EP0554151A1 - Selektives Hydrierungsverfahren, insbesondere von Diolefinen in Benzin, mit einem Katalysator in aufeinander verwendeten Betten - Google Patents

Selektives Hydrierungsverfahren, insbesondere von Diolefinen in Benzin, mit einem Katalysator in aufeinander verwendeten Betten Download PDF

Info

Publication number
EP0554151A1
EP0554151A1 EP93400164A EP93400164A EP0554151A1 EP 0554151 A1 EP0554151 A1 EP 0554151A1 EP 93400164 A EP93400164 A EP 93400164A EP 93400164 A EP93400164 A EP 93400164A EP 0554151 A1 EP0554151 A1 EP 0554151A1
Authority
EP
European Patent Office
Prior art keywords
bed
catalyst
charge
product
beds
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.)
Granted
Application number
EP93400164A
Other languages
English (en)
French (fr)
Other versions
EP0554151B1 (de
Inventor
Jean Cosyns
Patrick Sarrazin
Jean-Paul Boitiaux
Charles Cameron
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 EP0554151A1 publication Critical patent/EP0554151A1/de
Application granted granted Critical
Publication of EP0554151B1 publication Critical patent/EP0554151B1/de
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
    • 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
    • C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
    • C10G65/06—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins

Definitions

  • the present invention relates to a hydrogenation process and more particularly to a selective hydrogenation process for diolefins in liquid hydrocarbon fractions such as, for example, steam cracked gasolines.
  • liquid hydrocarbon fractions such as, for example, steam cracked gasolines.
  • These essences indeed contain gum-generating compounds that are diolefins mixed with olefinic compounds and aromatic compounds. To recover these olefinic compounds and these aromatic compounds, it is necessary to selectively hydrogenate the diolefins.
  • Such treatments are generally carried out on metal catalysts deposited on an amorphous or crystalline support.
  • the metals used are the Group VIII metals and among these, nickel and palladium can be noted.
  • the implementation of the hydrogenation operation itself involves a heat extraction system because the exotherm is such that the catalyst would be damaged by the excessively high temperatures which prevail at the outlet of the catalyst bed.
  • This extraction of calories can be done by exchange with a heat transfer fluid in a reactor-exchanger, the catalyst being maintained in the tubes and the heat transfer fluid being cut from the grille side.
  • Such an implementation, called isothermal is complicated and requires the use of very expensive reactors.
  • An improvement consists in separating the catalyst into two beds and cooling the effluent from the first bed with a quenching liquid consisting of cold hydrogenated product.
  • the object of the invention is therefore to extend the operating time of the catalyst payload by gradually bringing the entire catalyst charge into service instead of using it entirely from the start. It has indeed been surprisingly found that it is better to use the minimum quantity of catalyst rather than having a substantial excess at the start of operation, as is commonly done in order to compensate for the deactivation of the first part. bed.
  • the process which is the subject of the invention therefore consists in distributing the catalyst into several beds and preferably in the same reactor, but putting these beds into service successively, by adding a new catalyst bed at the head as soon as the need arises. is felt, that is to say when the performance of the mass of catalyst in operation is insufficient to give a product to the specifications.
  • the invention is a process for the hydrogenation of hydrocarbon feedstock by contact with p catalysts n1 ... n i ... n p , said beds being separated and containing the same catalyst, process characterized in that the feedstock is introduced into bed n p and the resulting product p p extracted, that, when the product p p does not reach the required quality, the introduction of the load in bed n p is stopped, and that simultaneously the load is introduced into bed n p-1 , the product obtained p p-1 being introduced into bed n p , and that then, generally, when the product p p reaches the minimum performance threshold, the introduction of the charge into bed n i is stopped, at the same time the charge is introduced into bed n i-1 , the product obtained p i-1 being introduced into read n i , and so on until i has taken all the integer values up to 1.
  • FIG. 1 represents the process applied with several separate reactors, FIG. 2 in a single reactor.
  • the known technique consisted in using an entire mass of catalyst to obtain a product p p having the required specifications, for a cycle time D (or operating time).
  • the reactor was stopped and the catalyst was regenerated.
  • the mass of catalyst or an amount less than this mass is divided into p beds (n1, n i , n p ) distributed in 1 or more reactors and each containing at least the minimum amount of catalyst necessary for obtaining the required specifications.
  • p beds n1, n i , n p
  • the feed of the load is moved to the bed n i-1 , located upstream of the bed n i , so that the load to be treated passes successively the bed n i-1 of new catalyst, then the product, coming from this bed through the spent catalyst bed ni, the product obtained pi crossing the spent catalyst bed n i + 1 etc ... until the bed n p is passed through, the product p p then being obtained.
  • valve 40 when p4 reaches its threshold , the valve 40 is closed (preferably progressively), thus stopping the introduction of charge into n4 and at the same time, the valve 30 is open so as to feed the bed n3 with the charge through the line 3.
  • the procedure is the same as above, forming the valve 30 while simultaneously opening the valve 20 for supplying the bed n2 via the pipe 2.
  • the product p ce from this bed then passes over the bed n3, the product p3 from n3 passes over the bed n4 and the final product p4 is extracted.
  • the hydrogen necessary for the reaction is brought for example by means of the pipes 41, 31, 21, 11 successively put into service on the reaction beds.
  • the use of a single reactor is particularly advantageous in terms of costs, but the reactor can only operate with a downflow, the bed n p having to be the lowest and the bed n1 the puys high.
  • the operator may also prefer to use smaller quantities of catalyst (total mass less than for comparable cycle times.
  • catalyst test unit comprising 4 reactors which can operate in series, the effluent from the first being transferred to the second then to the third and then to the fourth.
  • reactors modeling each bed consist of a steel tube 3 cm in diameter. Each of these reactors can be heated by an electric oven which makes it possible to maintain the desired temperature in each of the beds.
  • All of the reactors can be used as described above, that is to say N ° 1, N ° 2, N ° 3, N ° 4 but a device also makes it possible to use the reactor 4 only or else 3 and 4 in series, or 2, 3 and 4 in series.
  • catalyst LD 265 from the company Procatalyse containing 0.3% of palladium supported on alumina in the 4 reactors arranged in series at a rate of 100 cm3 per reactor.
  • This catalyst is reduced by hydrogen delivered for 6 hours at 150 ° C at a rate of 40 l / h.
  • the performances are measured by the variation of the maleic anhydride index (MAV) between the inlet of the first reactor and the outlet of the fourth.
  • MAV maleic anhydride index
  • the temperature is set at 80 ° C in all of the reactors at the start of operation and then regularly increased to 120 ° C to restore the conversion when it decreases.
  • the load gives an AVM of 106, the AVMs of the products are given as a function of time as well as the operating temperature in table 1.
  • Temperature MAV output 50 80 ⁇ 2 100 80 ⁇ 2 200 80 ⁇ 2 500 80 2.2 750 80 2.3 820 80 2.8 950 80 3.8 1160 95 ⁇ 2 1300 95 4 1400 110 ⁇ 2 1540 110 5 1600 120 ⁇ 2 1800 120 8 Table 1
  • a new reactor is put into service when the assembly in operation no longer makes it possible to obtain an AVM of less than 3 at output for a temperature of 80 ° C. Then, the temperature of the four reactors is gradually increased to restore performance.
  • the AVMs of the products are given as well as the arrangement of the reactors and the operating temperature as a function of time in Table 2. Walking time in hours Arrangement Temperature MAV output 50 4 80 ⁇ 2 100 4 80 ⁇ 2 200 4 80 2.4 500 4 80 2.8 600 4 80 3.8 700 3.4 80 ⁇ 2 800 3.4 80 ⁇ 2 1000 3.4 80 2.5 1200 3.4 80 3.2 1300 2,3,4 80 ⁇ 2 1400 2,3,4 80 ⁇ 2 1600 2,3,4 80 2.7 1800 2,3,4 80 3 1900 1,2,3,4 80 ⁇ 2 2000 1,2,3,4 80 ⁇ 2 2200 1,2,3,4 80 2.5 2400 1,2,3,4 80 3.8 2800 1,2,3,4 90 ⁇ 2 2950 1,2,3,4 90 3.7 3000 1,2,3,4 95 ⁇ 2 3280 1,2,3,4 95 2.6 3300 1,2,3,4 100 ⁇ 2 3480 1,2,3,4 100 3 3500 1,2,3,4 115 ⁇ 2 2590 1,2,3,4 115 3.7 3600 1,2,3,4 120 ⁇ 2 Table 2
  • LD 241 catalyst 400 cm3 of LD 241 catalyst from the Procatalyse company are available, containing 10% of nickel supported on alumina in the 4 reactors arranged in series at a rate of 100 cm3 per reactor.
  • This catalyst is reduced by hydrogen delivered for 15 hours at 400 ° C at a rate of 40 l / h.
  • the activity of the catalyst is then measured under the same conditions as in Example 1.
  • the AVMs of the products are given as a function of time as well as the operating temperature in table 3. Walking time in hours Temperature MAV output 40 80 ⁇ 2 70 80 ⁇ 2 100 80 2 400 80 4.2 420 95 ⁇ 2 470 95 2.7 500 95 3.2 520 110 ⁇ 2 540 110 ⁇ 2 600 110 3.1 620 120 ⁇ 2 640 120 ⁇ 2 650 120 2.5 670 120 2.9 700 120 3.2 Table 3
  • Table 4 presents the AVM of the products as well as the arrangement of the reactors and the operating temperature as a function of time.

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)
EP93400164A 1992-01-28 1993-01-25 Selektives Hydrierungsverfahren, insbesondere von Diolefinen in Benzin, mit einem Katalysator in aufeinander verwendeten Betten Expired - Lifetime EP0554151B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9200992A FR2686617B1 (fr) 1992-01-28 1992-01-28 Procede d'hydrogenation selective de charge hydrocarbonee avec des lets catalytiques mis en óoeuvre successivement.
FR9200992 1992-01-28

Publications (2)

Publication Number Publication Date
EP0554151A1 true EP0554151A1 (de) 1993-08-04
EP0554151B1 EP0554151B1 (de) 1996-07-10

Family

ID=39154468

Family Applications (1)

Application Number Title Priority Date Filing Date
EP93400164A Expired - Lifetime EP0554151B1 (de) 1992-01-28 1993-01-25 Selektives Hydrierungsverfahren, insbesondere von Diolefinen in Benzin, mit einem Katalysator in aufeinander verwendeten Betten

Country Status (8)

Country Link
US (1) US5306852A (de)
EP (1) EP0554151B1 (de)
JP (1) JPH05247475A (de)
CN (1) CN1045950C (de)
DE (1) DE69303505T2 (de)
ES (1) ES2093370T3 (de)
FR (1) FR2686617B1 (de)
IN (1) IN181752B (de)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0685552A1 (de) * 1994-06-01 1995-12-06 Institut Francais Du Petrole Verfahren und Anlage für die selektive Hydrierung von katalytischen Crackbenzinen
FR2724390A1 (fr) * 1994-09-08 1996-03-15 Inst Francais Du Petrole Hydrogenation selective de coupes hydrocarbonees renfermant des hydrocarbures monoinsatures et polyinsatures
WO1997024413A1 (fr) * 1995-12-27 1997-07-10 Institut Français Du Petrole Procede d'hydrogenation selective d'une coupe d'hydrocarbures
US5954950A (en) * 1995-09-07 1999-09-21 Institut Francais Du Petrole Intensive hydrofining of petroleum fractions

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5847251A (en) 1996-02-12 1998-12-08 Catalytic Distillation Technologies Multibed transalkylator and process
EP0921179A1 (de) * 1997-12-05 1999-06-09 Fina Research S.A. Herstellung von Olefinen
FR2970261B1 (fr) * 2011-01-10 2013-05-03 IFP Energies Nouvelles Procede d'hydrotraitement de charges lourdes d'hydrocarbures avec des reacteurs permutables incluant au moins une etape de permutation progressive
FR2970260B1 (fr) * 2011-01-10 2014-07-25 IFP Energies Nouvelles Procede d'hydrotraitement de charges lourdes d'hydrocarbures avec des reacteurs permutables incluant au moins une etape de court-circuitage d'un lit catalytique
EP2865440A1 (de) * 2013-10-28 2015-04-29 Haldor Topsoe A/S Verfahren und Reaktor für exotherme Reaktion
WO2017130081A1 (en) * 2016-01-27 2017-08-03 Sabic Global Technologies B.V. Processes and systems for increasing selectivity for light olefins in co2 hydrogenation

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1306238A (fr) * 1961-10-19 1962-10-13 Shell Int Research Procédé de raffinage d'essences obtenues par craquage et contenant des diènes
US3926784A (en) * 1973-08-22 1975-12-16 Gulf Research Development Co Plural stage residue hydrodesulfurization process with hydrogen sulfide addition and removal
EP0026508A1 (de) * 1979-09-26 1981-04-08 Shell Internationale Researchmaatschappij B.V. Verfahren und Apparat für den Demet-Prozess von Kohlenwasserstoffölen

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3705204A (en) * 1967-05-18 1972-12-05 Nippon Oil Co Ltd Process for recovering conjugated diolefins selectively from a c5 fraction
US4560815A (en) * 1983-04-25 1985-12-24 The Babcock & Wilcox Company Automated catalyst regeneration in a reactor
US4704492A (en) * 1986-12-24 1987-11-03 Mobil Oil Corporation Selective hydrogenation of acetylenic impurities in crude butadiene
GB8702654D0 (en) * 1987-02-06 1987-03-11 Davy Mckee Ltd Process

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1306238A (fr) * 1961-10-19 1962-10-13 Shell Int Research Procédé de raffinage d'essences obtenues par craquage et contenant des diènes
US3926784A (en) * 1973-08-22 1975-12-16 Gulf Research Development Co Plural stage residue hydrodesulfurization process with hydrogen sulfide addition and removal
EP0026508A1 (de) * 1979-09-26 1981-04-08 Shell Internationale Researchmaatschappij B.V. Verfahren und Apparat für den Demet-Prozess von Kohlenwasserstoffölen

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0685552A1 (de) * 1994-06-01 1995-12-06 Institut Francais Du Petrole Verfahren und Anlage für die selektive Hydrierung von katalytischen Crackbenzinen
FR2720754A1 (fr) * 1994-06-01 1995-12-08 Inst Francais Du Petrole Procédé et installation pour le traitement par hydrogénation sélective d'une essence de craquage catalytique.
FR2724390A1 (fr) * 1994-09-08 1996-03-15 Inst Francais Du Petrole Hydrogenation selective de coupes hydrocarbonees renfermant des hydrocarbures monoinsatures et polyinsatures
EP0700984A3 (de) * 1994-09-08 1996-04-10 Inst Francais Du Petrole
US5817901A (en) * 1994-09-08 1998-10-06 Institut Francais Du Petrole Selective hydrogenation of hydrocarbon cuts containing monounsaturated and polyunsaturated hydrocarbons
US5954950A (en) * 1995-09-07 1999-09-21 Institut Francais Du Petrole Intensive hydrofining of petroleum fractions
WO1997024413A1 (fr) * 1995-12-27 1997-07-10 Institut Français Du Petrole Procede d'hydrogenation selective d'une coupe d'hydrocarbures

Also Published As

Publication number Publication date
EP0554151B1 (de) 1996-07-10
DE69303505T2 (de) 1996-11-21
FR2686617B1 (fr) 1994-03-18
FR2686617A1 (fr) 1993-07-30
ES2093370T3 (es) 1996-12-16
CN1092756A (zh) 1994-09-28
CN1045950C (zh) 1999-10-27
DE69303505D1 (de) 1996-08-14
JPH05247475A (ja) 1993-09-24
IN181752B (de) 1998-09-12
US5306852A (en) 1994-04-26

Similar Documents

Publication Publication Date Title
CA1117146A (fr) Procede catalytique de reformage ou de production d'hydrocarbures aromatiques
EP0450997B1 (de) Verfahren zur Wasserstoffbehandlung von Erdölrückstand oder Schweröl zur Raffination und Umwandlung zu leichteren Schnitten
EP0554151B1 (de) Selektives Hydrierungsverfahren, insbesondere von Diolefinen in Benzin, mit einem Katalysator in aufeinander verwendeten Betten
FR2681871A1 (fr) Procede d'hydrotraitement d'une fraction lourde d'hydrocarbures en vue de la raffiner et de la convertir en fractions plus legeres.
WO2006067305A1 (fr) Procede de conversion directe d’une charge comprenant des olefines a quatre et/ou cinq atomes de carbone, pour la production de propylene avec une co-production d’essence
FR2784687A1 (fr) Procede d'hydrotraitement d'une fraction lourde d'hydrocarbures avec reacteurs permutables et introduction d'un distillat moyen
EP1343857A1 (de) Wasserstoffbehandlungsverfahren einer schweren kohlenwasserstofffraktion mit schaltbaren und kurzschliessbaren reaktoren
FR2761907A1 (fr) Procede et dispositif a combustion etagee pour la regeneration d'un catalyseur de reformage ou de production d'aromatiques en lit mobile
FR2746673A1 (fr) Procede de regeneration d'un catalyseur d'hydrogenation selective de diolefines et de nitriles
EP1346010B2 (de) Verbessertes flexibles verfahren zur herstellung von grundölen und destillaten durch hydroisomerisierung-konversion an einem schwach dispergierten katalysator und anschliessende katalytische entparaffinierung
EP0685552B1 (de) Verfahren und Anlage für die selektive Hydrierung von katalytischen Crackbenzinen
EP4189038A1 (de) Verfahren zur behandlung von kunststoffpyrolyseölen mit zweistufigem hydrocracking
CA3200635A1 (fr) Procede de traitement d'huiles de pyrolyse de plastiques incluant une etape d'hydrogenation
FR2818283A1 (fr) Procede de traitement d'une charge hydrocarbonee comprenant une etape d'hydrotraitement en lit fixe a contre-courant
EP1242568B1 (de) Verfahren und anlage zur herstellung von aromaten in wanderbett mit katalysator reduktion
EP1281669A1 (de) Verfahren zur Rückgewinnung von Wasserstoff aus einem Kohlenwasserstoffabgas mittels eines Membranreaktors
FR2852323A1 (fr) Nouveau procede de reformage regeneratif
EP3184610B1 (de) Selektives hydrierverfahren von olefinischen ladungen mit einem einzigen hauptreaktor und einem schutzreaktor geringerer grösse
FR3054558A1 (fr) Procede multi-lits en un seul reacteur a lit fixe pour l'hydrogenation selective et l'hydrodesulfuration d'essence de pyrolyse
FR2777806A1 (fr) Procede de regeneration en mode degrade d'un catalyseur
EP1252259B1 (de) Verfahren und vorrichtung zur herstellung aromatischer verbindungen unter verwendung katalytischer reduktion
WO2020144097A1 (fr) Procede d'hydrocraquage en deux etapes comprenant une etape d'hydrogenation en aval de la deuxieme etape d'hydrocraquage pour la production de distillats moyens
WO2020144096A1 (fr) Procede d'hydrocraquage en deux etapes comprenant une etape d'hydrogenation en amont de la deuxieme etape d'hydrocraquage pour la production de distillats moyens
FR3081166A1 (fr) Procédé de séparation des n paraffines et des isoparaffines d’une huile d’hydrocarbures
CA2372620C (fr) Procede de conversion de fractions lourdes petrolieres pour produire une charge de craquage catalytique et des distillats moyens de faible teneur en soufre

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 NL PT SE

17P Request for examination filed

Effective date: 19940127

17Q First examination report despatched

Effective date: 19950913

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

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

ITF It: translation for a ep patent filed

Owner name: DE DOMINICIS & MAYER S.R.L.

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

AK Designated contracting states

Kind code of ref document: B1

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

REF Corresponds to:

Ref document number: 69303505

Country of ref document: DE

Date of ref document: 19960814

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

Effective date: 19960820

SC4A Pt: translation is available

Free format text: 960712 AVAILABILITY OF NATIONAL TRANSLATION

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2093370

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
REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

REG Reference to a national code

Ref country code: DE

Ref legal event code: R081

Ref document number: 69303505

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: PT

Payment date: 20111206

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: 20120207

Year of fee payment: 20

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

Ref country code: BE

Payment date: 20120126

Year of fee payment: 20

Ref country code: IT

Payment date: 20120120

Year of fee payment: 20

Ref country code: GB

Payment date: 20120125

Year of fee payment: 20

Ref country code: SE

Payment date: 20120125

Year of fee payment: 20

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

Ref country code: NL

Payment date: 20120130

Year of fee payment: 20

REG Reference to a national code

Ref country code: DE

Ref legal event code: R071

Ref document number: 69303505

Country of ref document: DE

REG Reference to a national code

Ref country code: NL

Ref legal event code: V4

Effective date: 20130125

BE20 Be: patent expired

Owner name: INSTITUT FRANCAIS DU *PETROLE

Effective date: 20130125

REG Reference to a national code

Ref country code: PT

Ref legal event code: MM4A

Free format text: MAXIMUM VALIDITY LIMIT REACHED

Effective date: 20130125

REG Reference to a national code

Ref country code: GB

Ref legal event code: PE20

Expiry date: 20130124

REG Reference to a national code

Ref country code: SE

Ref legal event code: EUG

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: 20130124

Ref country code: DE

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20130126

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 EXPIRATION OF PROTECTION

Effective date: 20130201

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

Ref country code: ES

Payment date: 20120126

Year of fee payment: 20

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20130725

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: 20130126