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EP0625562A1 - Procédé pour la gazéification de substances solides et réacteur de gazéification - Google Patents

Procédé pour la gazéification de substances solides et réacteur de gazéification Download PDF

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Publication number
EP0625562A1
EP0625562A1 EP94107008A EP94107008A EP0625562A1 EP 0625562 A1 EP0625562 A1 EP 0625562A1 EP 94107008 A EP94107008 A EP 94107008A EP 94107008 A EP94107008 A EP 94107008A EP 0625562 A1 EP0625562 A1 EP 0625562A1
Authority
EP
European Patent Office
Prior art keywords
chamber
gas
fluidized bed
fluidizing
shaft
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
EP94107008A
Other languages
German (de)
English (en)
Other versions
EP0625562B1 (fr
Inventor
Eberhardt Dr.-Ing. Weiss
Ingo Heerens
Wolfgang Schmidt
Winfried Brunner
Markus Dr.-Ing. Pröll
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.)
Hitachi Zosen Inova Steinmueller GmbH
Original Assignee
Wamsler Umwelttechnik GmbH
Hugo Petersen 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 Wamsler Umwelttechnik GmbH, Hugo Petersen GmbH filed Critical Wamsler Umwelttechnik GmbH
Publication of EP0625562A1 publication Critical patent/EP0625562A1/fr
Application granted granted Critical
Publication of EP0625562B1 publication Critical patent/EP0625562B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • 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
    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • 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
    • C10J2300/0956—Air or oxygen enriched air

Definitions

  • the invention relates to a method for gasifying and burning solids, in particular residues, with the features of the preamble of claim 1 and a gasification reactor with the features of the preamble of claim 8.
  • the invention has for its object to provide a method and a gasification reactor of the type described in such a way that the duration of the gasification can be considerably shortened and the yield of the gasification can be optimized at the same time with a more compact design.
  • a method according to claim 1 serves to achieve this object.
  • a gasification reactor according to the invention is characterized by the features of claim 8.
  • solids that have fallen into the bed are not yet fully gasified or burned, are brought into suspension by means of the fluidizing and reaction gas in the fluidized bed formed according to the invention and are enveloped by gas on all sides.
  • the reaction gas which contains oxygen components, completely gasifies such solid components in a time that is many times shorter than the (short) degassing time, as if the solid components were in a solid bed or in the ash bed.
  • the gasification rate and the yield of gases is therefore significantly improved.
  • the gases produced are removed from the gasification reactor and burned in a separate combustion process to generate useful heat. Alternatively, they can at least partially be reintroduced into the shaft to support the degassing and gasification of the solids.
  • the unburned residual portions are of a negligible order. There are therefore no environmental problems because only ashes that are completely free of carbon and environmentally harmful components have to be disposed of.
  • the fluidizing space or a fluidized bed is formed in the shaft itself, namely in the ash bed.
  • the fluidizing chamber is formed separately below the shaft or next to it.
  • the shaft is separated from the fluidization chamber by a wall which can run horizontally and then form a partition, or can be formed vertically by a side wall of the shaft, in which case a passage is left for connecting the fluidization chamber which is divided into subspaces.
  • the gasification reactor shown in FIG. 1 has a vertical shaft 1 with an upper opening 3, through which 5 piece, carbon-containing solids such as wood, plastic, rubber, paper and textile waste and the like are introduced, for example by means of a cellular wheel sluice can.
  • the solids form a solid bed 7 in the upper part of the shaft 1 up to a support 9 in the form of a prism which can be pivoted about a pivot axis 11 is, and in the middle of its prismatic roof 13 has a rigid sheet metal plate 15, which serves to loosen the solid bed 7 and to close any gas channels formed in the bed during a pivoting movement of the prism 9 about the pivot axis 11.
  • the prism 9 forms constrictions 17, 19 on its two sides to the shaft inner walls 21, 23, so that when the prism oscillates, 13 solid particles are transported down through the constrictions 17, 19 into a chamber 25 in the shaft 1.
  • the gasification of the solid bed above the bottlenecks 17, 19 is promoted by supplying fresh air via nozzles 18, 20, in an amount that corresponds to a substoichiometric proportion of oxygen based on the amount of gas generated in the solid bed.
  • the nozzles 18, 20 penetrate the shaft side walls at different heights in the upper part of the shaft and can surround the shaft circumference in the form of nozzle rings with uniformly spaced nozzles.
  • the degassing of solid parts which have fallen through the narrow points 17, 19 is continued.
  • the gas generated is drawn off together with dust or ash parts via a lateral tube 27 and fed to a cyclone (not shown), where dust and ash are centrifugally separated, while the gas is fed to a combustion in a separate process for producing useful heat becomes.
  • An ash bed 29 is formed in the lower region of the shaft, into which solids that have not yet been completely gasified also fall.
  • a feed pipe 31 opens out laterally, via which a basic filling with a fine-grained inert is first of all provided by means of a screw conveyor 33 Material such as sand or ash and in operation is the material separated from the cyclone mentioned, and if necessary additional organic fine-grained material is conveyed into it.
  • the proportion of organic material should preferably not exceed 3% overall.
  • each nozzle tube 37 is formed by a tube piece which is closed at the top by a cover 39.
  • nozzle bores 41 are provided which are inclined downwards from the inside out. The nozzle bores 41 are thus directed downward into the fluidizing bed 29. Due to this construction of the nozzle tube, an outflow of inert material from the fluidizing bed 29 into a gas chamber 43 which is arranged under the bottom 35 and is fastened to the bottom 35 below the shaft 1 is avoided.
  • the gas chamber 43 has a side gas inlet 45 for an oxygen-containing fluidizing gas, which is pressed or sucked into the chamber 43 in the direction of the arrow f.
  • This fluidizing gas flows through the nozzle tubes 37 and the nozzle bores 41 into the bed 29 and fluidizes the inert material present there, so that a fluidized bed is formed from the fluidizing bed.
  • the differential pressure between the chamber 25 and the gas chamber 43 is measured via local pressure tapping openings 47 in the shaft wall and 49 in the chamber and is entered into a regulator 51. There is a comparison with a predetermined setpoint for the pressure difference.
  • a control deviation is activated by actuating the drive motor for a cellular wheel sluice 55 Output signal line 53 of controller 51 corrected.
  • the cellular wheel sluice 55 discharges a predetermined amount of inert material from the fluidized bed 29 via a discharge pipe 57 which penetrates the bottom 35 and the chamber 43 vertically.
  • the temperature in the fluidized bed 29 is recorded by means of a temperature sensor 59 and fed to a controller 61, which carries out a control comparison with a predetermined temperature setpoint in the order of 850 ° C. and, in the event of a control deviation, outputs an actuating signal via the control signal line 63 to a control valve 62.
  • the control valve 62 is in a branch line 60 for oxygen-rich gas, e.g. Air, turned on, which opens into line 46 downstream of a valve 65 set to a desired flow.
  • oxygen-rich gas e.g. Air
  • control loops with the controllers 51 and 61 are only shown in FIG. 1, but may also be provided in the same or modified form in the other design variants.
  • control of the oxygen content in a pressure source for oxygen-containing fluidizing gas can also be provided.
  • these different fluidized bed heights are taken into account in that the nozzle bores 41 of the lower-lying nozzle tubes 37a are dimensioned larger than the nozzle bores 41 of the higher ones located nozzle pipes 37b, so that larger amounts of gas flow through the lower-lying nozzle pipes 37a than through the higher-lying nozzle pipes 37b.
  • FIG. 2 Another difference of the embodiment according to FIG. 2 is that instead of a cellular wheel sluice 55, a screw conveyor 56 is provided for laterally discharging the ash to be removed from the fluidized bed 29 via the discharge pipe 57.
  • the screw 56 can convey into an ash container (not shown), from which the ash is then returned to the fluidized bed 29 via the screw 33.
  • the bottom 35 is inclined upwards in the manner of a funnel in the direction of the center of the shaft. It is thus favored that heavy or large parts, such as metal parts, which cannot be brought into suspension, get into the discharge pipe 57 due to their gravity and due to the movement in the fluidizing bed.
  • the ash is discharged here via an annular channel 58 surrounding the outer edge of the bottom 35, which communicates with the central discharge pipe 57 via vertical pipes 59 below the chamber 43.
  • the nozzles 37a with larger nozzle bores are to be arranged on the outside and the nozzle tubes 37b with smaller nozzle bores are to be arranged on the inside.
  • the highest central nozzle tube 37c expediently has the smallest nozzle bores, so that the least oxygen-containing fluidizing gas flows out there.
  • the chamber 25 tapers below the prism 9 in the shaft 1 downwards.
  • the left shaft wall 1a leaves a passage 67 down to the floor.
  • the gas chamber 43 is divided by a partition 44 into two chamber halves 43a and 43b, both of which are provided with their own gas inlets 45a and 45b.
  • a fluidized bed is formed here on the left and to the right of the wall 1a of the shaft in sections 29a, 29b which leaves the passage 67 open, the fluidized bed height in the fluidized bed part 29a in the shaft being considerably higher than the fluidized bed height in a closed chamber part 69 containing the fluidized bed part 29b.
  • the amount of fluidizing gas introduced into the fluidized bed portion 29a through the nozzles 37d must be considerably larger than the amount of fluidizing gas supplied through the nozzles 37e.
  • the nozzles 37e and 37d mentioned are to be dimensioned accordingly and the amounts of fluidizing gas supplied via the inlets 45a and 45b are metered.
  • Gas obtained from the closed space 69 above the fluidized bed part 29b is returned via a gas line 71 into the upper region of the shaft above the narrow points 17, 19 to promote degassing and gasification in this shaft part.
  • the gas discharged from the closed space 69 can also be used for other purposes, for example a separate combustion process for the recovery of useful heat.
  • the fluidizing chamber 75 containing the fluidized bed 29 is completely separated from the chamber 25 by a horizontal wall 73, so that a fluidizing chamber 75 which is completely closed off from the chamber 25 is formed.
  • the fluidized bed 29 produced in this fluidizing chamber 75 is fed with inert and gasified material as in the embodiment according to FIGS. 1 to 3 via a screw conveyor 33 and an inlet 31, the screw conveyor 33 also having a vertical pipe section 81 and a discharge screw 77 Drive motor 79 is fed with ash and only partially gasified solid particles discharged from the chamber 25.
  • FIG. 7 shows a further variant of a gasification reactor according to the invention.
  • the arrangement in this gasification reactor is similar to that according to FIG. 4, and the same reference numerals are used for identical or similar components.
  • the shaft wall 1 a leaves a lateral passage 67 down towards the bottom.
  • the gas chamber is divided by a partition 44 into two chamber halves 43a and 43b, both of which are provided with their own gas inlets, not shown here.
  • Fluidized bed parts 29a and 29b are each formed over the two chamber halves 43a and 43b, the bottom of the fluidized bed part 29 being inclined towards the partition wall 44.
  • nozzles 37m, 37n are provided, all of which end at the same level as in the embodiments according to FIGS. 4 and 5.
  • the nozzles have a length of 37m.
  • the partition wall 44 enables the pressures in the chamber halves 43a, 43b to be varied independently of one another, in particular a variation in the chamber half 43b. This makes it possible to set different free space speeds in the chamber parts 29a, 29b. As a result of this and because of the inclination of the bottom in the chamber half 43a, the mass transport for discharge into the chamber half 43b is ensured.
  • the gas generated mixes intensively with the gaseous and solid substances in the fluidized beds.
  • the residence time of the gases and dust particles in a zone of higher temperature is extended. This leads to a more intensive mass and heat exchange, so that the gas quality of the gas drawn off via the outlet 27a is improved, particularly with regard to the energy use in a downstream gas engine (cracking of long-chain hydrocarbons, such as tars).
  • the equilibrium reactions (Boudouard and / or methane equilibrium) and thus the gas quality with regard to the concentration of hydrogen or carbon monoxide can be improved by regulating the temperature of the fluidized bed.
  • FIG. 7 additionally shows a heat exchanger 90 arranged in the chamber 69 just before the gas outlet 27a.
  • This heat exchanger enables energy to be extracted in the form of heat by means of a heat transfer medium such as water or thermal oil flowing in the heat exchanger 90.
  • a heat transfer medium such as water or thermal oil flowing in the heat exchanger 90.
  • hot gas filters 92 made of ceramic material are used in the chamber part 69a, which ensure dust-free clean gas.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
  • Gasification And Melting Of Waste (AREA)
EP94107008A 1993-05-19 1994-05-04 Procédé pour la gazéification de substances solides et réacteur de gazéification Expired - Lifetime EP0625562B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4316869 1993-05-19
DE4316869A DE4316869C1 (de) 1993-05-19 1993-05-19 Verfahren zum Vergasen von Feststoffen und Vergasungsreaktor

Publications (2)

Publication Number Publication Date
EP0625562A1 true EP0625562A1 (fr) 1994-11-23
EP0625562B1 EP0625562B1 (fr) 1999-08-18

Family

ID=6488541

Family Applications (1)

Application Number Title Priority Date Filing Date
EP94107008A Expired - Lifetime EP0625562B1 (fr) 1993-05-19 1994-05-04 Procédé pour la gazéification de substances solides et réacteur de gazéification

Country Status (5)

Country Link
EP (1) EP0625562B1 (fr)
AT (1) ATE183541T1 (fr)
BR (1) BR9402015A (fr)
DE (2) DE4316869C1 (fr)
HU (1) HUT69015A (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19517527A1 (de) * 1995-05-12 1996-11-14 Petersen Hugo Verfahrenstech Vorrichtung zur Steuerung der Zufuhr von Vergasungsmedium zu einem Reaktor zum Vergasen von Feststoffen
US7223727B2 (en) 1998-04-09 2007-05-29 Serono Genetics Institute S.A. GSSP4 polynucleotides and polypeptides and uses thereof

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19718184C2 (de) * 1997-04-30 2003-05-28 Inst En Und Umwelttechnik E V Vorrichtung zur energetischen Nutzung von Brennstoffen, insbesondere Biobrennstoffen
DE19718611A1 (de) * 1997-05-02 1998-11-05 Hoffmeister Helmut Dr Verfahren und Vorrichtung zur thermischen Entsorgung vergasbarer Abfallstoffe
DE19836428C2 (de) * 1998-08-12 2000-07-13 Siempelkamp Guss Und Anlagente Verfahren und Vorrichtungen zum Vergasen von Biomasse, insbesondere Holzstoffen
DE10010358A1 (de) * 2000-03-07 2001-09-27 Bsbg Bremer Sonderabfall Berat Verfahren und Vorrichtung zum Vergasen von brennbarem Material
EP2126008A2 (fr) * 2007-03-06 2009-12-02 Lampros Elefsiniotis Gazogène à trois phases et lit fixe, qui comprend une zone tampon du courant gazeux entre la zone de pyrolyse et la zone de combustion
DE102023117169A1 (de) * 2023-06-29 2025-01-02 SHIT2POWER GmbH Downdraft-Festbett-Vergasungsreaktoranordnung zur Vergasung von Klärschlamm

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3945810A (en) * 1972-09-25 1976-03-23 Agency Of Industrial Science And Technology Apparatus for disposal of plastics
US4300914A (en) * 1980-03-20 1981-11-17 The United States Of America As Represented By The United States Department Of Energy Method and apparatus for gasifying with a fluidized bed gasifier having integrated pretreating facilities
US4388082A (en) * 1981-11-03 1983-06-14 Klockner-Humboldt-Deutz Ag Device for obtaining large amounts of combustible gas from carbonaceous materials
DE3523765A1 (de) * 1985-07-03 1987-01-08 Goe Ges Fuer Oekologische Ener Verfahren zur vergasung kohlenstoffhaltiger brennstoffe und vorrichtung zur durchfuehrung des verfahrens
DE3906790A1 (de) * 1989-03-03 1990-09-13 Forschungszentrum Juelich Gmbh Vergasungsreaktor fuer brennbare feststoffe
GB2259521A (en) * 1991-09-12 1993-03-17 Us Energy Moving bed coal gasifier
EP0554529A1 (fr) * 1992-02-03 1993-08-11 Deutsche Babcock Energie- und Umwelttechnik Aktiengesellschaft Procédé et appareil pour la gazéification de matériaux combustibles

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3924626A1 (de) * 1989-07-26 1991-01-31 Forschungszentrum Juelich Gmbh Vergasungsreaktor fuer brennbare feststoffe

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3945810A (en) * 1972-09-25 1976-03-23 Agency Of Industrial Science And Technology Apparatus for disposal of plastics
US4300914A (en) * 1980-03-20 1981-11-17 The United States Of America As Represented By The United States Department Of Energy Method and apparatus for gasifying with a fluidized bed gasifier having integrated pretreating facilities
US4388082A (en) * 1981-11-03 1983-06-14 Klockner-Humboldt-Deutz Ag Device for obtaining large amounts of combustible gas from carbonaceous materials
DE3523765A1 (de) * 1985-07-03 1987-01-08 Goe Ges Fuer Oekologische Ener Verfahren zur vergasung kohlenstoffhaltiger brennstoffe und vorrichtung zur durchfuehrung des verfahrens
DE3906790A1 (de) * 1989-03-03 1990-09-13 Forschungszentrum Juelich Gmbh Vergasungsreaktor fuer brennbare feststoffe
GB2259521A (en) * 1991-09-12 1993-03-17 Us Energy Moving bed coal gasifier
EP0554529A1 (fr) * 1992-02-03 1993-08-11 Deutsche Babcock Energie- und Umwelttechnik Aktiengesellschaft Procédé et appareil pour la gazéification de matériaux combustibles

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19517527A1 (de) * 1995-05-12 1996-11-14 Petersen Hugo Verfahrenstech Vorrichtung zur Steuerung der Zufuhr von Vergasungsmedium zu einem Reaktor zum Vergasen von Feststoffen
US7223727B2 (en) 1998-04-09 2007-05-29 Serono Genetics Institute S.A. GSSP4 polynucleotides and polypeptides and uses thereof

Also Published As

Publication number Publication date
BR9402015A (pt) 1995-07-11
HU9401450D0 (en) 1994-08-29
HUT69015A (en) 1995-08-28
DE59408630D1 (de) 1999-09-23
EP0625562B1 (fr) 1999-08-18
ATE183541T1 (de) 1999-09-15
DE4316869C1 (de) 1994-09-08

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