EP0768363B1 - Process for reducing the viscosity of heavy oil residues - Google Patents

Process for reducing the viscosity of heavy oil residues Download PDF

Info

Publication number
EP0768363B1
EP0768363B1 EP96202825A EP96202825A EP0768363B1 EP 0768363 B1 EP0768363 B1 EP 0768363B1 EP 96202825 A EP96202825 A EP 96202825A EP 96202825 A EP96202825 A EP 96202825A EP 0768363 B1 EP0768363 B1 EP 0768363B1
Authority
EP
European Patent Office
Prior art keywords
residue
thermal
visbreaking
heavy oil
heavy
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
EP96202825A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0768363A1 (en
Inventor
Franco Lattarulo
Pierluigi Bozza
Giacomo Rispoli
Agostino Cavanna
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.)
Agip Petroli SpA
Original Assignee
Agip Petroli SpA
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 Agip Petroli SpA filed Critical Agip Petroli SpA
Priority to SI9630137T priority Critical patent/SI0768363T1/xx
Publication of EP0768363A1 publication Critical patent/EP0768363A1/en
Application granted granted Critical
Publication of EP0768363B1 publication Critical patent/EP0768363B1/en
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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/023—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only thermal cracking steps

Definitions

  • the present invention relates to a process for reducing the viscosity of heavy oil residues.
  • visbreaking processes are widely used, described for example in Beuther et al. "Thermal Visbreaking of Heavy Residues", The Oil and Gas Journal", 57:46, Nov.9, 1959, pages 151-175; or described in Rhoe et al. "Visbreaking: A Flexible Process", Hydrocarbon Processing, January 1979, pages 131-136.
  • the above processes can be applied to various refinery streams, such as atmospheric or vacuum residues, furfural-extracts, propane-deasphalted tars, catalytic cracking bottoms.
  • Visbreaking processes are thermal processes, carried out under comparatively mild conditions, which produce lighter hydrocarbon fractions. Visbreaking processes typically produce gases, l.p.g., naphtha and gas oil, heavy distillates.
  • Visbreaking processes are often accompanied by thermal cracking processes in which the heavy vacuum gas oil coming from visbreaking, is subjected to thermal cracking under more drastic conditions than the previous visbreaking step. In this way other lighter fractions are recovered.
  • the present invention relates to a process for reducing the viscosity of heavy oil residues, which comprises a first step for the visbreaking (I) of heavy oil residues and a second step for the thermal cracking (II) of the heavy gas oil formed during the visbreaking process, the above thermal cracking producing a thermal residue as well as lighter products, said process being characterized in that:
  • visbreaking means the process, well known in the prior art, for reducing the viscosity of heavy oil fractions.
  • the above visbreaking processes can be carried out, as is known, on the heavy oil residue without or in the presence of hydrogen (hydrovisbreaking), or in the presence of so-called hydrogen donor solvents (see for example US-A-2.953.513), or in the presence of hydrogen and donor solvent (see US-A-4.292.168) and also in the presence of catalysts (see for example US-A-5.057.204).
  • the visbreaking process (I) is carried out without hydrogen, catalysts and hydrogen donor solvents. It consists in feeding the heavy oil residue into an oven heated to the desired temperature for a preset time.
  • reaction temperature As in most oil processes, there is a correlation between reaction temperature and residence time of the reagents. One visbreaking process will therefore be more rigid than another if, at the same temperature, the residence time is greater.
  • the visbreaking process can usually be carried out with one or more ovens, but in any case the temperature of the visbreaking oven or ovens is between 350 and 525°C, preferably between 380 and 500°C, with a residence time of between 2 and 20 minutes, preferably between 3 and 10.
  • the heavy oil residues to be subjected to the visbreaking step (I) can come from various refinery streams.
  • the visbreaking process can therefore be applied to a variety of heavy oil fractions, such as vacuum residues, atmospheric residues, furfural-extracts, propane-deasphalted tars, catalytic cracking bottoms, asphalts.
  • heavy oil fractions such as vacuum residues, atmospheric residues, furfural-extracts, propane-deasphalted tars, catalytic cracking bottoms, asphalts.
  • at least 75% by weight of the components of the heavy oil residue has a boiling point which is higher than 370°C.
  • the above heavy oil residues can also contain impurities due to heteroatoms, for example nitrogen or sulphur, and metals, particularly Vanadium.
  • the heavy oil residue fed to the visbreaking step (I) basically consists of atmospheric residue.
  • Atmospheric residues usually have the following characteristics: density of between 0.940 and 1,000 g/cm 3 ; initial distillation point (according to ASTM D 1160 method), of between 180 and 220°C; temperature at which 5% in volume distills from 330 to 370°C; temperature at which 10% in volume distills from 380 to 410°C; temperature at which 50% in volume distills from 490 to 520°C.
  • the visbreaking step (I) produces numerous hydrocarbon fractions.
  • the following fractions are normally recovered: a) gases and l.p.g., b) naphtha, c) gas oil, d) heavy vacuum distillate, e) vacuum residue + fuel oil and/or tar.
  • the separation of the visbreaking products into the above fractions is irrelevant. It is preferably however to recover the fractions with a high additional value such as naphtha and gas oil.
  • HVGO high vacuum gas oil
  • This heavy vacuum gas oil is usually recovered, at least mostly, by distillation under vacuum, normally at about 20-40 mm Hg.
  • Heavy vacuum gas oil can be recovered as a column bottom from a distillation column at atmospheric pressure, or at pressures slightly higher than atmospheric pressure, usually at pressures of 2-4 bars.
  • the characteristics of this fraction i.e. column residue at atmospheric pressure
  • reference to heavy vacuum gas oil obtained downstream of the vis-breaking process (I) means both that which is recovered by distillation at reduced pressure, and that recovered as an atmospheric residue.
  • Part or all of the heavy vacuum gas oil thus separated is fed to the thermal cracking step (II).
  • the remaining part can be any other oil fraction having the same physico-chemical characteristics mentioned above for the heavy vacuum gas oil.
  • the vacuum residue of the topping is a typical fraction which can possibly be used in the feeding of the thermal cracking (II) together with the heavy vacuum gas oil recovered downstream of the visbreaking process.
  • thermal cracking step it is preferably however for the thermal cracking step to be fed with all the heavy vacuum gas oil fraction recovered after the visbreaking.
  • the thermal cracking oven has dimensions for operating with quantities of heavy vacuum gas oil which are smaller than the isolated quantities after the visbreaking step, it will be necessary to bleed part of the heavy vacuum gas oil or separate only the desired quantity.
  • the thermal cracking step (II) is carried out under more severe conditions than the visbreaking step (I), and therefore either at higher temperatures, with the same residence time, or with greater residence times, at the same temperature.
  • the temperature of the thermal cracking step (II) is usually between 450 and 510°C and the residence times are between 20 and 60 minutes.
  • thermal residue is recovered, which consists of what results from the thermal cracking after removing the light fractions (350°C-).
  • the stream leaving the thermal cracking is normally fed into a separator where the lighter fractions, those at 350°C-, are separated.
  • the remaining product consists of the thermal residue, which has a density at 15°C of between 1.00 and 1.07, a P value (determined by the Shell method Nr. 1600 of 1983) of between 1.4 and 2.3, an initial distillation point (according to the regulation ASTM D 1160), of between 180 and 220°C, the temperature at which 50% distills of between 440 and 490°C, the temperature at which 90% distills of between 570 and 610°C.
  • the thermal residue thus recovered is mixed with another heavy oil residue, the same or different from the initial charge, and the mixture thus obtained is refed to the visbreaking step (I).
  • the mixture of heavy oil residue and thermal residue preferably consists of 5-50% by weight, more preferably from 10 to 40% by weight, even more preferably from 20 to 30% by weight, of thermal residue, the complement to 100 consisting of the heavy oil fraction.
  • the process of the present invention allows almost all the thermal residue to be eliminated in a combined visbreaking + thermal cracking plant.
  • FIG 1 represents the process scheme of the present invention.
  • (A) represents the vis-breaking plant
  • (1) is the heavy oil residue
  • (2) is the light Vacuum Gas oil
  • (3) is the heavy Vacuum Gas oil
  • (4) is the Visbreaking Residue
  • (5) is the external heavy vacuum Gas oil
  • (6) is the residue recycled from the fractionation unit
  • (7) is the thermal Residue.
  • FIG 1 shows the Visbreaker plant (A), fed by the heavy oil residue (1).
  • a light stream is obtained, which is sent to an atmospheric distillation unit (D), and a heavy stream, which is sent to a distillation unit under vacuum (B).
  • a light vacuum gas oil fraction is obtained (2), which is fed to the atmospheric distillation unit (D), together with the heavy vacuum gas oil fraction (3), and a visbreaking residue, which will be used as a component for fuel oils.
  • the heavy vacuum gas oil fraction (3) forms the charge for the Thermal Cracker plant (C), together with the heavy gas oil obtained as residue (6) of the atmospheric fractionation unit (D), and together with possible charges of a similar composition, of a different origin.
  • a light fraction is obtained from the Thermal Cracker plant (C), which is fed to the atmospheric distillation unit (D), and a thermal residue, which is recycled to the Visbreaker plant.
  • Figure 2 shows, for comparative purposes, a conventional process of the prior art, in which, there is no recycling of the thermal residue at the end of the thermal cracking step.
  • the feeding to the Thermal Cracking (II) had the following characteristics: Density at 15°C 0.975 Conradson carbonaceous residue 1.04% Distillation ASTM D1160 Initial boiling point 275°C 5% Volume evaporated 325°C 10% Volume evaporated 348°C 20% Volume evaporated 375°C 30% Volume evaporated 398°C 40% Volume evaporated 414°C 50% Volume evaporated 436°C 60% Volume evaporated 448°C 70% Volume evaporated 468°C 80% Volume evaporated 485°C 90% Volume evaporated 510°C 95% Volume evaporated 535°C Final point 587°C
  • the feeding to the Thermal Cracking consists (in both tests 1 and 2) of 60% of HVGO from the distillation unit under vacuum (B), 30% from the bottom of the atmospheric fractionation unit (D), and the remaining 10% of heavy gas oil ex vacuum pot of the topping, the latter fraction obviously coming from other parts of the refinery.
  • test 1 the thermal residue was mixed with other heavy oil residue, and the whole mixture was sent to the visbreaking step (I).
  • the above composition consisted of 25% of thermal residue and the remaining 75% of fresh heavy oil residue.
  • test 1 was carried out recycling almost all of the thermal residue leaving the thermal cracking step
  • comparative test 2 was carried out according to the scheme of figure 2, i.e. without recycling the thermal residue obtained leaving the thermal cracking step.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (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)
  • Lubricants (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
EP96202825A 1995-10-13 1996-10-10 Process for reducing the viscosity of heavy oil residues Expired - Lifetime EP0768363B1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
SI9630137T SI0768363T1 (en) 1995-10-13 1996-10-10 Process for reducing the viscosity of heavy oil residues

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ITMI952099 1995-10-13
IT95MI002099A IT1276930B1 (it) 1995-10-13 1995-10-13 Procedimento per ridurre la viscosita' di residui petroliferi pesanti

Publications (2)

Publication Number Publication Date
EP0768363A1 EP0768363A1 (en) 1997-04-16
EP0768363B1 true EP0768363B1 (en) 1999-12-29

Family

ID=11372354

Family Applications (1)

Application Number Title Priority Date Filing Date
EP96202825A Expired - Lifetime EP0768363B1 (en) 1995-10-13 1996-10-10 Process for reducing the viscosity of heavy oil residues

Country Status (17)

Country Link
EP (1) EP0768363B1 (cs)
AT (1) ATE188237T1 (cs)
BG (1) BG62815B1 (cs)
CZ (1) CZ292215B6 (cs)
DE (1) DE69605881T2 (cs)
DK (1) DK0768363T3 (cs)
EA (1) EA000032B1 (cs)
ES (1) ES2142016T3 (cs)
GR (1) GR3032398T3 (cs)
HR (1) HRP960464B1 (cs)
HU (1) HU218833B (cs)
IT (1) IT1276930B1 (cs)
PL (1) PL182542B1 (cs)
PT (1) PT768363E (cs)
RO (1) RO119310B1 (cs)
SI (1) SI0768363T1 (cs)
SK (1) SK281664B6 (cs)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7740750B2 (en) 2005-07-11 2010-06-22 Ge Betz, Inc. Application of visbreaker analysis tools to optimize performance
US8398849B2 (en) 2005-07-11 2013-03-19 General Electric Company Application of visbreaker analysis tools to optimize performance
WO2016069435A1 (en) * 2014-10-28 2016-05-06 Uop Llc Process for converting a vacuum tower bottoms stream

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007117919A2 (en) 2006-03-29 2007-10-18 Shell Oil Company Improved process for producing lower olefins from heavy hydrocarbon feedstock utilizing two vapor/liquid separators
CA2644355C (en) 2006-03-29 2014-11-25 Shell Internationale Research Maatschappij B.V. Process for producing lower olefins

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2054637B (en) * 1979-07-27 1983-04-07 Uop Inc Visbreaking process
SU1033532A1 (ru) * 1981-06-29 1983-08-07 Горьковский Государственный Институт По Проектированию Предприятий Нефтеперерабатывающей И Нефтехимической Промышленности Способ получени котельного топлива
US4508614A (en) * 1982-11-08 1985-04-02 Mobil Oil Corporation Visbreaker performance for production of heating oil
US4504377A (en) * 1983-12-09 1985-03-12 Mobil Oil Corporation Production of stable low viscosity heating oil
JPS61163991A (ja) * 1985-01-16 1986-07-24 Fuji Standard Res Kk 炭素繊維用原料として好適なピツチの連続的製造方法
DE3504941A1 (de) * 1985-02-13 1986-08-14 Linde Ag, 6200 Wiesbaden Verfahren zur spaltung eines kohlenwasserstoffeinsatzes
US4836909A (en) * 1985-11-25 1989-06-06 Research Association For Residual Oil Processing Process of thermally cracking heavy petroleum oil
DD249916B1 (de) * 1986-06-10 1989-11-22 Petrolchemisches Kombinat Verfahren zur erzeugung heller produkte und konventionell verwertbaren heizoeles aus schweren metall- und schwefelreichen erdoelrueckstaenden

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7740750B2 (en) 2005-07-11 2010-06-22 Ge Betz, Inc. Application of visbreaker analysis tools to optimize performance
US8398849B2 (en) 2005-07-11 2013-03-19 General Electric Company Application of visbreaker analysis tools to optimize performance
US8597484B2 (en) 2005-07-11 2013-12-03 General Electric Company Application of visbreaker analysis tools to optimize performance
WO2016069435A1 (en) * 2014-10-28 2016-05-06 Uop Llc Process for converting a vacuum tower bottoms stream

Also Published As

Publication number Publication date
BG62815B1 (bg) 2000-08-31
DK0768363T3 (da) 2000-04-17
DE69605881D1 (de) 2000-02-03
HUP9602821A3 (en) 1997-09-29
SK130396A3 (en) 1997-07-09
EA199600082A1 (ru) 1997-06-30
SK281664B6 (sk) 2001-06-11
ITMI952099A0 (cs) 1995-10-13
BG100905A (en) 1997-07-31
PL316489A1 (en) 1997-04-14
GR3032398T3 (en) 2000-05-31
ITMI952099A1 (it) 1997-04-13
DE69605881T2 (de) 2000-06-15
ATE188237T1 (de) 2000-01-15
HU218833B (hu) 2000-12-28
HRP960464A2 (en) 1998-06-30
EP0768363A1 (en) 1997-04-16
PT768363E (pt) 2000-04-28
CZ296396A3 (en) 1997-06-11
HU9602821D0 (en) 1996-11-28
CZ292215B6 (cs) 2003-08-13
HRP960464B1 (en) 2000-12-31
SI0768363T1 (en) 2000-04-30
IT1276930B1 (it) 1997-11-03
RO119310B1 (ro) 2004-07-30
HUP9602821A2 (en) 1997-05-28
EA000032B1 (ru) 1998-02-26
ES2142016T3 (es) 2000-04-01
PL182542B1 (pl) 2002-01-31

Similar Documents

Publication Publication Date Title
CA1127989A (en) Process for producing premium coke from vacuum residuum
US4200519A (en) Process for the preparation of gas oil
US4519898A (en) Low severity delayed coking
US4534854A (en) Delayed coking with solvent separation of recycle oil
EP0175511B1 (en) Visbreaking process
US2777802A (en) Extractive distillation operation for preparation of catalytic cracking feed stocks
US4389302A (en) Process for vis-breaking asphaltenes
US4201659A (en) Process for the preparation of gas oil
US7033486B2 (en) Residuum conversion process
US5089114A (en) Method for processing heavy crude oils
EP0768363B1 (en) Process for reducing the viscosity of heavy oil residues
US4501654A (en) Delayed coking process with split fresh feed and top feeding
US4235702A (en) Hydrocarbon processing
US4673485A (en) Process for increasing deasphalted oil production from upgraded residua
US4492625A (en) Delayed coking process with split fresh feed
US4434045A (en) Process for converting petroleum residuals
US4497705A (en) Fluid coking with solvent separation of recycle oil
EP3722392B1 (en) System and process for production of anisotropic coke
DE2914010A1 (de) Verfahren zur umwandlung von hochsiedenden kohlenwasserstoffrueckstaenden
US4859284A (en) Combined process for the separation and continuous coking of high softening point asphaltenes
US5000838A (en) Low efficiency deasphalting and catalytic cracking
EP0249052B1 (en) Process to produce light products and fuel oils for conventional use from heavy metal- and sulfur-rich crude oil residues
US4425224A (en) Process for converting petroleum residuals
CA1178231A (en) Process for obtaining a synthetic crude petroleum
US2944958A (en) Process of making pitch

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): AT BE CH DE DK ES FI FR GB GR IE LI LU MC NL PT SE

AX Request for extension of the european patent

Free format text: LT PAYMENT 961010;LV PAYMENT 961010;SI PAYMENT 961010

17P Request for examination filed

Effective date: 19970702

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

17Q First examination report despatched

Effective date: 19990218

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

RBV Designated contracting states (corrected)

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

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 LI LU MC NL PT SE

AX Request for extension of the european patent

Free format text: LT PAYMENT 19961010;LV PAYMENT 19961010;SI PAYMENT 19961010

REF Corresponds to:

Ref document number: 188237

Country of ref document: AT

Date of ref document: 20000115

Kind code of ref document: T

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: CH

Ref legal event code: NV

Representative=s name: PATENTANWAELTE SCHAAD, BALASS, MENZL & PARTNER AG

REF Corresponds to:

Ref document number: 69605881

Country of ref document: DE

Date of ref document: 20000203

ET Fr: translation filed
REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2142016

Country of ref document: ES

Kind code of ref document: T3

REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

REG Reference to a national code

Ref country code: PT

Ref legal event code: SC4A

Free format text: AVAILABILITY OF NATIONAL TRANSLATION

Effective date: 20000107

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: SI

Ref legal event code: IF

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

Ref country code: MC

Payment date: 20080918

Year of fee payment: 13

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

Ref country code: LU

Payment date: 20081031

Year of fee payment: 13

Ref country code: CH

Payment date: 20081027

Year of fee payment: 13

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

Ref country code: PT

Payment date: 20090923

Year of fee payment: 14

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

Ref country code: SE

Payment date: 20091028

Year of fee payment: 14

Ref country code: IE

Payment date: 20091026

Year of fee payment: 14

Ref country code: FI

Payment date: 20091029

Year of fee payment: 14

Ref country code: ES

Payment date: 20091026

Year of fee payment: 14

Ref country code: DK

Payment date: 20091026

Year of fee payment: 14

Ref country code: DE

Payment date: 20091028

Year of fee payment: 14

Ref country code: AT

Payment date: 20090921

Year of fee payment: 14

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

Ref country code: NL

Payment date: 20091024

Year of fee payment: 14

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

Ref country code: GB

Payment date: 20091026

Year of fee payment: 14

Ref country code: FR

Payment date: 20091029

Year of fee payment: 14

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

Ref country code: MC

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

Effective date: 20091031

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

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

Ref country code: GR

Payment date: 20091030

Year of fee payment: 14

Ref country code: BE

Payment date: 20091201

Year of fee payment: 14

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: 20091031

Ref country code: CH

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

Effective date: 20091031

REG Reference to a national code

Ref country code: PT

Ref legal event code: MM4A

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

Effective date: 20110411

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: 20091010

BERE Be: lapsed

Owner name: *AGIP PETROLI S.P.A.

Effective date: 20101031

REG Reference to a national code

Ref country code: NL

Ref legal event code: V1

Effective date: 20110501

LTLA Lt: lapse of european patent or patent extension

Effective date: 20101010

REG Reference to a national code

Ref country code: DK

Ref legal event code: EBP

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20101010

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: 20110411

Ref country code: GR

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

Effective date: 20110503

Ref country code: FR

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

Effective date: 20101102

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20110630

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

REG Reference to a national code

Ref country code: DE

Ref legal event code: R119

Ref document number: 69605881

Country of ref document: DE

Effective date: 20110502

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

Ref country code: FI

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

Effective date: 20101010

Ref country code: BE

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

Effective date: 20101031

Ref country code: AT

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

Effective date: 20101010

Ref country code: NL

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

Effective date: 20110501

Ref country code: GB

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

Effective date: 20101010

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 NON-PAYMENT OF DUE FEES

Effective date: 20101011

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 NON-PAYMENT OF DUE FEES

Effective date: 20101011

Ref country code: DK

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

Effective date: 20101031

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20111118

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: 20101011

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: 20110502