EP1485448A2 - Procede et dispositif de production de gaz - Google Patents

Procede et dispositif de production de gaz

Info

Publication number
EP1485448A2
EP1485448A2 EP02742810A EP02742810A EP1485448A2 EP 1485448 A2 EP1485448 A2 EP 1485448A2 EP 02742810 A EP02742810 A EP 02742810A EP 02742810 A EP02742810 A EP 02742810A EP 1485448 A2 EP1485448 A2 EP 1485448A2
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
heating tubes
heating
reactor
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP02742810A
Other languages
German (de)
English (en)
Inventor
Hubertus Winkler
Rolf Schmitt
Harald Hensler
Helmut WÖRZ
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.)
Bu Bioenergie & Umwelttechnik AG
Original Assignee
Bu Bioenergie & Umwelttechnik AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE10222604A external-priority patent/DE10222604A1/de
Application filed by Bu Bioenergie & Umwelttechnik AG filed Critical Bu Bioenergie & Umwelttechnik AG
Publication of EP1485448A2 publication Critical patent/EP1485448A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/0045—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by means of a rotary device in the flow channel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
    • 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
    • C10J3/46—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
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00752—Feeding
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • C10J2200/158—Screws
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1269—Heating the gasifier by radiating device, e.g. radiant tubes
    • 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
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Definitions

  • the invention relates to a device and a method for generating gas, in particular hydrogen-rich synthesis gas from biogenic or other carbon-containing material, the material being gasified allothermally in a reactor to produce a fluidized bed and the fluidized bed being heated.
  • Biogenic substances such as biomass, organic waste, sewage sludge or liquid manure, animal waste and other carbon-containing compounds are gasified using different processes and devices.
  • Autothermal heating means direct heating of the material to be gasified, for example by combustion with air or oxygen.
  • Autothermal systems are mainly implemented for small, decentralized applications and can only be used to a very limited extent with regard to downstream work machines due to the tar produced during the gasification reaction and the low calorific value of the gas generated. Gas engines can be significantly damaged by the tar in the gas produced.
  • the material to be gasified is indirectly heated by external heat.
  • external heat For example, it is conceivable to heat the walls of a reactor and thus transfer the heat to the material to be gasified.
  • water vapor gasification in a fluidized bed reactor supplies medium to high calorific gases with a high hydrogen content.
  • gas generated from biogenic substances corresponds to the syngas known in the chemical and petrochemical industry.
  • This gas offers great advantages in terms of energy use, since it has a very low tar content but a high hydrogen content having.
  • a gas of this composition can be used particularly well to generate electrical and thermal energy.
  • the heat can be introduced into the material to be gasified by circulating hot bed material.
  • the bed material is heated externally to high temperatures.
  • the second known method for introducing the required heat of reaction uses heating surfaces which are integrated into the fluidized bed of a fluidized bed reactor.
  • the external heating of bed material can result in high heat losses, so that complex insulation measures are necessary to prevent heat loss.
  • the other known technology which aims to integrate heating surfaces into the fluidized bed, geometrically complicated, extensive heating surfaces often have to be formed in order to realize a large heat exchange surface and an effective heat transfer. Because of these requirements for the heating surfaces, they have to be manufactured in a complex manner and often represent a considerable flow resistance in the fluidized bed.
  • the heating surfaces are often heated by external energy sources, for example electrically, and in this case large energy losses due to resistances, Thermal bridges or similar transport losses arise.
  • the present invention is therefore based on the object of designing a device and a method of the type mentioned at the outset and to further develop that an economical and effective production of gas can be realized.
  • a device for generating gas is characterized in that heating pipes in the area of the fluidized bed extend at least partially through the fluidized bed.
  • heating tubes enables a wide variety of media to be passed through the heating tubes, the media being able to heat the heating tubes. All fluid media are conceivable, so that a particularly effective heat transfer is made possible by choosing an appropriate flow rate of the media.
  • the use of heating pipes allows a high throughput of fluid, hot media, so that cooling of the heating pipes can be prevented very easily. As a result, effective heat transfer to the material to be gasified is possible.
  • heating tubes can be positioned in a fluidized bed reactor without any problems, since, owing to their aerodynamically favorable geometry, they hardly disturb the fluidized bed. It has also been ingeniously recognized that the use of heating tubes realizes a particularly high availability of the reactor, since each heating tube can be replaced and repaired individually without switching off the reactor.
  • a device for generating gas is specified in which an economical and effective generation of gas is realized.
  • the heating tubes could extend through the entire fluidized bed. With this configuration, an optimized heat transfer is also possible in the center of the reactor or the fluidized bed, since the heating tubes are, for example extend from one reactor wall to the opposite. A cylindrical configuration of the reactor or a configuration as a sphere is of course also possible.
  • the heating pipes could be oriented horizontally. This ensures that heat radiation can be emitted vertically upwards over a maximum area and thus a particularly effective heat transfer from the heating pipes to the material is possible.
  • the heating pipes could be oriented vertically. This embodiment realizes a low flow resistance, since flows running from bottom to top can form streamlines along the heating pipes.
  • the heating pipes could be oriented parallel to one another. In this way, for example in the case of vertical arrangement of the heating tubes, it is possible to stabilize the flow in the fluidized bed, since the tubes serve as a guide for the streamlines.
  • the heating tubes could form one or more different angles with the horizontal.
  • the effective heat radiation surface of the heating pipes acting vertically upwards can be set, so that areas of different heat radiation can be defined in the reactor.
  • the heating pipes could also enclose one or more different angles with one another.
  • the heating tubes could form the sides of a triangle or rectangle. This ensures that the material can flow through the surfaces spanned by the triangles or quadrilaterals. Here, the material can reach high speeds and is only disturbed by the pipes in its movement.
  • the heating pipes could be arranged in a star shape.
  • the tubes could converge in the middle of the star in a beam and touch or define a round or other shaped opening with their ends. If an opening is formed, a focusing effect on the flow of the fluidized bed can occur can be achieved, which causes a particularly suitable speed profile with regard to the gasification reaction. Material can pass through the opening at high speed and collide with other hot material particles. As a result, special effects can be achieved in certain reactions at phase interfaces, which can bring about an increase in sales.
  • the heating tubes could be arranged in mutually parallel or inclined planes. This configuration results in an even temperature distribution in the reactor.
  • the material to be gasified can collide several times in succession with the hot surfaces of the heating pipes and be stimulated to react.
  • the surfaces of heating tubes which only partially protrude into the fluidized bed and do not extend from the reactor wall to the reactor wall overlap those of other heating tubes.
  • the heating pipes could be heated by a flame burning in the heating pipe to radiate heat.
  • This specific configuration enables a uniform temperature profile along a heating tube, since the flame can burn in an elongated form along the heating tube. In this respect, there is no temperature gradient along the heating pipe.
  • a flame burning in the heating pipe can heat the heating pipe to such an extent that the radiant heat from the heating pipe enables effective heat transfer to the material to be gasified.
  • the wavelength of the thermal radiation can be influenced.
  • free convection can occur in the fluidized bed due to density differences within the fluidized bed. For example, it is conceivable that the density of the fluidized bed in the immediate vicinity of a heating pipe is significantly lower than at some distance.
  • the heat transfer coefficient could be significantly influenced by the resulting convection, which can ultimately have a positive effect on the effectiveness of the entire process.
  • the heating pipes could be heated by burning gas.
  • gas advantageously makes it possible that even process gas generated in the gasification process can be circulated and used for heating material to be gasified.
  • a modification of the flame could be created by adding air to the heating tubes. The addition of air could change the gas concentration and thus the temperature of the flame, so that the radiation characteristics of the heat radiation can be influenced. It is also conceivable that the air is supplied at a certain flow rate, so that the shape of the flame within the heating tube is modeled by the air flow. The shape of the flame has a significant influence on the heat transfer from the flame to the heating tube material.
  • Gases could be conducted in countercurrent in the heating pipes. This measure has the advantage that the temperatures of different gases can be used to heat or cool the heating pipes. For example, it is conceivable that hot gases flow along one side of the heating tube and cool gases along another. A spiral guide around the axis of the heating tube is also conceivable, which enables a particularly uniform temperature distribution in the entire heating tube.
  • Burnt gas especially flue gas
  • Burnt gas could be drawn out of the heating pipes in countercurrent to fresh gas to be burned. This measure effectively uses the temperature of the hot flue gas burned to heat the heating pipe and freshly supplied gas. In addition, a rapid supply of fuel to the flame is possible.
  • the temperature distribution in the fluidized bed and its fluidization could be adjusted by arranging the heating pipes in the reactor. It is conceivable that the heating tubes are arranged in any orientation within the reactor. For example, it is conceivable that the heating pipes define different levels in the fluidized bed. Triangular or rectangular fields or frames that are delimited by the heating pipes are also conceivable in any orientation. A suitable geometric arrangement of the heating pipes can prevent temperature gradients or unfavorable flows from forming inside the reactor. In this respect, an even temperature distribution and suitable swirling is always guaranteed.
  • the fluidized bed could be generated or fluidized by supplying water vapor. The use of water vapor in allothermal gasification processes enables the gas produced to be nitrogen-free and low in tar. In addition, it has a low dust load. The water vapor could be generated by waste heat from the process, the water vapor having a temperature between 650 ° C and 670 ° C degrees Celsius. This ensures an economic process while reducing the supply of external energy.
  • the water vapor could be introduced into the reactor from below.
  • This embodiment of the method effectively uses the effort of the water vapor to escape upwards, so that a fluidized bed is generated in a particularly favorable manner in terms of flow and energy.
  • the steam could be blown into the reactor through steam nozzles.
  • the provision of steam nozzles allows the fluidized bed to be modified so that the water vapor can be blown into the fluidized bed at different speeds.
  • various characteristic forms of the flow characteristics of the fluidized bed are conceivable, which can be adjusted depending on the application and reactivity of the material to be gasified.
  • the fluidized bed could be generated by injecting water vapor with the addition of the material to be gasified into the fluidized bed. This measure ensures that the material to be gasified is swirled immediately and is therefore subjected to heat exchange particularly quickly. This ensures that the desired reactions are particularly homogeneous and rapid.
  • a heating tube for radiating heat could be introduced.
  • the heat distribution could be adjusted both in the fluidized bed and in the rest of the reactor space through the heating tube. It is conceivable that there is a feedback between the individual heating pipes, which regulates the temperatures of the individual heating pipes according to a predetermined algorithm. It is advantageous here that overheating of the fluidized bed or similar undesirable effects can be regulated and controlled by an inherently dynamic process. In addition, suitable temperatures can be used to avoid or selectively limit undesirable post-reactions both in the fluidized bed and in the fluidized bed-free reactor space.
  • Solid particles could be introduced into the reactor space above the fluidized bed. Fine ash and coke particles in particular have a high surface area due to their very fine grain size and can therefore absorb heat radiation very well. The defined entry of solid particles in the expansion space allows very special reactions that can take place independently or overlaid to reactions in the fluidized bed.
  • the solid particles could be exposed to a higher temperature than that of the fluidized bed. This measure enables selective reactions which are not possible in the fluidized bed due to the lower temperature.
  • Particularly reactive gas components can advantageously be treated and possibly selectively subjected to a rapid aftertreatment.
  • a method for producing gas of the type mentioned at the outset is characterized in that heating tubes which extend at least partially through the fluidized bed are used in the region of the fluidized bed.
  • Fig. 1 is a sectional view of the reactor of the device, in which a
  • Fig. 2 is a schematic diagram of the inventive method for
  • FIG. 1 shows a sectional view of the reactor 1 of the device, in which a fluidized bed 2 is generated.
  • the fluidized bed 2 is heated by individual heating tubes 3 which extend through the fluidized bed 2.
  • the heating tubes 3 are arranged one above the other, horizontally and parallel to one another in the fluidized bed 2 and extend through the entire fluidized bed 2.
  • the heating tubes 3 are heated by a flame burning in the heating tube 3 to radiate heat.
  • Gas 4 is introduced into the heating pipes 3 and is burned by a flame.
  • Air 5 is also supplied to the heating pipes. Flue gas 6 is led out of the heating pipes 3 in countercurrent to fresh gas 4.
  • the fluidized bed 2 is fluidized by supplying water vapor 7.
  • the steam 7 is introduced into the reactor 1 from below.
  • the steam 7 is blown into the reactor 1 through steam nozzles 8.
  • the material 9 to be gasified is added to the fluidized bed 2 while injecting water vapor 7.
  • the material 9 is gasified in the reactor 1 allothermally Gas 10 is generated.
  • the generated gas 10 leaves the reactor 1 at its upper end via an outlet and can be treated further.
  • FIG. 2 shows an embodiment of the device in which a heating tube 11 is arranged in the reactor space above the fluidized bed 2.
  • the heat distribution both in the fluidized bed 2 and in the rest of the reactor space is adjusted by the heating tube 11. Undesired post-reactions are avoided by choosing suitable temperatures. Solids that are deposited on the bottom of the fluidized bed can optionally be removed by clocked slides.
  • Solid particles in particular ash or coke, are introduced into the reactor space above the fluidized bed 2. Due to their large surface area, the solid particles absorb heat radiation, the solid particles taking on a higher temperature than the fluidized bed temperature. This increases the conversion of carbon, which leads to an increase in the efficiency of gasification.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

Dispositif de production de gaz (10), en particulier de gaz de synthèse riche en hydrogène à partir d'une matière biogène (9) ou de toute autre matière carbonée (9), ladite matière (9) étant gazéifiée de manière allothermique dans un réacteur (1) avec production d'un lit fluidisé (2) et ledit lit fluidisé (2) étant chauffé. Selon la présente invention, pour obtenir une production économique et efficace de gaz, des tubes de chauffe (3) s'étendent au moins en partie à travers le lit fluidisé (2). La présente invention concerne en outre un procédé de production de gaz (10), en particulier de gaz de synthèse riche en hydrogène à partir de matière biogène (9) ou de toute autre matière carbonée (9), ladite matière (9) étant gazéifiée de manière allothermique dans un réacteur (1) avec production d'un lit fluidisé (2) et ledit lit fluidisé (2) étant chauffé. Le lit fluidisé (2) est chauffé par des tubes de chauffe (3) qui s'étendent au moins en partie à travers ledit lit fluidisé (2).
EP02742810A 2001-07-20 2002-06-19 Procede et dispositif de production de gaz Withdrawn EP1485448A2 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE10134442 2001-07-20
DE10134442 2001-07-20
DE10222604A DE10222604A1 (de) 2001-07-20 2002-05-17 Vorrichtung und ein Verfahren zur Erzeugung von Gas
DE10222604 2002-05-17
PCT/DE2002/002242 WO2003012014A2 (fr) 2001-07-20 2002-06-19 Procede et dispositif de production de gaz

Publications (1)

Publication Number Publication Date
EP1485448A2 true EP1485448A2 (fr) 2004-12-15

Family

ID=26009709

Family Applications (1)

Application Number Title Priority Date Filing Date
EP02742810A Withdrawn EP1485448A2 (fr) 2001-07-20 2002-06-19 Procede et dispositif de production de gaz

Country Status (2)

Country Link
EP (1) EP1485448A2 (fr)
WO (1) WO2003012014A2 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008058347A1 (fr) * 2006-11-17 2008-05-22 Millennium Synfuels, Llc Fabrication de combustibles
ITTO20110145A1 (it) * 2011-02-21 2012-08-22 Pierluigi Martini Apparato per la decomposizione di sostanze organiche vegetali e la produzione di gas combustibile per via termochimica, e relativo gassificatore.

Family Cites Families (7)

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Publication number Priority date Publication date Assignee Title
GB644013A (en) * 1946-08-15 1950-10-04 Standard Oil Dev Co Improvements in or relating to the supply of heat to fluidized solid systems
GB866481A (en) * 1957-10-16 1961-04-26 Jaroslav Beranek Apparatus for the performance of physical and chemical processes in a liquefied layer
GB1525222A (en) * 1973-05-05 1978-09-20 Pearce A Fluidised beds
GB2116686B (en) * 1982-02-18 1985-01-30 Tokyo Shibaura Electric Co Heat exchangers installed in fluidized beds
DE3600432A1 (de) * 1985-05-21 1987-02-05 Gutehoffnungshuette Man Verfahren zum vergasen eines kohlenstoffhaltigen brennstoffs, insbesondere kohle
US5059404A (en) * 1989-02-14 1991-10-22 Manufacturing And Technology Conversion International, Inc. Indirectly heated thermochemical reactor apparatus and processes
DE19900116C2 (de) * 1999-01-05 2002-02-14 Univ Muenchen Tech Vorrichtung zum Erzeugen von Brenngas durch allotherme Vergasung von Biomasse

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO03012014A3 *

Also Published As

Publication number Publication date
WO2003012014A2 (fr) 2003-02-13
WO2003012014A3 (fr) 2003-10-02

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