EP2207616B1 - Dispositif de production d'un produit gazeux combustible à partir de matières de charge carbonées - Google Patents

Dispositif de production d'un produit gazeux combustible à partir de matières de charge carbonées Download PDF

Info

Publication number
EP2207616B1
EP2207616B1 EP09763905A EP09763905A EP2207616B1 EP 2207616 B1 EP2207616 B1 EP 2207616B1 EP 09763905 A EP09763905 A EP 09763905A EP 09763905 A EP09763905 A EP 09763905A EP 2207616 B1 EP2207616 B1 EP 2207616B1
Authority
EP
European Patent Office
Prior art keywords
heat
liquid
transfer medium
loop
heat pipe
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.)
Not-in-force
Application number
EP09763905A
Other languages
German (de)
English (en)
Other versions
EP2207616A1 (fr
Inventor
Georg Gallmetzer
Felix Nelles
Martin Kröner
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.)
Highterm Research GmbH
Original Assignee
Highterm Research GmbH
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 Highterm Research GmbH filed Critical Highterm Research GmbH
Publication of EP2207616A1 publication Critical patent/EP2207616A1/fr
Application granted granted Critical
Publication of EP2207616B1 publication Critical patent/EP2207616B1/fr
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
    • F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
    • F28D15/0266—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with separate evaporating and condensing chambers connected by at least one conduit; Loop-type heat pipes; with multiple or common evaporating or condensing chambers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/10—Continuous processes using external heating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
    • F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
    • F28D15/04—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with tubes having a capillary structure
    • F28D15/043—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with tubes having a capillary structure forming loops, e.g. capillary pumped loops
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1246—Heating the gasifier by external or indirect heating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1853—Steam reforming, i.e. injection of steam only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam

Definitions

  • the invention relates to a device for producing combustible product gas from carbonaceous feedstocks by allothermic steam gasification according to the preamble of claim 1.
  • the pressure-charged allothermal steam gasification of carbonaceous fuels requires heat input into the gasification chamber at a temperature level of about 800-900 ° C.
  • heat pipe reformer as from the EP 1 187 892 B1 is known to be produced in a pressurized fluidized bed gasification chamber by allothermic steam gasification fuel gas from the carbonaceous feedstocks to be gasified. The necessary heat is passed from a fluidized bed by means of a réelleleitrohranssen in the carburetor or reformer. Due to the straight and tubular construction of heat pipes are in the from the EP 1 187 892 B1 known heat pipe reformer combustion chamber and reformer / gasification chamber arranged one above the other. The pressure vessel bottom is exposed to special stresses due to the high temperatures in the combustion chamber. Moreover, the soil is weakened by a variety of heat pipe bushings. The sealing of the bushings is also a problem.
  • both the line for liquid heat transfer medium and for vaporous heat transfer medium in the common tube shell is arranged.
  • the number of feedthroughs can be reduced to two, namely a liquid line and a steam line. If a plurality of such loop heat pipes is used, their separate running steam and liquid lines can be summarized in the carburetor pressure vessel to a common vapor or liquid line, which then enforce the gasification pressure vessel. Outside the carburetor pressure vessel then the two common lines can be split again.
  • the number of feedthroughs from or into the carburetor pressure vessel can be significantly reduced to a minimum of two.
  • Another advantage of the invention is that the spatial separation of the steam and liquid line of the loop heat pipes a larger Design freedom arises.
  • Carburetor or reformer and external heat source can be arranged and optimized completely independently.
  • claims 3 and 4 relate to different designs for loop heat pipes with separate running steam and liquid line.
  • the first heat carrier circuit or the associated heat pipe can be optimized with regard to the heat absorption in the heat source, while the second heat carrier circuit or the associated heat pipe can be optimized in terms of heat dissipation in the gasifier.
  • the pyrolysis residues are thermally utilized from the gasifier and on the other hand, the complete fuel supply into the fluidized bed combustion chamber can take place. An additional supply of fuel in the fluidized bed combustion chamber, with the exception of the startup is no longer necessary.
  • alkali metals and their alloys eg. B. Na, K, NaK, as a heat transfer medium in the loop heat pipes.
  • Fig. 1 shows the basic structure of a high-end reforming according to the present invention.
  • the high-temperature refomer comprises a pressurized carburetor or reformer 2 and an external heat source in the form of a combustion chamber 4.
  • the carburetor 2 comprises a carburetor pressure vessel 6, a fuel supply 8, a water supply 10 and a product gas discharge 12 at one temperature from 800 ° C to 900 ° C is produced by allothermic steam gasification of carbonaceous fuels in a known manner product gas.
  • the carburetor 2 and the external heat source 4 are connected to each other via a heat carrier circuit or a loop heat pipe 14.
  • the heat carrier circuit or the loop heat pipe 14 comprise a heat receiving side 16 and a heat-emitting side 18, which are connected to each other via a steam line 20 for vaporous heat transfer medium and a liquid line 22 for liquid heat transfer medium.
  • a lock 24 of the carburetor 2 is connected to the heat source 4.
  • About the lock 24 pyrolysis residues from the carburetor 2 of the combustion chamber 4 are supplied as fuel.
  • the combustion chamber 4 still has an air supply 26 and a flue gas outlet 28.
  • a hydrogen separation device 30 is arranged in the liquid line 22 between the carburetor 2 and the combustion chamber 4.
  • the hydrogen separation device 30 By the hydrogen separation device 30, the hydrogen and other foreign matter is separated from the liquid heat transfer medium and the remaining liquid heat transfer medium is returned to the combustion chamber 4, so that the heat carrier circuit is closed. Due to the high temperatures alkali metals or alloys thereof, z. As Na, K or NaK used.
  • Fig. 2 schematically shows a first, concrete embodiment of the invention, wherein for components corresponding to each other, the same reference numerals are used.
  • the combustion chamber 4 is a fluidized bed combustion chamber with circulating fluidized bed 32.
  • the combustion chamber 4 comprises a riser 34, a cyclone 36 and a lock 38 and a fluidized bed 40, which lead back into the riser 34.
  • the heat receiving side 16 of the loop heat pipe 14 comprises a first and a second shell and tube heat exchangers 42 and 44, which are connected in series and in which the liquid heat transfer medium is vaporized by absorbing heat.
  • the heat-emitting side 18 includes a third shell-and-tube heat exchanger 46 in which the vaporous heat exchange medium is recondensed by release of the previously received heat.
  • Fig. 2 has the combustion chamber 4 compared to the so-called heat pipe reformer after EP 1 187 892 B1 no limitation in the construction and operation.
  • all design and operational parameters can be optimally adapted to the requirements of high-temperature heat supply.
  • the use of the circulating fluidized bed 32 has the advantage of optimum combustion in the riser 34 and the optimal and material-conserving heat extraction from the fluidized bed 40- first shell and tube heat exchanger 42 - and membrane walls - second shell and tube heat exchanger 44 - in the turbulent Soil zone of the riser 34.
  • the exact structure of the combustion chamber 4 with circulating fluidized bed 32 is on " Handbook of Fludization and Fluid Particle Systems, "by Wen-Ching Yang, ISBN: 0-8247-0259-X , referenced.
  • the reformer or carburetor 2 can be designed without restrictions with respect to the combustion chamber 4, since combustion chamber 4 and carburetor 2 are not arranged as in the heat pipe reformer in a common container.
  • the implementation of the high-temperature steam and liquid line 20, 22 is moved to structurally favorable locations carburetor pressure vessel 6.
  • the liquid line 22 and the steam line 20 are guided laterally out of the barrel-shaped carburetor 2.
  • the lid and bottom of the carburetor pressure vessel 6 are free of the large number of heat pipe feedthroughs, as they are known from the heat pipe reformer. There are only weakenings through the steam supply 10 and the fuel supply 8, as well as product gas discharge 12 and lock 24 for discharging pyrolysis residues.
  • the reaction temperature in the gasifier can be substantially higher than the temperatures on the wall of the carburetor pressure vessel. As a result, stable constructions are achieved even when using less expensive materials with smaller wall thicknesses.
  • the pyrolysis residues of the carburettor 2 can be utilized directly in the combustion chamber 4 via the lock 24. With favorable process control, the pyrolysis residues are sufficient to cover the fuel requirement of the combustion chamber 4. Product gas leakage flows through the lock 24 can be safely and completely burned in the combustion chamber 4.
  • Fig. 3 shows a first embodiment of the high-temperature heat transfer circuit in Highterm reformer in the form of a pumped by capillary loop heat pipe 500 (Capillary Pumped Loop CPL), as shown in Publication, Heat Pipe Science and Technology, Amir Fahgri, 1995, page 583 is known.
  • the CPL 500 includes a heat receiving side Evaporator 516 and a heat-releasing side and a condenser 518, respectively.
  • Vaporizer 516 and condenser 518 are connected to each other via a vaporous vapor vapor manifold 520 and a liquid heat transfer medium liquid manifold 522. Steam manifold 520 and liquid manifold 522 are spaced apart from each other.
  • Both the evaporator 516 and the condenser 518 consist of a plurality of identical evaporator 524 or condenser elements 526 connected in parallel.
  • the evaporator elements 524 have a capillary structure 528 through which the liquid heat transfer medium is vaporized by absorbing heat. In the capacitor elements 526, the heat transfer medium condenses again with the release of heat.
  • the liquid manifold 522 is connected to a surge tank 532 via a surge line 530.
  • the expansion tank 532 ensures a steady level in the liquid collecting line 522.
  • the liquid flows back into the liquid collecting line 522 due to a small temperature gradient and thus also a pressure gradient.
  • the evaporation enthalpy recorded in the evaporator 516 (combustion chamber 4) is thus released again in the condenser 518 (carburettor 2).
  • the hydrogen separation device is integrated (in Fig. 3 not shown).
  • Fig. 4 shows a second embodiment of the high-temperature heat transfer circuit in Highterm reformer in the form of a loop heat pipe 600 (Loop Heat Pipe LHP), as it is known from Publication, Heat Pipe Science and Technology, Amir Fahgri, 1995, page 586 is known.
  • the LHP 600 includes a heat receiving side or evaporator 616 and a heat releasing side and a condenser 618, respectively.
  • Vaporizer 616 and condenser 618 are connected to each other via a steam line 620 for vaporous heat transfer medium and a liquid line 622 for liquid heat transfer medium. Steam line 620 and liquid line 622 are spaced apart from each other.
  • a capillary structure 628 is arranged, through which liquid Heat transfer medium is vaporized by absorption of heat.
  • the condenser 618 the heat transfer medium condenses again with the release of heat.
  • the capillary pressure differential in the capillary structure 628 be greater than the sum of the pressure losses from the vapor and liquid flow, the capillary structure 628, and the hydrostatic pressure. Ie. it must apply: ⁇ ⁇ p cap ⁇ Max ⁇ ⁇ p ⁇ + ⁇ ⁇ p l + ⁇ ⁇ p ⁇ + ⁇ ⁇ p G ,
  • Such a loop heat pipe is also from the WO / 2003/054469 known.
  • Fig. 6 shows a second embodiment of the high-temperature reformer according to the present invention with a two-stage high-temperature heat transfer circuit 700.
  • the high-temperature heat transfer circuit 700 includes a primary heat transfer circuit 701 and a secondary heat transfer circuit 702.
  • the primary heat transfer circuit 701 includes a heat receiving side 716 and a heat-releasing 718.
  • the heat receiving side 716 and the heat emitting side 718 are connected to each other via a steam line 720 for vaporous heat transfer medium and via a liquid line 722 for liquid heat transfer medium. Steam line 720 and liquid line 722 are spatially separated.
  • the heat releasing side 716 is disposed in the combustion chamber and the heat releasing side 718 is disposed in the carburetor.
  • the primary heat transfer circuit 701 may be through the loop heat pipes 500 and / or 600 in Fig. 3 and 4 will be realized.
  • the secondary heat transfer circuit 702 is implemented by a pulsed loop heat pipe (CLPHP), as shown in FIG Fig. 7 is shown.
  • the CLPHP 702 has a heat receiving side 736 and a heat releasing side 738.
  • the heat receiving side 736 and the heat releasing side 738 are interconnected via a closed meandering vapor / liquid conduit 740.
  • Both the heat releasing side 736 and the heat releasing side of the CLPHP 702 are disposed in the gas pressure vessel 706.
  • the heat receiving side 736 of the CLPHP 702 is integrated into the heat emitting side 718 of the primary heat transfer circuit 701.
  • the heat transfer medium is passed alternately via the vapor / liquid line 740 from the evaporator 736 in the condenser 738.
  • a temperature difference creates a pressure difference that causes the whole system to pulsate. This makes it possible to transport off hydrogen cushions and other inert gases convective and at a suitable location, eg. B. at the top of the condenser 738 via a degassing 730 deduct.
  • An advantage of the double heat carrier circuit is that can escape through the decoupling of the pulsating secondary heat transfer medium from the combustion chamber 4 in case of leaks less heat transfer medium.
  • Fig. 8 shows an exemplary structure of the hydrogen separation device 30 as can be used in the various embodiments of the high-temperature reformer.
  • the hydrogen separation device 30 in the liquid line 22, 522, 622, 722 comprises a collection container 300 in which a liquid level is set.
  • the collecting container 300 has a gas dome 302 in which vaporous heat transfer medium is located and in which hydrogen and other inert gases collect. From this gas dome 302 branches off a stub 304, which leads to a region with lower temperatures ends in a lock device 306.
  • materials such as EPDM (up to about 150 ° C.), etc. can be used for the valves 308, 310, 312, 314.
  • the temperature of the stub line 304 is decisive for the vapor pressure of the heat transfer medium.
  • a long stub 304 therefore results in an inert gas heat transfer separation.
  • the temperature of the stub line 304 may not be below the solidification temperature of the heat transfer medium to prevent clogging of the stub 304.
  • the degassing device 306 for degassing consists of 4 valves 308, 310, 312, 314, wherein in each case the first and second valves 308, 310 and the third and fourth valve, 312, 314 in series and the two pairs of rows 308, 310 and 312, 314 in parallel are switched.
  • the parallel connection results in a redundant lock system.
  • the degassing system or the hydrogen separation device 30 should be installed as possible at the coolest point of the heat transfer circuit.
  • a vacuum pump - not shown - generates a vacuum when valve 308 or 312 is closed and valve 310 or 314 is open, then valve 310 or 314 is closed and valve 308 or 312 is opened and closed again. Then this cycle starts again. In this way, hydrogen and other inert gases are eliminated from the heat transfer circuit.
  • Fig. 9 shows a third embodiment of the high-temperature reformer with a fluidized bed combustor 804 and a carburetor or reformer 802.
  • the carburetor 802 includes a carburetor pressure vessel 806 which is co-located with the fluidized bed combustor 804 in a common reactor vessel 805.
  • a loop heat pipe device 814 having a plurality of loop heat pipes according to FIGS Figures 3 and 4 used.
  • the plurality of loop heat pipes are assembled into an evaporator battery 816 and a capacitor battery 818.
  • Capacitor battery 818 and evaporator battery 816 are interconnected via a single steam line 820 and via a single fluid line 822.
  • the evaporator battery 816 is in the fluidized bed combustor 804 and the condenser battery 818 are disposed in the gasifier pressure vessel 805.
  • a degassing and filling tube 830 which leads out of the condenser battery 818 from the carburetor pressure vessel 806 and the common reactor vessel 805, hydrogen and other inert gases are withdrawn.
  • the degassing and filling tube 830 the filling of the loop heat pipe device 814 with heat transfer medium.
  • the advantage of this third embodiment of the invention is that the loop heat pipe device 814 can be integrated into an existing reactor design.
  • Fig. 10 shows an alternative embodiment of a heat pipe in the form of a so-called immersion heat pipe 900.
  • the immersion heat pipe 900 consists of an outer tube 902 with an open end 904 and a closed end 906.
  • the outer tube 902 is an open on both sides inner tube 908 is arranged a first open end 910 and a second open end 912.
  • Via the open end 904 of the outer tube 902 flows vaporous heat transfer medium and condenses on the way down to the closed end 906 of the outer tube 902.
  • the condensed heat transfer medium flows through the first open end 910 of the inner tube 908 back up and is on the second open end 912 of the inner tube 908 discharged from the immersion heat pipe 900.
  • a corresponding pressure gradient is necessary to promote the heat transfer medium condensate back up.
  • the supply of vaporous heat transfer medium via the open end 904 of the outer tube 902 and the discharge of the liquid heat transfer medium via the second open end 912 of the inner tube takes place transversely to the longitudinal extent of the outer and inner tubes 902, 908.
  • Meander-shaped heat exchanger pipe guides which are problematic in fluidized beds, in particular in the gasifier, can be avoided by the immersion heat pipe 900 described above since they disturb the structure and the stratification of the fluidized bed.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Claims (11)

  1. Dispositif de production d'un produit gazeux combustible à partir de matières de charge carbonées, par gazéification allothermique à la vapeur d'eau, avec :
    - un gazéificateur à suralimentation de pression (2), comprenant un récipient à pression de gazéificateur (6), un dispositif d'alimentation (8) pour les matières de charge carbonées, une alimentation en vapeur d'eau (10) et une conduite d'évacuation de produit gazeux,
    - une source de chaleur externe (4), et
    - un dispositif de transport de chaleur (14), avec une pluralité de caloducs, au moyen desquels de la chaleur est transportée, de la source de chaleur externe (4) dans le gazéificateur (2), au moyen d'un fluide caloporteur effectuant un changement de phase,
    les caloducs (14) comprenant un côté délivrant de la chaleur (18), disposé dans le-gazéificateur (2), et un côté recevant de la chaleur (16), disposé dans la source de chaleur externe (4),
    caractérisé
    en ce que la pluralité de caloducs (14) sont des caloducs à boucle (500 ; 600 ; 701 ; 702 ; 814), dont les côtés recevant de la chaleur (16 ; 516 ; 616 ; 716 ; 816) et les côtés délivrant de la chaleur (18 ; 518 ; 618 ; 738 ; 818) sont reliés ensemble par l'intermédiaire d'une conduite à liquide (22 ; 522 ; 62 ; 722 ; 822) pour un fluide caloporteur liquide et par l'intermédiaire d'une conduite à vapeur (20 ; 520 ; 620 ; 720 ; 820) pour un fluide caloporteur se présentant à l'état de vapeur,
    en ce que les conduites à liquide et à vapeur des différents caloducs à boucle (500 ; 600 ; 701 ; 702 ; 814) sont regroupées en des conduites à liquide et à vapeur (22 ; 522 ; 622 ; 722 ; 822 ; 20 ; 520 ; 620 ; 720 ; 820) communes, et
    en ce que les conduites à liquide (22 ; 522 ; 622 ; 722 ; 822) communes et les conduites à vapeur (20 ; 520 ; 620 ; 720 ; 820) communes sont des conduites séparées spatialement.
  2. Dispositif selon la revendication 1, caractérisé en ce qu'un dispositif de séparation d'hydrogène (30 ; 532 ; 730 ; 830) est disposé dans les conduites à liquide (22 ; 522 ; 622 ; 722 ; 822) des caloducs à boucle (500 ; 600 ; 701 ; 702 ; 814).
  3. Dispositif selon l'une des revendications précédentes, caractérisé en ce que le dispositif de transport de chaleur (14) comprend au moins un caloduc à boucle (500 ; 600 ; 701) pompé au moyen d'une structure capillaire (528 ; 628).
  4. Dispositif selon l'une des revendications précédentes, caractérisé en ce que le dispositif de transport de chaleur (14) comprend au moins un caloduc à boucle à immersion (900).
  5. Dispositif selon l'une des revendications précédentes, caractérisé
    en ce que le dispositif de transport de chaleur (14) comprend au moins un premier caloduc à boucle (701), présentant une conduite à vapeur (720) pour un fluide caloporteur se présentant à l'état de vapeur et une conduite à liquide (722) pour un fluide caloporteur liquide, la conduite à vapeur et la conduite à liquide étant séparées spatialement l'une de l'autre,
    en ce que le dispositif de transport de chaleur (14) présente au moins un deuxième caloduc (702),
    en ce que les deux caloducs (701, 702) présentent chacun un côté délivrant de la chaleur (718, 738) et un côté recevant de la chaleur (716, 736),
    en ce que le côté recevant de la chaleur (716) du au moins un premier caloduc à boucle (701) est disposé dans la source de chaleur externe (4), et
    en ce que le côté délivrant de la chaleur (718) du au moins un premier caloduc à boucle (701) est thermiquement intégré dans le côté recevant de la chaleur (736) du au moins un deuxième caloduc (702), et
    en ce que le côté délivrant de la chaleur (738) du au moins un deuxième caloduc (702) est disposé dans le récipient à pression de gazéificateur (706).
  6. Dispositif selon la revendication 5, caractérisé en ce que le au moins un deuxième caloduc (702) est un caloduc à boucle pulsé, présentant une conduite à vapeur/liquide (740) commune et disposé dans le récipient à pression de gazéificateur (706).
  7. Dispositif selon la revendication 6, caractérisé en ce que la conduite à vapeur/liquide (740) commune est conformée en méandre, en ce que le côté délivrant de la chaleur (738) du caloduc à boucle pulsé (702) est disposé dans la zone supérieure du récipient à pression de gazéificateur (706), et en ce que le côté recevant de la chaleur (736) est disposé dans la zone de fond du récipient à pression de gazéificateur (706).
  8. Dispositif selon l'une des revendications précédentes, caractérisé en ce que la source de chaleur externe (4) est une chambre de combustion pour lit fluidisé.
  9. Dispositif selon l'une des revendications précédentes, caractérisé en ce que le gazéificateur (2) est conçu sous forme de gazéificateur à lit fluidisé.
  10. Dispositif selon la revendication 8 ou 9, caractérisé en ce que le récipient à pression de gazéificateur (6) est relié à la chambre de combustion pour lit fluidisé (4) par l'intermédiaire d'un sas (24) pour des résidus de pyrolyse.
  11. Dispositif selon la revendication 9 ou 10, caractérisé en ce que le gazéificateur à lit fluidisé (802) et la chambre de combustion pour lit fluidisé (804) sont disposés dans un récipient (805) commun.
EP09763905A 2008-11-18 2009-11-18 Dispositif de production d'un produit gazeux combustible à partir de matières de charge carbonées Not-in-force EP2207616B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE202008015273 2008-11-18
PCT/EP2009/065389 WO2010057919A1 (fr) 2008-11-18 2009-11-18 Dispositif de production d'un produit gazeux combustible à partir de matières de charge carbonées

Publications (2)

Publication Number Publication Date
EP2207616A1 EP2207616A1 (fr) 2010-07-21
EP2207616B1 true EP2207616B1 (fr) 2011-08-03

Family

ID=41571782

Family Applications (1)

Application Number Title Priority Date Filing Date
EP09763905A Not-in-force EP2207616B1 (fr) 2008-11-18 2009-11-18 Dispositif de production d'un produit gazeux combustible à partir de matières de charge carbonées

Country Status (7)

Country Link
US (1) US20110259556A1 (fr)
EP (1) EP2207616B1 (fr)
CN (1) CN102215948A (fr)
AT (1) ATE518589T1 (fr)
BR (1) BRPI0921897A2 (fr)
CA (1) CA2743075C (fr)
WO (1) WO2010057919A1 (fr)

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009017854B4 (de) * 2009-04-17 2013-02-21 Highterm Research Gmbh Vorrichtung zur Erzeugung von Produktgas aus kohlenstoffhaltigen Einsatzstoffen mit Wärmerohren
DE102010043851A1 (de) 2010-11-12 2012-05-16 Highterm Research Gmbh Hochtemperatur-Wärmetransportvorrichtung
US8778212B2 (en) * 2012-05-22 2014-07-15 Cabot Microelectronics Corporation CMP composition containing zirconia particles and method of use
TWI580921B (zh) * 2014-05-09 2017-05-01 財團法人工業技術研究院 脈衝型多管式熱管
CN108458614A (zh) * 2018-04-13 2018-08-28 中国科学院理化技术研究所 一种回路热管
US11051428B2 (en) * 2019-10-31 2021-06-29 Hamilton Sunstrand Corporation Oscillating heat pipe integrated thermal management system for power electronics
JP7666033B2 (ja) * 2021-03-12 2025-04-22 株式会社リコー ウィック
FR3124585B1 (fr) * 2021-06-24 2023-11-10 Thales Sa Dispositif et procédé de contrôle passif du débit d’un fluide dans une boucle fluide diphasique à pompage mécanique
CN114214091B (zh) * 2021-12-20 2022-08-30 南京林业大学 生物质挥发分、水蒸气及生物质半焦三元气化反应制氢装置

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4474230A (en) * 1982-08-31 1984-10-02 Foster Wheeler Energy Corporation Fluidized bed reactor system
DE3929024A1 (de) 1989-09-01 1991-03-14 Deutsche Forsch Luft Raumfahrt Heatpipe
EP1187892B1 (fr) * 1999-06-09 2004-12-29 Technische Universität München Lehrstuhl für Thermische Kraftanlagen Dispositif permettant la gazeification de charges carbonees
US6810946B2 (en) 2001-12-21 2004-11-02 Tth Research, Inc. Loop heat pipe method and apparatus
DE102006016005A1 (de) 2006-04-05 2007-10-11 Bioage Gmbh Wärmerohr, Heatpipe-Reformer mit einem solchen Wärmerohr und Verfahren zum Betreiben eines solchen Heatpipe-Reformers

Also Published As

Publication number Publication date
BRPI0921897A2 (pt) 2015-12-29
EP2207616A1 (fr) 2010-07-21
CN102215948A (zh) 2011-10-12
WO2010057919A1 (fr) 2010-05-27
US20110259556A1 (en) 2011-10-27
CA2743075A1 (fr) 2010-05-27
CA2743075C (fr) 2014-05-06
ATE518589T1 (de) 2011-08-15

Similar Documents

Publication Publication Date Title
EP2207616B1 (fr) Dispositif de production d'un produit gazeux combustible à partir de matières de charge carbonées
DE69724792T2 (de) Brennstoffzellensystem zur stromerzeugung, heizung und kühlung und ventilation
EP2005100B1 (fr) Tube échangeur de chaleur, reformeur à caloduc comprenant un tel tube échangeur de chaleur et procédé pour utiliser un tel reformeur à caloduc
DE1881622U (de) Vorrichtung zur dampferzeugung mit einem atomreaktor als waermequelle.
DE112005000369T5 (de) Integrierte Brennstoffverarbeitungsanlage für eine dezentrale Wasserstoffproktion
EP2596218A2 (fr) Dispositif accumulateur de chaleur
EP4134609B1 (fr) Générateur de vapeur
DE102017001564A1 (de) Verfahren zum Starten einer Brennstoffzellenanordnung und Brennstoffzellenanordnung
EP0008633B1 (fr) Echangeur de chaleur pour l'application à haute pression et à haute température, procédé pour sa fabrication et application comme réacteur
DE102007050799B3 (de) Einrichtung zur Befeuchtung und Erhitzung eines zu reformierenden Brenngases für eine Brennstoffzellenanlage
DE2249581A1 (de) Waermetauscher
DE102006009062B4 (de) Kryoadsorptionssammelgefäß zur Verdampfungsverlustkompensation für Flüssiggasspeicherung
EP1836744A1 (fr) Reformeur pour une pile a combustible
DE102018118390A1 (de) Speichervorrichtung, thermochemische Speichereinheit und Verfahren zum Betreiben einer thermochemischen Speichereinheit
EP2588406B1 (fr) Dispositif de synthèse de hcl avec production de vapeur
DE2804187C2 (de) Wärmeaustauscher mit in einer Platte eingelassenen hängenden U-Rohren zur Abkühlung von unter hohem Druck und hoher Temperatur stehenden Prozeßgasen
DE102006029524B4 (de) Stromgenerator/Wasserstoffgewinnungs-Kombinationsanlage
EP2928818B1 (fr) Réacteur pour le dégagement d'hydrogène
AT521206B1 (de) Verdampfer für ein Brennstoffzellensystem sowie Brennstoffzellensystem
EP0045034A1 (fr) Dispositif pour éviter la formation de fissures sur les faces internes des ajutages d'admission de l'eau d'alimentation dans un récipient sous pression
WO2023041190A1 (fr) Réacteur, et dispositif et procédé de craquage d'ammoniac
DE102023136503B4 (de) Energiespeichereinheit
US3254705A (en) Steam generator
DE202009003094U1 (de) ORC-System für Verbrennungsmotoren
DE102011013026A1 (de) Verfahren und Anordnung zur Dampfreformierung kohlenwasserstoffhaltiger Gase

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: 20100525

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR

AX Request for extension of the european patent

Extension state: AL BA RS

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

DAX Request for extension of the european patent (deleted)
GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: GERMAN

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 502009001055

Country of ref document: DE

Effective date: 20111013

REG Reference to a national code

Ref country code: NL

Ref legal event code: VDEP

Effective date: 20110803

LTIE Lt: invalidation of european patent or patent extension

Effective date: 20110803

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

Ref country code: NO

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: 20111103

Ref country code: LT

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: 20110803

Ref country code: IS

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: 20111203

Ref country code: HR

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: 20110803

Ref country code: FI

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: 20110803

Ref country code: PT

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: 20111205

Ref country code: SE

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: 20110803

Ref country code: NL

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: 20110803

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

Ref country code: LV

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: 20110803

Ref country code: CY

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: 20110803

Ref country code: PL

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: 20110803

Ref country code: SI

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: 20110803

Ref country code: GR

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: 20111104

REG Reference to a national code

Ref country code: IE

Ref legal event code: FD4D

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

Effective date: 20110803

Ref country code: CZ

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: 20110803

Ref country code: SK

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: 20110803

BERE Be: lapsed

Owner name: HIGHTERM RESEARCH G.M.B.H.

Effective date: 20111130

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

Effective date: 20110803

Ref country code: EE

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: 20110803

Ref country code: RO

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: 20110803

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

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

Ref country code: DK

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: 20110803

Ref country code: MC

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

Effective date: 20111130

26N No opposition filed

Effective date: 20120504

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20120731

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 502009001055

Country of ref document: DE

Effective date: 20120504

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: 20111130

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: 20111130

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

Ref country code: MT

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: 20110803

Ref country code: MK

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: 20110803

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

Ref country code: SM

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: 20110803

Ref country code: ES

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: 20111114

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: 20111118

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

Ref country code: BG

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: 20111103

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

Ref country code: TR

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: 20110803

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

Ref country code: HU

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: 20110803

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

Ref country code: DE

Payment date: 20131112

Year of fee payment: 5

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

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

Effective date: 20131118

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

Ref country code: CH

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

Effective date: 20131130

Ref country code: LI

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

Effective date: 20131130

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: 20131118

REG Reference to a national code

Ref country code: DE

Ref legal event code: R119

Ref document number: 502009001055

Country of ref document: DE

REG Reference to a national code

Ref country code: DE

Ref legal event code: R082

Ref document number: 502009001055

Country of ref document: DE

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: 20150602

REG Reference to a national code

Ref country code: AT

Ref legal event code: MM01

Ref document number: 518589

Country of ref document: AT

Kind code of ref document: T

Effective date: 20141118

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

Ref country code: AT

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

Effective date: 20141118