JP6017449B2 - メソ構造化酸化物担体中に捕捉されたヘテロポリアニオンをベースとする触媒を用いる炭化水素留分の水素化分解方法 - Google Patents
メソ構造化酸化物担体中に捕捉されたヘテロポリアニオンをベースとする触媒を用いる炭化水素留分の水素化分解方法 Download PDFInfo
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- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
- C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
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- B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
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Description
1)水素化−脱水素相の良好な分散を、特に金属含有率が高い場合に確実なものにすること(例えば、遷移金属をベースとする粒子のサイズを制御する、熱処理後にこれらの粒子の特性を維持する、等によって)、
2)硫化に対して抵抗性の種の形成を制限すること(例えば、活性相を構成する遷移金属間のより良好な相乗効果を得る、活性な水素化−脱水素相(および/またはその前駆体)と用いられる多孔性担体の間の相互作用を制御する、等によって)、
3)高度に開発された活性な表面積を維持しながら、反応物質および反応生成物の良好な分散を確実なものとすること(多孔性担体の化学的、表面組織的、および構造的な特性の最適化)、
を可能にするであろう、これらの触媒を調製するための新しい方法を開発することによって改善され得るだろう。
本発明は、少なくとも1種の炭化水素含有供給原料であって、その化合物の少なくとも50重量%が340℃超の初留点および540℃未満の終点を有するものの水素化分解方法であって、触媒であって、その酸化物形態において、単独でまたは混合して用いられる、周期律表の第VIB族の金属、第VIII族の金属および第VB族の金属から選択される少なくとも1種の金属を含む、触媒を用い、該金属は、式(HhXxMmOy)q−の少なくとも1種のポリオキソメタラートの形態で存在し、ここで、Xは、リン(P)、ケイ素(Si)、ホウ素(B)、ニッケル(Ni)およびコバルト(Co)から選択される元素であり、前記元素は単独で用いられ、Mは、バナジウム(V)、ニオブ(Nb)、タンタル(Ta)、モリブデン(Mo)、タングステン(W)、ニッケル(Ni)およびコバルト(Co)から選択される1種以上の元素であり、Oは酸素であり、Hは水素であり、hは0〜12の整数であり、xは0〜4の整数であり、mは、5、6、7、8、9、10、11、12または18に等しい整数であり、yは17〜72の整数であり、qは1〜20の整数であり、前記ポリオキソメタラートは、メソ構造化マトリクス内に存在し、該メソ構造化マトリクスは、ケイ素、アルミニウム、チタン、ジルコニウム、ガリウム、およびセリウム、並びにこれらの元素の少なくとも1種の混合によって構成される群から選択される少なくとも1種の元素Yの酸化物をベースとし、前記マトリクスは、1.5〜50nmの細孔サイズを有し、かつ、1〜30nmの厚さの無定形壁を有し、前記触媒は、前記方法において用いられる前に硫化される、方法に関する。
本発明の利点の一つは、それが、少なくとも1種の炭化水素含有供給原料であって、その化合物の少なくとも50重量%が340℃超の初留点および540℃未満の終点を有するものの水素化分解方法において、ポリオキソメタラートの存在に起因する特定の触媒特性と、メソ構造化酸化物マトリクスの組織および表面の特性とを同時に有し、該メソ構造化酸化物マトリクス中に前記ポリオキソメタラートが捕捉されている、触媒を用いることにある。これにより、前記ポリオキソメタラートと前記マトリクスのメソ構造化無機ネットワークとの間の革新的な特性および相互作用がもたらされる。これらの相互作用は、340℃超の温度で沸騰する生成物の340℃未満の温度で沸騰する生成物への向上した転化、および/または向上した水素化脱硫(hydrodesulphrization:HDS)、水素化脱窒(hydrodenitrogenation:HDN)、および水素化脱金属(hydrodemetallation:HDM)において反映される。このことは、特に、メソ構造化酸化物マトリクスであって、ポリオキソメタラートがその中に捕捉されたものの使用を通じた活性相のより良好な分散に起因する。
(供給原料)
非常に幅広い供給原料が、本発明による水素化分解方法によって処理され得る。本発明による水素化分解方法において用いられる供給原料は、炭化水素含有供給原料であって、その化合物の少なくとも50重量%が340℃超の初留点および540℃未満の終点を有し、好ましくはその化合物の少なくとも60重量%、好ましくは少なくとも75重量%、より好ましくは少なくとも80重量%が340℃超の初留点および540℃未満の終点を有する、ものである。
本発明による活性相前駆体として有利に用いられる、好ましいケギン型ヘテロポリアニオンは、式PMo12O40 3−、PW12O40 3−、PMo3W9O40 3−、PMo6W6O40 3−、PVMo11O40 4−、PV2Mo10O40 5−、PV3Mo9O40 6−、PV4Mo8O40 7−およびPMo(11−z)WzO40 3−(式中、zは1〜11である)のヘテロポリアニオンから選択され、単独でまたは混合物中で用いられ、好ましくは、好ましいケギン型ヘテロポリアニオンは、式PW12O40 3−、PMo3W9O40 3−およびPMo6W6O40 3−のヘテロポリアニオンから、好ましくは式PW12O40 3−およびPMo6W6O40 3−のヘテロポリアニオンから選択され、単独でまたは混合物中で用いられる。
ェリエライトおよびEU−1から、好ましくは構造型MFI、BEA、FAUおよびLTAのゼオライトから選択される。ゼオライト結晶は、有利には、完全にケイ素性であるか、あるいはケイ素に加えて、アルミニウム、鉄、ホウ素、インジウム、ガリウムおよびゲルマニウムから選択される少なくとも1種の元素T、好ましくはアルミニウムを含有するかのいずれかの、少なくとも1種のゼオライトを含む。
本発明による水素化分解方法は、精製業者の自由裁量で、供給原料の性質、所望の生成物の質、およびプラントに応じて著しく可変であり得る操作条件(温度、圧力、水素の再循環の程度、毎時空間速度)下で実施される。本発明による水素化分解方法は、有利には、200℃超、好ましくは250〜480℃、好ましくは320〜450℃、より好ましくは、330〜435℃の温度で、1MPa超、好ましくは2〜25MPa、好ましくは3〜20MPaの圧力下で行われ、空間速度(供給原料の体積流を触媒の体積で除算したもの)は、0.1〜20h−1、好ましくは0.1〜6h−1、より好ましくは0.2〜3h−1であり、導入される水素の量は、水素の体積(リットル)/炭化水素の体積(リットル)の体積比が、80〜5000L/L、好ましくは100〜2000L/Lであるようにされる。
以下の実施例は、本発明をより詳細に記載するが、本発明の範囲を制限するものではない。
2.0gのF127(PEO70PPO106PEO70)を、撹拌下に、0.01mol/Lの塩酸の水溶液75ml中に分散させた。3.89gのオルトケイ酸テトラエチル(Si(OEt)4、TEOS)を、均一な溶液に添加した後、40℃での24時間にわたる撹拌を行った。0.46gのAl(OtBu)3を均一な溶液に添加して、全体を、40℃で24時間にわたり撹拌した。次いで、このようにして得られた懸濁液を、250mLのテフロン(登録商標)被覆オートクレーブに注ぎ、100℃で24時間にわたり放置した。次いで固体をろ過した。次いで、粉末を空気中100℃で乾燥させ、次いで550℃で空気下4時間にわたり焼成して、これにより、ポリマーを分解し、したがって、多孔度を開放した。固体Bの表面組織特性(比表面積、細孔容積、細孔径)は、それぞれ、(703m2/g、1.1mL/g、6.8nm)である。
Aldrichからの式PW12O40 3−・3H+のケギン型ヘテロポリ酸を水に溶解させた。触媒B1の調製は、メソ構造化アルミノケイ酸塩担体(担体A)に、式PW12O40 3−・3H+の溶解ケギンヘテロポリ酸を含有する水溶液を乾式含浸させることからなる方法により行った。
0.1gのCTABと2.0gのP123を、1.9mol/Lの塩酸の水溶液62.5gに溶解させた。次いで、3.71gのTEOSと0.44gのAl(OtBu)3を添加し、次いで、混合物を、45分間にわたり撹拌した。次いで、同じ塩酸溶液10g中のAldrichからの式PW12O40 3−・3H+のケギン型ヘテロポリ酸0.348gを添加した。
タングステン、モリブデンおよびニッケルを水性媒質中で担体A(380m2/g)上に同時含浸させた。PW12O40 3−・3H+、MoO3およびH3PO4を混合し、水中90℃で3時間にわたって還流させることによって含浸溶液を事前に調製し、これにより、溶液中に溶解した式PMo3W9O40 3−・3H+のケギン型ヘテロポリアニオンを得ることが可能となった。Ni5(CO3)2(OH)6・4H2Oを、Ni/(Mo+W)比=0.2を得るような量が加えられるように、この溶液に添加した。12時間にわたる成熟の後、触媒を120℃で終夜乾燥させた。この非硫化触媒NiMoWP/SiAlのうち、固体の全重量に対して、酸化タングステンの重量含有率は20%であり、酸化モリブデンの重量含有率は4%であり、酸化ニッケルの重量含有率は1.8%であり、酸化リンの含有率は0.7%であり、真のNi/(Mo+W)比:0.2に相当する。
0.040gの三酸化モリブデンMoO3を、0.009gのリン酸H3PO4の水溶液中に溶解させ、次いで、Aldrichからの式PW12O40 3−・3H+のケギン型ヘテロポリ酸0.198gを、溶液に添加した。12時間にわたる撹拌の後、式PMo3W9O40 3−のケギン型ヘテロポリアニオンを含有する透明溶液S1を得た。
アニリンの存在下でのトルエンの水素化の試験(「HTA」試験)の目的は、H2Sの存在下かつ水素圧下での担持型硫化触媒の水素化活性(HYD)を評価することである。水素化分解触媒の酸機能を特徴付ける異性化および分解は、NH3(アニリンの分解に由来する)の存在によって阻害され、その結果、HTA試験によって、触媒のそれぞれの水素化力を具体的に評価することが可能である。アニリンおよび/またはNH3は、したがって、酸塩基反応を介して、担体の酸点(acid site)と反応することとなる。各HTA試験を、いくつかのマイクロリアクタを並列に有する装置上で行った。各「HTA」試験について、触媒の硫化、および実際の触媒試験相のために同じ供給原料を用いた。カーボランダム(SiC、500μm)4cm3と混合された触媒4cm3を、反応器中に装填した。
− トルエン 20重量%、
− シクロヘキサン 73.62重量%、
− DMDS(ジメチルジスルフィド) 5.88重量%(3.8重量%S)、
− アニリン 0.5重量%(750ppmN)。
− P=6MPa、
− LHSV=2h−1(供給原料流量=8cm3/h)、
− H2/HC=450Nm3/m3(H2流量=3.6Nm3/m3)、
− T=350℃。
用いられた供給原料は、Axens社によって市販されているアルミナ上に担持された配合NiMoPの触媒を用いて事前に水素化処理した真空蒸留物タイプ「VD」の供給原料であった。供給原料の主な特徴を表3に示す。
− P=6MPa、
− LHSV=0.6h−1、
− H2/HC出口=480Nm3/m3、
− T=390℃。
触媒B1およびB2(これらの調製は、実施例1、2および3に記載されている)を、水素化処理されていない真空蒸留物の水素化分解を行うために用いた。水素化処理されていない真空蒸留物の主な特徴を表5に示す。
全圧:14MPa、
水素流量:注入される供給原料の体積(リットル)当たり気体水素1000リットル、
空間速度(LHSV):0.66h−1、
温度:400℃。
CS MD=[(150−370流出物のフラクション)]/[(370℃− 流出物の%)]
と等しいものとした。
Claims (14)
- 少なくとも1種の炭化水素含有供給原料の水素化分解方法であって、該供給原料において、その化合物の少なくとも50重量%が、340℃超の初留点と540℃未満の終点を有し、該方法は、触媒を用い、該触媒は、その酸化物形態で、単独でまたは混合物で用いられる、周期律表の第VIB族金属、第VIII族金属および第VB族金属から選択される少なくとも1種の金属を含み、前記金属は、式(HhXxMmOy)q−の少なくとも1種のポリオキソメタラートの形態で存在し、ここで、Xは、リン(P)、ケイ素(Si)、ホウ素(B)、ニッケル(Ni)およびコバルト(Co)から選択される元素であり、前記元素は単独で用いられ、Mは、バナジウム(V)、ニオブ(Nb)、タンタル(Ta)、モリブデン(Mo)、タングステン(W)、ニッケル(Ni)およびコバルト(Co)から選択される1種以上の元素であり、Oは酸素であり、Hは水素であり、hは0〜12の整数であり、xは0〜4の整数であり、mは、5、6、7、8、9、10、11、12または18に等しい整数であり、yは17〜72の整数であり、qは1〜20の整数であり、前記ポリオキソメタラートは、メソ構造化マトリクス内に存在し、該メソ構造化マトリクスは、ケイ素、アルミニウム、チタン、ジルコニウム、ガリウムおよびセリウム、並びにこれらの元素の少なくとも1種の混合によって構成される群から選択される少なくとも1種の元素Yの酸化物をベースとし、前記マトリクスは、1.5〜50nmの細孔サイズを有し、かつ、1〜30nmの厚さの無定形壁を有し、前記マトリクス内に存在する前記ポリオキソメタラートは前記マトリクスの該壁中に捕捉され、前記触媒は、前記方法において用いられる前に硫化される、方法。
- 前記供給原料は、真空蒸留物留分である、請求項1に記載の水素化分解方法。
- 真空蒸留物タイプの前記炭化水素含有供給原料は、他の炭化水素留分と混合されて用いられ、該他の炭化水素留分は、接触分解装置FCCに由来する流出物、接触分解装置に由来する軽質ガスオイルまたは重質油留分、常圧残渣および/または真空残渣の脱硫または水素化転化の固定床または沸騰床方法に由来する蒸留物、フィッシャー・トロプシュ合成に由来するパラフィン流出物、真空蒸留に由来する流出物、脱アスファルト油またはDAO、石炭液化方法に由来する流出物、バイオマスに由来する供給原料またはバイオマスから得られる供給原料の転化に由来する流出物、および芳香族化合物の抽出のための装置から得られる芳香族抽出物および供給原料から選択され、単独であるいは混合物で用いられる、請求項1または2に記載の水素化分解方法。
- ポリオキソメタラートは、式(HhXxMmOy)q−に相当する化合物であり、ここで、hは0〜6の整数であり、xは0、1または2に等しくあり得る整数であり、mは5、6、7、9、10、11または12に等しい整数であり、yは17〜48の整数であり、qは3〜12に等しい整数であり、X、M、HおよびOは上記に記載された意味を有する、請求項1〜3のいずれか1つに記載の水素化分解方法。
- 用いられるポリオキソメタラートは、単独でまたは混合物で用いられる、式PVMo11O40 4−、PV2Mo10O40 5−、PV3Mo9O40 6−、PV4Mo8O40 7−、HPNiMo11O40 6−、P2Mo5O23 6−、Ni2Mo10O38H4 8−、NiMo6O24H6 4−、PMo12O40 3−、PW12O40 3−、PMo3W9O40 3−およびPMo6W6O40 3−のポリオキソメタラートから選択される、請求項1〜4のいずれか1つに記載の水素化分解方法。
- ポリオキソメタラートは、一般式XM12O40 q−のいわゆるケギン型ヘテロポリアニオンであり、該式について、m/x比が12に等しく、および、一般式XM11O39 q−のいわゆる間隙ケギン型ヘテロポリアニオンであり、該式について、m/x比が11に等しく、ここで、元素XおよびMならびに電荷qは上記に示された意味を持つ、請求項1〜5のいずれか1つに記載の水素化分解方法。
- ケギン型ヘテロポリアニオンは、単独であるいは混合物で用いられる、式PW12O40 3−およびPMo3W9O40 3−のヘテロポリアニオンから選択される、請求項6に記載の水素化分解方法。
- 触媒は、触媒の全重量に対する酸化物の重量百分率で表される2〜35重量%の重量全含有率の第VIB族元素を含む、請求項1〜7のいずれか1つに記載の水素化分解方法。
- 触媒は、触媒の全重量に対する酸化物の重量百分率で表される0.1〜10重量%の重量含有率の第VIII族元素を含む、請求項1〜8のいずれか1つに記載の水素化分解方法。
- 触媒は、触媒の全重量に対する酸化物の重量百分率で表される0.1〜10重量%の重量含有率のリン、ホウ素およびケイ素から選択されるドーピング元素を含む、請求項1〜9のいずれか1つに記載の水素化分解方法。
- 前記メソ構造化マトリクスは、酸化ケイ素および酸化アルミニウムの混合物によって構成される、請求項1〜10のいずれか1つに記載の水素化分解方法。
- 前記触媒は、その酸化物形態で、非球状形状である、それが構成される基本球状粒子のそれぞれを有する、請求項1〜11のいずれか1つに記載の方法。
- 前記炭化水素含有供給原料の水素化処理または水素化精製の予備工程が、前記水素化分解方法において、少なくとも1種の水素化分解触媒の上流で適用される、請求項1〜12のいずれか1つに記載の方法。
- 前記方法は、200℃超の温度、1MPa超の圧力で行われ、空間速度は、0.1〜20h −1 であり、導入される水素の量は、水素の体積(リットル)/炭化水素の体積(リットル)の体積比が80〜5000L/Lであるようにされる、請求項1〜13のいずれか1つに記載の方法。
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CN113856754B (zh) * | 2021-09-25 | 2023-11-24 | 吉林化工学院 | 一种深度脱硫催化剂及其应用 |
US11746299B1 (en) | 2022-07-11 | 2023-09-05 | Saudi Arabian Oil Company | Methods and systems for upgrading mixed pyrolysis oil to light aromatics over mixed metal oxide catalysts |
WO2024048703A1 (ja) * | 2022-08-31 | 2024-03-07 | 三菱ケミカル株式会社 | 触媒前駆体及びその製造方法、触媒成形体及びその製造方法、触媒の製造方法、α,β-不飽和カルボン酸の製造方法、並びにα,β-不飽和カルボン酸エステルの製造方法 |
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US2547380A (en) | 1945-10-01 | 1951-04-03 | Union Oil Co | Catalyst for hydrocarbon conversion |
FR2749778B1 (fr) | 1996-06-13 | 1998-08-14 | Elf Antar France | Procede de preparation de catalyseurs d'hydrotraitement |
FR2764211B1 (fr) | 1997-06-09 | 1999-10-08 | Elf Antar France | Procede de preparation de catalyseurs d'hydrotraitement |
FR2903979B1 (fr) * | 2006-07-24 | 2009-02-20 | Inst Francais Du Petrole | Procede de preparation d'au moins un sel de cobalt et/ou de nickel d'au moins un heteropolyanion d'anderson combinant dans sa structure le molybdene et le cobalt ou le nickel |
JP2008235524A (ja) * | 2007-03-20 | 2008-10-02 | Mitsubishi Electric Corp | ガスレーザ発振器 |
CN101765651A (zh) * | 2007-06-13 | 2010-06-30 | 埃克森美孚研究工程公司 | 使用高生产率催化剂的联合加氢处理 |
FR2931705B1 (fr) * | 2008-05-28 | 2010-09-03 | Inst Francais Du Petrole | Catalyseur a base d'un materiau amorphe comprenant du silicium a porosite hierarchisee et organisee et procede ameliore de traitement de charges hydrocarbonees |
FR2935139B1 (fr) | 2008-08-19 | 2011-06-10 | Inst Francais Du Petrole | Heteropolyanion de type keggin lacunaire a base de tungstene pour l'hydrocraquage |
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- 2011-12-15 WO PCT/FR2011/000651 patent/WO2012085352A1/fr active Application Filing
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EP2655554B1 (fr) | 2016-07-27 |
ZA201303865B (en) | 2014-03-26 |
FR2969647B1 (fr) | 2012-12-21 |
FR2969647A1 (fr) | 2012-06-29 |
CN103270140A (zh) | 2013-08-28 |
JP2014507500A (ja) | 2014-03-27 |
EP2655554A1 (fr) | 2013-10-30 |
US20130334099A1 (en) | 2013-12-19 |
WO2012085352A1 (fr) | 2012-06-28 |
US9321973B2 (en) | 2016-04-26 |
CN103270140B (zh) | 2015-07-01 |
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