JP4490825B2 - 粗製炭化水素流品質向上法 - Google Patents
粗製炭化水素流品質向上法 Download PDFInfo
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- JP4490825B2 JP4490825B2 JP2004557688A JP2004557688A JP4490825B2 JP 4490825 B2 JP4490825 B2 JP 4490825B2 JP 2004557688 A JP2004557688 A JP 2004557688A JP 2004557688 A JP2004557688 A JP 2004557688A JP 4490825 B2 JP4490825 B2 JP 4490825B2
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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
- C10G27/00—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation
- C10G27/04—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation with oxygen or compounds generating oxygen
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- 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
- C10G27/00—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation
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- C—CHEMISTRY; METALLURGY
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- C10G27/00—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation
- C10G27/04—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation with oxygen or compounds generating oxygen
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- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/14—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one oxidation step
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Description
a) 粗製ナフサに基づき過酸化物溶液と有機酸との重量%を夫々少なくとも3及び4にして前記有機酸と前記過酸化物とを撹拌しながら混合し、次に硫黄、窒素、共役ジエン、及び不飽和化合物を含有する前記粗製炭化水素流を添加し、次に未処理鉄酸化物粉末乾燥触媒を1.0〜6.0のpHで、粗製炭化水素の重量に基づき0.01〜5.0重量%の量で添加し、気化した炭化水素を還流させながら抽出酸化を行うのに必要な時間反応を行わせることにより、前記粗製炭化水素流中に存在する硫黄、窒素、共役ジエン、及び不飽和化合物を酸化し、硫黄、窒素、共役ジエン、及び不飽和化合物が酸化剤スラリーにより部分的に酸化され、同時に抽出された炭化水素流を得、下方水性スラリー相及び上方酸化炭化水素相を生成させる工程、
b) 前記抽出酸化が終わった後、上方炭化水素相を分離し、中和し、それを水洗し、濾過し、そして乾燥し、処理済み無臭明黄色の安定な炭化水素相を得る工程、
c) 全窒素化合物が90重量%以上まで除去され、塩基性窒素化合物が99.7重量%まで除去され、共役ジエン化合物が22重量%以上まで除去され、硫黄化合物が13重量%まで除去され、次に4重量%〜16重量%の範囲のオレフィン除去が行われた(全ての%は最初の供給原料含有量に基づいている)処理済み無臭明黄色の安定な炭化水素相を回収する工程、
を含む。
本発明により、用語「粗製(raw)炭化水素」、又は「粗製ナフサ」とは、どのような水素化処理、メロックス、又は苛性洗浄処理でも、それらに未だ掛けられていないヘテロ原子極性化合物及び(又は)不飽和部分に富む炭化水素又はナフサ流を意味する。
本発明の抽出酸化法は、粗製軽質及び中間的蒸留物を含めた精製処理からのヘテロ原子極性化合物及び(又は)不飽和部分に富むどのような粗製炭化水素供給物に対しても有用である。
ここに与える抽出酸化法は、過酸化物と有機酸との組合せにより行われ、その酸化は、乾燥粉末未処理Fe酸化物触媒により活性化される。
本発明の抽出酸化は1ポット系である。生成した酸化化合物は、形成されるやいなや水性相により炭化水素媒体から抽出される。なぜなら、水性相とこれらの化合物の親和力が酸化により増大しているからである。
下の諸例は、頁岩油レトルト処理から得られた粗製ナフサ留分に適用された処理に言及している。
エチルアルコールで−16℃に冷却され、次に、非凝縮性ガスにより運ばれた非還流炭化水素物質のドライアイス・トラッパー(dry ice trapper)により冷却された還流凝縮器を具えた1リットル三口丸底フラスコに、35℃〜240℃の蒸留範囲を有し、814.6ppmの塩基性窒素、1,071.9ppmの全窒素、及び7,249.7ppmの全硫黄を含有する粗製頁岩油ナフサ500mlを入れた。次に5gのリモナイト鉱石(中央ブラジルに位置するニッケル鉱山から、Fe45重量%)を、0.149mmより大きく、0.177mmより小さく(−80〜+100タイラーメッシュに)粉砕し、150℃で1時間炉で乾燥した後、添加した。内容物を激しく撹拌した。フラスコを27分間50℃の温度へ加熱した。次に加熱を止め、酸化剤溶液を添加した。
エチルアルコールで−16℃に冷却され、次に、非凝縮性ガスにより運ばれた非還流炭化水素物質のドライアイス・トラッパーにより冷却された還流凝縮器を具えた1リットル三口丸底フラスコに、40mlの50重量%のH2O2、及び分析級蟻酸32mlから構成された酸化剤溶液を入れた。内容物を10分間撹拌した。次に41℃〜255℃の蒸留範囲を有し、813.2ppmの塩基性窒素、1,900ppmの全窒素、8,100ppmの全硫黄、2.37モル/lの共役ジエン、及び26.3重量%のオレフィンを含有する粗製頁岩油ナフサ500mlを添加した。混合物を2分間撹拌し、次に5gのリモナイト鉱石(中央ブラジルに位置するニッケル鉱山から、Fe45重量%)を、0.105mmより小さく(−150タイラーメッシュに)粉砕し、150℃で1時間炉で乾燥した後、添加した。12分の反応の後、最高温度は70℃に到達した。35分の反応の後、反応装置を既知の手段により外部から冷却した。全反応時間は80分に到達した。最後の温度は周囲温度であった。
エチルアルコールで−16℃に冷却され、次に、非凝縮性ガスにより運ばれた非還流炭化水素物質のドライアイス・トラッパーにより冷却された還流凝縮器を具えた1リットル三口丸底フラスコに、40mlの50重量%のH2O2、及び分析級蟻酸32mlから構成された酸化剤溶液を添加した。内容物を10分間撹拌した。次に41℃〜255℃の蒸留範囲を有し、813.2ppmの塩基性窒素、1,900ppmの全窒素、8,100ppmの全硫黄、2.37モル/lの共役ジエン、及び26.3重量%のオレフィンを含有する粗製頁岩油ナフサ500mlを添加した。混合物を2分間撹拌し、次に3gのリモナイト鉱石(中央ブラジルに位置するニッケル鉱山から、Fe45重量%)を、0.105mmより小さく(−150タイラーメッシュに)粉砕し、150℃で1時間炉で乾燥した後、添加した。15分間この温度に維持し、最高温度は69.2℃に到達した。25分の反応の後、温度は低下し始め、60分後に46.5℃に到達し、次に反応装置を外部から冷却し、周囲温度にした。
エチルアルコールで−16℃に冷却され、次に、非凝縮性ガスにより運ばれた非還流炭化水素物質のドライアイス・トラッパーにより冷却された還流凝縮器を具えた1リットル三口丸底フラスコに、32mlの60重量%のH2O2、及び分析級蟻酸24mlから構成された酸化剤溶液を入れた。内容物を10分間撹拌した。次に41℃〜255℃の蒸留範囲を有し、813.2ppmの塩基性窒素、1,900ppmの全窒素、8,100ppmの全硫黄、2.37モル/lの共役ジエン、及び26.3重量%のオレフィンを含有する粗製頁岩油ナフサ500mlを添加した。混合物を2分間撹拌し、次に3gのリモナイト鉱石(中央ブラジルに位置するニッケル鉱山から、Fe45重量%)を、0.105mmより小さく(−150タイラーメッシュに)粉砕し、150℃で1時間炉で乾燥した後、添加した。10分後、最高温度は71.5℃に到達し、この温度に更に20分間維持した。次に温度は低下し始め、60分の反応後に45.2℃に到達し、反応を周囲温度まで外部から冷却した。
Claims (24)
- 過酸化物溶液/有機酸の組合せ及び粉末未処理鉄酸化物触媒の存在下で、大気圧及び周囲温度に等しいか又はそれより高い温度で、ヘテロ原子極性化合物及び(又は)不飽和部分に富む粗製炭化水素流から硫黄、窒素、共役ジエン、及び他の不飽和化合物を酸化及び(又は)不活性化により粗製炭化水素流を品質向上する方法であって、次の工程:
a) 粗製炭化水素に基づき過酸化物溶液と有機酸との重量%を夫々少なくとも3及び4にして前記有機酸と前記過酸化物とを撹拌しながら混合し、次に硫黄、窒素、共役ジエン、及び不飽和化合物を含有する前記粗製炭化水素流を添加し、次に、0.177mm(80タイラーメッシュ)より小さい粒度にまで粉砕された未処理鉄酸化物粉末乾燥触媒を1.0〜6.0のpHで、粗製炭化水素の重量に基づき0.01〜5.0重量%の量で添加し、気化した炭化水素を還流させながら抽出酸化を行うのに必要な時間反応を行わせることにより、前記粗製炭化水素流中に存在する硫黄、窒素、共役ジエン、及び不飽和化合物を酸化し、硫黄、窒素、共役ジエン、及び不飽和化合物が酸化剤水性スラリーにより部分的に酸化され、同時に抽出された炭化水素流を得、下方水性スラリー相及び上方酸化炭化水素相を生成させる工程、
b) 前記抽出酸化が終わった後、上方炭化水素相を分離し、中和し、それを水洗し、濾過し、そして乾燥する工程、
c) 全窒素化合物が90重量%まで除去され、塩基性窒素化合物が99.7重量%まで除去され、共役ジエン化合物が22重量%まで除去され、硫黄化合物が13重量%まで除去され、次に4重量%〜16重量%の範囲のオレフィンが除去された(全ての%は最初の供給原料含有量に基づいている)、処理済み無臭明黄色の安定な炭化水素相を回収する工程、
を含む品質向上法。 - 前記鉄酸化物触媒の粒度が、0.105mm(150タイラーメッシュ)より小さい、請求項1に記載の方法。
- 別法として、粉末にし、乾燥した未処理鉄酸化物触媒を、最初に、硫黄、窒素、共役ジエン、及び他の不飽和化合物を含有する炭化水素流へ添加する、請求項1又は2に記載の方法。
- 粗製炭化水素供給物が、粗製軽質及び中間的蒸留物である、請求項1又は2に記載の方法。
- 粗製炭化水素供給物が、30〜300℃の沸点範囲の粗製ナフサである、請求項1又は2に記載の方法。
- 粗製ナフサが、頁岩油レトルト処理から得られたものである、請求項5に記載の方法。
- 鉄酸化物触媒が、式FeOOHのオキシ水酸化鉄、式FeOOH・nH2Oの水和オキシ水酸化鉄、及びα−FeOOH(針鉄鉱)、γ−FeOOH(鱗鉄鉱)、β−FeOOH(アカガナイト)、及びδ′−FeOOH(フェロキシハイト)のような結晶形態のものを含む、請求項1又は2に記載の方法。
- 過酸化物を、そのまま又は溶液として添加する、請求項1又は2に記載の方法。
- 過酸化物が、少なくとも30重量%の濃度の過酸化水素である、請求項8に記載の方法。
- 過酸化水素の濃度が、50重量%である、請求項9に記載の方法。
- 過酸化水素の濃度が、60重量%である、請求項9に記載の方法。
- 前記粗製炭化水素流からのヘテロ原子極性化合物の抽出酸化が、水性スラリー相に対するそれら化合物の強い親和力の結果として、酸化された化合物が、水性酸化剤それ自体により前記相中へ抽出されることを含む、請求項1又は2に記載の方法。
- 有機酸が蟻酸である、請求項1又は2に記載の方法。
- 有機酸が酢酸である、請求項1又は2に記載の方法。
- 粗製炭化水素に基づく過酸化物溶液及び有機酸の重量%が、夫々6〜15、及び8〜20である、請求項1又は2に記載の方法。
- 過酸化物/有機酸のモル比が、0.5〜1.2の範囲にある、請求項1又は2に記載の方法。
- 前記モル比が、0.9〜1.1の範囲にある、請求項16に記載の方法。
- 前記モル比が、0.95〜1の範囲にある、請求項17に記載の方法。
- 中和され、洗浄された炭化水素から、廃水及び廃棄アルカリ性中和溶液を完全にパージする、請求項1又は2に記載の方法。
- 中和され、洗浄された炭化水素から、廃水及び廃棄アルカリ性中和溶液を、部分的にパージした後、再循環する、請求項19に記載の方法。
- 使用済み酸化剤溶液及び鉄酸化物触媒を含む水性スラリー相を傾瀉して、固体触媒相を分離する、請求項1又は2に記載の方法。
- 固体触媒相を廃棄する、請求項21に記載の方法。
- 固体触媒相を、洗浄し、乾燥した後、再使用する、請求項21に記載の方法。
- 固体再使用触媒の一部分をパージし、新しいリモナイトを補充して使用済み触媒と置き換える、請求項23に記載の方法。
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JP2006509077A (ja) | 2006-03-16 |
ES2616866T3 (es) | 2017-06-14 |
BR0308158A (pt) | 2005-08-23 |
EP1570028A1 (en) | 2005-09-07 |
WO2004053026A1 (en) | 2004-06-24 |
BR0308158B1 (pt) | 2013-04-02 |
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