EP0980909A1 - Kohlenwasserstoff-Umwandlungsverfahren und seine Verwendung in der Hydrierung von Benzol - Google Patents

Kohlenwasserstoff-Umwandlungsverfahren und seine Verwendung in der Hydrierung von Benzol Download PDF

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Publication number
EP0980909A1
EP0980909A1 EP99402025A EP99402025A EP0980909A1 EP 0980909 A1 EP0980909 A1 EP 0980909A1 EP 99402025 A EP99402025 A EP 99402025A EP 99402025 A EP99402025 A EP 99402025A EP 0980909 A1 EP0980909 A1 EP 0980909A1
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Prior art keywords
zone
level
distillation
hydrogenation
effluent
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EP99402025A
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English (en)
French (fr)
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EP0980909B1 (de
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Jean-Louis Ambrosino
Jean-Charles Viltard
Blaise Didillon
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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons

Definitions

  • the invention relates to a process for converting hydrocarbons.
  • the process according to the invention combines a distillation zone with a reaction reaction zone of hydrocarbons at least partially external to the distillation zone in which one introduces an effluent comprising hydrogen. So this process allows you to convert selectively hydrocarbons separated from a hydrocarbon charge thanks to the distillation zone, in an associated reaction zone, with withdrawal from the zone distillation of the charge from the reaction zone and reintroduction of the charge converted in the distillation zone.
  • the method according to the invention applies to selective reduction the content of light unsaturated compounds (i.e. containing at most six atoms of carbon per molecule) comprising possible olefins and benzene, of a section of hydrocarbons having essentially at least 5 carbon atoms per molecule, without significant loss of the octane number.
  • light unsaturated compounds i.e. containing at most six atoms of carbon per molecule
  • benzene a section of hydrocarbons having essentially at least 5 carbon atoms per molecule
  • Benzene has carcinogenic properties and is therefore required to limit the maximum any possibility of polluting the ambient air, in particular by excluding it practically automotive fuels. In the United States reformulated fuels must not contain more than 1% by volume of benzene; in Europe it is recommended to gradually move towards this value.
  • Olefins have been recognized as among the most reactive hydrocarbons in the cycle of photochemical reactions with nitrogen oxides, which occurs in the atmosphere and which leads to the formation of ozone. An elevation of the concentration of ozone in the air can cause respiratory problems.
  • the benzene content of a gasoline is very largely dependent on that of the reformate component of this species.
  • the reformate results from a catalytic treatment naphtha for the production of aromatic hydrocarbons, comprising mainly from 6 to 9 carbon atoms in their molecule and whose index very high octane gives the essence its anti-knock properties.
  • the benzene in a reformate can be hydrogenated to cyclohexane.
  • a mixture of hydrocarbons also containing toluene and xylenes so it is necessary to fractionate beforehand this mixture so as to isolate a section containing only the benzene, which can then be hydrogenated.
  • Patent application WO 95/15 934 describes a reactive distillation which aims selectively hydrogenating diolefins and acetylenic compounds C2-C5.
  • the catalytic hydrogenation zone is completely internal to the distillation column, this which does not allow a good dissolution of the hydrogen in the charge nor of power increase the pressure.
  • the gaseous fraction containing the vaporized charge fraction and the gas stream containing hydrogen rises through said catalytic bed in gas columns.
  • the entropy of the system is strong and the loss of charge through the catalytic bed (s) is low. Therefore the way of operating according to this type of technology does not easily promote dissolution hydrogen in the liquid phase comprising the unsaturated compound (s).
  • the method according to the present invention is an improvement in the demand for Patent EP 0 781 830 A1 from the applicant, all of the characteristics of which are considered to be included in this description.
  • the invention relates to a method for converting a hydrocarbon feedstock. associating a distillation zone producing at the top a distillate and a bottom effluent, and a reaction zone at least partially external to the distillation zone. At at least one conversion reaction of at least part of at least one hydrocarbon takes place in a reaction zone comprising at least one catalytic bed, in presence of a catalyst and a gas stream comprising hydrogen.
  • Load of the reaction zone is taken at the height of at least one level of sample from the distillation zone and represents at least part of the liquid flowing into the distillation zone, and the effluent from the reaction zone is at least partly reintroduced into the distillation zone at least at a level of reintroduction, so as to ensure the continuity of the distillation.
  • the invention is characterized in that at least one from the distillation zone is withdrawn liquid effluent up to at least one racking level, at least part of said liquid effluent being at least partly treated in a separation zone lateral gas-liquid (splitter) whose gaseous effluent is at least partially reintroduced in the distillation zone and from which the liquid effluent is at least partly recovered as an intermediate cut.
  • a separation zone lateral gas-liquid (splitter) whose gaseous effluent is at least partially reintroduced in the distillation zone and from which the liquid effluent is at least partly recovered as an intermediate cut.
  • the process of the present invention makes it possible to recover at least one section of hydrocarbons at an intermediate level of the distillation zone, i.e. at a level between the bottom and the head of the distillation zone, with levels of sought-after products which can be adjusted as required, said cut being freed from most of the lighter compounds that are at least in part reintroduced into the distillation zone after separation in the lateral gas-liquid separation.
  • the method according to the invention makes it possible to separate products using the distillation area and specifically convert some compounds, under advantageous conditions of temperature and pressure, in order to recovering a distillate in which the conversion took place at the top of the distillation zone of the major part of the hydrocarbons to be converted and in order to recover at any point from the distillation zone at least one intermediate hydrocarbon fraction having the desired composition of hydrocarbons from the conversion reaction, hydrocarbons present in the charge of the distillation zone and others compounds introduced for the conversion reaction.
  • the process according to the invention applied to the hydrogenation of benzene is for example a process for treating a charge, consisting mainly of hydrocarbons containing at least 5, preferably between 5 and 9 carbon atoms per molecule, and comprising at least one unsaturated compound, comprising olefins benzene, as the said charge is treated in an area of distillation, associated with a hydrogenation reaction zone at least in part external, comprising at least one catalytic bed, in which the hydrogenation of at least part of the unsaturated compounds comprising at most six carbon atoms per molecule, i.e.
  • the method according to the invention makes it possible to withdraw an intermediate section containing for unsaturated compounds approximately the amount of benzene and light olefins desired.
  • the method according to the invention in one of its implementations, allows to directly recover a naphtha cut, i.e. a cut of light hydrocarbons, comprising mainly hydrocarbons having 5 11 carbon atoms per molecule, and reduced in benzene.
  • a naphtha cut i.e. a cut of light hydrocarbons, comprising mainly hydrocarbons having 5 11 carbon atoms per molecule, and reduced in benzene.
  • the most of the light hydrocarbons having up to 4 carbon atoms and at least part of the hydrocarbons with 5 carbon atoms per molecule.
  • the invention makes it possible to directly recover a cut usable, including approximately the amount of benzene required, and cleared of its lightest constituents, while avoiding the loss of these light constituents, by recycling of said compounds in the distillation zone.
  • the process according to the invention comprises the withdrawal of at least one liquid effluent from the distillation zone to at least one lateral gas-liquid separation zone from which comes a liquid intermediate cut and a gaseous effluent which is at least partly recycled to the distillation zone.
  • the liquid effluent to be separated can be withdrawn at at least one withdrawal level.
  • the drawdown level of the liquid effluent to be separated is generally located above the level of introduction of the charge from the distillation zone and can be any level between the level of introduction of the charge into the distillation zone and the distillation zone head level.
  • Said racking level can be located above or below the level of withdrawal of the charge from the reaction zone, above or below the level of reintroduction of effluent from the area reaction in the distillation zone.
  • the level of recycling of the gas fraction from the lateral separation zone is generally located above the level of introduction of the charge into the zone distillation.
  • Said recycling level is generally located above the level for drawing off the liquid distillate towards the lateral side separation zone.
  • Said recycling level can be located above or below the racking level of the reaction zone charge, above or below the level of reintroduction of the effluent from the reaction zone into the distillation zone.
  • the method according to the invention comprises a level of withdrawal of the liquid effluent to the lateral gas-liquid separation zone.
  • the process according to the invention comprises the recovery of a top distillate in which most of the conversion of hydrocarbons has been carried out using of the reaction zone associated with the distillation zone, said distillate therefore containing a minor part of the compounds to be converted in the reaction zone.
  • This distillate overhead can be recovered in the form of steam distillate, at least part of the steam distillate being condensed and then recycled in the distillation zone in order to ensure reflux.
  • the method comprises a stabilization zone.
  • a distillate is drawn from the distillation zone liquid stabilized at a withdrawal level located below the removal of the distillate from the head of the distillation zone. So the product you are looking for is recovered as stabilized liquid distillate, i.e. freed from most of it excess hydrogen and at least some of the light gases that are recovered in the steam distillate.
  • This recovery of the distinct liquid distillate allows eliminating by the gas distillate gases other than hydrogen present in the stream gaseous mainly comprising hydrogen introduced into the zone reaction to carry out the conversion reaction.
  • This preferred implementation makes it possible to recover several distillates: at least one stabilized distillate and at least one intermediate cut. Generally, the distillate stabilized is withdrawn at a level above the cup withdrawal level intermediate.
  • this preferred implementation in its particular application to the hydrogenation of benzene, makes it possible to recover directly by drawing off from the distillation zone a stabilized liquid distillate in which the selective hydrogenation of the benzene and any unsaturated compound comprising at most six carbon atoms per molecule and different from benzene, possibly present in the charge while limiting the hydrogenation of the C 7 + compounds (that is to say having at least seven atoms of carbon per molecule)
  • the stabilized liquid distillate contains essentially liquid compounds having at least 5 carbon atoms per molecule and usable directly as fuels.
  • the distillation zone generally comprises at least one column provided with at least minus one internal distillation chosen from the group formed by the trays, the bulk packings and structured packings, as is known to those skilled in the art profession, so that the total overall efficiency is at least equal to five floors theoretical.
  • the total overall efficiency is at least equal to five floors theoretical.
  • the charge of the distillation zone is introduced at at least one introduction level located below the level of withdrawal of the liquid towards the reaction zone, generally at a level of 2 to 40 theoretical platforms and preferably from 2 to 20 theoretical plates below the level of withdrawal of the liquid towards said zone reaction, said withdrawal level considered being the lowest.
  • the reaction zone generally comprises at least one catalytic bed, of preferably from 1 to 4 catalytic bed (s); if at least two beds are incorporated in the distillation zone, these two beds are optionally separated by at least one internal distillation.
  • the reaction zone is a zone hydrogenation.
  • the hydrogenation reaction zone performs at least partially the hydrogenation of the benzene present in the feed, generally of so that the benzene content of the stabilized liquid distillate drawn off below the level of extraction of the top distillate is at most equal to a certain content, and said reaction zone performs at least in part, preferably in major part, the hydrogenation of any unsaturated compound comprising at most six carbon atoms per molecule and different from benzene, possibly present in charge.
  • the reaction zone is at least partially external to the distillation zone.
  • the method according to the invention comprises from 1 to 6, preferably from 1 to 4 level (s) of sampling which feed (s) the external part of the zone.
  • the level of reintroduction of the converted charge at least partly in the zone external reaction is usually located substantially below, or substantially above, or substantially at the same height, at least one level of sampling, preferably of said level of sampling of the load of the zone distillation.
  • the reintroduction level is located above the levy level.
  • the reactor being at least partially external, a flow rate of liquid equal to, greater than or less than the liquid traffic of the distillation zone situated below the drawdown level of the load to be converted.
  • the flow rate of liquid withdrawn is preferably equal to or greater than the traffic liquid from the distillation zone located below the draw-off level.
  • the flow of liquid collected is preferably equal to or less than the liquid traffic in the area of distillation located below the racking level.
  • the method according to the invention makes it possible to convert a large part of (or) compound (s) to be converted outside the distillation zone possibly in pressure and / or temperature conditions different from those used in the distillation zone.
  • the process according to the invention is such that the flow of the liquid to be converted is generally co-current to the flow of the gas stream comprising hydrogen, for any catalytic bed in the external part of the reaction zone.
  • each bed catalytic is fed by a single level of sampling, preferably associated with a single level of reintroduction, said level of withdrawal being distinct from the level that feeds the other catalytic bed (s).
  • the charge at convert withdrawn from the distillation zone to the reaction zone is cooled before entering the reactor.
  • the converted charge leaving the reactor can be cooled before reintroduction into the distillation zone.
  • This cooling creates a circulating reflux.
  • one of the preferred embodiments of the invention is such that the level of reintroduction of the hydrogenated charge in the column is located above the level of withdrawal of the charge to be hydrogenated in an area where the Benzene content is the lowest. Even more preferably, the level of reintroduction is located at least 2 theoretical platforms above the level of even more preferably, the level of reintroduction of the load is located at least 4 theoretical platforms above the racking level of said charge.
  • the theoretical molar ratio of hydrogen necessary for the conversion desired benzene is 3.
  • the amount of hydrogen distributed before or in the hydrogenation zone is possibly in excess with respect to this stoichiometry, and this all the more that one must hydrogenate, in addition to the benzene present in the filler, at least partially any unsaturated compound comprising at most six atoms of carbon per molecule and present in said charge.
  • excess hydrogen if any, can be advantageously recovered for example according to one of the techniques described below.
  • the excess hydrogen which leaves the reaction zone is recovered either directly at the effluent level at the exit of the zone reaction, either in the gaseous distillate of the distillation zone, then compressed and reused in said reaction zone in order to create a reflux.
  • the excess hydrogen which leaves the reaction zone is recovered, then injected upstream of the compression stages associated with a reforming unit catalytic, mixed with hydrogen from said unit, said unit preferably operating at low pressure, i.e. generally pressure absolute less than 0.8 MPa.
  • Hydrogen included in the gas flow, used for example in the process particular of the invention for the hydrogenation of unsaturated compounds comprising at least plus six carbon atoms per molecule can come from all sources producing hydrogen at least 50% purity volume, preferably at least 80% volume of purity and even more preferably at least 90% volume of purity.
  • hydrogen from reforming processes. catalytic, methanation, P.S.A. (alternating pressure adsorption), electrochemical or steam cracking generation.
  • One of the preferred embodiments of the method according to the invention is such that the bottom effluent from the distillation is mixed at least in part with the stabilized liquid distillate recovered with a recovery level below the distillate recovery level steam.
  • the mixture thus obtained can be used as fuel either directly or by incorporation into fuel fractions.
  • the operating conditions of the part of the reaction zone internal to the zone of distillation are related to the operating conditions of the distillation.
  • Distillation is performed under absolute pressure generally between 0.1MPa and 2.5 MPa with a reflux rate of between 0.1 and 20.
  • the temperature of the distillation is between 10 and 300 ° C.
  • the liquid subjected to the conversion is mixed with a gas stream comprising hydrogen, the flow rate of which is at least equal to the stoichiometry of the conversion reactions carried out and at most equal to the flow corresponding to 10 times the stoichiometry.
  • the catalyst is placed in any catalytic bed following any technology known to those skilled in the art under operating conditions (temperature, pressure ...) independent or not, preferably independent, of operating conditions of the distillation zone.
  • operating conditions are usually the following.
  • the absolute pressure required is generally understood between 0.1 and 6 MPa.
  • the operating temperature is generally between 30 and 400 ° C.
  • the space velocity within said reaction zone, calculated with respect to with the catalyst, is generally between 0.5 and 60 h-1.
  • the flow of hydrogen corresponding to the stoichiometry of the conversion reactions carried out is understood between 1 and 10 times said stoichiometry.
  • the operating conditions are as follows.
  • the operating conditions of the part of the hydrogenation zone internal to the distillation zone are linked to the operating conditions of the distillation.
  • the distillation is carried out under an absolute pressure generally between 0.2 and 2 MPa, preferably between 0.4 and 1 MPa, with a reflux rate between 0.1 and 10, and preferably between 0.2 and 2.
  • the zone head temperature is generally between 30 and 180 ° C and the zone bottom temperature is generally between 120 and 280 ° C.
  • the hydrogenation reaction is carried out under conditions which are most generally intermediate between those established at the head and at the bottom of the distillation zone, at a temperature between 100 and 200 ° C., and preferably between 120 and 180 ° C. , and at an absolute pressure of between 0.2 and 3 MPa, preferably between 0.4 and 2 MPa.
  • the liquid subjected to hydrogenation is mixed with a gas stream comprising hydrogen, the flow rate of which depends on the concentration of benzene in said liquid and, more generally, unsaturated compounds containing at most six carbon atoms per molecule of the charge. from the distillation zone.
  • the hydrogen flow rate is generally at least equal to the flow rate corresponding to the stoichiometry of the hydrogenation reactions carried out (hydrogenation of benzene and of the other unsaturated compounds containing at most six carbon atoms per molecule, included in the hydrogenation charge) and at most equal to the flow rate corresponding to 10 times the stoichiometry, preferably between 1 and 6 times the stoichiometry, even more preferably between 1 and 3 times the stoichiometry.
  • the absolute pressure required for this hydrogenation step is generally between 0.1 and 6 MPa absolute, preferably between 0.2 and 5 MPa and even more preferably between 0.5 and 3.5 MPa.
  • the temperature of the hydrogenation zone is generally between 100 and 400 ° C, preferably between 120 and 350 ° C and preferably between 140 and 320 ° C.
  • the space velocity within said hydrogenation zone, calculated with respect to the catalyst, is generally between 1 and 60 and more particularly between 1 and 40 h -1 (volume flow rate of charge per volume of catalyst).
  • the hydrogen flow rate corresponding to the stoichiometry of the hydrogenation reactions carried out is between 1 and 10 times said stoichiometry, preferably between 1 and 6 times said stoichiometry and even more preferably between 1 and 3 times said stoichiometry.
  • the temperature and pressure conditions can also, within the scope of the process of the present invention, be between those which are established at the top and at the bottom of the distillation zone.
  • the rate of reflux means the ratio of the flow mass of the reflux on the mass flow rate of the column.
  • the catalyst used in the area hydrogenation generally comprises at least one metal chosen from the group VIII, preferably chosen from the group formed by nickel and platinum, used as such which or preferably deposited on a support.
  • the metal should generally be found in reduced form at least for 50% by weight of its totality. But any other hydrogenation catalyst known to those skilled in the art can also be chosen.
  • the proportion of nickel relative to the total weight of catalyst is between 5 and 70%, more particularly between 10 and 70% and preferably between 15 and 65%.
  • a catalyst is generally used such that the average size of the nickel crystallites is less than 100.10 -10 m, preferably less than 80.10 -10 m, even more preferably less than 60.10 -10 m.
  • the support is generally chosen from the group formed by alumina, silica-aluminas, silica, zeolites, activated carbon, clays, aluminous cements, rare earth oxides and alkaline earth oxides, alone or in mixture.
  • a support based on alumina or silica is preferably used, with a specific surface area of between 30 and 300 m 2 / g, preferably between 90 and 260 m 2 / g.
  • Figure 1 is an illustration of a possibility of carrying out the method according to the invention.
  • the hydrocarbon charge is sent to column 2 by line 1.
  • Said column contains internal distillation, which is for example in the case represented in FIG. 1 of the plates or of the lining, represented in part by dotted lines in said figure.
  • the least volatile fraction of the reformate is recovered by the line 5, a part is reboiled in the exchanger 6 and a part is evacuated via line 7.
  • Reboiling steam is reintroduced into the column by line 8.
  • the distillate stabilized liquid is extracted by line 18, the steam distillate is sent by line 9 in a condenser 10 then in a flask 11 from which the steam distillate is extracted by the line 14.
  • the liquid phase of the balloon 11 is partially returned via line 12, in column head to reflux, and another part of the liquid phase can be picked up by line 13.
  • the liquid effluent to be separated is withdrawn from the distillation zone by line 19, then sent to a gas-liquid side separation zone (20), from which it is recycled the gaseous effluent in the distillation zone via line 21 and a section is recovered intermediate through line 23, part of the section is rewashed in the exchanger 22.
  • the process has a configuration with withdrawal of a liquid effluent to a lateral gas-liquid separation zone, with reintroduction of the gaseous effluent into the distillation and recovery zone of the liquid effluent as an intermediate cut.
  • the unit is shown in Figure 1.
  • the process has a configuration with withdrawal of a liquid effluent stabilized in below the racking of a steam distillate and with a level of reintroduction of the hydrogenated charge 9 trays above the racking tray.
  • the column includes 57 theoretical plates (including condenser and reboiler) and has a diameter of 3.35 m.
  • the associated side column has 7 theoretical plates (including the reboiler).
  • the reflux rate relative to food is 1.02.
  • the reboiling power is 12800 kW.
  • the power of the side column reboiler is 271 kW.
  • the process is carried out with an external hydrogenation reactor containing 7 m 3 of catalyst and operating at an absolute pressure of 1.5 MPa.
  • the nickel catalyst is sold by the company PROCATALYSE under the reference LD746.
  • the stabilized liquid effluent is recovered (light reformate) at plate 3 via line 18 and the steam distillate at the top of the column via line 14.
  • the charge for the column is injected by line 1 into plate 37.
  • the charge for reactor 3 is withdrawn from tray 30 via line 15.
  • Hydrogen is introduced via line 4 before entering the reactor operating in downflow and at 1.5 MPa pressure absolute.
  • the hydrogen / benzene molar ratio is 2.63.
  • the effluent from reactor 3 is cooled and then re-injected into the column via line 17 on plate 21.
  • the pressure absolute at the reflux flask is 0.75 MPa.
  • the method according to the present invention where there is withdrawal of a liquid distillate treated in a lateral separation zone makes it possible to recover a directly usable intermediate cut.
  • the cut intermediate is a naphtha cut comprising approximately 3.8% by volume of benzene.
  • the light reformate (18) contains 0.35% by volume of benzene
  • the heavy reformate (7) contains 0.6% volume of benzene.
  • the REID vapor pressure of naphtha is 0.086 MPa
  • that of the mixture constituted by the light reformate and the heavy reformate is 0.022 MPa.

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
EP99402025A 1998-08-17 1999-08-10 Kohlenwasserstoff-Umwandlungsverfahren und seine Verwendung in der Hydrierung von Benzol Expired - Lifetime EP0980909B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9810497A FR2782322B1 (fr) 1998-08-17 1998-08-17 Procede de conversion d'hydrocarbures par traitement dans une zone de distillation comprenant le soutirage lateral d'une coupe d'hydrocarbures, associee a une zone reactionnelle et son utilisation en hydrogenation du benzene
FR9810497 1998-08-17

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EP0980909A1 true EP0980909A1 (de) 2000-02-23
EP0980909B1 EP0980909B1 (de) 2004-05-06

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US (1) US6365791B1 (de)
EP (1) EP0980909B1 (de)
JP (1) JP4491757B2 (de)
AT (1) ATE266078T1 (de)
AU (1) AU759782B2 (de)
DE (1) DE69916943T2 (de)
ES (1) ES2221332T3 (de)
FR (1) FR2782322B1 (de)

Cited By (1)

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WO2010007244A2 (fr) 2008-07-18 2010-01-21 Ifp Procede d'hydrogenation du benzene

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US20080116053A1 (en) * 2006-11-20 2008-05-22 Abb Lummus Global Inc. Non-refluxing reactor stripper
EP2277980B1 (de) * 2009-07-21 2018-08-08 IFP Energies nouvelles Verfahren zur selektiven reduzierung des benzolgehalts und des gehalts an leichten ungesättigten verbindungen von verschiedenen kohlenwasserstoffverschnitten
FR2948380B1 (fr) * 2009-07-21 2011-08-12 Inst Francais Du Petrole Procede de reduction selective de la teneur en benzene et en composes insatures legers de differentes coupes hydrocarbures
CA2825115C (en) * 2011-01-19 2018-02-20 Limited Company "Reactive Rectification Technology" Naphtha isomerisation on three catalytic reaction zones inside a distillation column

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EP0781830A1 (de) * 1995-12-27 1997-07-02 Institut Francais Du Petrole Verfahren zur Erniedrigung des Gehaltes von Benzol und von leichten ungesättigten Verbindungen in Kohlenwasserstofffraktionen

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EP0781830A1 (de) * 1995-12-27 1997-07-02 Institut Francais Du Petrole Verfahren zur Erniedrigung des Gehaltes von Benzol und von leichten ungesättigten Verbindungen in Kohlenwasserstofffraktionen

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Publication number Priority date Publication date Assignee Title
WO2010007244A2 (fr) 2008-07-18 2010-01-21 Ifp Procede d'hydrogenation du benzene
FR2933987A1 (fr) * 2008-07-18 2010-01-22 Inst Francais Du Petrole Procede d'hydrogenation du benzene
WO2010007244A3 (fr) * 2008-07-18 2010-03-11 Ifp Procede d'hydrogenation du benzene

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ATE266078T1 (de) 2004-05-15
FR2782322A1 (fr) 2000-02-18
FR2782322B1 (fr) 2000-10-06
DE69916943D1 (de) 2004-06-09
AU4449599A (en) 2000-03-09
EP0980909B1 (de) 2004-05-06
US6365791B1 (en) 2002-04-02
JP4491757B2 (ja) 2010-06-30
JP2000063294A (ja) 2000-02-29
DE69916943T2 (de) 2004-09-02
ES2221332T3 (es) 2004-12-16
AU759782B2 (en) 2003-05-01

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