EP0874880B1 - Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures - Google Patents

Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures Download PDF

Info

Publication number
EP0874880B1
EP0874880B1 EP97919102A EP97919102A EP0874880B1 EP 0874880 B1 EP0874880 B1 EP 0874880B1 EP 97919102 A EP97919102 A EP 97919102A EP 97919102 A EP97919102 A EP 97919102A EP 0874880 B1 EP0874880 B1 EP 0874880B1
Authority
EP
European Patent Office
Prior art keywords
catalyst
section
hydrocarbons
cracking
mixing chamber
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
EP97919102A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0874880A1 (fr
Inventor
Marc Fersing
Mariano Del Pozo
Thierry Gauthier
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.)
TotalEnergies Marketing Services SA
Original Assignee
TotalFinaElf France SA
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 TotalFinaElf France SA filed Critical TotalFinaElf France SA
Publication of EP0874880A1 publication Critical patent/EP0874880A1/fr
Application granted granted Critical
Publication of EP0874880B1 publication Critical patent/EP0874880B1/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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique

Definitions

  • the present invention relates to a method and a catalytic cracker of a charge of hydrocarbons in a descending bed, implementing a improved zone of contact between the load and the catalyst.
  • the cracking of the charge is carried out in the absence of hydrogen, in the gas phase; temperature reaction temperature is around 500 ° C and the pressure generally close to atmospheric pressure.
  • the catalyst is covered with coke and traces of heavy oil and heat resulting from the combustion of this coke, during the operation regeneration in the presence of air or oxygen, allows bring the catalyst to the desired temperature for provide the calories necessary for the cracking reaction, after re-injection of the catalyst into the reactor.
  • the ratio C / O, between the flow rate C of catalyst and the flow rate O of charge to be treated is limited by a maximum generally between 3 and 7, in the current reactors, and usually close to 5.
  • upflow reactors occurs an accumulation of particles in the vicinity of the walls of the reactor, resulting in overcracking of the hydrocarbons at this level, which results in the formation of coke, hydrogen, methane and ethane, at location of the desired high octane products, while than at the center of the reactor, where fewer particles are present, an insufficient conversion of the charge.
  • reaction times seem to be able to be significantly reduced compared to riser and be significantly less than 1 second, and it seems possible to freely increase the flow of catalyst, which has no of harmful influence on the movement of particles like in the case of the riser.
  • the downer has, in particular, a related drawback to the initial mixture between catalyst and charge: in fact, the catalyst tends to fall off immediately without reflux or recirculation, which has a negative effect on the initial mass and heat transfer with the load.
  • this device appears difficult to achieve on a plan mechanical and it does not allow a very efficient mixing in the case high catalyst flow rates. Indeed, when the direction of flow of the charge-catalyst mixture is reversed, the catalyst tends to agglomerate in the vicinity of the walls of the device and is therefore found isolated from the vaporized charge.
  • the object of the invention is therefore to reconcile the advantages of the flow ascending, namely a satisfactory mixture between large flow rates of charge and catalyst, and downflow, ie good selectivity of the actual cracking reactions.
  • the contacting zone according to the invention makes it possible to achieve the above objectives. Its geometry is particularly applicable to short time insofar as it allows a complete and rapid spraying of the load.
  • EP-A-0 209 442 discloses a cracking device catalytic of hydrocarbons, including the contact zone between the catalyst and hydrocarbon consists only of one area elongated reaction vessel (see claim 6, column 3, rows 21 to 24), that is to say of a single part.
  • EP-A-0 344 032 a bed reactor entrained fluidized, usable in particular for catalytic cracking hydrocarbons.
  • This reactor substantially vertical and shaped elongated, has a particle flow regulator solids comprising a fixed part projecting inside the reactor as well as a mobile part which slides by means of a rod (cf. claim 1).
  • This "regulatory body” is a system analogous to a piston, and its function is to regulate the flow of particles catalysts entering the contact zone between the catalyst and hydrocarbons (see column 11, lines 5 to 10).
  • the ratio S 1 / S 3 between the section S 1 of passage of the catalyst through the annular orifice and the section S 3 of the intermediate orifice, is between 0.8 and 1, 25 and preferably between 0.9 and 1.1, in order to allow optimal mixing within the mixing chamber.
  • the hydrocarbons are injected at counter-current of the downward flow of catalyst particles, according to an angle to the horizontal, between 2 ° and 45 °, and preferably between 5 and 35 °.
  • the mixture between the charge and the catalyst is optimized, because this direction of injection allows the charge to break down the mass of descending catalyst as well as possible.
  • the reaction zone widens from the intermediate orifice at an angle with the vertical of between 1 and 20 °, and preferably 2 and 15 °, until it reaches its cross section. maximum S 4 .
  • This flare allows to gradually transform perfectly agitated flow, prevailing within the mixture, in a piston type flow in the reaction zone. Since such a flow is particularly favorable to the selectivity of cracking reactions, the process of the invention combines so also the specific advantages of the downflow reactor usual.
  • the ratio S 4 / S 3 between the maximum section S 4 of the reaction zone and the section S 3 of the intermediate orifice has a value between 1.5 and 8 and, preferably, between 2, 5 and 6.
  • the ratio S 2 / S 4 between the maximum section S 4 of the reaction zone is between 0.8 and 1.25 and, preferably, between 0.9 and 1.1 .
  • the invention also relates to a process for the catalytic cracking of hydrocarbons, comprising a phase of contacting the hydrocarbons and particles of a catalyst, a cracking reaction phase in a descending bed, a separation phase of the deactivated catalyst. and effluent hydrocarbons, at least one phase of stripping of the deactivated catalyst, then a phase of regeneration of said catalyst under conditions of combustion of the coke carried by the catalyst and, finally, a phase of recycling of the regenerated catalyst in the supply zone , this process being characterized in that a substantial part of the hydrocarbons is sprayed and brought into contact with the catalyst in a specific contacting zone of the catalytic cracking device defined above.
  • the device shown comprises a tubular flow reactor 1 descending, or "downer”, fed at its upper part, from an enclosure 2, which is coaxial to it, made of catalyst particles regenerated.
  • a valve 3 intended to regulate the mass ratio of catalyst to the mass of feedstock to be treated in the reactor, is interposed between reactor 1 and enclosure 2. Below this valve opens a line 4 for supplying reactor 1 with the load of hydrocarbons to be treated, preheated so known per se. This charge is sprayed into fines droplets, by injectors, at the top of the brought into contact 5, to mix with the particles of catalyst, in contact with which the reaction of cracking.
  • the direction of charge injection, as well that the geometry of the contact area, will be detailed below.
  • the catalyst particles and the charge to process therefore flow from top to bottom in reactor 1.
  • the spent catalyst particles pour into a stripping chamber 6, provided at its base of a diffuser 7, supplied with water vapor by a line 8.
  • the stripped catalyst particles are removed by gravity of the enclosure 6, by an inclined conduit 22, towards a ascending column 12, in which they are routed to the top, towards a regenerator 13, using a carrier gas, disseminated at 14 at the base of column 12, from the line 15.
  • the regenerated catalyst particles are removed by gravity through the conduit 19 in the direction of the enclosure 2, without heat losses.
  • Figure 2 shows the area more precisely contact 5 object of the invention.
  • the contacting zone 5 is formed by a mixture 24 and a reaction zone 25 arranged immediately below it.
  • the mixing chamber 24 is supplied at its upper part with hot regenerated catalyst by the cylindrical conduit 26, of section S C , which is in communication with the enclosure 2 described in FIG. 1 (but not shown in FIG. 2) .
  • a bulkhead 28, known per se, is disposed at the lower end of the conduit 26, thereby defining an upper annular orifice 30 of the mixing chamber 24, through which the catalyst pours into it. This orifice 30 thus delimits a section S 1 for passage of the catalyst, which is less than the section S c of the conduit 26.
  • the mixing chamber 24 widens from its upper orifice 30 along a frustoconical portion 32 with an angle at the apex A, until it reaches its maximum cross section S 2 .
  • the angle A for example equal to 40 °, can be between 10 and 60 °, while the section S 2 is for example equal to 5 S 1 , but can be between 1.5 and 8 S 1 .
  • the periphery 34 of the mixing chamber 24, at the level of the maximum section of the latter, is provided with a series of injectors 36, allowing the charge to be injected after atomization thereof outside the device.
  • the injectors 36 are oriented so as to direct the charge droplets countercurrent to the downward flow of catalyst particles, at an angle B with respect to the horizontal equal for example to 15 °, but which can be between 2 ° and 45 °.
  • the number of injectors will be such that the entire descending catalyst can be reached by the load droplets.
  • the mixing chamber 24 then narrows from its maximum section S 2 along a frustoconical portion 38, until it reaches its lower end of cross section S 3 .
  • the tapered portion 38 has an apex angle C, which is for example equal to 30 °, but may be between 10 and 50 °, while the section S 3 is for example equal to S 2/4, but can be understood between 2 S 2/3 and S 2/8.
  • This mixing chamber which consists of two cone portions 32, 38 widening then narrowing, is shaped so that there is a type flow perfectly agitated, allowing reflux and recirculation of catalyst necessary for a good mixture of the latter with the vaporized charge.
  • reaction zone 25 Downstream of the mixing chamber 24, in the direction of flow of the charge, extends the reaction zone 25, which is in communication with the mixing chamber through the lower end of the latter, which constitutes an orifice intermediate 40 of section S 3 .
  • the reaction zone 25 widens from the intermediate orifice in a frustoconical portion 42 of angle at the apex D, until it reaches its maximum cross section S 4 .
  • the angle D is for example equal to 6 °, but can be between 1 and 15 °, while the section S 4 is for example equal to 5 S 3 , but can be between 1.5 and 8 S 3 .
  • This flare allows a progressive modification of the nature of the flow of the charge-catalyst mixture.
  • the agitated flow within the mixing chamber is transformed in this way into a piston type flow in the reaction zone, which is perfectly suited for ensure good selectivity of the cracking reactions which occur there.
  • the reaction zone Downstream of this frustoconical portion 42, in the direction of flow of the charge, the reaction zone is constituted by a cylindrical extension 44 and has a substantially constant section, close to S 4 , so as to best conserve the flow of piston type which was established during the passage of the load in the frustoconical section 42.
  • the section S 1 of passage of the catalyst through the upper orifice 30, and the section S 3 of the intermediate orifice 40 are for example equal to 65 cm 2 , but can be between 10 and 500 cm2.
  • the maximum section S 2 of the mixing chamber 24, and the maximum section S 4 of the reaction zone 25 are for example equal to 300 cm 2 , but can be between 30 and 2000 cm 2 .
  • This description refers to an area of contact which consists of a series of surfaces of revolution, namely cylindrical portions or frustoconical whose cross section is circular.
  • the present invention also relates to any area of contact for which there are certain reports between the sections of its constituent parts, that these sections are either polygonal, ovoid or shaped any.
  • the contact area according to the invention finds its application to any cracking device catalytic whose reactor is downflow from charge, whatever the means of stripping and regeneration of the deactivated catalyst.
  • the process according to the invention therefore makes it possible to increase the selectivity of cracking by authorizing a mass ratio catalyst / charge higher than in the prior art (and therefore a lower ⁇ coke, i.e. a lower difference between the quantities of coke present on the catalyst at the entrance to the regeneration zone and at the exit from it).
  • the process according to the invention also allows, when we are targeting a given conversion, to process more difficult, especially denser and the percentage of Conradson carbon residue is higher.

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)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
EP97919102A 1996-09-18 1997-09-16 Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures Expired - Lifetime EP0874880B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR9611369 1996-09-18
FR9611369A FR2753453B1 (fr) 1996-09-18 1996-09-18 Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures, mettant en oeuvre une zone de mise en contact amelioree
PCT/FR1997/001627 WO1998012279A1 (fr) 1996-09-18 1997-09-16 Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures

Publications (2)

Publication Number Publication Date
EP0874880A1 EP0874880A1 (fr) 1998-11-04
EP0874880B1 true EP0874880B1 (fr) 2004-07-07

Family

ID=9495845

Family Applications (1)

Application Number Title Priority Date Filing Date
EP97919102A Expired - Lifetime EP0874880B1 (fr) 1996-09-18 1997-09-16 Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures

Country Status (15)

Country Link
US (1) US5997726A (es)
EP (1) EP0874880B1 (es)
JP (1) JP3955332B2 (es)
KR (1) KR100493978B1 (es)
CN (1) CN1125867C (es)
AR (1) AR008431A1 (es)
AT (1) ATE270700T1 (es)
CA (1) CA2236839C (es)
DE (1) DE69729785T2 (es)
ES (1) ES2224238T3 (es)
FR (1) FR2753453B1 (es)
ID (1) ID20024A (es)
TW (1) TW366359B (es)
WO (1) WO1998012279A1 (es)
ZA (1) ZA978333B (es)

Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2778859B1 (fr) * 1998-05-25 2000-08-11 Total Raffinage Distribution Procede et dispositif d'introduction de particules de catalyseur dans un reacteur de craquage catalytique a l'etat fluide
FR2785907B1 (fr) * 1998-11-13 2001-01-05 Inst Francais Du Petrole Procede et dispositif de craquage catalytique comprenant des reacteurs a ecoulements descendant et ascendant
FR2811327B1 (fr) 2000-07-05 2002-10-25 Total Raffinage Distribution Procede et dispositif de craquage d'hydrocarbures mettant en oeuvre deux chambres reactionnelles successives
US6613290B1 (en) 2000-07-14 2003-09-02 Exxonmobil Research And Engineering Company System for fluidized catalytic cracking of hydrocarbon molecules
AU2003236150A1 (en) 2002-04-26 2003-11-10 China Petroleum And Chemical Corporation Downflow catalytic cracking reactor and use thereof
FR2895413B1 (fr) 2005-12-27 2011-07-29 Alstom Technology Ltd Installation de conversion d'hydrocarbures petroliers a installation de combustion integree comprenant une capture du dioxyde de carbone
CN103814114B (zh) * 2011-07-27 2018-04-24 沙特阿拉伯石油公司 在下流式反应器中流化催化裂化链烷烃族石脑油
JP5823911B2 (ja) * 2012-04-27 2015-11-25 Ｊｘ日鉱日石エネルギー株式会社 流動接触分解装置における原料と触媒を混合する混合装置
US10913043B2 (en) 2018-09-28 2021-02-09 Uop Llc Apparatuses for mixing of staged methanol injection
FR3140778A1 (fr) * 2022-10-13 2024-04-19 IFP Energies Nouvelles Réacteur à lit fluidisé à co-courant gaz-solide descendant à injecteur orienté.
FR3140776A1 (fr) 2022-10-13 2024-04-19 IFP Energies Nouvelles Réacteur à lit fluidisé à co-courant gaz-solide descendant à écoulement homogène.
FR3140777A1 (fr) 2022-10-13 2024-04-19 IFP Energies Nouvelles Chambre de mélange pour réacteur à lit fluidisé à co-courant gaz-solide descendant.

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS624784A (ja) * 1985-07-16 1987-01-10 コンパニ−・フランセ−ズ・ド・ラフイナ−ジユ 炭化水素仕込物の接触クラツキングのための方法および装置の改良
US4985136A (en) * 1987-11-05 1991-01-15 Bartholic David B Ultra-short contact time fluidized catalytic cracking process
FR2631857B1 (fr) * 1988-05-24 1990-09-14 Inst Francais Du Petrole Reacteur a lit fluidise entraine comprenant un moyen de regulation du flux de particules solides et son utilisation dans un procede de craquage catalytique
FR2667609B1 (fr) * 1990-10-03 1993-07-16 Inst Francais Du Petrole Procede et dispositif de craquage catalytique en lit fluide a courant descendant.
FR2715163B1 (fr) * 1994-01-18 1996-04-05 Total Raffinage Distribution Procédé de craquage catalytique en lit fluidisé d'une charge d'hydrocarbures, notamment d'une charge à forte teneur en composés azotés basiques.

Also Published As

Publication number Publication date
KR100493978B1 (ko) 2005-09-02
CA2236839C (fr) 2007-03-20
CN1125867C (zh) 2003-10-29
US5997726A (en) 1999-12-07
ATE270700T1 (de) 2004-07-15
TW366359B (en) 1999-08-11
FR2753453B1 (fr) 1998-12-04
CA2236839A1 (fr) 1998-03-26
ES2224238T3 (es) 2005-03-01
DE69729785T2 (de) 2005-07-14
EP0874880A1 (fr) 1998-11-04
KR19990067533A (ko) 1999-08-25
ZA978333B (en) 1998-03-24
FR2753453A1 (fr) 1998-03-20
CN1205028A (zh) 1999-01-13
DE69729785D1 (de) 2004-08-12
AR008431A1 (es) 2000-01-19
JP2000500820A (ja) 2000-01-25
WO1998012279A1 (fr) 1998-03-26
ID20024A (id) 1998-09-10
JP3955332B2 (ja) 2007-08-08

Similar Documents

Publication Publication Date Title
EP0479645B1 (fr) Procédé et dispositif de craquage catalytique en lit fluide à courant descendant
EP0208609B1 (fr) Procédé et dispositif pour le craquage catalytique de charges d'hydrocarbures, avec contrôle de la température de réaction
EP0191695B1 (fr) Procédé et dispositif d'injection de catalyseur dans un procédé de craquage catalytique à l'état fluide, notamment de charges lourdes
EP0874880B1 (fr) Procede et dispositif de craquage catalytique en lit fluidise d'une charge d'hydrocarbures
EP0226483B1 (fr) Procédé et appareil de craquage catalytique d'une charge hydrocarbonée soumise à un prétraitement par des particules de solides peu actives
EP0184517B1 (fr) Perfectionnement aux procédés et dispositifs pour le craquage catalytique de charges d'hydrocarbures
EP0485259B1 (fr) Procédé et dispositif d'homogénéisation, à l'intérieur d'un réacteur tubulaire de craquage d'hydrocarbures à lit de particules solides fluidisées, du mélange de ces particules et des vapeurs d'hydrocarbures à traiter
FR2654435A1 (fr) Procede et dispositif de mise en contact d'une charge d'hydrocarbures avec des particules solides chaudes, dans un reacteur tubulaire a lit fluidise ascendant.
EP0489726B1 (fr) Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee
EP0282371B1 (fr) Procédé et dispositif pour le craquage catalytique de charges d'hydrocarbures
FR2753454A1 (fr) Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne
EP0291408B1 (fr) Procédé de vapocraquage dans une zone réactionnelle en lit fluide
EP0573316B1 (fr) Procédé et dispositif de craquage catalytique dans deux zones réactionnelles successives
EP0911379A1 (fr) Procédé et dispositif de vaporisation sélective des charges d'hydrocarbures en craquage catalytique
FR2605643A1 (fr) Procede et dispositif pour le craquage catalytique en lit fluidise d'une charge d'hydrocarbures
EP0322276A1 (fr) Procédé et dispositif pour le craquage catalytique de charges lourdes comportant un second strippage en lit fluide
WO2024078904A1 (fr) Procédé de craquage catalytique en lit fluidisé à co-courant gaz-solide descendant avec injecteur de charge orienté
WO2024078905A1 (fr) Réacteur à lit fluidisé à co-courant gaz-solide descendant à écoulement homogène
WO2024078942A1 (fr) Chambre de mélange pour réacteur à lit fluidisé à co-courant gaz-solide descendant
WO1991003527A1 (fr) Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee
FR2658833A1 (fr) Procede de craquage a l'etat fluide d'une charge d'hydrocarbures.
FR2599376A1 (fr) Procede et appareil de craquage catalytique d'une charge hydrocarbonee soumise a un pretraitement par des particules de solides peu actives
FR2628436A1 (fr) Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee de particules caloporteuses
FR2521157A1 (fr) Preparation d'une charge de craquage catalytique fluide par vaporisation selective

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

17P Request for examination filed

Effective date: 19980224

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LI NL PT SE

17Q First examination report despatched

Effective date: 20010508

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

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: TOTALFINAELF FRANCE

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LI NL PT SE

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

Ref country code: IE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20040707

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20040707

Ref country code: AT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20040707

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

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

Effective date: 20040707

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: FRENCH

REF Corresponds to:

Ref document number: 69729785

Country of ref document: DE

Date of ref document: 20040812

Kind code of ref document: P

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

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040930

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040930

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

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20041007

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20041007

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20041007

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2224238

Country of ref document: ES

Kind code of ref document: T3

REG Reference to a national code

Ref country code: IE

Ref legal event code: FD4D

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

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: 20050408

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

Ref country code: PT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20041207

REG Reference to a national code

Ref country code: FR

Ref legal event code: CD

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 19

REG Reference to a national code

Ref country code: FR

Ref legal event code: TP

Owner name: TOTAL RAFFINAGE FRANCE, FR

Effective date: 20151222

REG Reference to a national code

Ref country code: DE

Ref legal event code: R082

Ref document number: 69729785

Country of ref document: DE

Representative=s name: PRUEFER & PARTNER MBB PATENTANWAELTE RECHTSANW, DE

Ref country code: DE

Ref legal event code: R081

Ref document number: 69729785

Country of ref document: DE

Owner name: TOTAL RAFFINAGE FRANCE, FR

Free format text: FORMER OWNER: TOTALFINAELF FRANCE, PUTEAUX, FR

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 20

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

Ref country code: GB

Payment date: 20160920

Year of fee payment: 20

Ref country code: DE

Payment date: 20160921

Year of fee payment: 20

Ref country code: NL

Payment date: 20160920

Year of fee payment: 20

REG Reference to a national code

Ref country code: ES

Ref legal event code: PC2A

Owner name: TOTAL RAFFINAGE FRANCE

Effective date: 20161107

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

Ref country code: FR

Payment date: 20160830

Year of fee payment: 20

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

Ref country code: ES

Payment date: 20160916

Year of fee payment: 20

Ref country code: BE

Payment date: 20160920

Year of fee payment: 20

REG Reference to a national code

Ref country code: NL

Ref legal event code: PD

Owner name: TOTAL RAFFINAGE FRANCE; FR

Free format text: DETAILS ASSIGNMENT: CHANGE OF OWNER(S), ASSIGNMENT; FORMER OWNER NAME: TOTAL MARKETING SERVICES

Effective date: 20170120

Ref country code: NL

Ref legal event code: HC

Owner name: TOTAL MARKETING SERVICES; FR

Free format text: DETAILS ASSIGNMENT: CHANGE OF OWNER(S), CHANGE OF OWNER(S) NAME; FORMER OWNER NAME: TOTALFINAELF FRANCE

Effective date: 20170120

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

Ref country code: IT

Payment date: 20160922

Year of fee payment: 20

REG Reference to a national code

Ref country code: GB

Ref legal event code: 732E

Free format text: REGISTERED BETWEEN 20170209 AND 20170215

REG Reference to a national code

Ref country code: DE

Ref legal event code: R071

Ref document number: 69729785

Country of ref document: DE

REG Reference to a national code

Ref country code: NL

Ref legal event code: MK

Effective date: 20170915

REG Reference to a national code

Ref country code: GB

Ref legal event code: PE20

Expiry date: 20170915

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: 20170915

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20171227

REG Reference to a national code

Ref country code: BE

Ref legal event code: PD

Owner name: TOTAL RAFFINAGE FRANCE; FR

Free format text: DETAILS ASSIGNMENT: CHANGE OF OWNER(S), AFFECTATION / CESSION; FORMER OWNER NAME: TOTAL RAFFINAGE MARKETING

Effective date: 20161129

Ref country code: BE

Ref legal event code: MK

Effective date: 20170916

Ref country code: BE

Ref legal event code: HC

Owner name: TOTAL RAFFINAGE MARKETING; FR

Free format text: DETAILS ASSIGNMENT: CHANGE OF OWNER(S), CHANGEMENT NOM PROPRIETAIRE; FORMER OWNER NAME: TOTAL FRANCE

Effective date: 20161129

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: 20170917