EP1602637A1 - Verfahren zur Verbesserung von Benzinschnitten und zur Umwandlung zu Gasölen - Google Patents

Verfahren zur Verbesserung von Benzinschnitten und zur Umwandlung zu Gasölen Download PDF

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Publication number
EP1602637A1
EP1602637A1 EP05291116A EP05291116A EP1602637A1 EP 1602637 A1 EP1602637 A1 EP 1602637A1 EP 05291116 A EP05291116 A EP 05291116A EP 05291116 A EP05291116 A EP 05291116A EP 1602637 A1 EP1602637 A1 EP 1602637A1
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EP
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Prior art keywords
cut
olefins
membrane
process according
separation
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EP05291116A
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English (en)
French (fr)
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EP1602637B8 (de
EP1602637B1 (de
Inventor
Patrick Briot
Arnaud Baudot
Vincent Coupard
Alain Methivier
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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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
    • 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
    • C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
    • C10G31/10—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force

Definitions

  • the present invention relates to a method allowing a simple and economical way of modulate the respective productions of gasoline and diesel. More precisely, according to the method object of the present application, it is possible to transform an initial charge of hydrocarbons comprising from 4 to 15 carbon atoms, and preferably from 4 to 11 atoms of carbon, in a gasoline fraction of improved octane number with respect to that of the charge, and a gas oil fraction with a high cetane number.
  • the purpose of the present invention is, from a gasoline cut having from 4 to 15 carbon atoms carbon, and preferably from 4 to 11 carbon atoms to produce a gasoline cut at improved octane number compared to that of the starting cut, and a diesel cut of index cetane at least equal to 35, and preferably greater than 45.
  • the effluents resulting from the processes of conversion of residues more or less atmospheric or vacuum distillation of crude oil such as, for example, species from the fluidized catalytic cracking (FCC) process have a olefins generally between 10 and 80%.
  • One of the objects of the present invention is to separate olefins from an initial gasoline feedstock.
  • linear branched olefins are preferred.
  • Another object of the present invention is to provide a solution allowing flexibility increased management of products from the refinery.
  • the use of the present process can advantageously modulate the gasoline / diesel proportions obtained at the refinery outlet according to the needs of the walk.
  • the isobutane addition processes of alkenes having between 2 and 5 carbon atoms make it possible to produce highly branched molecules having between 7 and 9 carbon atoms, and generally characterized by high octane numbers.
  • the oligomerization processes based essentially on the dimerization and trimerization of light olefins generally from the cracking process catalytic, and having between 2 and 4 carbon atoms, allow the production of slices essences or distillates.
  • US Pat. No. 5,382,705 proposes to couple the previously described oligomerization and etherification processes in order to produce, from a C 4 fraction, tertiary alkyl ethers such as MTBE or ETBE and lubricants.
  • the light cut ⁇ resulting from the separation step by distillation and comprising the majority of linear paraffins and a part of olefins linear is at least partially recycled to the input of the oligomerization unit.
  • the light cut ⁇ resulting from the separation step by distillation and comprising the majority of linear paraffins and a part of olefins linear is at least partly mixed with the effluent from the membrane separation unit containing the majority of branched olefins.
  • the oligomerization step is generally carried out in the presence of a catalyst comprising at least one Group VIB metal from the Periodic Table.
  • the step of separating linear olefins and paraffins on the one hand, and olefins and branched paraffins on the other hand, is carried out in a so-called membrane separation unit which may use a wide variety of membrane types, the invention being in no way connected with a particular type of membrane.
  • membranes that may be used in the context of the invention are preferentially membranes used in nanofiltration and reverse osmosis (membranes falling within the membrane category for filtration process) or membranes used in permeation in the gas phase or in pervaporation (membrane falling within the category of membranes for permeation or pervaporation processes).
  • these membranes could be either membranes of the type zeolitic, either membranes of polymeric (or organic) type, or membranes of ceramic (or mineral) type, or of composite type in the sense that they can be consisting of a polymer and at least one mineral compound.
  • the membranes that can be used in the process that is the subject of the invention may also be based on of movie.
  • film-based membranes may be mentioned. formed of molecular sieve or membrane-based film formed from molecular sieve of silicates, aluminosilicates, aluminophosphates, silicoaluminophosphates, metalloaluminophosphates, stanosilicates, or a mixture of at least one of these two types of components.
  • zeolite-based membranes With regard to zeolite-based membranes, mention may be made more particularly of Membranes based on zeolites of type MFI or ZSM-5, native or having been exchanged with H + ions; Na +; K +; Cs +; Ca +; Ba + and membranes based on zeolites type LTA.
  • the method according to the invention may comprise a removal step of less a part of the nitrogenous or basic impurities contained in the initial charge of hydrocarbons, said purification step being situated upstream of the separation step by membrane.
  • the initial charge of hydrocarbon will be from a cracking process catalytic, thermal cracking or dehydrogenation of paraffins. It can be treated separately or mixed with other loads while respecting the fact that the resulting mixture will have a number of carbon atoms always between 4 and 15 atoms carbon, and preferably between 4 and 11 carbon atoms.
  • An example of a filler that can be mixed with the feedstock is the gasoline cut of direct distillation of the end-point crude generally close to 200 ° C.
  • FIG. 1 corresponds to the diagram of FIG. process according to the invention.
  • FIG. 1 represents a diagram of the method according to the invention comprising a unit of purification of the charge A, which is optional, a membrane separation unit B, a oligomerization unit C, a separation unit by distillation or flash D and a unit Hydrogenation E.
  • the hydrocarbon feedstock is conveyed by line 1 to a unit A of purification.
  • This unit A makes it possible to eliminate a large part of the nitrogenous and / or basic compounds contained in the load. This elimination, although optional, is necessary when the Hydrocarbon feedstock comprises a high level of nitrogen and / or basic compounds, as these constitute a poison for the catalysts of the following steps of the present process.
  • Said compounds can be removed by adsorption on an acidic solid.
  • This solid can be selected from the group consisting of silicoaluminates, titanosilicates, mixed oxides titanium alumina, clays, resins.
  • the solid may also be chosen from mixed oxides obtained by grafting at least an organometallic compound, organosoluble or water-soluble, of at least one selected element in the group formed by titanium, zirconium, silicon, germanium, tin, tantalum, niobium, on at least one oxide support such as alumina (gamma, delta, eta forms, only or in a mixture) silica, silica aluminas, titanium silicas, zirconia silicas, resins ion exchange type Amberlyst, or any other solid having any acidity.
  • organometallic compound organosoluble or water-soluble
  • oxide support such as alumina (gamma, delta, eta forms, only or in a mixture) silica, silica aluminas, titanium silicas, zirconia silicas, resins i
  • a particular embodiment of the invention may consist in implementing a mixture at least two of the previously described catalysts.
  • the pressure of the charge purification unit is between the pressure atmospheric pressure and 10 MPa, preferably between atmospheric pressure and 5 MPa, and will preferably choose a pressure under which the charge is in the liquid state.
  • VVH The ratio of the volume flow rate of charge to the volume of catalytic solid
  • the temperature of the purification unit is between 15 ° C and 300 ° C, preferably between 15 ° C and 150 ° C, and very preferably between 15 ° C and 60 ° C.
  • the elimination of the nitrogenous and / or basic compounds contained in the feed may also be carried out by washing with an acidic aqueous solution, or by any other known equivalent means of the man of the art.
  • the purified ⁇ -cut feed is conveyed via line 2 to separation unit B on membrane.
  • separation unit B the olefins and linear paraffins forming the ⁇ -section are separated on a membrane from the rest of the petrol cut and are evacuated via line 3 for feed an oligomerization unit C.
  • the membrane separation step performed on the unit B can implement any type of membrane such as those used in nanofiltration or reverse osmosis processes, or else in the gas phase permeation or pervaporation processes.
  • any type of membrane making it possible to effect the separation between paraffins and linear olefins and branched paraffins and olefins can be used, whether either organic or polymeric membranes (for example, the PDMS 1060 membrane of Sulzer Chemtech Membrane Systems), ceramics or minerals (for example less partly zeolite, silica, alumina, glass or carbon), or composites consisting of polymer and at least one mineral or ceramic compound (for example, the PDMS membrane 1070 of Sulzer Chemtech Membrane Systems).
  • organic or polymeric membranes for example, the PDMS 1060 membrane of Sulzer Chemtech Membrane Systems
  • ceramics or minerals for example less partly zeolite, silica, alumina, glass or carbon
  • composites consisting of polymer and at least one mineral or ceramic compound for example, the PDMS membrane 1070 of Sulzer Chemtech Membrane Systems.
  • membranes based on MFI zeolites be they membranes based on silicalite, based on MFI zeolite completely dealuminated, have a selectivity normal / isoparaffins and can therefore be used in the context of the present invention.
  • the selectivity of this type of membrane is essentially based on a difference in diffusivity between linear compounds, diffusing faster because offering a diameter significantly lower kinetics than the micropore diameter of the zeolite, and the connected compounds, diffusing more slowly because having a kinetic diameter close to that micropores.
  • the operating temperature of the membrane will be between the temperature ambient temperature and 400 ° C, and preferably between 80 ° C and 300 ° C.
  • the olefins and linear paraffins ( ⁇ -section) separated from the petrol fraction in unit B, are sent to an oligomerization reactor, represented by unit C, by means of line 3.
  • This unit C contains an acid catalyst.
  • the hydrocarbons present in the mixture of paraffins and linear olefins undergo moderate oligomerization reactions; in general, dimerizations or trimerizations, the conditions of the reaction being optimized for the production of a majority of hydrocarbons whose carbon number is between 9 and 25, and preferably between 10 and 20.
  • the catalyst of unit C can be chosen from the group formed by silicoaluminates, titanosilicates, mixed titanium alumina, clays, resins, mixed oxides obtained by grafting of at least one organometallic, organosoluble or water-soluble compound (chosen in the group consisting of alkyl-metals and / or alkoxy-metals having at least one element such as titanium, zirconium silicon, germanium, tin, tantalum, niobium) on a oxide support such as alumina (gamma, delta, eta, alone or in combination), silica, alumina silicas, titanium silicas, zirconia silicas, or any other solid having a any acidity.
  • organometallic, organosoluble or water-soluble compound chosen in the group consisting of alkyl-metals and / or alkoxy-metals having at least one element such as titanium, zirconium silicon, germanium, tin, tantalum, niobi
  • the catalyst used to carry out the oligomerization comprises at least one group VIB metal of the periodic table, and advantageously an oxide of said metal.
  • Said catalyst may further comprise an oxide support selected from the group formed by aluminas, titanates, silicas, zirconia, alumino-silicates.
  • a particular embodiment of the invention consists in implementing a mixture of at least two of the catalysts mentioned above.
  • the pressure of the unit C is most often such that the charge is in liquid form.
  • This pressure is in principle between 0.2 MPa and 10 MPa, preferably between 0.3 MPa and 6 MPa, and more preferably between 0.3 MPa and 4 MPa.
  • the ratio of the volume flow rate of charge to the volume of catalyst (also called the speed hourly volume or VVH) may be between 0.05 liter / liter.hour and 50 liters /litre.ffle, preferably between 0.1 liter / liter.hour and 20 liters / liter.hour, and still preferred between 0.2 liter / liter.hour and 10 liters / liter.hour.
  • reaction temperature should have been between 15 ° C and 300 ° C, preferably between 60 ° C and 250 ° C, and more particularly between 100 ° C and 250 ° C to optimize product quality finally obtained.
  • the heavy cut ⁇ is a section whose initial point corresponds to a diesel cut.
  • This cut can be hydrogenated in a conventional hydrogenation unit E in the presence of a catalyst and under operating conditions well known to those skilled in the art.
  • the effluent of unit E constitutes a diesel with a cetane number greater than 35, and preferably higher at 45.
  • Example 1 is according to the invention and will be better understood by following the diagram of FIG.
  • Example 2 is a comparative example.
  • Examples 1 and 2 have units A, C, D and E in common. The only difference is that Example 2 does not include the membrane separation unit B.
  • Example 1 (according to the invention):
  • the feedstock is a FCC gasoline with a boiling point between 40 ° C and 150 ° C.
  • This gasoline contains 10 ppm nitrogen.
  • This charge is sent to a purification reactor A containing a solid consisting of a mixture of 20% alumina and 80% by weight of zeolite Mordenite type.
  • the zeolite used in the present example has a silicon / aluminum ratio of 45.
  • the pressure of the purification unit is 0.2 MPa.
  • the ratio of the volume flow rate of the charge to the volume of acid solid (VVH) is 1 liter / litre.will.
  • the temperature of the reactor is 20 ° C.
  • Table 1 gives the composition of the initial charge and that of the effluent from unit A.
  • the charge rate is 1 kg / h.
  • Characteristics of the effluents of unit B Charge of unit A Effluent of unit A (cut ⁇ ) Nitrogen (ppm) 10 0.2 Paraffins (% wt) 25.2 25.1 Naphthenes (% wt) 9.6 9.8 Aromatic (% by weight) 34.9 35 Olefins (% by weight) 30.3 30.1
  • the effluent from unit A is then sent to a membrane reactor B, the membrane being consisting of an ⁇ -alumina support on which is deposited a layer of MFI zeolite with a thickness of between 5 and 15 ⁇ m.
  • the pressure of the membrane reactor is equal to 1 bar (0.1 MPa) and the temperature to 150 ° C.
  • Table 2 gives the composition of effluents from unit B ( ⁇ -section, ⁇ ). characteristics of effluents from unit B.
  • the ⁇ cut resulting from the membrane separation unit B is introduced into an oligomerization reactor C containing a catalyst consisting of a mixture of 50% by weight of zirconia and 50% by weight of H 3 PW 12 O 40 .
  • the pressure of the oligomerization unit C is 2 MPa, the ratio of the volume flow rate of load on the catalyst volume is equal to 1.5 liters / liter.hour.
  • the temperature is set to 170 ° C.
  • the heavy cut ⁇ is sent to a hydrogenation reactor E containing a catalyst comprising an alumina support on which nickel and molybdenum are deposited (marketed by AXENS under the trade name HR 348, registered trademark).
  • the pressure of the unit is 5 MPa.
  • the ratio of the volume flow rate of the charge on the volume of catalyst is equal to 2 liters /litre.will.
  • the ratio of the volume flow rate of hydrogen injected on the volume flow rate of charge is equal to 600 liters / liter.
  • the reactor temperature is 320 ° C.
  • the characteristics of the effluent from step E are shown in Table 4. characteristics of effluent from unit E Effluent of unit E Density at 20 ° C (kg / l) 0.787 Sulfur (ppm) 1 Cetane engine 55
  • the light fraction ⁇ of the 40 ° C-200 ° C distillation range from unit D is mixed with the ⁇ cut obtained from unit B.
  • the properties of the mixture of ⁇ and ⁇ sections are shown in the table. 5 and compared to those of the initial cut ⁇ . Comparison of the characteristics of the initial cut ⁇ and the final cut ⁇ + ⁇ ⁇ cut Cups ⁇ + ⁇ Production (g / l) 1000 951.6 Paraffins (% wt) 25.2 26.2 Naphthenes (% wt) 9.6 10 Aromatic (% by weight) 34.9 36.2 Olefins (% by weight) 30.3 26.5 RON octane number 92 96
  • the present method provides a gasoline cut from an FCC unit a gasoline cut ( ⁇ + ⁇ cut) with an improved octane number compared to the cut initial (96 against 92) and a diesel cut, effluent of the unit E, with high cetane number (55), compatible with marketing to European and US specifications.
  • This example corresponds to the prior art and consists of sending directly to a unit of oligomerization a gasoline cut after purification, without prior separation of olefins linear and branched.
  • the effluents resulting from the oligomerization are separated into a light section and a heavy cut, denoted respectively ⁇ 'and ⁇ '.
  • step A is a charge purification step identical to that of Example 1 according to the invention.
  • the effluent from step A is sent to step C oligomerization without going through step B membrane separation, that is to say without separate linear and branched olefins.
  • the catalyst used and the operating conditions of Step C are identical to those of Example 1 according to the invention.
  • the heavy cut ⁇ ' is sent to a hydrogenation reactor E containing a catalyst Alumina base on which nickel and molybdenum are deposited.
  • the pressure of the unit of step E is 5 MPa, the ratio of the charge flow rate on the volume of catalyst is equal to 2 liters / liter.hour.
  • the ratio of the injected hydrogen flow rate to the feed rate is equal to 600 liters / liter.
  • the reactor temperature is 320 ° C.
  • the final gasoline fraction ⁇ ' has an octane number lower than that obtained in Example 1 according to the invention, which can make marketing problematic.

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP05291116A 2004-06-04 2005-05-24 Verfahren zur Verbesserung von Benzinschnitten und zur Umwandlung zu Gasölen Not-in-force EP1602637B8 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0406096A FR2871167B1 (fr) 2004-06-04 2004-06-04 Procede d'amelioration de coupes essences et de transformation en gazoles
FR0406096 2004-06-04

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EP1602637A1 true EP1602637A1 (de) 2005-12-07
EP1602637B1 EP1602637B1 (de) 2008-11-19
EP1602637B8 EP1602637B8 (de) 2009-06-03

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US (1) US7847141B2 (de)
EP (1) EP1602637B8 (de)
JP (1) JP2005344118A (de)
CN (1) CN1724617A (de)
DE (1) DE602005011070D1 (de)
FR (1) FR2871167B1 (de)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007050446A3 (en) * 2005-10-24 2008-05-22 Shell Int Research Methods of filtering a liquid stream produced from an in situ heat treatment process
FR2975103A1 (fr) * 2011-05-12 2012-11-16 IFP Energies Nouvelles Procede de production de coupes kerosene ou gazole a partir d'une charge olefinique ayant majoritairement de 4 a 6 atomes de carbone
FR3134110A1 (fr) 2022-04-05 2023-10-06 Axens Procédé amélioré de production de distillats moyens par oligomérisation d’une charge oléfinique

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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
AU2006223412A1 (en) * 2005-03-11 2006-09-21 Uop Llc High flux, microporous, sieving membranes and separators containing such membranes and processes using such membranes
US7846322B2 (en) * 2005-03-11 2010-12-07 Uop Llc Integrated refinery with enhanced olefin and reformate production
US7638676B2 (en) * 2007-09-07 2009-12-29 Uop Llc Processes for the isomerization of feedstocks comprising paraffins of 5 to 7 carbon atoms
US7638674B2 (en) * 2007-09-07 2009-12-29 Uop Llc Processes for the isomerization of paraffins of 5 and 6 carbon atoms with methylcyclopentane recovery
US7812207B2 (en) * 2007-09-07 2010-10-12 Uop Llc Membrane separation processes and systems for enhanced permeant recovery
US7638675B2 (en) * 2007-09-07 2009-12-29 Uop Llc Processes for the isomerization of normal butane to isobutane
CN102051223B (zh) * 2009-10-27 2013-08-28 中国石油化工股份有限公司 一种催化裂化汽油加氢工艺方法
FR2980195B1 (fr) 2011-09-20 2013-08-23 IFP Energies Nouvelles Procede de separation du pentene-2 d'une coupe c5 contenant du pentene-2 et du pentene-1 par oligomerisation selective du pentene-1
FR2984916B1 (fr) * 2011-12-23 2014-01-17 IFP Energies Nouvelles Procede ameliore de conversion d'une charge lourde en distillat moyen faisant appel a un pretraitement en amont de l'unite de craquage catalytique
WO2014074833A1 (en) 2012-11-12 2014-05-15 Uop Llc Process for making gasoline by oligomerization
US9434891B2 (en) 2012-11-12 2016-09-06 Uop Llc Apparatus for recovering oligomerate
US10508064B2 (en) 2012-11-12 2019-12-17 Uop Llc Process for oligomerizing gasoline without further upgrading
US9567267B2 (en) 2012-11-12 2017-02-14 Uop Llc Process for oligomerizing light olefins including pentenes
US9914673B2 (en) 2012-11-12 2018-03-13 Uop Llc Process for oligomerizing light olefins
US9522373B2 (en) 2012-11-12 2016-12-20 Uop Llc Apparatus for oligomerizing light olefins
US9663415B2 (en) 2012-11-12 2017-05-30 Uop Llc Process for making diesel by oligomerization of gasoline
US9834492B2 (en) 2012-11-12 2017-12-05 Uop Llc Process for fluid catalytic cracking oligomerate
US9644159B2 (en) 2012-11-12 2017-05-09 Uop Llc Composition of oligomerate
US9441173B2 (en) 2012-11-12 2016-09-13 Uop Llc Process for making diesel by oligomerization
US9522375B2 (en) 2012-11-12 2016-12-20 Uop Llc Apparatus for fluid catalytic cracking oligomerate
CA2984052A1 (en) 2016-10-27 2018-04-27 Fccl Partnership Process and system to separate diluent
KR102521452B1 (ko) * 2017-12-20 2023-04-13 주식회사 엘지화학 파라핀 혼합물 및 이의 제조 방법
KR102521448B1 (ko) * 2017-12-20 2023-04-13 주식회사 엘지화학 파라핀 혼합물 및 이의 제조 방법
FR3089518B1 (fr) 2018-12-10 2020-11-20 Ifp Energies Now Procede ameliore de conversion d’une charge lourde en distillats moyens faisant appel a un enchainement d’unites d’hydrocraquage, de vapocraquage et d’oligomerisation
FR3089519B1 (fr) 2018-12-10 2020-11-20 Ifp Energies Now Procédé amélioré de conversion d’une charge lourde en distillats moyens faisant appel à un enchainement d’unités d’hydrocraquage, de craquage catalytique de naphta et d’oligomérisation

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US20030171632A1 (en) * 2000-07-10 2003-09-11 Du Toit Francois Benjamin Process and apparatus for the production of diesel fuels by oligomerisation of olefinic feed streams
US20040033370A1 (en) * 2002-06-03 2004-02-19 Institut Francais Du Petrole Thin zeolite membrane, its preparation and its use in separation

Cited By (7)

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Publication number Priority date Publication date Assignee Title
WO2007050446A3 (en) * 2005-10-24 2008-05-22 Shell Int Research Methods of filtering a liquid stream produced from an in situ heat treatment process
EA012941B1 (ru) * 2005-10-24 2010-02-26 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Способ фильтрации жидкого потока, полученного способом термической переработки in situ
FR2975103A1 (fr) * 2011-05-12 2012-11-16 IFP Energies Nouvelles Procede de production de coupes kerosene ou gazole a partir d'une charge olefinique ayant majoritairement de 4 a 6 atomes de carbone
WO2012153011A3 (fr) * 2011-05-12 2013-01-03 IFP Energies Nouvelles Procede de production de coupes kerosene ou gazole a partir d'une charge olefinique ayant majoritairement de 4 a 6 atomes de carbone
WO2012153010A3 (fr) * 2011-05-12 2013-01-03 IFP Energies Nouvelles Procédé production de coupes kérosène ou gazole a partir d'un charge oléfinique ayant majoritairement de 4 a 6 atomes de carbone faisant appel a deux unités d'oligomérisation
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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US7847141B2 (en) 2010-12-07
FR2871167B1 (fr) 2006-08-04
CN1724617A (zh) 2006-01-25
EP1602637B8 (de) 2009-06-03
EP1602637B1 (de) 2008-11-19
DE602005011070D1 (de) 2009-01-02
US20050283037A1 (en) 2005-12-22
JP2005344118A (ja) 2005-12-15
FR2871167A1 (fr) 2005-12-09

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