EP0949316B1 - Procédé de conversion d'hydrocarbures par traitement dans une zone de distillation associée à une zone réactionnelle et son utilisation en hydrogénation du benzène - Google Patents

Procédé de conversion d'hydrocarbures par traitement dans une zone de distillation associée à une zone réactionnelle et son utilisation en hydrogénation du benzène Download PDF

Info

Publication number
EP0949316B1
EP0949316B1 EP99400740A EP99400740A EP0949316B1 EP 0949316 B1 EP0949316 B1 EP 0949316B1 EP 99400740 A EP99400740 A EP 99400740A EP 99400740 A EP99400740 A EP 99400740A EP 0949316 B1 EP0949316 B1 EP 0949316B1
Authority
EP
European Patent Office
Prior art keywords
zone
level
distillation
hydrogenation
range
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.)
Expired - Lifetime
Application number
EP99400740A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0949316A1 (fr
Inventor
Jean-Louis Ambrosino
Blaise Didillon
Pierre Marache
Jean-Charles Viltard
Gérald Witte
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
IFP Energies Nouvelles IFPEN
Original Assignee
IFP Energies Nouvelles IFPEN
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN
Publication of EP0949316A1 publication Critical patent/EP0949316A1/fr
Application granted granted Critical
Publication of EP0949316B1 publication Critical patent/EP0949316B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00

Definitions

  • the invention relates to a process for converting hydrocarbons.
  • the process according to invention associates a distillation zone with a reaction reaction zone of hydrocarbons at least partially external to the distillation zone. So this process allows to selectively convert hydrocarbons separated from a charge hydrocarbons through the distillation zone.
  • the invention can be applied to a reduction process selective for the content of light unsaturated compounds (i.e. containing at most six carbon atoms per molecule) including benzene, from a cut of hydrocarbons essentially having at least 5 carbon atoms per molecule, without loss sensitive to octane number, said process comprising passing said cut in a distillation zone associated with a hydrogenation reaction zone.
  • light unsaturated compounds i.e. containing at most six carbon atoms per molecule
  • benzene from a cut of hydrocarbons essentially having at least 5 carbon atoms per molecule, without loss sensitive to octane number
  • 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.
  • 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 95/15934 describes a reactive distillation which aims selectively hydrogenating diolefins and acetylenic compounds C2-C5.
  • the distillate can be recovered separately from the light ones.
  • the catalytic zone hydrogenation is completely internal to the distillation column, which does not allow not a good dissolution of the hydrogen in the charge nor to be able to 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 and a reaction zone at least in part external to the distillation zone producing a steam distillate and a bottom effluent. At least one conversion reaction of at least part of at least one hydrocarbon takes place in a reaction zone comprising at least one bed catalytic, in the presence of a catalyst and a gas flow comprising hydrogen. The charge of the reaction zone is taken off at the level of a level and represents at least part of the liquid flowing in the area of distillation, and the effluent from the reaction zone is at least partly reintroduced into the distillation zone at the level of at least one reintroduction level, so to ensure the continuity of the distillation.
  • the invention is characterized in that the part of the effluent from the reaction zone reintroduced into the distillation zone is at a temperature lower than the temperature of the charge of the reaction zone sampled at the level of a level of sampling situated below the level of reintroduction.
  • the Applicant has surprisingly found that performing at least a circulation of a liquid withdrawn from the distillation zone at a withdrawal level and reintroduced at a reintroduction level located above said withdrawal level, the temperature of said liquid at the reintroduction level being lower than the temperature of said liquid at the withdrawal level improves the performance of the process.
  • the method according to the present invention can be applied to a process for the hydrogenation of benzene and other unsaturated compounds in an area hydrogenation associated with a distillation zone.
  • the process according to the invention is a process for treating a charge, consisting of mainly by hydrocarbons containing at least 5, preferably between 5 and 9 carbon atoms per molecule, and comprising at least one unsaturated compound, comprising possible olefins and benzene, as the said charge is treated in a distillation zone, associated with a reaction zone of hydrogenation at at least partially external, comprising at least one catalytic bed, in which performs the hydrogenation of at least part of the unsaturated compounds comprising at least plus six carbon atoms per molecule, i.e.
  • the method according to the invention makes it possible to reduce the reflux rate (flow ratio mass of the reflux measured at the top of the column on the mass feed rate of distillation zone) of the distillation zone and thus obtain a reduction in the size of the distillation zone with a higher hydrocarbon conversion or equal to that obtained with the methods according to the prior art.
  • the process according to the present invention reduces the total heat exchange surface necessary compared to the prior art methods.
  • the method according to the invention is characterized by the creation of an intermediate circulating reflux. This circulating reflux is created by reintroduction at a reintroduction level above the level of withdrawal of at least one liquid at a temperature lower than the temperature of said liquid at the level of withdrawal from the distillation zone.
  • liquid withdrawn from the distillation zone is cooled and the liquid is reintroduced. at a temperature below the temperature of said liquid at the draw-off level so to create a reflux circulating in the distillation zone.
  • the liquid withdrawn at the distillation zone at a withdrawal level and reintroduced at a reintroduction level located above said withdrawal level, the temperature of said liquid at the reintroduction level being lower than the temperature of said liquid at the withdrawal level is the liquid which serves as a charge for the zone reaction.
  • Cooling can be done before the load enters the area reaction or at the exit from the reaction zone before reintroduction into the distillation zone.
  • the temperature of the liquid at the reintroduction level is at least 10 ° C lower, preferably at least 15 ° C and even more so preferred at least 18 ° C, at the temperature of said liquid at the level of withdrawal of the distillation zone.
  • the level of reintroduction of the effluent from the external reaction zone is generally located substantially below or substantially above or at substantially the same height of at least one level of sampling, preference of said level of removal of the load to be converted.
  • the reintroduction level is located above the sampling level.
  • the reintroduction level is located at least 2 theoretical plates above the level of sampling and still more preferred, the level of reintroduction of the load is located at least 4 trays theoretical above the draw-off level of said charge.
  • the distillation zone generally comprises at least one column provided with at least minus one internal distillation chosen from the group formed by the plates, the bulk packings and structured packings, as is known to those skilled in the art profession, such that the total overall efficiency is at least equal to five theoretical stages.
  • the unit charge is introduced into the distillation zone at at least one level introduction point below the level of withdrawal of the liquid towards the zone reactionary, generally at a level of 10 to 40 theoretical platforms and preferably 15 to 25 theoretical trays below the racking level of the liquid towards said reaction zone, said withdrawal level considered being the most low.
  • the reaction zone generally comprises at least one catalytic bed hydrogenation, preferably from 1 to 4 catalytic bed (s); in the event that at least two catalytic beds are incorporated in the distillation zone, these two beds are optionally separated by at least one internal distillation.
  • the reaction zone hydrogenation at least partially performs the hydrogenation of the benzene present in the feed, generally such that the benzene content of the distillate liquid is at most equal to a certain content, and said reaction zone at least partially, preferably mostly, hydrogenates everything unsaturated compound comprising at most six carbon atoms per molecule and different from benzene, possibly present in the feed.
  • 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 reaction zone.
  • the reflux flowing from the distillation zone created by cooling at least one circulating liquid withdrawn from the distillation zone and reintroduced at a temperature lower, is implemented by at least one cooling means, for example by at least one heat exchanger.
  • the reactor being at least partly external, an equal liquid flow rate is taken, higher or lower than the liquid traffic of the distillation zone located below the draw-off level of the load to be converted.
  • the flow rate of liquid withdrawn depends on the load.
  • 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 rate of liquid withdrawn is preferably equal or lower than the liquid traffic of the distillation zone located below the level of racking.
  • 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 under conditions of absolute pressure and / or temperature different from that used in the distillation zone.
  • the conversion in at least one reaction zone partly external to the distillation zone this creates a reflux circulating in the distillation zone, by cooling the liquid withdrawn from the distillation zone to be converted outside.
  • 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 liquid distillate is recovered directly by drawing off the distillation zone.
  • This embodiment is set works by dissociating the level of withdrawal of the liquid distillate from the level of withdrawal of the steam distillate, the liquid distillate being withdrawn at least a level of sampling below the level of sampling of the steam distillate.
  • the desired product is recovered as a stabilized liquid distillate.
  • the stabilized liquid distillate is freed from the major part of the excess hydrogen and light gases essentially containing hydrocarbons with at most 5 carbon atoms and a very small amount heavier hydrocarbons.
  • this recovery of the distinct steam distillate eliminates gases other than hydrogen present in the gas distillate the gas flow mainly comprising hydrogen introduced to carry out the conversion reaction.
  • the recovery level of the stabilized liquid distillate is generally located above or below or at approximately the same height at least one level of reintroduction of the converted charge at least in part in the external reaction zone.
  • 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 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 has 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 zone of distillation is mixed at least in part with the liquid distillate.
  • 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 linked to the operating conditions of the distillation.
  • Distillation is performed under absolute pressure generally between 0.1 MPa 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 1.
  • 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 top 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 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, preferably between 0.2 and 5 MPa and even more preferably between 0.5 and 3.5 MPa.
  • the operating 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 relative 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 conditions of temperature and absolute pressure 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 ratio of reflux within the meaning of this description denotes the ratio of the flow mass of the reflux measured at the top of the column on the mass feed rate of the column.
  • the catalyst used in the hydrogenation zone generally comprises at least one metal chosen from group VIII, chosen from preferably in the group formed by nickel and platinum, used as such or from preferably deposited on a support.
  • the metal should generally be in the form reduced at least for 50% by weight of its whole. But any other catalyst hydrogenation 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 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 is preferably used based on alumina or silica, with a specific surface of between 30 and 300 m 2 / g, preferably between 90 and 260 m 2 / g.
  • FIGS. 1 and 2 are each an illustration of a possible embodiment of the process according to the invention. Similar devices are represented by the same figures in all figures.
  • a first embodiment of the process is shown in Figure 1.
  • the charge of hydrocarbons is sent to column 2 via line 1.
  • Said column contains distillation internals, which are for example in the case shown on Figure 1 of the trays or the lining, represented in part by lines dotted on 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 light hydrocarbon vapor is sent through line 9 in a condenser 10 then in a flask 11 where there is a separation between a phase liquid and a vapor phase mainly consisting of hydrogen possibly in excess.
  • the vapor phase is evacuated from the flask by line 14.
  • the liquid phase liquid from balloon 11 is partly returned via line 12 to the column head for reflux while the other part constitutes the liquid distillate which is evacuated by line 13.
  • the unit is as shown in Figure 1 but without cooling after hydrogenation reactor.
  • a metal distillation column with a diameter of 3.81 m is used, the column comprises from the head to the foot 45 theoretical plates which are numbered from top to bottom (including the condenser and the reboiler).
  • the reboiling power is 15660 kw.
  • the absolute pressure of the reflux flask is 0.5 Mpa.
  • the reflux rate is 0.82.
  • the hydrogen to benzene molar ratio is 2.74.
  • the hydrogenation reaction is completely external and a reactor is used located outside of the distillation column which contains 12 m 3 of nickel catalyst sold by the company PROCATALYSE under the reference LD746.
  • the charge for the column is injected through line 1 into plate 33.
  • the charge for the reactor 3 is withdrawn from tray 12 via line 15 at a temperature of 150 ° C.
  • Hydrogen is introduced via line 4, before entering the operating reactor in downflow and under 1.5 MPa absolute pressure.
  • the effluent from reactor 3 is re-injected into the column via line 17 at plate 8 at a temperature of 182 ° C.
  • the liquid distillate depleted in unsaturated compounds is withdrawn at the top of the column.
  • Example 2 The unit of Example 2 is shown in Figure 1 appended to the text of this requests and includes a means of cooling the hydrogenated charge in the outdoor reactor.
  • a metal distillation column with a diameter of 3.50 m is used, the column comprising from the head to the foot 45 theoretical plates which are numbered from top to bottom (including the condenser and the reboiler).
  • the reboiling power is 15660 kw.
  • the absolute pressure of the reflux flask is 0.5 Mpa.
  • the reflux rate is 0.40.
  • the hydrogen to benzene molar ratio is 2.84.
  • the hydrogenation reaction is completely external and a reactor is used located outside of the distillation column which contains 12 m 3 of nickel catalyst sold by the company PROCATALYSE under the reference LD746.
  • the charge for the column is injected through line 1 into plate 33.
  • the charge for the reactor 3 is withdrawn from tray 12 via line 15 at a temperature of 148 ° C.
  • Hydrogen is introduced via line 4, before entering the operating reactor in downflow and under 1.5 MPa absolute pressure.
  • the effluent from reactor 3 passes through a cooler 16 and is then reinjected into the column via the line 17 on plate 8 at a temperature of 115 ° C., the liquid distillate depleted in unsaturated compounds is drawn off at the top of the column.
  • the process has a configuration with withdrawal of a liquid distillate stabilized in below the racking of a steam distillate but without circulating reflux.
  • the unit is shown in Figure 2 but without cooling the hydrogenated charge.
  • a metal distillation column with a diameter of 3.35 m is used, the column comprises from the head to the foot 45 theoretical plates which are numbered from top to bottom (including the condenser and the reboiler).
  • the reboiling power is 12350 kw.
  • the absolute pressure of the reflux flask is 0.5 Mpa.
  • the reflux rate is 0.92.
  • the hydrogen to benzene molar ratio is 2.91.
  • the exchange surface of the condenser at the head of the distillation zone 10 is 1510 m 2 .
  • the hydrogenation reaction is completely external and a reactor is used located outside of the distillation column which contains 20.4 m 3 of nickel catalyst sold by the company PROCATALYSE under the reference LD746.
  • the charge for the column is injected through line 1 into plate 33.
  • the charge for the reactor 3 is withdrawn from tray 12 via line 15 at a temperature of 133 ° C.
  • Hydrogen is introduced via line 4, before entering the operating reactor in downflow and under 1.5 MPa absolute pressure.
  • the effluent from reactor 3 is re-injected into the column via line 17 at plate 8 at a temperature of 167 ° C.
  • the liquid distillate depleted in unsaturated compounds is withdrawn to tray 6.
  • the unit shown in Figure 2 has a cooling system the effluent from the hydrogenation zone.
  • a metal distillation column with a diameter of 3.05 m is used, the column comprises from the head to the foot 45 theoretical plates which are numbered from top to bottom (including the condenser and the reboiler).
  • the reboiling power is 12350 kw.
  • the absolute pressure of the reflux flask is 0.5 MPa.
  • the reflux rate is 0.23.
  • the hydrogen to benzene molar ratio is 2.91.
  • the heat exchange surface of the condenser at the head of the distillation zone 10 is 385 m 2 and the surface of the exchanger located after the reaction zone 16 is 406 m 2 .
  • the hydrogenation reaction is completely external and a reactor is used located outside of the distillation column which contains 20.4 m 3 of nickel catalyst sold by the company PROCATALYSE under the reference LD746.
  • the charge for the column is injected through line 1 into plate 33.
  • the charge for the reactor 3 is withdrawn from tray 12 via line 15 at a temperature of 132 ° C.
  • Hydrogen is introduced via line 4, before entering the operating reactor in downflow and under 1.5 MPa absolute pressure.
  • the effluent from reactor 3 cooled in a cooler 16 then is re-injected into the column via the line 17 on plate 8 at a temperature of 114 ° C.
  • the effluent depleted in compounds unsaturated is withdrawn at the level of the tray 6.
  • Example 2 shows that the method according to the invention allows conversion of the benzene higher than that obtained with the implementation according to Example 1.
  • Example 4 shows that the necessary exchange surface is lower in the process according to the present invention, to that which must be used in the case of a implementation according to example 3.
  • the method according to the present invention makes it possible to work with a column of circumference less than that of the methods of the prior art.

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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP99400740A 1998-04-06 1999-03-25 Procédé de conversion d'hydrocarbures par traitement dans une zone de distillation associée à une zone réactionnelle et son utilisation en hydrogénation du benzène Expired - Lifetime EP0949316B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9804352 1998-04-06
FR9804352A FR2777013B1 (fr) 1998-04-06 1998-04-06 Procede de conversion d'hydrocarbures par traitement dans une zone de distillation comprenant un reflux circulant, associee a une zone reactionnelle et son utilisation en hydrogenation du benzene

Publications (2)

Publication Number Publication Date
EP0949316A1 EP0949316A1 (fr) 1999-10-13
EP0949316B1 true EP0949316B1 (fr) 2004-08-04

Family

ID=9524985

Family Applications (1)

Application Number Title Priority Date Filing Date
EP99400740A Expired - Lifetime EP0949316B1 (fr) 1998-04-06 1999-03-25 Procédé de conversion d'hydrocarbures par traitement dans une zone de distillation associée à une zone réactionnelle et son utilisation en hydrogénation du benzène

Country Status (7)

Country Link
US (1) US6174428B1 (2)
EP (1) EP0949316B1 (2)
JP (1) JP4482837B2 (2)
CA (1) CA2266003C (2)
DE (1) DE69919061T2 (2)
ES (1) ES2226301T3 (2)
FR (1) FR2777013B1 (2)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1425196A (zh) 1999-11-24 2003-06-18 霍尼韦尔国际公司 导电互连
US6855853B2 (en) * 2002-09-18 2005-02-15 Catalytic Distillation Technologies Process for the production of low benzene gasoline
FR2933987B1 (fr) 2008-07-18 2010-08-27 Inst Francais Du Petrole Procede d'hydrogenation du benzene
US7910070B2 (en) * 2008-12-09 2011-03-22 Uop Llc Process for reducing benzene concentration in reformate
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
US8808533B2 (en) * 2010-04-23 2014-08-19 IFP Energies Nouvelles Process for selective reduction of the contents of benzene and light unsaturated compounds of different hydrocarbon fractions
EP2277980B1 (fr) * 2009-07-21 2018-08-08 IFP Energies nouvelles Procédé de réduction sélective de la teneur en benzène et en composés insatures legers de differentes coupes hydrocarbures
SG11201404461WA (en) 2012-02-01 2014-09-26 Saudi Arabian Oil Co Catalytic reforming process and system for producing reduced benzene gasoline

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3926785A (en) * 1971-11-01 1975-12-16 Chevron Res Integrated distillation and hydrodesulfurization process for jet fuel production
US4302356A (en) * 1978-07-27 1981-11-24 Chemical Research & Licensing Co. Process for separating isobutene from C4 streams
US5073236A (en) * 1989-11-13 1991-12-17 Gelbein Abraham P Process and structure for effecting catalytic reactions in distillation structure
US5258560A (en) * 1992-06-22 1993-11-02 Uop Etherification of C5 -plus olefins by catalytic distillation
FR2743080B1 (fr) * 1995-12-27 1998-02-06 Inst Francais Du Petrole Procede de reduction selective de la teneur en benzene et en composes insatures legers d'une coupe d'hydrocarbures

Also Published As

Publication number Publication date
EP0949316A1 (fr) 1999-10-13
JP4482837B2 (ja) 2010-06-16
US6174428B1 (en) 2001-01-16
CA2266003A1 (fr) 1999-10-06
JPH11323353A (ja) 1999-11-26
CA2266003C (fr) 2009-06-23
ES2226301T3 (es) 2005-03-16
FR2777013A1 (fr) 1999-10-08
DE69919061T2 (de) 2004-12-23
DE69919061D1 (de) 2004-09-09
FR2777013B1 (fr) 2000-05-05

Similar Documents

Publication Publication Date Title
EP0781830B1 (fr) Procédé de réduction sélective de la teneur en benzène et en composés insaturés légers d'une coupe d'hydrocarbures
EP0781829B1 (fr) Procédé et dispositif d'hydrogénation sélective par distillation catalytique
EP2321385B1 (fr) Procédé de conversion d'une charge lourde en essence et en propylène présentant une structure de rendement modulable
EP2303992B1 (fr) Procede d'hydrogenation du benzene
EP0245124A1 (fr) Procédé combiné d'hydroréformage et d'hydroisomérisation
EP0781831B1 (fr) Procédé de réduction sélective de la teneur en benzène et en composés insaturés légers d'une coupe d'hydrocarbures
EP3137583B1 (fr) Procédé de production d'essence comprenant une étape d'isomerisation suivie d'au moins deux étapes de séparation
FR2635112A1 (fr) Procede de fractionnement et d'extraction d'hydrocarbures permettant l'obtention d'une essence a indice d'octane ameliore et d'un kerosene a point de fumee ameliore
EP0949316B1 (fr) Procédé de conversion d'hydrocarbures par traitement dans une zone de distillation associée à une zone réactionnelle et son utilisation en hydrogénation du benzène
CA2738541C (fr) Procede ameliore de reduction selective de la teneur en benzene et en composes insatures legers de differentes coupes hydrocarbures
CA2265991C (fr) Procede de conversion d'hydrocarbures par traitement dans une zone de distillation associee a une zone reactionnelle, et son utilisation en hydrogenation du benzene
EP1640436B1 (fr) Procédé d'isomérisation d'une coupe C7 avec coproduction d'une coupe cycliques riche en méthylcyclohexane
FR2847260A1 (fr) Procede de desulfuration comprenant une etape d'hydrogenation selective des diolefines et une etape d'extraction des composes soufres
EP0922018B1 (fr) Procede de production d'isobutene de haute purete a partir d'une coupe c4 contenant de l'isobutene et du butene-1
EP0980909B1 (fr) Procédé de conversion d'hydrocarbures et son utilisation en hydrogénation du benzène
FR2787117A1 (fr) Procede de conversion d'hydrocarbures par traitement dans une zone de distillation associee a une zone reactionnelle comprenant le recontactage du distillat vapeur avec la charge, et son utilisation en hydrogenation du benzene
EP1737934B1 (fr) Procede et dispositif de traitement d'une charge comportant du butadiene
EP1640435B1 (fr) Procédé d'isomérisation d'une coupe C7 avec coproduction d'une coupe aromatique riche en toluène
EP2277980B1 (fr) Procédé de réduction sélective de la teneur en benzène et en composés insatures legers de differentes coupes hydrocarbures
EP2426189B1 (fr) Procédé de production de carburants kérosène et diesel à partir de coupes insaturées légeres et de coupes aromatiques riches en BTX
EP1699905A1 (fr) Procede de traitement d'une charge hydrocarbonee incluant un enlevement des resines
FR2948380A1 (fr) Procede de reduction selective de la teneur en benzene et en composes insatures legers de differentes coupes hydrocarbures

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): BE DE ES GB GR IT NL

AX Request for extension of the european patent

Free format text: AL;LT;LV;MK;RO;SI

RIN1 Information on inventor provided before grant (corrected)

Inventor name: WITTE, GERALD

Inventor name: VILTARD, JEAN-CHARLES

Inventor name: MARACHE, PIERRE

Inventor name: DIDILLON, BLAISE

Inventor name: AMBROSINO, JEAN-LOUIS

17P Request for examination filed

Effective date: 20000413

AKX Designation fees paid

Free format text: BE DE ES GB GR IT NL

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE ES GB GR IT NL

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REF Corresponds to:

Ref document number: 69919061

Country of ref document: DE

Date of ref document: 20040909

Kind code of ref document: P

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)

Effective date: 20041019

REG Reference to a national code

Ref country code: GR

Ref legal event code: EP

Ref document number: 20040403346

Country of ref document: GR

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2226301

Country of ref document: ES

Kind code of ref document: T3

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed

Effective date: 20050506

REG Reference to a national code

Ref country code: DE

Ref legal event code: R081

Ref document number: 69919061

Country of ref document: DE

Owner name: IFP ENERGIES NOUVELLES, FR

Free format text: FORMER OWNER: INSTITUT FRANCAIS DU PETROLE, RUEIL-MALMAISON, HAUTS-DE-SEINE, FR

Effective date: 20110331

Ref country code: DE

Ref legal event code: R081

Ref document number: 69919061

Country of ref document: DE

Owner name: IFP ENERGIES NOUVELLES, FR

Free format text: FORMER OWNER: INSTITUT FRANCAIS DU PETROLE, RUEIL-MALMAISON, FR

Effective date: 20110331

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20180319

Year of fee payment: 20

Ref country code: GB

Payment date: 20180319

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GR

Payment date: 20180327

Year of fee payment: 20

Ref country code: BE

Payment date: 20180312

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20180329

Year of fee payment: 20

Ref country code: ES

Payment date: 20180420

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20180330

Year of fee payment: 20

REG Reference to a national code

Ref country code: DE

Ref legal event code: R071

Ref document number: 69919061

Country of ref document: DE

REG Reference to a national code

Ref country code: NL

Ref legal event code: MK

Effective date: 20190324

REG Reference to a national code

Ref country code: GB

Ref legal event code: PE20

Expiry date: 20190324

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20190324

REG Reference to a national code

Ref country code: BE

Ref legal event code: MK

Effective date: 20190325

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20210129

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20190326