EP2707462A2 - Verfahren zur herstellung von diesel- oder kerosinschnitten aus einem olefinstrom mit hauptsächlich 4 bis 6 kohlenstoffatomen unter verwendung von zwei oligomerisationseinheiten - Google Patents

Verfahren zur herstellung von diesel- oder kerosinschnitten aus einem olefinstrom mit hauptsächlich 4 bis 6 kohlenstoffatomen unter verwendung von zwei oligomerisationseinheiten

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Publication number
EP2707462A2
EP2707462A2 EP12713203.3A EP12713203A EP2707462A2 EP 2707462 A2 EP2707462 A2 EP 2707462A2 EP 12713203 A EP12713203 A EP 12713203A EP 2707462 A2 EP2707462 A2 EP 2707462A2
Authority
EP
European Patent Office
Prior art keywords
carbon atoms
oligomerization
predominantly
cut
zsm
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP12713203.3A
Other languages
English (en)
French (fr)
Other versions
EP2707462B1 (de
Inventor
Pierre Alain BREUIL
Nicolas Cadran
François Hugues
Vincent Coupard
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IFP Energies Nouvelles IFPEN
Original Assignee
IFP Energies Nouvelles IFPEN
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Filing date
Publication date
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Publication of EP2707462A2 publication Critical patent/EP2707462A2/de
Application granted granted Critical
Publication of EP2707462B1 publication Critical patent/EP2707462B1/de
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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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
    • C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
    • C10G25/02—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material
    • C10G25/03—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material with crystalline alumino-silicates, e.g. molecular sieves
    • C10G25/05—Removal of non-hydrocarbon compounds, e.g. sulfur compounds
    • 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
    • C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
    • 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
    • C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
    • C10G25/003—Specific sorbent material, not covered by C10G25/02 or C10G25/03
    • 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
    • C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
    • 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
    • C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
    • C10G57/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with polymerisation
    • 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
    • C10G67/06—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 a sorption process 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
    • C10G69/126—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 polymerisation, e.g. oligomerisation
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1088—Olefins
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2400/04—Diesel 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/08—Jet fuel

Definitions

  • the present invention is in the field of refining processes for converting an olefinic fraction having predominantly 4 to 6 carbon atoms in a so-called middle distillate cut having predominantly 10 to 20 carbon atoms.
  • This middle distillate cut may be a kerosene cut or a diesel cut.
  • the present invention uses a first purification step to remove the nitrogen compounds contained in the feed followed by two different oligomerization,
  • a first oligomerization making it possible to essentially react the isoolefins and leading to a gasoline cut composed of isoolefins having predominantly from 8 to 10 carbon atoms, an excellent octane number which can be separated and recovered as such, and
  • hydrocarbon cut (02) comprising at least partly hydrocarbons having a number of carbon atoms of between 6 and 10, of which at least 2% by weight of olefins, in the presence of at least one catalyst promoting the dimerization and alkylation reactions of the species present in the mixture resulting from said contacting,
  • step b) a separation of the effluents from step b) into at least two slices of which:
  • This patent does not describe any pretreatment step, in particular purification of the feedstock (01).
  • Patent FR 2,887,555 describes a process for preparing a diesel cut from an olefinic C2 Cl 2 cut comprising the following steps:
  • step 2) a separation of the product mixture obtained in step 1), in three sections, including an intermediate section with a final boiling point of between 200 and 220 ° C.
  • This process therefore uses a very broad olefinic fraction as filler and uses two distinct oligomerizations. It does not mention the possibility of a pretreatment of said charge, including purification against any nitrogen compounds contained in said charge.
  • the patents FR 2 871 167 and FR 2 871 168 describe processes for producing diesel fuel cut from gasoline cuts comprising a first step of separation of the normal and isoolef, the oligomerization step relating only to the normal olefins.
  • the process according to the present invention does not require any prior separation of the normal and iso olefins.
  • the process according to the present invention does not use any alkylation step and therefore does not require any BTX-type cutting.
  • FIG. 1 represents a diagram of the process according to the invention using two distinct oligomerization units preceded by a step of purification of the charge on a capture mass.
  • the process according to the present invention uses two distinct oligomerization units working on different catalysts and under different operating conditions.
  • the process according to the invention can be defined as a process for producing an average distillate cut having predominantly from 12 to 25 carbon atoms from an olefinic feed having predominantly between 4 and 6 carbon atoms, comprising the following process: 'following steps:
  • a second oligomerization step of the remaining effluents (that is to say effluents reduced by the gasoline cut extracted in the previous step) from the first oligomerization step carried out at a temperature greater than 120 ° C on an amorphous silico aluminate catalyst, or on a zeolite catalyst,
  • the starting olefins cut must comprise a minimum of branched olefins, called isoolefins, minimum which can be set at 10% by weight and preferably at 20% by weight, relative to all olefms of the charge.
  • the feed consists of a section of olefinic hydrocarbons containing from 3 to 8 carbon atoms, preferably from 4 to 6 carbon atoms. It contains from 20% to 100% of olefins, preferably from 20% to 80% of olefins, and more preferably from 40% to 60% of olefins.
  • It can come from a fluidized catalytic cracking unit or a naphtha steam cracking unit, or an alcohol dehydration unit or a Fischer-Tropsch synthesis unit or other available sources. from refining or petrochemical units.
  • the charge to be treated (1) is sent to a purification unit (PUR) using an adsorbent such as a molecular sieve (for example of the Na X or NaY type) working under the following operating conditions:
  • PUR purification unit
  • an adsorbent such as a molecular sieve (for example of the Na X or NaY type) working under the following operating conditions:
  • adsorbents used in the purification unit include metal oxides such as aluminas, crystallized silico-aluminates such as zeolites (often called molecular sieves), or mixtures of these compounds.
  • zeolite-based molecular sieves of the faujasite type are preferred.
  • An example is the NaX zeolite, for example that marketed by Axens under the name SBE 13X.
  • This purifying unit is mainly intended to eliminate the nitrogenous compounds contained in the feed and which constitute poisons with respect to the catalysts used in downstream oligomerization units.
  • the effluent (2) of the purification unit (PUR) is sent in a first oligomerization step (OLG1) working at a temperature below 120 ° C on a silica-alumina catalyst.
  • the oligomerization catalyst for the first oligomerization step (OLG1) is an amorphous catalyst based on silico-aluminate, preferably chosen from silica-aluminas and silica aluminas, and preferably silicified alumina.
  • the mass ratio SiO 2 / Al 2 O 3 is between 0.05 and 10, and preferably between 0.2 and 1.
  • a preferred catalyst is for example that marketed by AXENS under the name IP 811.
  • the effluent (3) leaving the first oligomerization step (OLG1) is optionally sent to a separation unit (DISTl) for extracting a gasoline cut (3 ') with a good octane number and which can therefore join the gasoline pool (POOL). Part of this species (3 ') can also be directed to the oligomerization unit (OLG2).
  • the effluent (3) of the first oligomerization step (OLG1), or the effluent (4) of the optional separation step (DIST1) when it exists, is sent to a second oligomerization step (OLG2) working at a temperature above 120 ° C,
  • zeolitic type catalyst such as, for example, a catalyst containing a zeolite ZSM-5.
  • the zeolite catalyst used in the second oligomerization step (OLG2) preferably comprises at least one zeolite selected from the group consisting of aluminosilicate zeolites having an overall Si / Al atomic ratio greater than 10 and a pores 8, 10 or 12MR.
  • Said zeolite is even more preferably selected from the group consisting of zeolites: ferrierite, chabazite, zeolites Y and US-Y, ZSM-5, ZSM-12, NU-86, mordenite, ZSM-22, NU-10, ZBM-30, ZSM-11, ZSM-57, ZSM-35, ⁇ -2, ITQ-6 and IM-5, SAPO, taken alone or in admixture.
  • said zeolite is selected from the group consisting of ferrierite zeolites, ZSM-5, Mordenite and ZSM-22, taken alone or as a mixture.
  • the zeolite used is ZSM-5.
  • the effluents (5) of the second oligomerization step (OLG2) are then separated in a separation unit (DIST2) from which at least 4 sections are extracted:
  • raffinate corresponding to an LPG cut
  • intermediate cut (7) which corresponds to a gasoline with a number of carbon atoms of between 5 and 10
  • Example 1 Charge C5-C6 (LCN)
  • the various beds are arranged in series.
  • the filler used is a so-called light gasoline C5-C6 cut that comes from an FCC unit, under the name LCN (Light Cut Naphta).
  • the charge has a density of 0.6548.
  • It also contains organic nitrogen compounds totaling a content of 11.6 ppm by weight expressed as elemental nitrogen and 15 ppm by weight of elemental sulfur.
  • the effluent of the first bed is sent integrally into the second bed carrying out the first oligomerization step (OLGl) in which the temperature is gradually raised between 60 ° C and 120 ° C, in order to keep constant the conversion of the iso-olefins into C5, between 80% and 85%
  • the effluent from the second bed is sent integrally into the third bed carrying out the second oligomerization step (OLG2), in which the temperature is gradually raised between 150 ° C and 230 ° C, in order to keep the conversion of the olefins in C5 constant. between 75% and 80%.
  • OLG2 second oligomerization step
  • the effluent of the third stage is separated by distillation into four sections:
  • the hydrogenation is carried out with a nickel catalyst at 180 ° C. under 50 bar of hydrogen with a VVH of 0.5 and a hydrogen flow rate of 50 NL / h and a feed rate of 48 g / h.
  • the catalysts used in the OLG1 and OLG2 steps and the capture mass used in the PUR step are the same as in Example 1.
  • the feedstock used is a C4 ex-catalytic cracking unit (FCC) feed to which a so-called light gasoline C5-C6 cut has been added from one FCC unit under the name LCN (Light Cut Naphtha).
  • FCC C4 ex-catalytic cracking unit
  • the pressure is maintained at 50 bars effective at room temperature.
  • the effluent from the first bed is sent integrally into the second bed carrying out the first oligomerization step (OLG1), in which the temperature gradually increases between 50 ° C and 110 ° C, in order to keep the conversion of the iso-olefins constant.
  • OLG1 first oligomerization step
  • C5 between 80% and 85%.
  • the effluent from the second bed is sent integrally into the third bed carrying out the second oligomerization step (OLG2), in which the temperature is gradually raised between 150 ° C and 230 ° C, in order to keep the conversion of the olefins in C5 constant. between 75% and 80%.
  • OLG2 second oligomerization step
  • the conversion of olefins to C4 is greater than 80%.
  • the effluent of the third stage is separated by distillation into four sections:

Landscapes

  • 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)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP12713203.3A 2011-05-12 2012-03-13 Verfahren zur erzeugung von diesel oder kerosin aus olefinischen beschickungen mit 4 bis 6 kohlenstoffatomen unter verwendung zweier oligomerisierungseinheiten Active EP2707462B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR1101444A FR2975103B1 (fr) 2011-05-12 2011-05-12 Procede de production de coupes kerosene ou gazole a partir d'une charge olefinique ayant majoritairement de 4 a 6 atomes de carbone
FR1102873A FR2975104B1 (fr) 2011-05-12 2011-09-19 Procede de production de coupes kerosene ou gazole a partir d'une charge olefinique ayant majoritairement de 4 a 6 atomes de carbone faisant appel a deux unites d'oligomerisation
PCT/FR2012/000087 WO2012153010A2 (fr) 2011-05-12 2012-03-13 Procédé de production de coupes kérosène ou gazole a partir d'une charge oléfinique ayant majoritairement de 4 a 6 atomes de carbone faisant appel a deux unités d'oligomérisation

Publications (2)

Publication Number Publication Date
EP2707462A2 true EP2707462A2 (de) 2014-03-19
EP2707462B1 EP2707462B1 (de) 2016-06-08

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Family Applications (2)

Application Number Title Priority Date Filing Date
EP12713204.1A Ceased EP2707461A2 (de) 2011-05-12 2012-03-13 Verfahren zur herstellung von diesel- oder kerosinschnitten aus einem olefinstrom mit hauptsächlich 4 bis 6 kohlenstoffatomen
EP12713203.3A Active EP2707462B1 (de) 2011-05-12 2012-03-13 Verfahren zur erzeugung von diesel oder kerosin aus olefinischen beschickungen mit 4 bis 6 kohlenstoffatomen unter verwendung zweier oligomerisierungseinheiten

Family Applications Before (1)

Application Number Title Priority Date Filing Date
EP12713204.1A Ceased EP2707461A2 (de) 2011-05-12 2012-03-13 Verfahren zur herstellung von diesel- oder kerosinschnitten aus einem olefinstrom mit hauptsächlich 4 bis 6 kohlenstoffatomen

Country Status (4)

Country Link
EP (2) EP2707461A2 (de)
FR (2) FR2975103B1 (de)
HU (1) HUE030396T2 (de)
WO (2) WO2012153011A2 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3134110A1 (fr) 2022-04-05 2023-10-06 Axens Procédé amélioré de production de distillats moyens par oligomérisation d’une charge oléfinique

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3002770B1 (fr) * 2013-03-04 2015-03-27 IFP Energies Nouvelles Procede de production de distillats moyens a partir d'une charge comprenant du butanol et du pentanol
WO2014154803A1 (en) * 2013-03-28 2014-10-02 Bp P.L.C. Production of middle distillate hydrocarbon composition

Family Cites Families (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2547830B1 (fr) * 1983-06-22 1988-04-08 Inst Francais Du Petrole Procede de production de supercarburant par polymerisation des coupes c4
JPH01259089A (ja) * 1988-03-04 1989-10-16 Res Assoc Util Of Light Oil 重質油熱分解軽質留分の処理方法
DE69012295T2 (de) * 1989-11-16 1995-01-05 Mobil Oil Corp Verfahren zur Qualitätserhöhung von Leichtolefinströmen.
EP0734766B1 (de) * 1995-03-29 2001-08-29 Koa Oil Company, Limited Katalysator für die Oligomerisation von Olefinen, Verfahren zur Herstellung desselben und seine Anwendung zur Oligomerisation von Olefinen
US6398946B1 (en) * 1999-12-22 2002-06-04 Chevron U.S.A., Inc. Process for making a lube base stock from a lower molecular weight feedstock
US20030136706A1 (en) * 2001-10-25 2003-07-24 Mcdaniel Stacey Sulfur removal process
FR2843969B1 (fr) 2002-09-04 2007-03-23 Inst Francais Du Petrole Procede de valorisation d'une charge d'hydrocarbures et de diminution de la tension de vapeur de ladite charge
FR2849051B1 (fr) * 2002-12-23 2005-02-04 Inst Francais Du Petrole Procede de transformation d'hydrocarbures en une fraction presentant un indice d'octane ameliore et une fraction a fort indice de cetane
FR2871167B1 (fr) * 2004-06-04 2006-08-04 Inst Francais Du Petrole Procede d'amelioration de coupes essences et de transformation en gazoles
FR2871168B1 (fr) 2004-06-04 2006-08-04 Inst Francais Du Petrole Procede d'amelioration de coupes essences et de transformation en gazoles avec traitement complementaire permettant d'augmenter le rendement de la coupe gazole
FR2873116B1 (fr) * 2004-07-15 2012-11-30 Inst Francais Du Petrole Procede d'oligomerisation des olefines utilisant un catalyseur a base de silice-alumine
US7473349B2 (en) * 2004-12-30 2009-01-06 Bp Corporation North America Inc. Process for removal of sulfur from components for blending of transportation fuels
FR2887555B1 (fr) 2005-06-28 2009-06-26 Inst Francais Du Petrole Procede de preparation d'une coupe diesel par oligomerisation
US7588738B2 (en) * 2005-08-23 2009-09-15 Exxonmobil Chemical Patents Inc. Series catalyst beds
EP1993980B1 (de) * 2006-03-10 2015-02-25 ExxonMobil Chemical Patents Inc. Verminderung der konzentration an stickstoffhaltigen lewis-basen bei der oligomerisierung mit molekularsieb
WO2011135206A1 (fr) 2010-04-28 2011-11-03 IFP Energies Nouvelles Procede d'oligomerisation des olefines utilisant au moins un catalyseur organique possedant une forte densite de sites acides

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2012153010A2 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3134110A1 (fr) 2022-04-05 2023-10-06 Axens Procédé amélioré de production de distillats moyens par oligomérisation d’une charge oléfinique
WO2023194337A1 (fr) 2022-04-05 2023-10-12 Axens Procédé amélioré de production de distillats moyens par oligomérisation d'une charge oléfinique

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Publication number Publication date
EP2707462B1 (de) 2016-06-08
WO2012153010A3 (fr) 2013-01-03
HUE030396T2 (hu) 2017-05-29
FR2975103B1 (fr) 2014-08-29
EP2707461A2 (de) 2014-03-19
FR2975103A1 (fr) 2012-11-16
WO2012153011A2 (fr) 2012-11-15
WO2012153010A2 (fr) 2012-11-15
WO2012153011A3 (fr) 2013-01-03
FR2975104A1 (fr) 2012-11-16
FR2975104B1 (fr) 2015-03-20

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