JP6105630 B2 JP 6105630B2 JP 2014555671 A JP2014555671 A JP 2014555671A JP 2014555671 A JP2014555671 A JP 2014555671A JP 6105630 B2 JP6105630 B2 JP 6105630B2
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- oxidation catalyst
- sulfur
- boiling
- hydrodesulfurization
- organic sulfur
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Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including oxidation as the refining step in the absence of hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/80—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with zinc, cadmium or mercury
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
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Description
本出願は、2012年2月2日に出願された、米国仮特許出願番号第61/594,174号の利益を主張し、参照によりその全体が本明細書に組み込まれる。
本発明は、効率的に炭化水素の硫黄含有量を減少させるために、統合された気相接触酸化脱硫プロセスに関する。
処理中の硫黄化合物の大気中への排出及び、硫黄含有原粗油由来の石油製品の最終用途は、健康及び環境問題を提起する。輸送用及び他の燃料製品に適用可能な厳しく減少された硫黄仕様は、精製産業へ影響を及ぼし、100万分の10重量部(ppmw)以下へ経由中の硫黄分を大幅に低減するために、精製業者は設備投資をする必要がある。米国、日本、欧州連合諸国などの先進国では、輸送用燃料のための製油所は、既に、環境的にクリーンな輸送用燃料を製造することが求められている。例えば、2007年に米国環境保護庁は、高速道路のディーゼル燃料の硫黄含有量を、500ppmw(低硫黄ディーゼル)から15ppmw(超低硫黄ディーゼル)へ、97%減少させることを必要とした。欧州連合(EU)は更に厳しい基準を制定しており、2009年に販売されたディーゼル及びガソリン燃料は、10ppmw未満の硫黄を含有することが求められている。他の国々は、米国及び欧州連合(EU)の足跡を追いかけており、超低硫黄レベルの輸送用燃料を生産する製油所を必要とする規制を進めている。
不安定な有機硫黄化合物を除去するための燃料流の穏やかな水素化脱硫、及び不応性有機硫黄化合物を除去するための標的画分の気相酸化的脱硫による、不応性の及び不安定な有機硫黄化合物の両方を含む炭化水素原料の脱硫のための装置及びプロセスにより、上記の目的及び他の利点が提供されている。
有機硫黄化合物の超低レベルの炭化水素燃料を生成するために、統合された脱硫プロセスが設けられている。プロセスは以下のステップを含む:
a.穏やかな操作条件下で、水素化脱硫反応領域において、炭化水素流の全体を、水素化処理触媒と接触させるステップ。
b.二つの画分を得るために、約320℃〜約360℃、特定の実施形態において、約340℃の標的カット点温度で、排出物水素化処理流をフラッシングする(Flashing)ステップ。
c.不安定な有機硫黄化合物は、水素化脱硫工程の間に変換されるため、標的カット点温度より下で沸騰する画分は、有機硫黄化合物を実質的に含まない。
d.標的カット点温度以上で沸騰する画分中の有機硫黄化合物は、主に不応性有機硫黄化合物であり、特定のベンゾチオフェン(例えば、長鎖アルキル化ベンゾチオフェン)、ジベンゾチオフェン及びアルキル誘導体、例えば、4,6−ジメチルジベンゾチオフェンなどの芳香族分子を含む。硫黄を含まない炭化水素及びSOxへ有機硫黄化合物を変換するために、気相触媒酸化反応領域において、この画分を酸化触媒上でガス状の酸化剤と接触させる。
e.気液分離器及び/又はストリッパー及び/又は蒸留カラム及び/又は膜を含む装置により、副生成物のSOxは、その後、液体生成物から分離領域において除去される。
f.超低硫黄レベルの炭化水素生成物、例えば、フルレンジディーゼル燃料などを生成するために、標的カット点温度未満で沸騰するフラッシングカラム溶出画分、及び分離領域からの流を、再結合することができる。
実施例1
気相酸化的脱硫触媒材料を作るための方法(2〜12)及び、それらの触媒を用いた試験(13)を記載する実施例2〜13を提供する。
37.5gのCu(NO3)2(0.2モル)、13.3gのZn(NO3)3(0.07モル)及び50.1gのAl(NO3)3(0.235モル)を、500mLの蒸留水中に溶かし、以下で「溶液A」と呼ばれるものを形成した。溶液のpHは2.3であった。
溶液Aの500mLのサンプルを、実施例2の手順に従って調製した。
500mLの溶液Aのサンプルを、実施例2の手順に従って調製した。
実施例2のステップに従ったが、沈殿物を熱濾過し、熟成しなかった。詳細された組成物は、40.2重量%の元素Cu、9.7重量%の元素Zn、17.2重量%の元素Al、及び0.22重量%の元素Naを含んでいた。Cu:Zn:Alの原子比は、4.2:1:4.3であった。比表面積は75m2/gであり、細孔容積は0.29cm3/gであった。平均孔直径は、12.5nmであった。相組成物は高度に分散した、CuO、ZnO及びAl2O3の結晶相であった。
本実施例において、0.18gのCe(NO3)3(5.5×10−4モル)も溶液Aの調製の際に加えることを除き、実施例3に従った。沈殿が形成した後、55℃で6時間熟成させた。焼成した組成物の分析は、20.9重量%の元素Cu、17.1重量%の元素Zn、23.9重量%の元素Al及び0.5重量%の元素Ceを示した。Cu:Zn:Ce:Alの原子比は、3.0:1:0.01:3.8であった。組成物は、83m2/gの比表面積、0.20cm3/gの細孔容積、及び10.0nmの平均孔直径を有していた。それは、Cu0.5Zn0.5Al2O4の組成を有するX−線アモルファス酸化物相及び高度に分散された結晶相を示し、これは、60%未満のCu及び、また5nmを超えない粒径を有するCe相を含んでいた。
本実施例は、Ce(NO3)3の量を、3.1g(9.5×10−3モル)へ増加させることを除き、実施例6に従った。沈殿物形成及び濾過を、6時間65℃で行った。
本実施例において「溶液A」は、9.4gのCu(NO3)2(0.05モル)、13.3gのZn(NO3)2(0.07モル)及び27.7gのAl(NO3)2(0,13モル)を、500mLの蒸留水中に含んでいた。溶液Aは、2.6のpHを有していた。溶液Bは、53.0gのNa2CO3(0.5モル)及び18gのNaOH(0.45モル)を600mLの水中に含んでいた。溶液Bは、13.7のpHを有していた。
本実施例において、実施例3における溶液と同じ方法で、溶液A及びCを調製した。
本実施例において、溶液Aは、9.4gのCu(NO3)2(0.05モル)、3.8gのZn(NO3)2(0.02モル)及び95.8gのAl(NO3)2(0.45モル)を、500mLの蒸留水中に溶かした。溶液Aは、2.25のpHを有していた。
本実施例において、溶液Aは46.9gのCu(NO3)2(0.25モル)、13.3gのZn(NO3)2(0.07モル)及び42.6gのAl(NO3)2(0.20モル)を、500mLの蒸留水中に溶かした。溶液Aは、2.3のpHを有していた。溶液Bは、53.0gのNa2CO3(0.5モル)及び12gのNaOH(0.3モル)を、600mLの蒸留水中に含んでいた。溶液Bは、13.3のpHを有していた。
本実施例において、溶液Aは、Al(NO3)3を含まないが、7.5gのCu(NO3)2(0.04モル)、3.8gのZn(NO3)2(0.02モル)及び45.7gのCe(NO3)3(0.14モル)のみが500mLの蒸留水中に溶けていた。溶液Aは4.2のpHを有していた。
実施例2〜12において調製された触媒を、酸化硫黄含有化合物を含む燃料油を脱硫するそれらの能力について試験した。チオフェン、DBT(ジベンゾチオフェン)及び4,6−DMDBTを含有する燃料を調製した。燃料を気体状態へ加熱し、触媒化合物全体を通過させた。以下の表において、触媒(「Cu−Zn−Al」、「Cu−Zn−Al−Ce」又は「Cu−Zn−Ce」)の式は、(1)又は(2)に続く。これは、実施例2〜12の溶液B、C及びDの性質を指し、(1)は、Na含有溶液(溶液B中)を指し、(2)は、アンモニウム含有溶液(溶液C及びD中)を指す。最終的な数は、触媒を製造するためにどの実施例を使用したかを示す。
Claims (33)
- a.水素化処理された排出物を生成するために、炭化水素原料を水素化脱硫プロセスへ供すること、
b.低減されたレベルの有機硫黄化合物を含む低沸点画分及び、不応性有機硫黄化合物を有する高沸点画分を提供するために、水素化処理した排出物をフラッシングすること、
c.高沸点画分及び低沸点画分を分離すること、および
d.C−S結合を切断することにより、高沸点画分の範囲の沸点を有する、ジベンゾチオフェン、ジベンゾチオフェンのアルキル誘導体及びベンゾチオフェンの長鎖アルキル誘導体を含む不応性有機硫黄化合物を、SOxへ変換するために、前記高沸点画分を、ガス状酸化剤及び、式中xは0〜1の範囲である式CuxZn1−xAl2O4を有する酸化触媒と接触させること、
を含む、所望ではない有機硫黄化合物を除去するための炭化水素原料を処理する方法であって、前記酸化触媒が、30重量%(wt%)〜45wt%の範囲の量で酸化銅を、12wt%〜20wt%未満の範囲の量で酸化亜鉛を、及び20wt%〜40wt%の範囲の量で酸化アルミニウムを含み、前記酸化触媒がX−線アモルファス酸化物相、及び高度に分散した結晶性ZnO及びCuOを有する、方法。 - ステップ(b)における温度カット点が340℃である、請求項1に記載の方法。
- 前記低沸点画分が、脂肪族有機硫黄化合物を含む、請求項1に記載の方法。
- 前記脂肪族有機硫黄化合物が、スルフィド、ジスルフィド及びメルカプタンを含む、請求項3に記載の方法。
- 前記低沸点画分が更に、チオフェン及びチオフェンのアルキル誘導体を含む、請求項3に記載の方法。
- 前記高沸点画分が、高沸点画分の範囲の沸点を有する、ジベンゾチオフェン、ジベンゾチオフェンのアルキル誘導体及びベンゾチオフェンの長鎖アルキル化誘導体を含む、請求項1に記載の方法。
- 前記炭化水素原料が、180℃〜450℃の範囲で沸騰する直留ガス油である、請求項1に記載の方法。
- 前記水素化脱硫プロセスが、穏やかな操作条件で操作される、請求項7に記載の方法。
- 水素分圧が55bar未満である、請求項8に記載の方法。
- 水素分圧が25bar〜40barである、請求項8に記載の方法。
- 操作温度が300℃〜400℃である、請求項8に記載の方法。
- 操作温度が320℃〜380℃である、請求項8に記載の方法。
- 水素化脱硫プロセスステップにおける水素供給速度が、油のリットル当たり100リットルの水素〜油のリットル当たり1000リットルの水素である、請求項8に記載の方法。
- 水素化脱硫プロセスステップにおける水素供給速度が、油のリットル当たり200リットルの水素〜油のリットル当たり300リットルの水素である、請求項8に記載の方法。
- 前記酸化剤が、窒素酸化物、酸素及び空気から成る群から選択される、請求項1に記載の方法。
- ステップ(a)の水素化処理された排出物を回収することを更に含む、請求項1に記載の方法。
- ステップ(d)において使用される前記酸化触媒が更にCe2O3を含む、請求項1に記載の方法。
- ステップ(d)において使用される前記酸化触媒が、顆粒状である、請求項1に記載の方法。
- ステップ(d)において使用される前記酸化触媒が、円柱、球体、三葉として形成されているか、又は四葉形状を有する、請求項1に記載の方法。
- 前記酸化触媒の粒子が、1mm〜4mmの有効径を有する、請求項19に記載の方法。
- 前記酸化触媒の粒子が、10m2/g〜100m2/gの比表面積を有する、請求項19に記載の方法。
- 前記酸化触媒の粒子が、50m2/g〜100m2/gの比表面積を有する、請求項19に記載の方法。
- 前記酸化触媒の粒子が、8nm〜12nmの有効径の孔を有する、請求項19に記載の方法。
- 前記酸化触媒の粒子が、8nm〜10nmの有効径の孔を有する、請求項19に記載の方法。
- 前記酸化触媒の粒子が、0.1cm3/g〜0.5cm3/gの体積の孔を有する、請求項19に記載の方法。
- ステップ(d)において使用される前記酸化触媒中のxが、0.1〜0.6である、請求項1に記載の方法。
- ステップ(d)において使用される前記酸化触媒中のxが、0.2〜0.5である、請求項1に記載の方法。
- 炭化水素原料と流体連通する入口及び水素化処理した排出物を排出するための出口を有する水素化脱硫領域、
320℃〜360℃の温度カット点で水素化処理した排出物をフラッシュするために操作可能なフラッシングカラムであって、前記フラッシングカラムが、
前記水素化処理された排出物を受け取るための入口、
低沸点画分を排出するための低沸点出口、及び
不応性有機硫黄化合物を含有する高沸点画分を排出するための、高沸点出口を含むフラッシングカラム、
式中xは0〜1の範囲である式CuxZn1−xAl2O4を有する酸化触媒及びガス状酸化剤を含有する気相接触酸化脱硫領域、前記高沸点出口と流体連通する入口を有する気相接触酸化脱硫領域、並びに、低硫黄炭化水素及びSOxの排出用出口
を含む、所望ではない有機硫黄化合物を含有する炭化水素原料を処理するための装置であって、前記酸化触媒が、30重量%(wt%)〜45wt%の範囲の量で酸化銅を、12wt%〜20wt%未満の範囲の量で酸化亜鉛を、及び20wt%〜40wt%の範囲の量で酸化アルミニウムを含み、前記酸化触媒がX−線アモルファス酸化物相、及び高度に分散した結晶性ZnO及びCuOを有する、装置。 - ステップ(d)を気相中で行う、請求項7に記載の方法。
- e.硫黄を含まない炭化水素から、分離領域において副生成物のSOxを除去すること;及び
f.超低硫黄レベルの炭化水素生成物を回収すること
を更に含む、請求項1に記載の方法。 - ステップ(a)の排出物及びステップ(f)の排出物を組み合わせることを更に含む、請求項30に記載の方法。
- Ce2O3は、前記酸化触媒の0.1wt%〜10wt%の範囲の量で、5nm〜10nmの直径の範囲の粒子形態で存在する、請求項17に記載の方法。
- 気相接触酸化脱硫領域操作を気相中で行う、請求項28に記載の装置。
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KR20150035490A (ko) | 2015-04-06 |
US20130199968A1 (en) | 2013-08-08 |
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JP2015511255A (ja) | 2015-04-16 |
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WO2013116338A1 (en) | 2013-08-08 |
EP2809747B1 (en) | 2019-06-19 |
CN104204146A (zh) | 2014-12-10 |
CN104204146B (zh) | 2016-06-29 |
EP2809747A1 (en) | 2014-12-10 |
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