EP0609191B1 - Vorrichtung zum thermischen Spalten eines Gemisches mit flüssigen und gasförmigen Kohlenwasserstoffen - Google Patents

Vorrichtung zum thermischen Spalten eines Gemisches mit flüssigen und gasförmigen Kohlenwasserstoffen Download PDF

Info

Publication number
EP0609191B1
EP0609191B1 EP94890007A EP94890007A EP0609191B1 EP 0609191 B1 EP0609191 B1 EP 0609191B1 EP 94890007 A EP94890007 A EP 94890007A EP 94890007 A EP94890007 A EP 94890007A EP 0609191 B1 EP0609191 B1 EP 0609191B1
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
mixture
line
liquid
gas
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
EP94890007A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0609191A1 (de
Inventor
Peter Dipl.-Ing. Illyes
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.)
OMV Downstream GmbH
Original Assignee
OMV AG
OEMV AG
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 OMV AG, OEMV AG filed Critical OMV AG
Publication of EP0609191A1 publication Critical patent/EP0609191A1/de
Application granted granted Critical
Publication of EP0609191B1 publication Critical patent/EP0609191B1/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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means

Definitions

  • the invention relates to a device for thermal splitting of a mixture with liquid and gaseous hydrocarbons in heat exchangers.
  • gaseous hydrocarbons are also used. These gaseous hydrocarbons come from mostly from the processing facilities according to Splitting plants or production plants for the most varied Product blends. This gaseous Products are usually delivered to the slitting line leading supply lines for the liquid hydrocarbons initiated. As a result, the range of uses of the Plant significantly increased and on the other hand occurs a substantial reduction in piping since parallel pipelines, u. for the gaseous Hydrocarbons and the liquid hydrocarbons, can be avoided.
  • the hydrocarbon mixtures usually need to be in several stages up to the temperature of the thermal Cleavage to be heated.
  • the throughput in each Stages, d. H. the heat exchangers is usually by volume, especially in the first stage, on partial evaporation of liquid hydrocarbons.
  • the device according to the invention for thermal splitting a mixture of liquid and gaseous hydrocarbons, with at least one pipe for that Mixture opens into a heat exchanger, which if necessary with one leading out of the heat exchanger Pipeline through a detour line with one in flow controllable shut-off device is fluidly connected, and the pipeline leading from the heat exchanger into which at least one more pipe for overheated Water vapor flows into another Heat exchanger opens, the output line in one downstream heat exchanger, if necessary with Catalyst, opens, the outlet line in a cooling and Splitting device opens, essentially exists in that seen in the direction of flow before Heat exchanger at least one gas separator for the Separation of a gaseous fraction from the mixture is provided, the detour line being a gas line, which has a shut-off device which can be regulated in the flow, from the gas separator into another heat exchanger, in particular via the further pipeline.
  • the gaseous in front of the first heat exchanger Portion separated from the starting product mixture double supply lines for the liquid or gaseous starting products can be avoided. Furthermore a mixture enters the heat exchanger, which can be essentially gas-free, so that the preferred Heat exchange to the liquid products can take place which due to the higher specific heat of Liquids are particularly effective against gases can.
  • the gas can pass through a gas separator Pipeline either in the further heat exchanger or already opens into the actual cracking furnace, be led.
  • the gas line thus serves as a detour line for the first heat exchanger, which also means the temperature the heat exchange medium, e.g. B. flue gases controlled can be. On the one hand, this allows a particularly high Heat exchange can be achieved, on the other hand one too great cooling, e.g. B. the flue gases, and thus one Falling below the dew point temperature and thus occurring corrosion can be avoided.
  • gas separator is designed as a gravity separator, so can be a simple one without great pressure loss Separation of the gaseous components from the gas / liquid mixture respectively.
  • a particularly effective separation between gas and Liquid can be done via a cyclone.
  • the gas line opens into the gas separator Flow direction seen before the further line for the Water vapor in the outgoing pipe from the heat exchanger, so can already in the further heat exchanger a product mixture of the liquid hydrocarbons, the gaseous hydrocarbons and water vapor occur so that the partial steam lowering in the Heat exchanger is taken into account particularly cheaply, which makes the liquid hydrocarbons particularly quick can evaporate and another high absorption of heat is achieved in this heat exchanger.
  • the gas line flows from the gas separator into the downstream heat exchanger, i.e. in the cracking furnace, especially in the output line from the rest Heat exchanger, so with a particularly large range of gaseous products in the mixture also in the further Heat exchanger a heat transfer without disadvantageous Influencing the gaseous starting products achieved will.
  • the gas line flows from the gas separator into the other Pipe for the water vapor, so a mixture of Water vapor and gaseous products can be achieved in turn then into the supply line for the further Heat exchanger can be initiated.
  • the gas line flows out of the gas separator into one Steam superheater, so the gas along with the water vapor be heated.
  • a shut-off device which can be regulated in the flow, provided by the pipeline after the Gas separator, which opens into the heat exchanger, branches off, and preferably in the further pipeline after the Confluence of the gas pipeline, so can also bursty oversupply of liquid hydrocarbons without pressure overload of the heat exchanger intercepted and controlled if necessary.
  • Heat exchangers can also be used as groups of heat exchangers be constructed.
  • the pipes R 1 and R 2 which conduct liquid hydrocarbons (gasoline) or gaseous hydrocarbons with two to four carbon atoms, lead to the pipe R 3 , which in turn opens into the gas separator G.
  • the liquid products are then passed through the pipe R 3 into the heat exchanger W 1 .
  • the gaseous products from the gas separator G pass through the gas line G 1 , which serves as a detour line for the heat exchanger W 1 , into the pipeline R 4 leading from the heat exchanger W 1 .
  • a steam line D 1 which forwards the steam from the steam superheater D, also opens into this pipeline R 4 .
  • the further heat exchanger W 2 in which the pipeline R 4 opens, is connected via an output line R 5 to the cracking furnace, the downstream heat exchanger S.
  • a pipe R 6 leads from the heat exchanger S into a cooling and separation device K + A.
  • the steam superheater D in which steam is optionally generated, the cracking furnace, the heat exchanger S and the heat exchangers W 1 and W 2 are designed as shell-and-tube heat exchangers, with flue gas serving as the heat transfer medium.
  • a valve V 1 which can be regulated in the flow can be provided in the gas line G 1 and is closed when it is desired that the entire product mixture is passed through the pipe R 3 into the heat exchanger W 1 .
  • a gas line G 2 can also lead into the outlet line R 5 of the heat exchanger W 2 , or, like the gas line G 3, also lead directly into the cracking furnace, the heat exchanger S.
  • These gas lines can have valves V 2 and V 3 which can be regulated in the flow.
  • the gas can be fed via a line G 4 to the steam superheater D or, if appropriate, to a steam generator.
  • a further detour line U 1 can also be provided, which branches off from the pipe line R 3 in front of the heat exchanger W 1 and opens into the pipe line R 4 after the heat exchanger W 1 .
  • This detour line U 1 has a flow controllable valve V 4 .
  • the heat exchangers W 1 and W 2 as well as the steam superheater D and the cracking furnace, the heat exchanger S are successively flowed through by flue gases, which serve as heat exchange medium.
  • the flue gases pass according to arrow X 1 through the cracking furnace, the heat exchanger S, then into a high-pressure steam superheater, not shown, in which high-pressure steam can be generated, which does not have to be fed to the process.
  • the flue gas then enters the steam superheater D according to the arrow X 3, in which process steam is introduced according to the arrow Z.
  • the flue gas From the steam superheater D, the flue gas enters according to the arrow X 4 into the heat exchanger W 2 , from which it can enter a boiler feed water preheater, not shown, which is also not required in the process according to the invention. From this preheating, the flue gas enters the heat exchanger W 1 according to arrow X 6 , from which the flue gases are then fed to the chimney according to arrow X 7 .
  • the arrangement of the heat exchangers is carried out in accordance with the required heat potential, the cracking furnace, the heat exchanger S requiring the highest temperature of the flue gases, whereas the heat exchanger W 1 requires flue gases with a much lower temperature.
  • the gas separator G shown schematically in FIG. 2 has a cylindrical tube 1 which serves as an outer container.
  • the pipeline R 3 into which the product mixture is introduced in liquid and gaseous form, opens into this outer container.
  • the cylindrical tube 1 there is an extreme slowdown in the flow velocity, at the same time a separation of the gaseous and the liquid phase occurs.
  • the liquid phase is discharged via the exiting pipeline R 3
  • the gaseous phase is discharged via the cylindrical pipe 2, which continues into the gas line G 1 , and thus reaches the pipeline R 4 with the valve V 1 open.
  • FIG. 3 there is a cyclone, the pipe R 3 opening tangentially into the conical container 3.
  • the product mixture moves downwards in a spiral along the outer container wall and separates.
  • the liquid phase is withdrawn via the pipeline R 3 located on the bottom, whereas the gaseous phase is withdrawn via the gas line G 1 .
  • the incoming product mixture was heated to 440 ° C in the heat exchanger W 2 .
  • the product mixture heated in this way is then passed through the pipe R 5 with a nominal diameter of 80 mm into the cracking furnace S.
  • the cracking furnace is designed as a heat exchanger in which the mixture has been heated further.
  • a mixture at 855 ° C. emerged from the pipeline R 6 .
  • a gas separator with a gas line G 1 was provided.
  • the product mixture entering the heat exchanger W 1 had a temperature of 60 ° C.
  • heating to 220 ° C occurred.
  • 15 vol .-% of the gaseous phase and no portion of the liquid phase of the product were passed through the gas line G 1 , which was therefore not heated.
  • the product mixture then reached the pipeline R 4 , into which water vapor at 483 ° C. and in an amount of 1,300 kg / h with a nominal width of 80 mm was introduced into the heat exchanger W 2 .
  • the incoming product mixture was heated to 450 ° C in the heat exchanger W 2 .
  • the product mixture heated in this way was then fed into the cracking furnace S via the pipeline R 5 with a nominal diameter of 80 mm. Heating was also carried out in the cracking furnace itself.
  • a mixture at 855 ° C. emerged from the pipeline R 6 .

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)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
EP94890007A 1993-01-27 1994-01-14 Vorrichtung zum thermischen Spalten eines Gemisches mit flüssigen und gasförmigen Kohlenwasserstoffen Expired - Lifetime EP0609191B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT0013793A AT398428B (de) 1993-01-27 1993-01-27 Vorrichtung zum thermischen spalten eines gemisches mit flüssigen und gasförmigen kohlenwasserstoffen
AT137/93 1993-01-27

Publications (2)

Publication Number Publication Date
EP0609191A1 EP0609191A1 (de) 1994-08-03
EP0609191B1 true EP0609191B1 (de) 1998-07-29

Family

ID=3482516

Family Applications (1)

Application Number Title Priority Date Filing Date
EP94890007A Expired - Lifetime EP0609191B1 (de) 1993-01-27 1994-01-14 Vorrichtung zum thermischen Spalten eines Gemisches mit flüssigen und gasförmigen Kohlenwasserstoffen

Country Status (11)

Country Link
EP (1) EP0609191B1 (sl)
AT (1) AT398428B (sl)
CZ (1) CZ283129B6 (sl)
DE (1) DE59406524D1 (sl)
DK (1) DK0609191T3 (sl)
ES (1) ES2121177T3 (sl)
FI (1) FI115466B (sl)
HU (1) HU214480B (sl)
NO (1) NO306681B1 (sl)
SI (1) SI9400032A (sl)
SK (1) SK279373B6 (sl)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4259751A1 (en) 2020-12-10 2023-10-18 TotalEnergies OneTech Belgium Method for improving feedstock flexibility of steam cracking
EP4074809A1 (en) 2021-04-14 2022-10-19 Total Research & Technology Feluy Process and apparatus for cracking of thermally unstable feedstock

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4479869A (en) * 1983-12-14 1984-10-30 The M. W. Kellogg Company Flexible feed pyrolysis process
JPH0819420B2 (ja) * 1988-09-05 1996-02-28 三井石油化学工業株式会社 低品位原料の分解処理方法
DE4105095A1 (de) * 1991-02-19 1992-08-20 Linde Ag Verfahren zur prozesssteuerung in spaltoefen zur olefinherstellung

Also Published As

Publication number Publication date
FI940385A0 (fi) 1994-01-26
EP0609191A1 (de) 1994-08-03
AT398428B (de) 1994-12-27
HUT69458A (en) 1995-09-28
CZ17394A3 (en) 1994-08-17
FI115466B (fi) 2005-05-13
NO940252D0 (no) 1994-01-25
ES2121177T3 (es) 1998-11-16
ATA13793A (de) 1994-04-15
NO306681B1 (no) 1999-12-06
CZ283129B6 (cs) 1998-01-14
SK279373B6 (sk) 1998-10-07
DE59406524D1 (de) 1998-09-03
NO940252L (no) 1994-07-28
HU214480B (hu) 1998-03-30
HU9400231D0 (en) 1994-05-30
FI940385A (fi) 1994-07-28
SI9400032A (en) 1994-09-30
SK8194A3 (en) 1994-11-09
DK0609191T3 (da) 1999-04-26

Similar Documents

Publication Publication Date Title
EP0425717B1 (de) Durchlaufdampferzeuger
EP1009920B1 (de) Dampferzeuger, insbesondere abhitzedampferzeuger, und verfahren zum betrieb dieses dampferzeugers
EP0359735B1 (de) Abhitze-Dampferzeuger
DE2726302A1 (de) Verfahren und anlage zur reinigung von abwaessern
CH650162A5 (de) Verbrennungsverfahren mit reinigung der verbrennungsluft und/oder der abgase.
DE2849344C2 (de) Verfahren zur Abtrennung einer C↓2↓↓+↓-Kohlenwasserstoff-Fraktion aus Erdgas
EP0918151A1 (de) Verfahren und Vorrichtung zur Brennstoffvorwärmung einer Feuerungsanlage
EP0357590B1 (de) Abhitze-Dampferzeuger
EP0781583B1 (de) Verfahren und Apparateanordnung zur Aufwärmung und mehrstufigen Entgasung von Wasser
EP0609191B1 (de) Vorrichtung zum thermischen Spalten eines Gemisches mit flüssigen und gasförmigen Kohlenwasserstoffen
EP3235784A1 (de) Verfahren und anlage zur erzeugung von wasserstoff mittels katalytischer dampfreformierung eines kohlenwasserstoffhaltigen einsatzgases
EP0272378B1 (de) Verfahren und Vorrichtung zum Kühlen von Spaltgas
DE69717165T2 (de) Verfahren zum betrieb eines zwanglaufdampferzeugers und dampferzeuger zur ausführung des verfahrens
DE2850019A1 (de) Verfahren und einrichtung zum abscheiden von kondensierten und/oder kondensierbaren komponenten aus einem rohgasgemisch
WO2010086092A1 (de) Verfahren und vorrichtung zur abtrennung von festen partikeln aus einer wasserphase
DE4218016A1 (de) Verfahren und Vorrichtung zur Regelung der Rauchgastemperatur am Austritt eines Dampferzeugers
EP0848208A2 (de) Reinigung des Wasser-Dampfkreislaufs in einem Zwangsdurchlaufdampferzeuger
DE102016103321A1 (de) Vorrichtung und Verfahren zur Dampfreformierung
DE202019100599U1 (de) Vorrichtung zum Behandeln von Altöl
DE899346C (de) Verfahren zur kontinuierlichen Herstellung eines Gasdampfgemisches von erhoehter Endtemperatur
EP3418253B1 (de) Verfahren zur kühlung von synthesegas
AT406165B (de) Vorrichtung zur kontinuierlichen destillativen auftrennung von rohöl
DE629524C (de) Verfahren zur Druckwaermespaltung von Kohlenwasserstoffoelen
DE2923326A1 (de) Verfahren zur thermischen entkokung einer vorrichtung zum thermischen spalten von kohlenwasserstoffen
DE535276C (de) Verfahren und Vorrichtung zur Druckwaermespaltung von schweren Kohlenwasserstoffoelen

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 CH DE DK ES FR GB GR IE IT LI LU MC NL PT SE

17P Request for examination filed

Effective date: 19950119

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

Owner name: OMV AKTIENGESELLSCHAFT

17Q First examination report despatched

Effective date: 19970129

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

RAP3 Party data changed (applicant data changed or rights of an application transferred)

Owner name: OMV AKTIENGESELLSCHAFT

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 CH DE DK ES FR GB GR IE IT LI LU MC NL PT SE

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REF Corresponds to:

Ref document number: 59406524

Country of ref document: DE

Date of ref document: 19980903

REG Reference to a national code

Ref country code: CH

Ref legal event code: NV

Representative=s name: BUECHEL, VON REVY & PARTNER

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

Effective date: 19980928

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: GERMAN

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2121177

Country of ref document: ES

Kind code of ref document: T3

ET Fr: translation filed
REG Reference to a national code

Ref country code: PT

Ref legal event code: SC4A

Free format text: AVAILABILITY OF NATIONAL TRANSLATION

Effective date: 19981007

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: 19990114

REG Reference to a national code

Ref country code: DK

Ref legal event code: 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
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: 19990731

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

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

Ref country code: PT

Payment date: 20041209

Year of fee payment: 12

Ref country code: IE

Payment date: 20041209

Year of fee payment: 12

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

Ref country code: GR

Payment date: 20041210

Year of fee payment: 12

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

Ref country code: FR

Payment date: 20041217

Year of fee payment: 12

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

Ref country code: DK

Payment date: 20050105

Year of fee payment: 12

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: 20050114

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

Ref country code: CH

Payment date: 20050214

Year of fee payment: 12

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

Ref country code: SE

Payment date: 20050304

Year of fee payment: 12

REG Reference to a national code

Ref country code: CH

Ref legal event code: PUE

Owner name: OMV REFINING & MARKETING GMBH

Free format text: OMV AKTIENGESELLSCHAFT#OTTO WAGNER-PLATZ 5#1090 WIEN (AT) -TRANSFER TO- OMV REFINING & MARKETING GMBH#LASSALLESTRASSE 3#1020 WIEN (AT)

NLS Nl: assignments of ep-patents

Owner name: OMV REFINING & MARKETING GMBH

REG Reference to a national code

Ref country code: GB

Ref legal event code: 732E

REG Reference to a national code

Ref country code: ES

Ref legal event code: PC2A

REG Reference to a national code

Ref country code: PT

Ref legal event code: PD4A

Free format text: OMV REFINING & MARKETING GMBH AT

Effective date: 20050414

Ref country code: PT

Ref legal event code: PC4A

Free format text: OMV REFINING & MARKETING AG AT

Effective date: 20050414

REG Reference to a national code

Ref country code: FR

Ref legal event code: TP

Ref country code: FR

Ref legal event code: CJ

Ref country code: FR

Ref legal event code: CD

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

Ref country code: GB

Payment date: 20051223

Year of fee payment: 13

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

Ref country code: NL

Payment date: 20051229

Year of fee payment: 13

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

Ref country code: ES

Payment date: 20060112

Year of fee payment: 13

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: 20060115

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: 20060116

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

Ref country code: BE

Payment date: 20060117

Year of fee payment: 13

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: 20060131

Ref country code: DK

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

Effective date: 20060131

Ref country code: CH

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

Effective date: 20060131

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

Ref country code: DE

Payment date: 20060228

Year of fee payment: 13

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: 20060714

REG Reference to a national code

Ref country code: DK

Ref legal event code: EBP

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

EUG Se: european patent has lapsed
REG Reference to a national code

Ref country code: PT

Ref legal event code: MM4A

Effective date: 20060714

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

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: 20070801

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

Effective date: 20070114

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee

Effective date: 20070801

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20070930

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 NON-PAYMENT OF DUE FEES

Effective date: 20070114

BERE Be: lapsed

Owner name: *OMV REFINING & MARKETING G.M.B.H.

Effective date: 20070131

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: 20070131

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: 20070801

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20070115

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

Ref country code: FR

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

Effective date: 20070131

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: 20070115

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

Ref country code: FR

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

Effective date: 20060131

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

Ref country code: GR

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

Effective date: 20060802