JP6224896B2 - 天然油供給原料から燃料を精製および製造する方法 - Google Patents
天然油供給原料から燃料を精製および製造する方法 Download PDFInfo
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- JP6224896B2 JP6224896B2 JP2012534266A JP2012534266A JP6224896B2 JP 6224896 B2 JP6224896 B2 JP 6224896B2 JP 2012534266 A JP2012534266 A JP 2012534266A JP 2012534266 A JP2012534266 A JP 2012534266A JP 6224896 B2 JP6224896 B2 JP 6224896B2
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- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/08—Jet fuel
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/22—Higher olefins
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2200/00—Components of fuel compositions
- C10L2200/04—Organic compounds
- C10L2200/0461—Fractions defined by their origin
- C10L2200/0469—Renewables or materials of biological origin
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
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Description
[0001]本出願は米国仮特許出願61/250743号(2009年10月12日提出)の利益を請求し、その内容は参考文献としてここに取り込まれる。
[0003]交差複分解は、図式的には式IIに示すように表すことができる。
[0004]近年、一般的には石油を供給源とする物質を製造するための、環境に優しい技術に対する必要性が増大している。例えば、研究者らは、野菜や種子をベースとする油のような天然油供給原料を用いてバイオ燃料、ワックス、プラスチック、その他同種類のものを製造する可能性を研究している。一つの非限定的な例として、ろうそくを製造するために複分解触媒が用いられ、それは例えばPCT/US2006/000822号に記載されている。その記載の全体は参考文献としてここに取り込まれる。天然油供給原料を伴う複分解反応は、今日および将来の有望な解決策を提供する。
[0008]一つの態様において、この方法は、複分解生成物が形成されるのに十分な条件の下、複分解触媒の存在下で天然油を含む供給原料を反応させることを含み、ここで複分解生成物はオレフィン類とエステル類を含む。この方法はさらに、エステル類からオレフィン類を分離することを含む。この方法はさらに、アルコールの存在下でエステル類をエステル交換させ、それによりエステル交換生成物を形成させることを含む。
[0011]特定の態様において、複分解反応の前に、複分解触媒は溶媒中に溶解される。幾つかの態様において、溶媒はトルエンである。
[0016]特定の態様において、反応工程は、供給原料とそれ自体との間の自己複分解反応を含む。他の態様において、反応工程は、低分子量オレフィンと供給原料との間の交差複分解反応を含む。幾つかの態様において、低分子量オレフィンは、エチレン、プロピレン、1−ブテン、2−ブテンのそれぞれ、あるいはこれらの組み合わせからなる群から選択される少なくとも1種の低分子量オレフィンを含む。幾つかの態様において、低分子量オレフィンはアルファ−オレフィンである。一つの態様において、低分子量オレフィンは、4〜10の間の炭素数を有する少なくとも1種の枝分れオレフィンを含む。
[0029]ここで用いられるとき、単数形の語は、文脈において特に明確に規定していない限り、複数の指示物を含む。例えば、「置換基」と言及した場合、それは単一の置換基と二つ以上の置換基、その他同種類のものを包含する。
[0033]ここで用いられるとき、「天然油」、「天然供給原料」または「天然油供給原料」という用語は、植物または動物の供給源から得られた油を指すだろう。「天然油」という用語は、特に断らない限り、天然油の誘導体を含む。天然油の例としては、これらに限定はされないが、植物油、藻類油、動物脂肪、タル油、これらの油の誘導体、これらの油の任意の組み合わせ、その他同種類のものがある。植物油の典型的で非限定的な例としては、カノーラ油、菜種油、ココナツ油、コーン油、綿実油、オリーブ油、パーム油、落花生油、ベニバナ油、ゴマ油、大豆油、ヒマワリ油、亜麻仁油、パーム核油、桐油、ジャトロファ油、マスタード油、グンバイナズナ油、ツバキ油、およびヒマシ油がある。動物脂肪の典型的で非限定的な例としては、ラード、獣脂、家禽脂肪、イエローグリース、および魚油がある。タル油は木材パルプ製造の副産物である。
[00114]清浄で乾燥したステンレス鋼を、5ガロンの外被とした。浸漬管、頂部攪拌機、内部冷却・加熱コイル、温度プローブ、試料採取弁、およびヘッドスペースガス放出弁を備えたパー(Parr)反応容器が、アルゴンを用いて15psigまでパージされた。大豆油(SBO(Soybean oil)、2.5kg、2.9モル、Costco、MWn=864.4g/モル、GCによって決定して85重量%不飽和、5ガロンの容器中でアルゴンを1時間散布)を、パー反応器中に添加した。パー反応器は密封され、そしてSBOは2時間にわたってアルゴンでパージされ、同時に10℃まで冷却された。2時間後、内部の圧力が10psigになるまで反応器がガス抜きされた。反応器上の浸漬管弁が1−ブテンシリンダー(エアガス、CPグレード、33psigのヘッドスペース圧力、99重量%超)に接続され、そして1−ブテンの15psigまで再加圧された。ヘッドスペース内の残留アルゴンを除去するために、反応器は再び10psigになるまでガス抜きされた。18〜28psigの1−ブテンの下でSBOは350rpmおよび9〜15℃において攪拌され、この攪拌は、SBOのオレフィン結合当り3モルの1−ブテンが反応器中へ移されるまで行われた(約4〜5時間の間に約2.2kgの1−ブテン)。[1,3−ビス(2,4,6−トリメチルフェニル)−2−イミダゾリジニリデン]ジクロロルテニウム(3−メチル−2−ブテニリデン)(トリシクロヘキシルホスフィン)(C827、Materia)のトルエン溶液が、フィッシャー・ポーター圧力容器中で、触媒担体(SBOのオレフィン結合当り10モルppm)としての30グラムのトルエン中に130mgの触媒を溶解することによって調製され、そしてこの溶液が、フィッシャー・ポーター容器内のヘッドスペースをアルゴンで50〜60psigに加圧することによって、反応器の浸漬管を通して反応器に添加された。フィッシャー・ポーター容器と浸漬管は、追加の30gのトルエンですすぎ洗いされた。反応混合物は60℃において2.0時間攪拌された。反応混合物は周囲温度まで冷却され、同時にヘッドスペース内のガスは排気された。圧力が解放された後、反応混合物は、58gの漂白粘土(2%w/wのSBO、Pure Flow B80 CG)と磁気攪拌棒を収容している三つ口丸底フラスコに移された。反応混合物は、アルゴンの下で85℃において攪拌することによって処理された。2時間後、この時間の間に、残りの全ての1−ブテンが排気され、反応混合物は40℃まで冷却され、そしてガラスろ過器を通してろ過された。(60℃におけるメタノール中の1%w/wのNaOMeを用いたエステル交換の後に)ガスクロマトグラフィー分析によって、生成混合物のアリコートは、約22重量%のメチル9−デセノエート、約16重量%のメチル9−ドデセノエート、約3重量%のジメチル9−オクタデセンジオエート、および約3重量%のメチル9−オクタデセノエートを含んでいることが見いだされた(ガスクロマトグラフィーによって)。これらの結果は、23.4重量%のメチル9−デセノエート、17.9重量%のメチル9−ドデセノエート、3.7重量%のジメチル9−オクタデセンジオエート、および1.8重量%のメチル9−オクタデセノエートの平衡における計算された収量に首尾よく匹敵する。
[00115]実施例1に記載された一般的手順によって、1.73kgのSBOと3モルの1−ブテン/SBO二重結合を用いて反応が行われた。60℃におけるメタノール中の1%w/wのNaOMeを用いたエステル交換の後に、ガスクロマトグラフィー分析によって、生成混合物のアリコートは、約24重量%のメチル9−デセノエート、約18重量%のメチル9−ドデセノエート、約2重量%のジメチル9−オクタデセンジオエート、および約2重量%のメチル9−オクタデセノエートを含んでいることが見いだされた(ガスクロマトグラフィーによって決定されたもの)。
[00116]実施例1に記載された一般的手順によって、1.75kgのSBOと3モルの1−ブテン/SBO二重結合を用いて反応が行われた。60℃におけるメタノール中の1%w/wのNaOMeを用いたエステル交換の後に、ガスクロマトグラフィー分析によって、生成混合物のアリコートは、約24重量%のメチル9−デセノエート、約17重量%のメチル9−ドデセノエート、約3重量%のジメチル9−オクタデセンジオエート、および約2重量%のメチル9−オクタデセノエートを含んでいることが見いだされた(ガスクロマトグラフィーによって決定されたもの)。
[00117]実施例1に記載された一般的手順によって、2.2kgのSBO、3モルの1−ブテン/SBO二重結合、および60gのトルエン(触媒を移動させるためにSBOと交換されたもの)を用いて反応が行われた。60℃におけるメタノール中の1%w/wのNaOMeを用いたエステル交換の後に、ガスクロマトグラフィー分析によって、生成混合物のアリコートは、約25重量%のメチル9−デセノエート、約18重量%のメチル9−ドデセノエート、約3重量%のジメチル9−オクタデセンジオエート、および約1重量%のメチル9−オクタデセノエートを含んでいることが見いだされた(ガスクロマトグラフィーによって決定されたもの)。
[00118]磁気攪拌棒、加熱マントル、および温度調節器を備えた12リットルの三つ口ガラス丸底フラスコに、実施例1〜4からの混合反応生成物を8.42kg充填した。真空導入口を有する凝縮器をフラスコの中間口に装着し、受けフラスコを凝縮器に接続した。反応生成物から炭化水素オレフィン類が、下記の範囲の条件で減圧蒸留によって除去された:22〜130℃のポット温度、19〜70℃の蒸留ヘッドの温度、および2000〜160μトルの圧力。揮発性の炭化水素類が除去された後に残った物質の重量は5.34kgであった。60℃におけるメタノール中の1%w/wのNaOMeを用いたエステル交換の後に、ガスクロマトグラフィー分析によって、非揮発性の生成混合物のアリコートは、約32重量%のメチル9−デセノエート、約23重量%のメチル9−ドデセノエート、約4重量%のジメチル9−オクタデセンジオエート、および約5重量%のメチル9−オクタデセノエートを含んでいることが見いだされた(ガスクロマトグラフィーによって決定されたもの)。
[00119]磁気攪拌棒、凝縮器、加熱マントル、温度プローブ、およびガスアダプターを備えた12リットルの三つ口丸底フラスコに、MeOH中の1%w/wのNaOMeを4リットルと、実施例5で生成された非揮発性の生成混合物5.34kgを充填した。生じた薄黄色の不均質混合物は60℃で攪拌された。約1時間後、混合物は均質なオレンジ色に変わった(pH=11と検出された)。2時間の合計反応時間の後、混合物は周囲温度まで冷却され、そして二つの層が観察された。有機相が3リットルの50%(v/v)水性MeOHで二回洗浄され、分離され、そして冷たいMeOH中のHOAc(1モルHOAc/モルNaOMe)で洗浄することによって中和され、その結果、pHが6.5と検出され、5.03kgの収量が得られた。
[00120]磁気攪拌器、充填塔、および温度調節器を備えたガラス製で12リットルの三つ口丸底フラスコに、実施例6で生成されたメチルエステル混合物(5.03kg)を充填し、そして加熱マントル中に置いた。フラスコに装着した充填塔は、0.16インチのPro−Pak(登録商標)ステンレス鋼サドルを有する2インチ×36インチのガラス塔であった。この蒸留塔は分別蒸留ヘッドに装着され、このヘッドに、蒸留の留分を捕集するために1リットルの予め秤量された丸底フラスコが装着された。100〜120μトルの減圧下で蒸留が実施された。メチル9−デセノエート(9−DAME)とメチル9−ドデセノエート(9−DDAME)の両者を単離するために、1:3の還流比が用いられた。1:3の還流比は、蒸留塔へ戻される3滴ごとに捕集される1滴に相当する。蒸留を行う間に捕集された試料、減圧蒸留の条件、およびガスクロマトグラフィーによって決定された留分の9−DAMEと9−DDAMEの含有量を表1に示す。留分2〜7を合わせた収量は1.46kgのメチル9−デセノエートで、これは99.7%の純度であった。留分16を捕集した後、2.50kgの物質が蒸留ポット中に残り、これはガスクロマトグラフィーによって約14重量%の9−DDAME、約42重量%のメチルパルミテート、および約12重量%のメチルステアレートを含んでいることが見いだされた。
[00121]実施例1に記載された一般的手順によって反応が行われたが、下記のことが変更された:40℃の反応温度において、2.2kgのSBO、7モルのプロペン/モルSBO二重結合、および200mgの[1,3−ビス(2,4,6−トリメチルフェニル)−2−イミダゾリジニリデン]ジクロロルテニウム(ベンジリデン)(トリシクロヘキシルホスフィン)(C848触媒、Materia Inc.、Pasadena、カリフォルニア州、米国、90ppm(w/w)対SBO)が用いられた。漂白粘土を用いる触媒除去工程も以下の工程によって置き換えられた:過剰なプロペンを排気した後、反応混合物は三つ口丸底フラスコの中に移され、これにトリス(ヒドロキシメチル)ホスフィン(THMP、イソプロパノール中の1.0M、50モルTHMP/モルC848)が添加された。生じた曇った黄色の混合物が60℃で20時間攪拌され、6リットルの分液漏斗へ移され、そして2×2.5リットルの脱イオンH2Oを用いて抽出された。有機相が分離され、そして無水Na2SO4上で4時間乾燥され、次いで、シリカゲルの層を収容したガラスろ過器を通してろ過された。
[00122]実施例8に記載された一般的手順によって反応が行われたが、ただし3.6kgのSBOと320mgのC848触媒が用いられた。触媒が除去された後、実施例9からの反応生成物が実施例8からの反応生成物と一緒にされ、得られた物質の収量は5.12kgであった。60℃におけるメタノール中の1%w/wのNaOMeを用いたエステル交換の後に、ガスクロマトグラフィー分析によって、一緒にされた生成混合物のアリコートは、約34重量%のメチル9−デセノエート、約13重量%のメチル9−ウンデセノエート、1重量%未満のジメチル9−オクタデセンジオエート、および1重量%未満のメチル9−オクタデセノエートを含んでいることが見いだされた(ガスクロマトグラフィーによって決定されたもの)。
[00124]実施例8に記載された一般的手順によって二つの反応が行われたが、ただし、各々の反応について3.1kgのSBOと280mgのC848触媒が用いられた。触媒が除去された後、二つの調製物からの反応生成物が一緒にされ、得られた物質の収量は5.28kgであった。60℃におけるメタノール中の1%w/wのNaOMeを用いたエステル交換の後に、ガスクロマトグラフィー分析によって、一緒にされた生成混合物のアリコートは、約40重量%のメチル9−デセノエート、約13重量%のメチル9−ウンデセノエート、約2重量%のジメチル9−オクタデセンジオエート、および約1重量%のメチル9−オクタデセノエートを含んでいることが見いだされた(ガスクロマトグラフィーによって決定されたもの)。
[00126]実施例10に記載された一般的手順によって、SBO、7モルのシス−2−ブテン/モルSBO二重結合、および220mgのC848触媒/kgSBOを用いて二つの複分解反応が行われた。触媒が除去された後、二つの調製物からの反応生成物が一緒にされ、得られた物質の収量は12.2kgであった。60℃におけるメタノール中の1%w/wのNaOMeを用いたエステル交換の後に、ガスクロマトグラフィー分析によって、一緒にされた生成混合物のアリコートは、約49重量%のメチル9−ウンデセノエート、約2重量%のジメチル9−オクタデセンジオエート、および約1重量%のメチル9−オクタデセノエートを含んでいることが見いだされた(ガスクロマトグラフィーによって決定されたもの)。
[00128]実施例1に記載された一般的手順によって、43mgのC827触媒/kgSBOを用いて、SBOと3モルの1−ブテン/モルSBO二重結合を反応させることによって、約7kgの交差複分解生成物が生成され、次いで、THMPを用いて触媒の除去が行われた。105gのJohnson−Matthey A−7000スポンジメタル(登録商標)触媒を用いて1ガロンバッチのオートクレーブ中で水素の吸収(uptake)が停止するまで、複分解生成物の最初の2.09kgの部分が136℃および400psig H2において水素化された。生じた混合物が温かい中で(22〜55℃)ろ過され、1.40kgのろ液と、触媒と水素化生成物からなる350gの混合物が得られた。触媒を含む混合物の全体が複分解生成物の第二の2.18kgの部分とともに1ガロンの反応器に戻され、そして第二の水素化反応が、水素の吸収が停止するまで同様にして行われた。触媒を沈降させ、そして有機生成物の大部分がデカントされ、そしてろ過され、1.99kgのろ液と、触媒と水素化生成物からなる380gの混合物が得られた。残りの約3kgの複分解生成物が二つの追加のバッチ反応で水素化され、これは前の反応からの触媒を用いて同様にして行われ、その結果、それぞれ1.65kgと1.28kgの水素化生成物が得られた。ろ過された後に単離された水素化生成物の総重量は6.32kgであった。ガスクロマトグラフィー分析によって、水素化生成物のアリコートは、約30重量%のC6〜C18n−パラフィン類と約70重量%のトリグリセリド類を含んでいることが見いだされた。水素化生成物中に含まれるC8〜C18n−パラフィン類の相対的分布は、下記の炭素数による計算されたオレフィン類の分布と十分に類似している:観察された値(計算された値)2.3(0.6)重量%C8、35.6(36.2)重量%C9、30.0(27.6)重量%C10、0.6(0.1)重量%C11、22.2(23.6)重量%C12、3.4(3.7)重量%C13、0.1(0.0)重量%C14、4.4(6.3)重量%C15、0.4(0.4)重量%C16、0.1(0.0)重量%C17、および1.0(1.6)重量%C18。
[00130]1−オクテンを伴ったパーム油の交差複分解から生成した1−オレフィン/1,4−ジエン(92重量%の1−デセン、4.5重量%の1,4−デカジエン、2重量%の1,4−ウンデカジエン)のオリゴマー化反応が、1.1モル%のエチルアルミニウムジクロリド(ヘキサン中の1M溶液)/1.1モル%のtert−ブチルクロリドを用いて、10℃において3時間にわたって、550gのスケールで行われた。水と1Mの水酸化ナトリウムの溶液を用いて反応混合物が急冷され、そして無色になるまで攪拌された。ヘキサン(300ml)が添加され、そして混合物が分液漏斗へ移された。水とブラインを用いて有機相が洗浄され、次いで、ヘキサンを除去するために回転蒸発器上で濃縮された。オリゴマー混合物がショートパス減圧蒸留(100℃、5トル)によって脱蔵され、そしてGC/MSによって生成物の分布が97%の混合オリゴマー類であると決定された。試料の動力学粘度(ブルックフィールド、#34スピンドル、100rpm、22℃)は540cpsである。40℃における試料の動粘度は232cStである。
[00132]揮発性生成物は、ガスクロマトグラフィーと火炎イオン化検出器(FID)によって分析された。アルケンの分析は、Agilent 6890装置と下記の条件を用いて行われた:
分離管: Restek Rtx−5、30m×0.25mm(ID)×0.25μm膜厚
インジェクター温度:250℃
検出器温度:280℃
オーブン温度:35℃の出発温度、4分の保持時間、260℃まで12℃/分の勾配率、8分の保持時間
キャリヤーガス:ヘリウム
平均のガス速度:31.3±3.5%cm/秒(計算値)
分離比率:〜50:1。
分離管: Restek Rtx−65、30m×0.32mm(ID)×0.1μm膜厚
インジェクター温度:250℃
検出器温度:350℃
オーブン温度:55℃の出発温度、5分の保持時間、350℃まで20℃/分の勾配率、10分の保持時間
キャリヤーガス:水素
流量:1.0mL/分
分離比率:40:1。
分離管: J&W Scientific、DB−Wax、30m×0.32mm(ID)×0.5μm膜厚
インジェクター温度:250℃
検出器温度:300℃
オーブン温度:70℃の出発温度、1分の保持時間、180℃まで20℃/分の勾配率、220℃まで3℃/分の勾配率、10分の保持時間
キャリヤーガス:水素
流量:1.0mL/分。
以下に、本願出願時の特許請求の範囲を記載する。
[請求項1]
天然油を精製する方法であって、
天然油を含む供給原料を用意すること、
複分解触媒の存在下で供給原料を反応させ、それによりオレフィン類とエステル類を含む複分解生成物を形成させること、および
複分解生成物中のエステル類から複分解生成物中のオレフィン類を分離すること、
を含む前記方法。
[請求項2]
アルコールの存在下でエステル類がエステル交換され、それによりエステル交換生成物を形成させる、請求項1に記載の方法。
[請求項3]
液−液分離によってエステル交換生成物からグリセリンを分離すること、
グリセリンを分離した後、エステル交換生成物を水で洗浄し、それによってグリセリンをさらに除去すること、および
洗浄の後、エステル交換生成物を乾燥し、それによってエステル交換生成物から水を分離すること、
をさらに含む、請求項2に記載の方法。
[請求項4]
エステル交換生成物を蒸留し、それによって9−デセン酸エステル、9−ウンデセン酸エステル、9−ドデセン酸エステルのそれぞれ、あるいはこれらの組み合わせからなる群から選択される少なくとも1種の特殊化学物質を分離することをさらに含む、請求項3に記載の方法。
[請求項5]
少なくとも1種の特殊化学物質を加水分解し、それによって9−デセン酸、9−ウンデセン酸、9−ドデセン酸のそれぞれ、あるいはこれらの組み合わせからなる群から選択される少なくとも1種の酸を形成させることをさらに含む、請求項4に記載の方法。
[請求項6]
加水分解の工程によってさらに、少なくとも1種の酸のアルカリ金属塩とアルカリ土類金属塩のそれぞれ、あるいはこれらの組み合わせを生成させる、請求項5に記載の方法。
[請求項7]
エステル交換生成物をそれ自体と反応させ、それによって二量体を形成させることをさらに含む、請求項2に記載の方法。
[請求項8]
複分解触媒の存在下で供給原料を反応させる前に、供給原料中の触媒毒を減少させるのに十分な条件の下で供給原料を処理することをさらに含む、請求項1〜7のいずれかに記載の方法。
[請求項9]
触媒毒を減少させるために、供給原料は化学反応によって化学的に処理される、請求項8に記載の方法。
[請求項10]
供給原料は酸素が存在しない中で100℃を超える温度に加熱され、そして触媒毒が減少するのに十分な時間にわたってその温度に保たれる、請求項8に記載の方法。
[請求項11]
水溶性のホスフィン試薬を用いてオレフィン類とエステル類から複分解触媒を分離することをさらに含む、請求項1〜5のいずれかに記載の方法。
[請求項12]
複分解触媒は溶媒中に溶解される、請求項1〜6のいずれかに記載の方法。
[請求項13]
溶媒はトルエンである、請求項12に記載の方法。
[請求項14]
オレフィン類をオリゴマー化し、それによりポリ−アルファ−オレフィン類、ポリ−内部−オレフィン類、鉱油代替え品、またはバイオディーゼルのうちの少なくとも1種を形成させることをさらに含む、請求項1〜13のいずれかに記載の方法。
[請求項15]
反応工程は、供給原料とそれ自体との間の自己複分解反応を含む、請求項1〜14のいずれかに記載の方法。
[請求項16]
低分子量オレフィンを用意することをさらに含み、反応工程は、供給原料と低分子量オレフィンとの間の交差複分解反応を含む、請求項1〜15のいずれかに記載の方法。
[請求項17]
低分子量オレフィンは、エチレン、プロピレン、1−ブテン、2−ブテンのそれぞれ、あるいはこれらの組み合わせからなる群から選択される少なくとも1種の低分子量オレフィンを含む、請求項16に記載の方法。
[請求項18]
低分子量オレフィンはアルファ−オレフィンである、請求項16に記載の方法。
[請求項19]
低分子量オレフィンは、4〜10の間の炭素数を有する少なくとも1種の枝分れオレフィンを含む、請求項16に記載の方法。
[請求項20]
オレフィン類を水素化し、それにより燃料組成物を形成することをさらに含む、請求項1〜19のいずれかに記載の方法。
[請求項21]
燃料組成物は、5〜16の間の炭素数分布を有するジェット燃料組成物かまたは8〜25の間の炭素数分布を有するディーゼル燃料組成物のいずれかを含む、請求項20に記載の方法。
[請求項22]
燃料組成物は、(a)8〜16の間の炭素数分布と、約38℃〜約66℃の間の引火点と、約210℃の自動発火温度、および約−47℃〜約−40℃の間の凝固点を有する灯油のタイプのジェット燃料、(b)5〜15の間の炭素数分布と、約−23℃〜約0℃の間の引火点と、約250℃の自動発火温度、および約−65℃の凝固点を有するナフサのタイプのジェット燃料、または(c)8〜25の間の炭素数分布と、約15.6℃において約0.82〜約1.08の間の比重と、約40よりも大きいセタン価、および約180℃〜約340℃の間の蒸留範囲を有するディーゼル燃料である、請求項20に記載の方法。
[請求項23]
エステル類からオレフィン類を分離する前に、複分解生成物から軽い末端流れをフラッシュ分離することをさらに含み、その軽い末端流れはその大部分が2〜4の間の炭素数を有する炭化水素である、請求項1〜22のいずれかに記載の方法。
[請求項24]
オレフィン類を水素化する前に、オレフィン類から軽い末端流れを分離することをさらに含み、その軽い末端流れはその大部分が3〜8の間の炭素数を有する炭化水素である、請求項20〜23のいずれかに記載の方法。
[請求項25]
オレフィン類を水素化する前に、オレフィン類からC18+の重い末端流れを分離することをさらに含み、その重い末端流れはその大部分が少なくとも18の炭素数を有する炭化水素である、請求項20〜24のいずれかに記載の方法。
[請求項26]
燃料組成物からC18+の重い末端流れを分離することをさらに含み、その重い末端流れはその大部分が少なくとも18の炭素数を有する炭化水素である、請求項20〜25のいずれかに記載の方法。
[請求項27]
燃料組成物を異性化することをさらに含み、このとき燃料組成物中の直鎖パラフィン化合物の部分はイソパラフィン化合物に異性化される、請求項20〜26のいずれかに記載の方法。
[請求項28]
燃料組成物を製造する方法であって、
天然油を含む供給原料を用意すること、
オレフィン類とエステル類を含む複分解生成物が形成されるのに十分な条件の下、複分解触媒の存在下で供給原料を反応させること、
複分解生成物を水素化し、それにより燃料組成物と少なくとも部分的に飽和したエステル類を形成させること、および
少なくとも部分的に飽和したエステル類から燃料組成物を分離すること、
を含む、前記方法。
[請求項29]
燃料組成物を異性化することをさらに含み、このとき燃料組成物中の直鎖パラフィン化合物の部分はイソパラフィン化合物に異性化される、請求項28に記載の方法。
[請求項30]
燃料組成物からC18+の重い末端流れを分離することをさらに含み、その重い末端流れはその大部分が少なくとも18の炭素数を有する炭化水素である、請求項28または29に記載の方法。
Claims (13)
- 天然油のグリセリド類を含む供給原料を交差複分解するための方法であって、
(a)天然油のグリセリド類を含む供給原料、および(b)1−ブテンからなる低分子量オレフィン類を用意すること;
複分解触媒の存在下で、前記天然油のグリセリド類と前記低分子量オレフィン類とを複分解反応器中で交差複分解反応させ、それによりオレフィン類とエステル類とを含む複分解生成物を形成させること;
前記複分解生成物中のエステル類から複分解生成物中のオレフィン類を分離し、分離したオレフィンの流れを形成すること、ここで、分離したオレフィン流はC2−C6オレフィン類である;そして
前記分離したオレフィンの流れの少なくとも一部を前記複分解反応器に再循環させること
を含む方法。 - メタノールの存在下でエステル類をエステル交換し、それにより飽和もしくは不飽和脂肪酸メチルエステル、グリセリン、メタノールおよびまたは遊離脂肪酸類を含むエステル交換生成物を形成させることをさらに含む、請求項1に記載の方法。
- 液−液分離によってエステル交換生成物からグリセリンを分離すること、
グリセリンを分離した後、エステル交換生成物を水で洗浄し、それによってグリセリンをさらに除去すること、および
洗浄の後、エステル交換生成物を乾燥し、それによってエステル交換生成物から水を分離すること、
をさらに含む、請求項2に記載の方法。 - エステル交換生成物中の不飽和脂肪酸メチルエステル類を蒸留し、それによって9−デセン酸エステル、および9−ドデセン酸エステルのそれぞれ、あるいはこれらの組み合わせを分離することをさらに含む、請求項3に記載の方法。
- 9−デセン酸エステル、および9−ドデセン酸エステルのそれぞれ、あるいはこれらの組み合わせを加水分解し、それによって9−デセン酸、および9−ドデセン酸からなる群から選択される少なくとも1種の酸を形成させることをさらに含む、請求項4に記載の方法。
- 加水分解の工程によってさらに、少なくとも1種の酸のアルカリ金属塩とアルカリ土類金属塩のそれぞれ、あるいはこれらの組み合わせを生成させる、請求項5に記載の方法。
- エステル交換生成物中の不飽和脂肪酸メチルエステル類をそれら自体と反応させ、それによって二量体を形成させることをさらに含む、請求項2に記載の方法。
- 複分解触媒の存在下で供給原料を反応させる前に、供給原料を処理し、供給原料中の触媒毒を減少させることをさらに含む、請求項1〜7のいずれかに記載の方法。
- 供給原料を還元剤または陽イオン無機塩基組成物を用いた化学反応によって化学的に処理し触媒毒を減少させる、請求項8に記載の方法。
- 酸素が存在しない中で100℃を超える温度に供給原料を加熱し、触媒毒を減少させる、請求項8に記載の方法。
- 水溶性のホスフィン試薬を用いてオレフィン類とエステル類から複分解触媒を分離することをさらに含む、請求項1〜5のいずれかに記載の方法。
- 複分解触媒は溶媒中に溶解される、請求項1〜6のいずれかに記載の方法。
- 前記溶媒はトルエンである、請求項12に記載の方法。
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