EP1058051A1 - Wirbelschichtbettvergasungsofen - Google Patents

Wirbelschichtbettvergasungsofen Download PDF

Info

Publication number
EP1058051A1
EP1058051A1 EP99906525A EP99906525A EP1058051A1 EP 1058051 A1 EP1058051 A1 EP 1058051A1 EP 99906525 A EP99906525 A EP 99906525A EP 99906525 A EP99906525 A EP 99906525A EP 1058051 A1 EP1058051 A1 EP 1058051A1
Authority
EP
European Patent Office
Prior art keywords
fluidized
bed
gasification furnace
medium
fluidized medium
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
EP99906525A
Other languages
English (en)
French (fr)
Other versions
EP1058051A4 (de
EP1058051B1 (de
Inventor
Norihisa Miyoshi
Seiichiro Toyoda
Daisaku Fukuoka
Takashi Imaizumi
Shinichirou Chiba
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.)
Ebara Corp
Original Assignee
Ebara Corp
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 Ebara Corp filed Critical Ebara Corp
Publication of EP1058051A1 publication Critical patent/EP1058051A1/de
Publication of EP1058051A4 publication Critical patent/EP1058051A4/de
Application granted granted Critical
Publication of EP1058051B1 publication Critical patent/EP1058051B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/24—Devices for removal of material from the bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed

Definitions

  • the present invention relates to a fluidized-bed gasification furnace, and more particularly to a fluidized-bed gasification furnace characterized by discharge of a fluidized medium.
  • a fluidized bed is formed by supplying a gas upwardly into a particle-filled bed filled with particles of a fluidized medium, such as silica sand or iron oxide, having a size of about several tens of micrometers to about several millimeters for thereby fluidizing the fluidized medium.
  • a fluidized-bed reactor the properties possessed by the fluidized bed such as the fluidity, uniformity, high heat capacity, and large surface area are utilized to rapidly, stably, and homogeneously conduct a chemical reaction.
  • the fluidized-bed reactor has been applied to a catalytic cracking furnace in petroleum refining, and a combustion furnace and an incineration furnace for solid fuels such as coal, and extensively utilized in these fields.
  • Fluidized-bed gasification furnaces possess excellent mixing properties and heat transfer efficiency because of the fluidized medium, and hence are advantageous in that size and properties of introducible fuels are less limited than entrained bed reactors.
  • the fluidized-bed gasification furnaces have a drawback that the operation temperature should be lower than that of the entrained bed reactors to prevent the fluidized medium and ash content in fuels from melting and adhering to each other at high temperatures, and hence inhibiting fluidization of the fluidized medium. Therefore, it is necessary that the operation temperature is about 900°C or lower when coal is used as the fuel, and about 600°C to about 800°C when wastes are used as the fuel, although influenced by the properties of wastes. When the wastes contain alkali metals, the operation temperature should be further lower.
  • tar is a problem in the case of pyrolysis and gasification of wastes or coal at a relatively low temperature.
  • tar is in a vapor form at a temperature of around 600°C, and when the temperature is lowered to 200°C or below, tar is liquefied to develop adhesiveness, thus causing various troubles associated with handling of particles.
  • the fluidized-bed gasification furnace has a feature that since a large amount of char stays within the furnace, when incombustibles and the like are withdrawn from the bed, high-temperature char is brought into contact with air and then combusted to increase the temperature thereof, thus tending to form clinker.
  • the fluidized bed gasification reactor has a feature in less restriction on the size and properties of introducible fuels.
  • a fuel containing incombustibles such as coal or wastes
  • the incombustibles remaining within the reactor become large, and thus such incombustibles are required to be discharged from the reactor by some methods.
  • withdrawing the fluidized medium at a high temperature of 500°C to 600°C from the fluidized bed is very difficult due to its high temperature even in the atmospheric-pressure reactor, and hence is hardly possible in the gasification furnace operated under pressure.
  • Cooling the fluidized medium for avoiding the above problem causes liquefaction of tar vapor, often leading to various troubles. Therefore, the fuel should be crushed to a small size and then introduced into the fluidized-bed gasification furnace to dispense with withdrawal of incombustibles. This fails to utilize the feature of the fluidized-bed reactor.
  • the present invention has been made in view of the above drawbacks. It is therefore an object of the present invention to provide a fluidized-bed gasification furnace having excellent practicability which can be safely operated not only under atmospheric pressure but also under high pressure, while utilizing such feature of the fluidized-bed reactor that less restriction on the size and properties of introducible fuels are imposed.
  • a fluidized-bed gasification furnace utilizing a fluidized-bed reactor, comprising: a discharge port provided in the vicinity of a floor in a fluidized bed for discharging a fluidized medium, the discharge port being connected to a fluidized medium discharge chute extending downwardly; and a gas blow device provided below the chute.
  • a device for mechanically withdrawing the fluidized medium is provided in the vicinity of the lowermost part of the fluidized medium discharge chute.
  • This device preferably comprises a screw conveyor.
  • a gas blow device is preferably provided also at the lowermost part of the fluidized medium discharge chute.
  • steam, CO 2 , or oxygen-free gas may be used as a gas to be blown.
  • the fluidized-bed reactor used in the present invention is preferably divided into units performing respective functions so that the fluidized-bed reactor can easily deal with fuels having different properties by changing the combination of each of units.
  • FIGS. 1A, 1B, and 1C are cross-sectional views showing the structure of a cylindrical fluidized-bed gasification furnace according to an embodiment of the present invention.
  • FIG. 1A is a vertical cross-sectional view showing the fluidized-bed gasification furnace
  • FIG. 1B is a cross-sectional view taken along a line A-A of FIG. 1A
  • FIG. 1C is a cross-sectional view taken along a line B-B of FIG. 1A.
  • the fluidized-bed gasification furnace using a cylindrical fluidized-bed reactor shown in FIGS. 1A through 1C comprises a fluidized-bed unit 1, an under-furnace hopper unit 2, a medium discharge device unit 3, a free board unit 4, and a deflector unit 5.
  • the fluidized-bed reactor comprises the fluidized-bed unit 1, the under-furnace hopper unit 2, and the medium discharge device unit 3. Adjacent units are connected to each other by flanges.
  • a fluidizing gas dispersion device 6 having a conical top surface is provided inside the fluidized-bed unit 1, and has a plurality of fluidizing gas dispersion nozzles 7 on the top surface thereof.
  • the interiors of the fluidized-bed unit 1 and the units below the fluidized-bed unit 1 are filled with a fluidized medium 11.
  • the fluidized medium above the fluidizing gas dispersion device 6 is fluidized by a fluidizing gas blown from the fluidizing gas dispersion nozzles 7 to form a fluidized bed 8.
  • An fluidizing gas header 9 comprising at least two divided segments are housed in the fluidizing gas dispersion device 6, and the velocity of the fluidizing gas blown from the fluidizing gas dispersion nozzles 7 is regulated so that the velocity of the fluidizing gas blown into the peripheral portion is larger than the velocity of the fluidizing gas blown into the central portion, thereby developing internal revolving flows 12 of the fluidized medium in the fluidized bed.
  • the temperature of the fluidized medium over the fluidizing gas dispersion device 6 is kept at 400°C to 1,000°C, preferably 500°C to 800°C.
  • a discharge port 16 extending radially outwardly for the fluidized medium is provided inside the fluidized-bed unit 1 and above the periphery of the fluidizing gas dispersion device 6. Below the discharge port 16, there is provided a gap 20 defined between the fluidizing gas dispersion device 6 and the inner wall of the fluidized-bed unit 1.
  • This gap 20 serves as a discharge chute for the fluidized medium, and is divided into four chutes 20a to 20d by supports 10 for fixing the fluidizing gas dispersion device 6 to the inner wall of the fluidized-bed unit 1.
  • Pipes for supplying fluidizing gases from the exterior of the fluidized-bed unit 1 into the fluidizing gas header 9 may be provided inside the supports 10.
  • the chutes 20a to 20d are preferably provided so as to face the whole side surface of the fluidizing gas dispersion device 6 in order to prevent incombustibles from accumulating in the fluidized bed 8.
  • the support 10 necessarily has an angled upper portion, the top of which is acute.
  • the support 10 should have a certain width. Therefore, the support 10 should have a shape broadened downwardly, with the result that the width of the chutes 20a to 20d is reduced in the circumferential direction.
  • the lower side 6a of the fluidizing gas dispersion device 6 is downwardly inclined toward the centerline.
  • the dimension in the radial direction of the chutes 20a to 20d is downwardly increased to prevent the horizontal sectional area thereof from decreasing downwardly.
  • Each of gas blow nozzles 13 is provided below each of the chutes 20a to 20d and in the vertical direction of each of the chutes 20a to 20d.
  • the interiors of the chutes can be purged with steam or inert gas introduced from the gas blow nozzles 13 in order to prevent tar and oxygen from diffusing therethrough, or to eliminate the clogging of the chutes by vigorously fluidizing the fluidized medium.
  • the medium discharge device unit 3 is connected to the lower end of the under-furnace hopper unit 2.
  • the inner side of the under-furnace hopper unit 2 in the gasification furnace according to this embodiment is inclined so as to correspond to the size of the inlet of the medium discharge device unit 3, and hence is throttled as a whole.
  • a straight vertical wall may, of course, be adopted, or alternatively the inner side may be eccentric so as to have both vertical section and inclined section.
  • a medium discharge device 15 is provided at the lower part of the medium discharge device unit 3.
  • a screw conveyor is used as the medium discharge device 15.
  • a discharge device which can discharge incombustibles in the transverse direction such as a chain conveyor, may be used depending on the properties of incombustibles.
  • the medium discharge device 15 is transversely provided in the horizontal direction. Alternatively, the medium discharge device 15 may be vertically inclined.
  • a gas blow nozzle 14 is provided at the lowermost part of the medium discharge device unit 3 and below the medium discharge device 15.
  • the number of nozzles may be increased as necessary.
  • the concentration of incombustibles can be expected by classification effect caused by a gas blown through the gas blow nozzle 14, thus reducing the amount of the discharged fluidized medium, and simultaneously carry-over heat loss.
  • the gasification furnace shown in FIGS. 1A through 1C is divided into units performing respective functions.
  • the whole gasification furnace may, of course, be formed as an integral structure.
  • the whole gasification furnace may be formed as an integral structure.
  • the separable unit-type gasification furnace as shown in FIGS. 1A through 1C may be effective.
  • the separable unit-type structure has another advantage in that the structure can be easily changed depending on the properties of fuels.
  • a straight pipe section 1a may be additionally provided between the deflector unit 5 and the fluidized-bed unit 1 to increase the bed height.
  • a free board unit 4 bulged outwardly in its portion slightly above the flange may be used to increase the internal volume of the free board.
  • FIGS. 2A, 2B, and 2C are cross-sectional views showing the structure of a rectangular fluidized-bed gasification furnace according to another embodiment of the present invention.
  • FIG. 2A is a vertical cross-sectional view showing the fluidized-bed gasification furnace
  • FIG. 2B is a cross-sectional view taken along a line A-A of FIG. 2A
  • FIG. 2C is a cross-sectional view taken along a line B-B of FIG. 2A.
  • FIGS. 2A through 2C which are designated by the same reference numerals as those shown in FIGS. 1A through 1C have the same function, structure, and operation as those shown in FIGS. 1A through 1C.
  • the outer wall of the fluidized-bed unit 1 is in the form of rectangle.
  • a rectangular fluidizing gas dispersion device 6 provided in the fluidized-bed unit 1 has an angled upper portion.
  • two internal revolving flows 12, which are symmetrical with respect to a central plane, are formed respectively between the central portion and the left peripheral portion and between the central portion and the right peripheral portion.
  • An outwardly extending fluidized medium discharge port 16 is provided in the fluidized-bed unit 1 and above the periphery of the fluidizing gas dispersion device 6. Below the discharge port 16, there is provided a gap 20 defined between the fluidizing gas dispersion device 6 and the inner wall of the fluidized-bed unit 1.
  • This gap 20 serves as a fluidized medium discharge chute. As shown in FIG. 2B, the gap 20 comprises two chutes 20a and 20b. Three gas blow nozzles 13 are provided below each of the chutes 20a, 20b and in the vertical direction of the chutes 20a, 20b.
  • FIG. 3 is a schematic view showing the whole construction of components around the gasification furnace used under pressure according to an embodiment of the present invention.
  • a lock hopper 102 for pressure seal is connected to the downstream side of the medium discharge device unit provided at the lower part of the gasification furnace 101 having a structure shown in FIGS. 1A through 1C or FIGS. 2A through 2C.
  • a vibrating screen 103 is provided downstream of the lock hopper 102.
  • Incombustibles 61 are separated from a fluidized medium 60 by the vibrating screen 103. The incombustibles 61 are discharged to the outside of the system, while the fluidized medium 60 is returned into the furnace.
  • the fluidized medium 60 separated from the incombustibles 61 by the vibrating screen 103 is carried by a fluidized medium conveyor 104, passed through the lock hopper 105 for a fluidized medium, and returned to the gasification furnace 101 by a fluidized medium feed conveyor 106.
  • a fluidized medium conveyor 104 since the portion up to the lock hopper 102 is pressurized, dew condensation tends to occur. Therefore, measures such as heat insulation or steam heat tracing are preferably taken for preventing dew condensation.
  • FIG. 4 is a schematic view showing the whole construction of components around the gasification furnace used under pressure according to another embodiment of the present invention.
  • the fluidized medium carried by the fluidized medium conveyor 104 in the same manner as in FIG. 3 is once received in a fluidized medium hopper 107.
  • the flow rate of the fluidized medium can be adjusted by a constant-rate medium supply device 108.
  • a changeover chute 109 permits the fluidized medium to be fed through the lock hopper 105 into the furnace, or alternatively permits the fluidized medium together with a fuel 50 to be fed through a lock hopper 110 into the furnace by a feed conveyor 111.
  • FIG. 5 is a schematic view showing the whole construction of components around the gasification furnace used under atmospheric pressure according to another embodiment of the present invention.
  • a mixture of incombustibles and a fluidized medium discharged from the gasification furnace 101 is carried by a conveyor 104 and is separated into incombustibles 61 and a fluidized medium 60 by a vibrating screen 103. Thereafter, the fluidized medium 60 is fed into the gasification furnace 101 by a fluidized medium feed conveyor 106.
  • the passage is switched by the changeover chute 109 to store an excessive fluidized medium in a fluidized medium hopper 107, and, as needed, the fluidized medium is supplied to the fluidized medium feed conveyor 106 by a constant-rate supply device 108, and then introduced into the furnace.
  • One method is to use a conveyor 104 of such a type that the interior of the conveyor is filled with the fluidized medium.
  • This type of conveyor has a problem that required power is large because the fluidized medium present in the interior of the conveyor should be always agitated.
  • Another method is to provide a seal damper between the outlet of the fluidized medium discharge conveyor provided at the bottom of the gasification furnace 101 and the conveyor 104.
  • a double damper system is preferably adopted.
  • a single damper cooperated with the operation and stop of the fluidized medium discharge conveyor can be expected to provide a certain degree of such effect.
  • the present invention has the following effects.
  • the present invention is preferably applicable to an apparatus for producing a gas from fuels such as wastes or coal with a fluidized bed.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Gasification And Melting Of Waste (AREA)
EP99906525A 1998-02-27 1999-02-26 Wirbelschichtbettvergasungsofen Expired - Lifetime EP1058051B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
JP6188698 1998-02-27
JP6188698 1998-02-27
PCT/JP1999/000946 WO1999043985A1 (fr) 1998-02-27 1999-02-26 Four de gazeification a lit fluidise

Publications (3)

Publication Number Publication Date
EP1058051A1 true EP1058051A1 (de) 2000-12-06
EP1058051A4 EP1058051A4 (de) 2001-09-19
EP1058051B1 EP1058051B1 (de) 2005-07-20

Family

ID=13184087

Family Applications (1)

Application Number Title Priority Date Filing Date
EP99906525A Expired - Lifetime EP1058051B1 (de) 1998-02-27 1999-02-26 Wirbelschichtbettvergasungsofen

Country Status (5)

Country Link
EP (1) EP1058051B1 (de)
CN (1) CN1239841C (de)
AU (1) AU2641999A (de)
DE (1) DE69926217T2 (de)
WO (1) WO1999043985A1 (de)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002086026A2 (en) * 2001-04-19 2002-10-31 Ebara Corporation Gasification apparatus and method of operating the same
WO2004046612A1 (en) * 2002-11-15 2004-06-03 Ebara Corporation Fluidized-bed gasification furnace
CN102051247A (zh) * 2010-12-11 2011-05-11 水煤浆气化及煤化工国家工程研究中心 一种改善煤粘温特性的助剂

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5694690B2 (ja) * 2010-06-22 2015-04-01 株式会社神鋼環境ソリューション 流動層炉及び廃棄物処理方法
JP5778069B2 (ja) * 2012-03-30 2015-09-16 株式会社神鋼環境ソリューション 流動床式ガス化炉への流動粒子供給装置
CN109185869B (zh) * 2018-09-05 2019-12-20 江西黄龙油脂有限公司 一种分层燃烧室流态化锅炉

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1166675A (en) * 1965-11-01 1969-10-08 Mitsura Tada Apparatus for Continuously Burning Waste
JPS6370008A (ja) * 1986-09-10 1988-03-30 Babcock Hitachi Kk 成長流動媒体排出装置
US4823740A (en) * 1986-01-21 1989-04-25 Ebara Corporation Thermal reactor

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5843318A (ja) * 1981-09-09 1983-03-14 Ebara Corp 排出装置
JPS59197715A (ja) * 1983-04-25 1984-11-09 Babcock Hitachi Kk 異物排出口をシ−ルした流動層燃焼装置

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1166675A (en) * 1965-11-01 1969-10-08 Mitsura Tada Apparatus for Continuously Burning Waste
US4823740A (en) * 1986-01-21 1989-04-25 Ebara Corporation Thermal reactor
JPS6370008A (ja) * 1986-09-10 1988-03-30 Babcock Hitachi Kk 成長流動媒体排出装置

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
PATENT ABSTRACTS OF JAPAN vol. 012, no. 292 (M-729), 10 August 1988 (1988-08-10) & JP 63 070008 A (BABCOCK HITACHI KK), 30 March 1988 (1988-03-30) *
See also references of WO9943985A1 *

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002086026A2 (en) * 2001-04-19 2002-10-31 Ebara Corporation Gasification apparatus and method of operating the same
WO2002086026A3 (en) * 2001-04-19 2003-12-04 Ebara Corp Gasification apparatus and method of operating the same
WO2004046612A1 (en) * 2002-11-15 2004-06-03 Ebara Corporation Fluidized-bed gasification furnace
CN102051247A (zh) * 2010-12-11 2011-05-11 水煤浆气化及煤化工国家工程研究中心 一种改善煤粘温特性的助剂

Also Published As

Publication number Publication date
EP1058051A4 (de) 2001-09-19
WO1999043985A1 (fr) 1999-09-02
CN1239841C (zh) 2006-02-01
DE69926217T2 (de) 2006-04-20
AU2641999A (en) 1999-09-15
CN1295661A (zh) 2001-05-16
DE69926217D1 (de) 2005-08-25
EP1058051B1 (de) 2005-07-20

Similar Documents

Publication Publication Date Title
US4941779A (en) Compartmented gas injection device
US5106240A (en) Aerated discharge device
US5129766A (en) Aeration tube discharge control device
JP6122793B2 (ja) 直立のガス化装置
KR102203125B1 (ko) 단계식 가스화에서의 제 2 단 가스화기
AU2009256101B2 (en) Fluidized bed gasifier with solids discharge and classification device
RU2594410C2 (ru) Усовершенствованные плазменные газификаторы для производства сингаза
US20100199557A1 (en) Plasma gasification reactor
CN101668833B (zh) 由诸如生物质的燃料生成产品气的设备
CN101977675B (zh) 从存储容器计量取出细粒至粗粒固体或固体混合物的方法和装置
CA2751859C (en) Plasma gasification reactor
RU2607662C2 (ru) Способ и устройство для газификации твердых горючих материалов под давлением в стационарном слое
KR20070068218A (ko) 용철 제조 장치 및 제조 방법
EP1058051B1 (de) Wirbelschichtbettvergasungsofen
EP0348008A1 (de) Entladungssteuerungsvorrichtung mit Belüftungsrohr
JP5450800B2 (ja) 石炭の熱分解ガス化方法および石炭の熱分解ガス化装置
JP4660874B2 (ja) 廃棄物の二段ガス化システムの運転制御方法
EP0308024B1 (de) Facheinrichtung für Gas-Injektion
JP2006322004A (ja) 廃棄物の二段ガス化システム
US9222038B2 (en) Plasma gasification reactor
US4934876A (en) Aeration apparatus for discharge control of particulate matter
US20100199556A1 (en) Plasma gasification reactor
US4943190A (en) Aeration tube discharge control device with variable fluidic valve
JP2000319670A (ja) 廃棄物の二段ガス化システム
JP2540284B2 (ja) 石炭ガス化炉

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20000829

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): DE FR GB IT

A4 Supplementary search report drawn up and despatched

Effective date: 20010806

AK Designated contracting states

Kind code of ref document: A4

Designated state(s): DE FR GB IT

17Q First examination report despatched

Effective date: 20030711

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

RIC1 Information provided on ipc code assigned before grant

Ipc: 7F 23G 5/027 B

Ipc: 7F 23G 5/30 B

Ipc: 7F 23C 10/00 A

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): DE FR GB IT

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

REF Corresponds to:

Ref document number: 69926217

Country of ref document: DE

Date of ref document: 20050825

Kind code of ref document: P

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

Effective date: 20060421

EN Fr: translation not filed
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 FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20060915

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 FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20050720

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

Ref country code: IT

Payment date: 20100220

Year of fee payment: 12

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

Ref country code: GB

Payment date: 20100202

Year of fee payment: 12

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

Effective date: 20110226

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

Effective date: 20110226

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: 20110226

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

Ref country code: DE

Payment date: 20120222

Year of fee payment: 14

REG Reference to a national code

Ref country code: DE

Ref legal event code: R119

Ref document number: 69926217

Country of ref document: DE

Effective date: 20130903

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: 20130903