WO2005019391A1 - Desulfurisation de naphta sans perte d'octane et avec retention d'olefines accrue - Google Patents

Desulfurisation de naphta sans perte d'octane et avec retention d'olefines accrue Download PDF

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Publication number
WO2005019391A1
WO2005019391A1 PCT/US2004/024861 US2004024861W WO2005019391A1 WO 2005019391 A1 WO2005019391 A1 WO 2005019391A1 US 2004024861 W US2004024861 W US 2004024861W WO 2005019391 A1 WO2005019391 A1 WO 2005019391A1
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Prior art keywords
naphtha
sulfur
iso
olefins
feed
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PCT/US2004/024861
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English (en)
Inventor
Gordon F. Stuntz
Randolph J. Smiley
Thomas R. Halbert
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Exxonmobil Research And Engineering Company
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Publication of WO2005019391A1 publication Critical patent/WO2005019391A1/fr

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Classifications

    • 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
    • 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
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/20—Organic compounds not containing metal atoms
    • C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
    • 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
    • C10G67/10—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 alkaline treatment as the refining step in the absence of hydrogen
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
    • C10G69/123—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step alkylation

Definitions

  • the invention relates to a process for removing sulfur from naphtha, with olefin retention and no octane loss.
  • the process comprises (a) forming, from a sulfur-containing naphtha, an iso-olefinic naphtha feed containing sulfur and iso-olefins having from eight to twelve carbon atoms, and (b) selectively hydrodesulfurizing the iso-olefinic naphtha feed with no octane number loss and increased olefin retention.
  • Patent 5,599,441 and patent publication WO 01/53432 Al It would be an improvement if a way could be found to remove sulfur from a naphtha that contains olefins and organic sulfur compounds, including thiophenic sulfur compounds, with reduced olefin loss and little or no reduction in octane number. It would be an even greater improvement if these goals could be achieved with an increase in octane number.
  • the invention relates to a process for selectively removing sulfur from a sulfur and olefin-containing naphtha feed with little or no octane number loss and with retention of most of the feed olefins.
  • the process comprises (a) forming, from a sulfur-containing naphtha, an iso-olefinic naphtha feed containing sulfur and iso-olefins having from eight to twelve carbon atoms (C 8 - C ⁇ 2 ), and (b) selectively hydrodesulfurizing the iso-olefinic naphtha feed with a sulfur selective hydrodesulfurizing catalyst, at reaction conditions selective for sulfur removal, to remove most of the sulfur while retaining most of the olefins and form a desulfurized naphtha useful for mogas, with little or no octane number loss.
  • the selective hydrodesulfurizing will result in an octane number increase.
  • no octane number loss and octane number increase is respectively meant the octane number of the desulfurized naphtha is no less than, and preferably greater than, that of the iso-olefinic naphtha feed prior to being selectively hydrodesulfurized.
  • iso-olefinic naphtha feed is meant naphtha comprising at least about 25 vol.% and preferably at least about 40 vpl.% olefins, of which at least about 20 vol.%, preferably at least about 30 vol.% and more preferably at least about 35 vol.% are iso-olefins having from eight to twelve carbon atoms.
  • sulfur is meant sulfur-containing organic compounds.
  • octane number is meant the average of the Research octane number (R) and Motor octane number (M), or (R + M)/2.
  • the iso-olefinic naphtha feed can be formed by (i) adding Cs-Ci 2 iso-olefins to a sulfur-containing naphtha, by (ii) converting an olefinic naphtha that contains sulfur and C 6- olefins to an iso-olefinic naphtha feed, by contacting the feed with a catalytically effective amount of a conversion catalyst at conversion reaction conditions effective to convert at least some of the C 6- olefms to iso-olefins having from eight to twelve carbon atoms, or (iii) a combination thereof.
  • the sulfur-containing naphtha will be a highly olefinic cracked naphtha, such as an FCC naphtha, which typically contains more than about 25 vol.% olefins and in which most of the sulfur is in the form of thiophenic sulfur compounds. If the sulfur-containing naphtha contains thiophenic sulfur compounds, it is preferred that the conversion step also convert the thiophenic sulfur compounds in the naphtha to higher boiling sulfur compounds ("converted thiophenic sulfur compounds") boiling above about 182°F and preferably above about 200°F, to produce an iso-olefinic naphtha feed containing converted thiophenic sulfur compounds.
  • Converted thiophenic sulfur compounds boiling above about 182°F and preferably above about 200°F
  • the iso-olefinic naphtha formed by the conversion step (ii) may be selectively hydrodesulfurized, it is preferred to separate it into heavy and light fractions, with the heavy fraction containing the C 8 -Ci 2 iso-olefins and the light fraction containing C 6- olefins, and then selectively hydrodesulfurize only the heavy fraction under conditions where the octane number of the selectively hydrodesulfurized heavy fraction will be no less than it was prior to the desulfurization.
  • the light fraction may then be recombined with the hydrotreated heavy fraction to form a mogas naphtha stock, which will typically have an octane number higher than the iso-olefinic naphtha formed in step (ii). This minimizes the loss of C 6- olefins by saturation, which would otherwise occur if the light fraction remains and is selectively hydrodesulfurized with the heavy fraction.
  • the heavy fraction would also contain the higher boiling sulfur compounds formed by converting thiophenic sulfur compounds, for the preferred embodiment in which the sulfur in the sulfur- containing naphtha feed is mostly thiophenic sulfur.
  • the iso-olefinic naphtha feed will have a Bromine Number greater than about 50.
  • the iso-olefinic naphtha feed is formed by converting a naphtha in which most of the sulfur is in the form of thiophenic sulfur compounds, more than about 50 wt.% and preferably more than about 75 wt.% of the sulfur in iso-olefinic feed will be in the form of the higher boiling, converted thiophenic sulfur compounds.
  • the sulfur-selective hydrodesulfurizing catalyst and conditions are chosen so that most of the sulfur is removed from the naphtha as H 2 S, while most of the olefins are retained.
  • the sulfur-selective hydrodesulfurizing catalyst can be, for example, a low metal-loaded catalyst of the type disclosed and described in U.S. Patent 6,013,598 the disclosure of which is incorporated herein by reference.
  • This catalyst comprises an inorganic refractory support component, from about 2 to about 8 wt.% M0O 3 , about 0.1 to about 5 wt.% CoO, has a Co/Mo atomic ratio of about 0.1 to about 1.0, a median pore diameter of from about 6 ⁇ A to about 20 ⁇ A, a MoO surface concentration in g Mo0 3 /m 2 of about 0.5xl0 "4 to about 3x10 "4 , an average particle size diameter of less than 2.0 mm, and a metal sulfide edge plane area of from about 800 to about 2,800 ⁇ mol oxygen/g M0O 3 as measured by oxygen chemisorption.
  • Suitable conversion catalysts comprise solid acid catalysts having alkylating activity, such as those disclosed in the patents and patent publications referred to in paragraph [0003], and are discussed in more detail below.
  • Single stage selective hydrodesulfurization reaction conditions will include a temperature in the range of about 450°F to about 675°F and preferably about 500°F to about 625°F, a pressure in the range of from about 200 to about 800 psig and preferably about 200 to about 500 psig, a liquid hourly space velocity in the range of from about 1.2 to about 15 V/V/Hr and preferably about 1.5 to about 10 V/V/Hr, a hydrogen treat gas feed rate of about 200 to about 5000 SCF/B and preferably about 200 to bout 2500 SCF/B, with the hydrogen content of the (hydrogen) treat gas ranging from 50-100 and preferably 65-100 volume %.
  • the invention relates to a process for removing sulfur from a naphtha boiling-range hydrocarbon with little or no loss in the hydrocarbon's octane number and preferably an increase.
  • the hydrocarbon can be a naphtha feed or feedstock including petroleum naphthas, steam cracked naphthas, coker naphthas, thermally cracked naphthas, FCC naphthas and blends and fractions thereof, with boiling points typically in the range of from about C 5 up to about 450°F for full range naphthas.
  • Light fraction naphthas typically have a boiling range of from about C 4 , C 5 , or Ce up to about 330°F and heavy naphthas boil in the range of about 250°F to about 450°F. All cracked naphthas inherently contain olefins and organic sulfur compounds, with most of the sulfur in the form of thiophenic sulfur compounds. Such naphthas have an initial boiling point typically starting at about C 5 .
  • thiophenes and thiophenic is meant thiophene and derivatives thereof such as methylthiophene, dimethylthiophene, tetrahydrothiophene and methyl- tetrahydrothiophene.
  • the feed is a thermally or cat cracked naphtha, e.g., an FCC naphtha, which typically contains up to about 60 vol.% olefins and from about 1,000 to about 7,000 wppm (about 0.1 to about 0.7 wt.%) sulfur, more typically up to about 3,000 wppm, most of which is in the form of thiophenic sulfur compounds.
  • the actual olefin content of a sulfur-containing cracked naphtha typically ranges from about 5 to bout 60 vol.%, with about 10 to about 40 vol.%) being more typical.
  • the iso-olefins formed by the conversion are made from olefins having from four to six carbon atoms (C 6- ).
  • the total olefin content should be sufficient to form C 8 -C 12 iso-olefins and to convert thiophenes to the higher boiling sulfur compounds. If the sulfur-containing naphtha does not contain sufficient C 6- olefins, then C 6- olefins may be added.
  • the olefin content of the sulfur-containing naphtha is naturally present in an amount of at least about 25, preferably about 30 vol.%, up to at least about 60 and preferably between about 50 and about 60 vol.%.
  • C 6- olefins in the context of the invention is meant one or more of four, five or six carbon atom olefins, typically five and six carbon atoms, and preferably olefins having four, five and six carbon atoms.
  • C 6- olefins and a naphtha containing C 6- olefins is not meant to exclude the presence of C + olefins (e.g., C -C 12 ) in the naphtha. In at least some cases C 7+ olefins will also be present in a naphtha containing C 6 _ olefins.
  • Nitrogen compounds are removed from the naphtha feed prior to the conversion reaction, if needed to avoid deactivation of the acid catalyst.
  • Conventional nitrogen removal means can be used, including washing with an aqueous acidic solution and/or passing the naphtha feed through one or more guard beds to adsorb or absorb these compounds, prior to the feed contacting the acid catalyst.
  • Such guard beds can be conventional, and may contain one or more solid materials such as fresh cracking catalyst, fluorided alumina, any of a number of zeolite materials, alumina, silica, silica-alumina, activated carbon, various clays, etc.
  • the iso-olefinic feed is formed using an acidic material having alkylating activity and which is capable of (i) converting C -C 6 olefins to Cg-C ⁇ 2 iso-olefins and, for a naphtha feed having 10 wt.%» or more thiophenic sulfur, (ii) catalyzing the reaction of an olefin or alcohol with thiophenic sulfur compounds to form higher boiling sulfur compounds.
  • Solid acidic catalysts are particularly desirable and include liquid acids supported on a solid substrate, as well as acidic inorganic oxides and acidic polymeric resins. See, e.g., U.S.
  • a catalyst comprising phosphoric acid supported on kieselguhr has been used with particular effectiveness. The preparation and use of this particular type of catalyst is l ⁇ iown and disclosed in for example, the '419 patent and in published patent application 20020148757.
  • Catalysts comprising acidic inorganic oxides useful for treating the naphtha include, by way of example, aluminas, silica-aluminas, natural and synthetic pillared clays, and natural and synthetic zeolites. Illustrative, but non- limiting examples include faujasites, mordenites, L, omega, X, Y, beta, and ZSM zeolites.
  • Highly suitable zeolites include zeolite beta, Y, ZSM-3, ZSM-4, ZSM-5 types, ZSM-12, ZSM-18, ZSM-20, ZSM-35 and ZSM-48, TEA, mordenite, faujasites, USY and members of the MCM group, such as MCM-2.
  • the naphtha feed conversion treatment reduces the Bromine Number because at least some of the feed olefins participate in the conversion reaction as alkylating agents for converting the thiophenic sulfur compounds, while others are converted to branched isoparaffins useful for octane number.
  • Alcohols are also known to be useful alkylating agents and, while it is permissible to add one or more alcohols to the naphtha feed as alkylating agents prior to the conversion treatment, it is preferred use only olefins as alkylating agents.
  • Reaction conditions useful for treating the naphtha feed to produce a converted naphtha include a temperature in the range of from about 100°F to about 700°F (about 38°C to about 371°C), preferably about 200°F to about 600°F (about 93°C to about 316°C) and more preferably about 300°F to about 400°F (about 149°C to about 204°C).
  • the pressure may range from about 50 to about 10,000 kPa, preferably from about 100 to about 2,000 kPa.
  • Preferred olefins in the naphtha feed for converting thiophenes and forming the iso-olefins will have from about 4 to about 12 carbon atoms and preferably from about 4 to about 8 carbon atoms.
  • the Cs-C ⁇ 2 iso-olefins present in the iso-olefinic naphtha feed formed by the conversion reaction will also be in the heavy fraction.
  • the iso-olefinic naphtha feed or fraction thereof to be selectively hydrodesulfurized has a high olefin concentration, as reflected in a Bromine number greater than about 50, preferably greater than about 60 and more preferably at least about 75.
  • Selective hydrodesulfurization uses a sulfur-selective hydrodesulfurization catalyst, sulfur-selective process conditions, or both, to remove sulfur with little or no attendant octane number reduction.
  • Conventional selective hydrodesulfurization can be used.
  • One conventional sulfur-selective hydrodesulfurization catalyst comprises an inorganic refractory support component, from about 1 to about 10 wt.% Mo0 3 , preferably about 2 to about 8 wt.% and more preferably about 4 to about 6 wt.%.
  • the amount of CoO will range from about 0.1 to about 5 wt.%, preferably about 0.5 to about 4 wt.% and more preferably about 1 to about 3 wt.%.
  • the weight percents expressed herein are all based on the total weight of the catalyst.
  • the Co/Mo atomic ratio will range from about 0.1 to about 1, preferably about 0.20 to about 0.80 and more preferably about 0.25 to about 0.72.
  • the catalyst will have a median pore diameter of from about 6 ⁇ A to about 200 A, preferably from about 75 A to about 175 A and more preferably about 8 ⁇ A to about 15 ⁇ A.
  • the MoO surface concentration in g Mo0 3 /m 2 will range between about 0.5xl0 "4 to about 3xl0 "4 , preferably about 0.75xl0 "4 to about 2.5xl0 "4 and more preferably about lxlO "4 to about 2.x 10 "4 .
  • the average particle size diameter is less than about 2 mm, preferably less than about 1.6 and more preferably less than about 1.4. It will have a metal sulfide edge plane area of from about 800 to about 2,800 ⁇ mol oxygen g Mo0 3 as measured by oxygen chemisorption, preferably about 1,000 to about 2,200 and more preferably about 1,200 to about 2,000.
  • the amounts and types of contaminants permitted, as well as the amount of phosphorus and alkali metal additives desired to be present and suitable catalyst preparation techniques, may be found in U.S. patent 6,013,589. Selective hydrodesulfurizing conditions, including conventional selective hydrodesulfurization conditions can be used.
  • Such conditions can include a temperature in the range of about 450°F to about 675°F and preferably about 500°F to about 625°F, a pressure in the range of from about 200 to about 800 psig and preferably about 200 to about 500 psig, a liquid hourly space velocity in the range of from about 1.2 to about 15 V/V/Hr and preferably about 1.5 to about 10 V/V/Hr, a hydrogen treat gas feed rate of about 200 to about 5000 SCF/B and preferably about 200 to about 2500 SCF/B, with the hydrogen content of the (hydrogen) treat gas ranging from about 50 to about 100 and preferably about 65 to about 100 volume %.
  • the selective hydrodesulfurization removes most of the sulfur from the converted naphtha, while retaining most of the olefins in it, to produce a desulfurized naphtha having an octane number within about 95 %, preferably no less than, and more preferably greater than its octane number value prior to the desulfurization.
  • selectively hydrodesulfurizing with the naphtha in the vapor state and/or using two or more stages with interstage removal of H 2 S will permit the use of slightly higher temperatures and slightly lower space velocities.
  • a multiple-stage process with interstage removal of H 2 S is disclosed, for example, in U.S. Patent No. 6,231,753 referred to above, the disclosure of which is incorporated herein by reference and which relates to selective naphtha hydrodesulfurization.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

Selon l'invention, du naphta est désulfurisé sans perte d'octane, par formation d'une charge de naphta iso-oléfinique suivi de son hydrodésulfurisation sélective afin de produire du naphta pour essence automobile. La charge de naphta iso-oléfinique peut être formée à partir de naphta craqué, par sa mise en contact avec un catalyseur acide solide afin de convertir des oléfines C6 en iso-oléfines C8-C12 et convertir des thiophènes en composés de soufre à point d'ébullition plus élevé. De préférence, uniquement une fraction lourde contenant les iso-oléfines et le soufre à point d'ébullition plus élevé est sélectivement hydrodésulfurisée.
PCT/US2004/024861 2003-08-19 2004-08-03 Desulfurisation de naphta sans perte d'octane et avec retention d'olefines accrue WO2005019391A1 (fr)

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
US49631403P 2003-08-19 2003-08-19
US60/496,314 2003-08-19
US49978703P 2003-09-03 2003-09-03
US49978803P 2003-09-03 2003-09-03
US60/499,788 2003-09-03
US60/499,787 2003-09-03

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WO2005019391A1 true WO2005019391A1 (fr) 2005-03-03

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PCT/US2004/024832 WO2005019387A1 (fr) 2003-08-19 2004-08-03 Production de flux de naphta faible en soufre par adoucissement et fractionnement combines avec une alkylation de thiofene
PCT/US2004/024848 WO2005019390A1 (fr) 2003-08-19 2004-08-03 Addition d'olefines permettant une desulfuration du naphte avec perte reduite d'octanes
PCT/US2004/024861 WO2005019391A1 (fr) 2003-08-19 2004-08-03 Desulfurisation de naphta sans perte d'octane et avec retention d'olefines accrue

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PCT/US2004/024848 WO2005019390A1 (fr) 2003-08-19 2004-08-03 Addition d'olefines permettant une desulfuration du naphte avec perte reduite d'octanes

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US6231753B1 (en) * 1996-02-02 2001-05-15 Exxon Research And Engineering Company Two stage deep naphtha desulfurization with reduced mercaptan formation
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WO2006073963A2 (fr) * 2004-12-30 2006-07-13 Bp Corporation North America Inc. Procede de suppression de soufre de composants pour le flechissement de combustibles de transport
WO2006073963A3 (fr) * 2004-12-30 2007-02-15 Bp Corp North America Inc Procede de suppression de soufre de composants pour le flechissement de combustibles de transport
JP2008527089A (ja) * 2004-12-30 2008-07-24 ビーピー・コーポレーション・ノース・アメリカ・インコーポレーテッド 輸送燃料の配合用成分からイオウを除去する方法
EA013841B1 (ru) * 2004-12-30 2010-08-30 Бп Корпорейшн Норт Америка Инк. Способ десульфации компонентов топлива
US8057661B2 (en) 2004-12-30 2011-11-15 Bp Corporation North America Inc. Process for removal of sulfur from components for blending of transportation fuels
WO2006114510A1 (fr) * 2005-04-28 2006-11-02 Institut Francais Du Petrole Procede de desulfuration d'essences olefiniques
FR2885137A1 (fr) * 2005-04-28 2006-11-03 Inst Francais Du Petrole Procede de desulfuration d'essences olefiniques
JP2008539296A (ja) * 2005-04-28 2008-11-13 アンスティテュ フランセ デュ ペトロール オレフィンガソリンの脱硫方法
KR101286872B1 (ko) * 2005-04-28 2013-07-16 아이에프피 에너지스 누벨 올레핀계 가솔린의 탈황 방법

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