EP0552070B1 - Réduction de la teneur en benzène dans les essences - Google Patents
Réduction de la teneur en benzène dans les essences Download PDFInfo
- Publication number
- EP0552070B1 EP0552070B1 EP93400021A EP93400021A EP0552070B1 EP 0552070 B1 EP0552070 B1 EP 0552070B1 EP 93400021 A EP93400021 A EP 93400021A EP 93400021 A EP93400021 A EP 93400021A EP 0552070 B1 EP0552070 B1 EP 0552070B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- isomerization
- catalyst
- hydrogenation
- process according
- charge
- 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
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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of reforming naphtha
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
Definitions
- the invention relates to a process allowing the reduction of the benzene content in gasoline fractions by a process combining the hydrogenation of the benzene contained in the light reformate and optionally the hydrogenation of a C 5 -C 6 cut and isomerization. effluent from hydrogenation and possibly from said cut.
- the catalytic reforming used under conditions of severe severity, and the isomerization of normal C 5 -C 6 paraffins of low octane number are the most commonly used processes currently for obtaining high octane numbers without the addition of lead.
- the catalytic reforming process produces large quantities of high octane benzene. This is why it is necessary to develop new processes which make it possible to reduce the benzene content of gasolines while meeting the specifications for the octane number.
- the reduction of the benzene content of the reformate can also be carried out in various ways, such as for example the modification of the cutting point of the naphtha between reforming and isomerization or the separation of the reformate into two fractions: a heavy reformate and a light reformate in which all the benzene is concentrated.
- This light fraction is then sent to a hydrogenation unit which makes it possible to transform the benzene into naphthenes, which are then decyclized in an isomerization unit working under severe conditions.
- the normal paraffins thus formed are isomerized by a conventional isomerization process (US-A 5,003,118).
- a conventional isomerization process US-A 5,003,118.
- the naphthenes adsorb on the catalyst and thus contribute to deteriorating its activity.
- US-A-3,611,117 also describes a process for hydroisomerization cyclic hydrocarbons that uses a Group VIII metal supported on zeolite as a catalyst for opening cycles in severe operating conditions and as an isomerization catalyst in mild operating conditions.
- the object of the present invention is to carry out jointly the reduction of the benzene content contained in the light reformate and the isomerization of the paraffins contained on the one hand in this light reformate and on the other hand in a C 5 -C cut 6 generally paraffinic and resulting from direct distillation.
- the process of the present invention therefore comprises the hydrogenation of benzene contained in the charge defined below in a zone hydrogenation and then isomerization of the effluent from the hydrogenation in an isomerization zone, the process being characterized in that one mixing said effluent a C5-C6 cut.
- EP-A-0 552 072 relates to a similar process but without the addition of a C5-C6 cut to the effluent resulting from the hydrogenation.
- the hydrogenation zone and the isomerization zone according to the invention can be included in the same reactor, or in separate reactors such that each of said zones is included in at least one reactor.
- the conditions under which the hydrogenation is carried out and isomerization i.e. the operating conditions, the catalyst, etc.
- the conditions known to those skilled in the art are the conditions known to those skilled in the art. They are nevertheless specified below.
- Benzene is generally essentially the only compound aromatic included in said fraction.
- said fraction can comprise between 1 and 3% of hydrocarbons olefinic.
- the weight composition of the C 5 -C 6 cut is variable. It depends on the nature of the crude to be treated in the case where the C 5 -C 6 cut is obtained from direct distillation.
- the paraffin content of said cut is generally greater than 90% by weight, its naphthene content generally less than 10% by weight and the benzene content generally less than 1.5% by weight.
- His index typically research octane is between 60 and 75.
- the C 5 -C 6 cut is mixed with the effluent from the hydrogenation, that is to say with the saturated light reformate leaving the hydrogenation zone, the effluent content from the hydrogenation of the charge entering the isomerization zone being between 10 and 90% and preferably between 20 and 80%.
- the pressure required for this step hydrogenation is generally between 1 and 60 bar absolute, particularly between 2 and 50 bar and more advantageously between 5 and 45 bar.
- the operating temperature is generally between 100 and 400 ° C, more advantageously between 150 and 350 ° C and preferably between 160 and 320 ° C.
- the space velocities calculated with respect to the catalyst are generally between 1 and 50 h -1 and more particularly between 1 and 30 h -1 (volume of charge per volume of catalyst and per hour).
- the flow of hydrogen, relative to the catalyst is generally between 1 and 2000 volumes (gas under normal conditions) per volume of catalyst and per hour.
- the heat released at this stage is advantageously used to preheat the isomerization charge.
- the catalyst used in the hydrogenation zone according to the process of present invention comprises at least one metal M chosen from the group formed by nickel, platinum and palladium, deposited on a support.
- Metal M must be in reduced form at less for 50% of its totality.
- nickel or platinum is used, and even more preferably platinum.
- the catalyst may contain advantageously at least one halogen in a proportion by weight per ratio to the catalyst of between 0.5 and 2%.
- halogen in a proportion by weight per ratio to the catalyst of between 0.5 and 2%.
- the proportion of metal M relative to the total weight of catalyst is between 0.1 and 60%, more particularly between 5 and 60% and preferably between 5 and 30%.
- the total proportion of metal M by relative to the total weight of catalyst is between 0.1 and 10% and so preferred between 0.05 and 5%.
- the support can be chosen from the group formed by alumina, silica-aluminas, silica, zeolites, activated carbon, clays and aluminous cements.
- An alumina is preferably used, with a specific surface at least equal to 50 m 2 / g and a pore volume at least equal to 0.4 cm 3 / g, for example with a specific surface of between 50 and 350 m 2 / g and of pore volume between 0.4 and 1.2 cm 3 / g.
- the effluent from the hydrogenation zone generally contains less 0.1% aromatics and generally has between 4 and 6 octane points less than the load entering said area.
- the isomerization zone is fed by the effluent from the hydrogenation zone comprising the light reformate mixture plus the non-hydrogenated C 5 -C 6 cut.
- the isomerization is generally carried out in said isomerization zone under the following usual conditions: the temperature is between 230 and 280 ° C., and the partial pressure of hydrogen is between atmospheric pressure and 70 bar and preferably between 5 and 50 bar.
- the space velocity is between 0.2 and 10 liters and preferably between 0.5 and 5 liters of liquid hydrocarbons per liter of catalyst per hour.
- the hydrogen / charge molar ratio is normally between 0.5 and 10 and preferably between 1 and 3.
- the catalyst used in the isomerization zone according to the process of the present invention is a catalyst comprising at least one group VIII metal and a zeolite.
- Different zeolites can be used for said catalyst, such as, for example, mordenite or ⁇ zeolite.
- Use is preferably made of a mordenite having an Si / Al (atomic) ratio of between 5 and 50 and preferably between 5 and 30, a sodium content of less than 0.2% and preferably of less than 0.1% ( relative to the weight of dry zeolite), a volume of mesh V of the elementary mesh of between 2.78 and 2.73 nm 3 and preferably between 2.77 and 2.74 nm 3 , an absorption capacity of benzene greater than 5% and preferably greater than 8% (relative to the weight of dry solid).
- the mordenite thus prepared is then mixed with a generally amorphous matrix (alumina, silica alumina, kaolin, etc.) and shaped by any method known to those skilled in the art (extrusion, pelletizing, coating).
- the mordenite content of the support thus obtained must be greater than 40% and preferably greater than 60% by weight.
- At least one hydrogenating metal from group VIII preferably chosen from the group formed by platinum, palladium, and nickel, is then deposited on this support, either in the form of a tetramine complex by cation exchange, either in the form of hexachloroplatinic acid in the case of platinum or either in the form of palladium chloride by anion exchange.
- the content by weight is between 0.05 and 1% and preferably between 0.1 and 0.6%.
- the weight content is between 0.1 and 10% and preferably between 0.2 and 5%.
- the effluent obtained at the exit from the isomerization zone has an index octane high enough to be incorporated into gasoline fractions after stabilization and generally has a maximum benzene content equal to 0.1% by weight. Preferably, it is completely free of benzene.
- the single figure shows an arrangement of the method according to the invention, in which hydrogenation and isomerization are carried out in two reactors (or units) separate.
- the stabilized reformate (1) is sent to a distillation column (6), which is a heavy reformate (3) comes out at the bottom which can be used directly in the essence fractions and at the top a slight reformate (2).
- the latter is sent to a hydrogenation unit (7).
- a direct distillation C 5 -C 6 cut (10) is mixed with the saturated light reformate (4) just before the isomerization unit (8).
- the cut obtained is treated in an isomerization unit (8) giving the final product (5) which, after stabilization, can be incorporated into the gasoline fractions.
- the molar ratio of hydrogen to hydrocarbons contained in the charge is equal to 0.85, and the liquid space speed is equal to 4 h -1 .
- the catalyst used in the hydrogenation section consists of 15% of Ni deposited on alumina.
- the effluent from the hydrogenation unit no longer contains benzene but has an octane number of 76.5. It is then mixed in an amount of 50% by weight with a C 5 -C 6 cut of direct distillation containing 0.7% of benzene and having an octane number of 65.
- the composition of this cut as well as the composition of the mixture which constitutes the charge of the isomerization unit are given in table II.
- the isomerization unit operates at a temperature of 260 ° C., a pressure of 30 bar with an LHSV equal to 2 and a hydrogen to hydrocarbon molar ratio of the charge equal to 4.
- the effluent leaving the isomerization unit has the composition given in Table II; it no longer contains benzene and has an octane number of 78.1. This effluent can be directly incorporated into the gasoline fractions after stabilization.
Description
- la fraction légère du réformat,
- une coupe C5-C6 généralement issue de la distillation directe.
- paraffines : entre 40,0 et 80,0 %,
- naphtènes : entre 0,9 et 7,0 %,
- aromatiques : entre 6,0 et 45,0 %.
- le poids moléculaire moyen est compris entre 70 et 90 g/mol.,
- la masse volumique, mesurée à 15° C, est comprise entre 0,670 et 0,780 g/cm3,
- la valeur de l'indice d'octane recherche est généralement comprise entre 75 et 90.
Réformat | Coupe C5-C6 de distillation | Effluent de l'hydrogénation | Charge de l'isomérisation | Effluent de l'isomérisation | |
légers | 6,5 | 1,0 | 6,5 | 3,7 | 4,6 |
iC5 | 9,9 | 18,9 | 9,9 | 14,4 | 18,8 |
nC5 | 7,1 | 25,4 | 7,1 | 16,25 | 12,5 |
22DMC4 | 3,0 | 0,4 | 3,0 | 1,7 | 6,3 |
23DMC4 | 4,1 | 1,85 | 4,1 | 3,0 | 4,8 |
2MC5 | 15,8 | 11,1 | 15,8 | 13,45 | 17,6 |
3MC5 | 12,5 | 9,4 | 12,5 | 11,0 | 11,55 |
nC6 | 12,1 | 19,6 | 12,1 | 15,9 | 8,75 |
C7 | 3,5 | 4,4 | 3,5 | 3,9 | 1,9 |
CC5 | 0,4 | 1,4 | 0,4 | 0,9 | 0,9 |
MCC5 | 3,6 | 4,1 | 3,6 | 3,85 | 9,9 |
Benzène | 21,5 | 0,7 | - | 0,35 | |
CC6 | 0 | 1,75 | 21,5 | 11,6 | 2,4 |
R.O.N. | 80,3 | 65 | 76,5 | 71,2 | 78,1 |
• iC5 correspond à isoparaffine C5 • nC5 correspond à normal paraffine C5 • 22DMC4 correspond à 2,2-diméthylbutane • 23DMC4 correspond à 2,3-diméthylbutane • 2MC5 correspond à 2-méthylpentane • 3MC5 correspond à 3-méthylpentane • nC6 correspond à normal paraffine C6 • CC5 correspond à cyclopentane • MCC5 correspond à méthylcyclopentane • CC6 correspond à cyclohexane |
Claims (7)
- Procédé de réduction de la teneur en benzène dans les fractions essences dans lequel on effectue, dans une zone d'hydrogénation, une hydrogénation de la charge caractérisée par :
une composition pondérale comprise dans les intervalles suivants :entre 40 et 80 % de paraffinesentre 0,5 et 7 % de naphtènesentre 6 et 45 % d'aromatiques
puis à une isomérisation, dans une zone d'isomérisation, de l'effluent issu de la zone l'hydrogénation, le procédé étant caractérisé en ce que le catalyseur d'hydrogénation comprend au moins un métal choisi dans le groupe formé par le nickel, le platine et le palladium, sur support, en ce que le catalyseur d'isomérisation comprend une zéolithe et au moins un métal du groupe VIII, en ce que l'isomérisation est mise en oeuvre à une température comprise entre 230°C et 280°C, et en ce que l'on mélange une coupe C5-C6 audit effluent. - Procédé selon la revendication 1 dans lequel le mélange comprend 10 à 90 % dudit effluent.
- Procédé selon l'une des revendications 1 ou 2 dans lequel le métal du groupe VIII du catalyseur d'isomérisation est choisi dans le groupe formé par le platine, le palladium et le nickel.
- Procédé selon l'une des revendications 1 à 3 tel que la zéolithe est une mordénitc ou une zéolithe oméga.
- Procédé selon l'une des revendications 1 à 4 dans lequel l'étape d'hydrogénation se fait selon les conditions opératoires suivantes : la température est comprise entre 100 et 400 °C, la pression est comprise entre 1 et 60 bars, la vitesse spatiale est comprise entre 1 et 50 volumes de charge par volume de catalyseur et par heure et le débit d'hydrogène est compris entre 1 et 2000 volumes par volume de catalyseur et par heure.
- Procédé selon l'une des revendications 1 à 5 dans lequel l'étape d'isomérisation est effectuée à une pression partielle d'hydrogène comprise entre la pression atmosphérique et 70 bars, à une vitesse spatiale comprise entre 0,2 et 10 litres de charge par litre de catalyseur et par heure, et avec un rapport molaire hydrogène sur charge compris entre 0,5 et 10.
- Procédé selon l'une des revendications 1 à 6 dans lequel la coupe C5-C6 est une coupe de distillation directe.
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9200435A FR2686094B1 (fr) | 1992-01-15 | 1992-01-15 | Production de base pour carburant exempt de benzene, presentant un indice d'octane eleve. |
FR9200435 | 1992-01-15 | ||
FR9209758 | 1992-08-04 | ||
FR929209758A FR2694565B1 (fr) | 1992-08-04 | 1992-08-04 | Réduction de la teneur en benzène dans les essences. |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0552070A1 EP0552070A1 (fr) | 1993-07-21 |
EP0552070B1 true EP0552070B1 (fr) | 1999-08-18 |
Family
ID=26229197
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP93400021A Expired - Lifetime EP0552070B1 (fr) | 1992-01-15 | 1993-01-07 | Réduction de la teneur en benzène dans les essences |
Country Status (6)
Country | Link |
---|---|
EP (1) | EP0552070B1 (fr) |
CA (1) | CA2087385A1 (fr) |
DE (1) | DE69326030T2 (fr) |
ES (1) | ES2137974T3 (fr) |
MY (1) | MY109122A (fr) |
TW (1) | TW218377B (fr) |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2714388B1 (fr) * | 1993-12-29 | 1996-02-02 | Inst Francais Du Petrole | Procédé de réduction de la teneur en benzène dans les essences. |
US5599997A (en) * | 1995-03-14 | 1997-02-04 | Chemical Research & Licensing Company | Process for the production of cyclohexyl amine |
US5773670A (en) * | 1995-03-06 | 1998-06-30 | Gildert; Gary R. | Hydrogenation of unsaturated cyclic compounds |
FR2743079B1 (fr) * | 1995-12-27 | 1998-02-06 | Inst Francais Du Petrole | Procede et dispositif d'hydrogenation selective par distillation catalytique comportant une zone reactionnelle a co-courant ascendant liquide-gaz |
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 |
FR2743081B1 (fr) * | 1995-12-27 | 1998-01-30 | Inst Francais Du Petrole | Procede de reduction selective de la teneur en benzene et en composes insatures legers d'une coupe d'hydrocarbures |
FR2776667B1 (fr) | 1998-03-31 | 2000-06-16 | Total Raffinage Distribution | Procede et dispositif d'isomerisation d'essences a teneur elevee en benzene |
EP0953626A1 (fr) * | 1998-04-27 | 1999-11-03 | FE Forschungs & Entwicklung GmbH | Procédé de préparation d'un mélange hydrocarburé à haut indice d'octane et pauvre en benzène |
US6855853B2 (en) | 2002-09-18 | 2005-02-15 | Catalytic Distillation Technologies | Process for the production of low benzene gasoline |
CN115397951A (zh) | 2019-08-02 | 2022-11-25 | 阿布扎比炼油公司泰克瑞尔 | 用于轻质重整产物的苯饱和/异构化的单反应器方法 |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3009002A (en) * | 1960-06-20 | 1961-11-14 | Phillips Petroleum Co | High purity cyclohexane from natural cyclohexane-containing fraction |
CA975384A (en) * | 1971-04-19 | 1975-09-30 | Graham K. Hilder | Isomerisation of paraffin hydrocarbons |
US5003118A (en) * | 1989-12-29 | 1991-03-26 | Uop | Isomerization of benzene-containing feedstocks |
-
1993
- 1993-01-07 ES ES93400021T patent/ES2137974T3/es not_active Expired - Lifetime
- 1993-01-07 DE DE69326030T patent/DE69326030T2/de not_active Expired - Fee Related
- 1993-01-07 EP EP93400021A patent/EP0552070B1/fr not_active Expired - Lifetime
- 1993-01-14 MY MYPI93000061A patent/MY109122A/en unknown
- 1993-01-15 CA CA002087385A patent/CA2087385A1/fr not_active Abandoned
- 1993-01-18 TW TW082100287A patent/TW218377B/zh active
Also Published As
Publication number | Publication date |
---|---|
MY109122A (en) | 1996-12-31 |
DE69326030D1 (de) | 1999-09-23 |
ES2137974T3 (es) | 2000-01-01 |
CA2087385A1 (fr) | 1993-07-16 |
TW218377B (fr) | 1994-01-01 |
DE69326030T2 (de) | 2000-01-05 |
EP0552070A1 (fr) | 1993-07-21 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0242260B1 (fr) | Procédé de réformage catalytique | |
FR2757533A1 (fr) | Procede de preparation d'une matiere premiere de melange pour essence exempte de benzene et isomerisee utlisant un catalyseur a double fonction | |
WO1997009397A1 (fr) | Procede d'hydroisomerisation selective de paraffines longues lineaires et/ou peu ramifiees avec un catalyseur a base de tamis moleculaire | |
EP0552070B1 (fr) | Réduction de la teneur en benzène dans les essences | |
EP0661370B1 (fr) | Catalyseur pour la réduction de la teneur en benzène dans les essences | |
CA2194085C (fr) | Procede de reduction selective de la teneur en benzene et en composes insatures legers d'une coupe d'hydrocarbures | |
EP0661095B1 (fr) | Catalyseur pour la réduction de la teneur en benzène dans les essences | |
FR2548204A1 (fr) | Procede de transformation d'hydrocarbures | |
EP0552069B1 (fr) | Réduction de la teneur en benzène dans les essences par un procédé d'isomérisation | |
FR2676750A1 (fr) | Procede d'hydrocraquage de paraffines issue du procede fischer-tropsch a l'aide de catalyseurs a base de zeolithe h-y. | |
EP1417283B1 (fr) | Procede d'isomerisation d'une coupe c5-c8 mettant en oeuvre deux reacteurs en parallele | |
EP0552072B1 (fr) | Réduction de la teneur en benzène dans les essences | |
EP0288362B1 (fr) | Procédé d'isomérisation du butène-1 en butènes-2 dans une coupe d'hydrocarbures en c4 contenant du butadiène et des composés sulfurés | |
EP0787786B1 (fr) | Procédé d'isomérisation de paraffines par distillation réactive | |
FR2694565A1 (fr) | Réduction de la teneur en benzène dans les essences. | |
FR2744441A1 (fr) | Procede d'isomerisation de paraffines | |
FR2686094A1 (fr) | Production de base pour carburant exempt de benzene, presentant un indice d'octane eleve. | |
WO2023117594A1 (fr) | Unité de production et de séparation des aromatiques avec valorisation d'un extrait et/ou d'un raffinat provenant d'un procédé d'extraction liquide-liquide | |
EP0922747B1 (fr) | Procédé d'isomérisation des coupes paraffiniques C5-C8 riches en paraffines à plus de sept atomes de carbone | |
FR2738243A1 (fr) | Procede d'hydroisomerisation de paraffines longues lineaires et/ou peu ramifiees avec un catalyseur a base de zeolithe nu-10 | |
FR2597496A1 (fr) | Procede de reformage catalytique |
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 IT LU NL |
|
17P | Request for examination filed |
Effective date: 19940107 |
|
17Q | First examination report despatched |
Effective date: 19950712 |
|
GRAG | Despatch of communication of intention to grant |
Free format text: ORIGINAL CODE: EPIDOS AGRA |
|
GRAG | Despatch of communication of intention to grant |
Free format text: ORIGINAL CODE: EPIDOS AGRA |
|
GRAH | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOS IGRA |
|
GRAH | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOS IGRA |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
ITF | It: translation for a ep patent filed |
Owner name: DE DOMINICIS & MAYER S.R.L. |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): BE DE ES GB IT LU NL |
|
REF | Corresponds to: |
Ref document number: 69326030 Country of ref document: DE Date of ref document: 19990923 |
|
GBT | Gb: translation of ep patent filed (gb section 77(6)(a)/1977) |
Effective date: 19990922 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2137974 Country of ref document: ES Kind code of ref document: T3 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: LU Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20000107 Ref country code: GB Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20000107 |
|
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 NON-PAYMENT OF DUE FEES Effective date: 20000108 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: BE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20000131 |
|
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 |
|
BERE | Be: lapsed |
Owner name: INSTITUT FRANCAIS DU PETROLE Effective date: 20000131 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: NL Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20000801 |
|
26N | No opposition filed | ||
GBPC | Gb: european patent ceased through non-payment of renewal fee |
Effective date: 20000107 |
|
NLV4 | Nl: lapsed or anulled due to non-payment of the annual fee |
Effective date: 20000801 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: DE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20001101 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FD2A Effective date: 20010910 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED. Effective date: 20050107 |