EP0062363B1 - Verfahren zur gleichzeitigen Erzeugung von Brenngas und Prozesswärme aus kohlenstoffhaltigen Materialien - Google Patents

Verfahren zur gleichzeitigen Erzeugung von Brenngas und Prozesswärme aus kohlenstoffhaltigen Materialien Download PDF

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Publication number
EP0062363B1
EP0062363B1 EP82200261A EP82200261A EP0062363B1 EP 0062363 B1 EP0062363 B1 EP 0062363B1 EP 82200261 A EP82200261 A EP 82200261A EP 82200261 A EP82200261 A EP 82200261A EP 0062363 B1 EP0062363 B1 EP 0062363B1
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Prior art keywords
gas
fluidized bed
combustion
process according
stage
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EP82200261A
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German (de)
English (en)
French (fr)
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EP0062363A1 (de
Inventor
Hans Beisswenger
Georg Dr. Daradimos
Martin Hirsch
Ludolf Dr. Plass
Harry Dr. Serbent
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GEA Group AG
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Metallgesellschaft AG
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    • 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
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/86—Other features combined with waste-heat boilers
    • 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
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
    • 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
    • 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
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
    • 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
    • C10J2300/0959—Oxygen
    • 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
    • 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
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2206/00—Fluidised bed combustion
    • F23C2206/10—Circulating fluidised bed
    • F23C2206/101—Entrained or fast fluidised bed

Definitions

  • the invention relates to a process for the simultaneous generation of fuel gas and process heat from carbon-containing materials by gasification in a first fluidized bed and subsequent combustion of the combustible constituents remaining in the gasification in a second fluidized bed, the gasification being carried out at a pressure of at most 5 bar and one Temperature of 800 to 1100 ° C by means of oxygen-containing gases in the presence of water vapor and 40 to 80 wt .-% of the carbon contained in the starting material are reacted, and then the residue from the gasification together with the by-products from gas cleaning are fed to a further fluidized bed becomes.
  • DE A 27 29 764 relates to a process for the gasification of carbon-containing material by means of oxygen-containing gases and water vapor, in which the gasification residue is then burned and the combustion gas is used as an additional gasification agent and heat transfer medium in the gasification reactor. Both gasification and combustion take place in the "classic fluidized bed", ie in a fluidized state which is completely different compared to the "circulating fluidized beds” used in the application.
  • the process envisages entering the by-products from mechanical gas cleaning (dust) and gas cooling (water) into the combustion stage. There is no detailed information on the desulfurization of the gases produced.
  • US Pat. No. 4,026,679 deals with the production of fuel gas by two-stage gasification of carbon-containing material using two expanded fluidized beds connected in a crosswise manner. The desulfurization of the gas produced takes place for the most part in the gasification reactor itself. A combustion and thus generation of process heat is not provided.
  • the object of the invention is to provide a method for the simultaneous generation of fuel gas and process heat from carbon-containing materials which does not have the known, in particular the aforementioned disadvantages, high flexibility in converting the energy content of the starting material into fuel gas on the one hand and process heat on the other hand owns and thus enables a short-term adjustment to the respective energy form requirement.
  • the object is achieved by designing the method of the type mentioned at the outset in accordance with the invention in such a way that both the gasification and the combustion take place in a separate, circulating fluidized bed and the two gas streams obtained are cleaned, cooled and dedusted separately, the in the gasification stage generated fuel gas at a temperature in the range of 800 to 1000 ° C i. Whirl state is freed of sulfur compounds with the aid of CaS-forming materials and the combustion of the remaining combustible constituents takes place at an air ratio of ⁇ 1.05 to 1.40.
  • the method according to the invention can be used for all carbon-containing materials which can be gasified and burned independently. It is suitable for all types of coal, but is particularly attractive for coal of inferior quality, such as coal washing mountains, mud coal, coal with a high salt content. However, lignite and oil shale can also be used.
  • the principle of the circulating fluidized bed used in the gasification and combustion stages It is characterized in that, in contrast to the "classic" fluidized bed, in which a dense phase is separated from the gas space above by a clear density jump, there are distribution states without a defined boundary layer. A leap in density between the dense phase and the dust space above it does not exist; however, the solids concentration within the reactor decreases continuously from bottom to top.
  • the desulfurization of the gas produced can take place in any vortex state, e.g. in a Venturi fluidized bed with solids discharge in a downstream separator.
  • a circulating fluidized bed can also advantageously be used for desulfurization.
  • a particularly advantageous embodiment of the invention consists in converting 40 to 60% by weight of the carbon contained in the starting material into the gasification. In this way, a fuel gas with a particularly high calorific value can be generated. In addition, it is possible to dispense with the use of otherwise significantly higher amounts of water vapor, which in the subsequent process steps are again produced as gas water which is undesirable per se.
  • water vapor and the required oxygen-containing gas should be entered at different levels.
  • An expedient embodiment of the invention consists in that in the gasification stage water vapor, predominantly in the form of fluidizing gas, and oxygen-containing gas, predominantly in the form of secondary gas, are supplied. This procedure does not rule out that the entry of minor amounts of water vapor can also take place together with the oxygen-containing secondary gas and the entry of minor amounts of oxygen-containing gases together with water vapor as the fluidizing gas.
  • the residence time of the gases above the entry point of the carbon-containing material is 1 to 5 seconds in the gasification stage.
  • This condition is usually realized by entering the carbonaceous material at a higher level in the gasification stage.
  • this creates a gas that is richer in smoldering products and has a correspondingly higher calorific value, and on the other hand it ensures that the gas has practically no hydrocarbons with more than 6 carbon atoms.
  • the gas can be desulfurized using the usual desulfurization agents.
  • a preferred embodiment consists of desulfurizing the gases emerging from the gasification stage in a circulating fluidized bed by means of lime or dolomite or the corresponding fired products with a particle size dp 50 of 30 to 200 tim, and for this purpose an average suspension density of 0.1 to 10 kg / m in the fluidized bed reactor 3 , preferably 1 to 5 kg / m 3; and to set an hourly solids circulation rate which is at least 5 times the solids weight in the reactor shaft.
  • This procedure is characterized in that the desulfurization can be carried out at high Oas throughputs and at a very constant temperature.
  • the high temperature stability has a positive effect on the desulfurization in that the desulfurizing agent retains its activity and thus its absorption capacity against sulfur.
  • the high degree of granularity of the desulfurization agent complements this advantage, since the ratio of surface area to volume is particularly favorable for the binding rate of the sulfur, which is essentially determined by the rate of diffusion.
  • the desulphurization agent dosage should be at least 1.2 to 2.0 times the stoichiometric requirement be. It should be noted that when using dolomite or burnt dolomite, practically only the calcium component reacts with the sulfur compounds.
  • the desulfurizing agent is most advantageously introduced into the fluidized bed reactor via one or more lances, e.g. by pneumatic blowing.
  • a preferred embodiment of the invention consists in adding all of the desulfurization agent also required for the combustion stage to the gas desulfurization stage. In this way, the thermal energy required for heating and possibly for deacidification is withdrawn from the gas and thus preserved in the combustion stage.
  • the combustion of the combustible constituents not converted in the gasification stage takes place in a further circulating fluidized bed, at the same time also eliminating the by-products obtained in gas cleaning in an environmentally friendly manner.
  • the loaded desulphurization agents coming from the gas purification stage in particular insofar as they are in sulfidic form, such as calcium sulfide, are sulfated and thereby converted into landfill-compatible compounds, such as calcium sulfate.
  • the heat of reaction released in the sulfation process is also obtained as process heat, and the other by-products, such as dust from gas dedusting and gas water, are also removed.
  • process heat is a heat transfer medium, the energy content of which can be used in various ways to carry out processes. It can be gas for heating or, if it is an oxygen-containing gas, for the operation of combustion devices of various types.
  • the generation of saturated steam or superheated steam is also particularly advantageous for heating, for example of reactors or for driving electrical generators, or for heating heat transfer salts, for example for heating tubular reactors or autoclaves.
  • the combustion is in two stages with different levels supplied oxygen-containing gases performed.
  • Their advantage lies in "soft" combustion, in which local overheating phenomena are avoided and NO o formation is largely suppressed.
  • the upper supply point for oxygen-containing gas should be so far above the lower one that the oxygen content of the gas supplied at the lower part has already been largely consumed.
  • an advantageous embodiment of the invention consists in creating an average suspension density of 15 to 100 kg / m3 above the upper gas supply by adjusting the amounts of fluidization and secondary gas and at least a substantial part of the heat of combustion by means of above the upper gas supply within the dissipate cooling surfaces in the free reactor space.
  • the gas velocities prevailing in the fluidized bed reactor above the secondary gas supply are generally above 5 m / s at normal pressure and can be up to 15 m / s and the ratio of diameter to height of the fluidized bed reactor should be chosen such that gas residence times of 0.5 to 8. 0 s, preferably 1 to 4 s, are obtained.
  • a plurality of supply openings for secondary gas are advantageous within each entry level.
  • the advantage of this procedure is in particular that a change in the production of process heat is possible in the simplest way by changing the suspension density in the furnace space of the fluidized bed reactor located above the secondary gas supply.
  • a certain heat transfer is associated with a prevailing operating state under predetermined fluidizing gas and secondary gas volumes and the resultant specific average bus pension density.
  • the heat transfer to the cooling surfaces can be increased by increasing the suspension density by increasing the amount of fluidizing gas and possibly also the amount of secondary gas. With the increased heat transfer at practically constant combustion temperature, it is possible to dissipate the amounts of heat generated with increased combustion output.
  • the increased oxygen requirement required due to the higher combustion output is here virtually automatically present due to the higher fluidization gas and possibly secondary gas quantities used to increase the suspension density.
  • the combustion output can be regulated by reducing the suspension density in the furnace space of the fluidized bed reactor located above the secondary gas line. By lowering the suspension density, the heat transfer is also reduced, so that less heat is removed from the fluidized bed reactor.
  • the combustion performance can be reduced essentially without a change in temperature.
  • the entry of the carbonaceous material is also most conveniently via one or more lances, e.g. by pneumatic blowing.
  • Another expedient, more universally applicable design of the combustion process consists in creating an average suspension density of 10 to 40 kg / m 3 above the upper gas supply by adjusting the amounts of fluidization and secondary gas, removing hot solids from the circulating fluidized bed and in the fluidized state by direct and indirect heat exchange cool and return at least a partial flow of cooled solid into the circulating fluidized bed.
  • the temperature constancy can be achieved practically without changing the operating conditions prevailing in the fluidized bed reactor, that is to say without changing the suspension density, among other things, solely by controlled recycling of the cooled solid.
  • the recirculation rate is more or less high.
  • the combustion temperatures can range from very low temperatures, which are close above the ignition limit, to very high temperatures
  • Set temperatures as required which are limited by softening the combustion residues. They can be between 450 ° C and 950 ° C.
  • the combustion temperature in the fluidized bed reactor is controlled by recycling at least a partial stream of cooled solid from the fluidized bed cooler.
  • the required partial flow of cooled solid can be fed directly into the fluidized bed reactor.
  • the exhaust gas can also be cooled by introducing cooled solid matter, which is fed, for example, to a pneumatic conveyor line or a floating exchanger stage, the solid matter which is later separated off from the exhaust gas then being returned to the fluidized bed cooler.
  • the exhaust gas heat ultimately ends up in the fluidized bed cooler. It is particularly advantageous to enter cooled solid as a partial stream directly and as another indirectly after cooling the exhaust gases in the fluidized bed reactor.
  • the recooling of the hot solid of the fluidized bed reactor should take place in a fluidized bed cooler with several cooling chambers flowing through one after the other, into which interconnected cooling registers are immersed, in countercurrent to the coolant. This enables the heat of combustion to be bound to a comparatively small amount of coolant.
  • the universality of the last-mentioned embodiment is particularly given by the fact that almost any heat transfer media can be heated in the fluidized bed cooler. Of particular importance from a technical point of view is the generation of steam in various forms and the heating of heat transfer salt.
  • the flexibility of the method according to the invention can be further increased if, in a further advantageous embodiment of the invention, the combustion stage is additionally fed with carbon-containing materials.
  • This embodiment has the advantage that the production of process heat can be increased as desired in the combustion stage without influencing the combustion gas generation in the gasification stage.
  • air or oxygen-enriched air or technically pure oxygen can be used as the oxygen-containing gases.
  • the use of an oxygen-rich gas is recommended.
  • an increase in performance can be achieved within the combustion stage by carrying out the combustion under pressure, up to about 20 bar.
  • the fluidized bed reactors used in carrying out the method according to the invention can be of rectangular, square or circular cross section.
  • the lower region of the fluidized bed reactor can also be conical, which is particularly advantageous in the case of large reactor cross sections and thus high gas throughputs.
  • Carbon-containing material is added to the circulating fluidized bed formed from the fluidized bed reactor 1, the cyclone separator 2 and the return line 3 via line 4 and gasified there by adding oxygen via secondary gas line 5 and water vapor via fluidizing gas line 6.
  • the gas generated is dedusted in a second cyclone separator 7 and introduced into a Venturi reactor 8, which is supplied with desulfurizing agent via line 9.
  • the desulfurization agent is introduced together with the gas into a waste heat boiler 10, separated there and discharged via line 11.
  • the gas enters a scrubber 12, in which it is freed of residual dust.
  • the washing liquid is pumped through line I3, a filter device 14 and a further line 15. Finally, the gas arrives in a condenser 16 for water separation and is then discharged via line 44 after passing through a wet electrostatic precipitator 17.
  • the gasification residue is taken from the circulating fluidized bed 1, 2, 3 via line 18, via a cooler 19 and line 20 of the second circulating fluidized bed used for combustion and formed from a fluidized bed reactor 21, cyclone separator 22 and return line 23.
  • Oxygen-containing gas is supplied via lines 24 and 25 as fluidizing gas and as secondary gas.
  • a separate addition of fuel is possible via line 26 and of desulfurizing agent via line 27.
  • desulphurization agents, sludge and gas water are also introduced, which are introduced via lines 11, 42 and 43, respectively.
  • the gas emerging from the separator 22 of the fluidized bed reactor 21 is freed of dust in a further cyclone separator 29 and cooled in a waste heat boiler 30. Further ash is extracted from the exhaust gas in the separator 31.
  • the exhaust gas is finally discharged via line 32.
  • a partial flow of solid circulated via fluidized bed reactor 21, separating cyclone 22 and return line 23 is withdrawn from return line 23 by means of line 33 and cooled in fluidized bed cooler 34.
  • the dust which is deposited in the separating cyclone 29 and in the waste heat boiler 30 is fed via lines 35, 36 and 37, respectively.
  • a heat transfer salt is used as the coolant, which is passed in countercurrent through the fluidized bed cooler 34 by means of cooling registers 38.
  • the oxygen-containing fluidizing gas which is supplied to the fluidized bed cooler 34 via line 41 and heated there passes via line 39 as secondary gas into the fluidized bed reactor 21 Solid is fed to the fluidized bed reactor 21 via line 40 to absorb the heat of combustion.
  • the desulfurized gas together with the loaded desulfurizing agent emerged at a temperature of 920 ° C. and was introduced into the waste heat boiler 10. 155 kg / h of loaded desulfurizing agent were obtained in the waste heat boiler 10, and saturated steam of 45 bar was also produced in an amount of 1.75 t / h.
  • the dedusted and cooled gas then reached the scrubber 12, in which it was cleaned with washing liquid pumped over line 13, filter device 14 and line 15. It was then transferred to the condenser 16 by being cooled to 35 ° C by indirect cooling. After passing through a wet electrostatic precipitator 17, 3940 Nm 3 / h of fuel gas were removed via line 44. The calorific value of the fuel gas generated was 10.6 MJ / Nm 3 .
  • the gasification circulating fluidized bed of gasification residue was removed via line 18 and fed to the fluidized bed reactor 21 via line 20 together with the loaded desulphurizing agent discharged via line 11 and the filter residue discharged via line 43.
  • the total feed rate was 1869 kg / h.
  • the fluidized bed reactor 21 was also supplied with 34 3400 Nm 3 of air via the fluidizing gas line 24 and 25 4900 Nm 3 / h of air via the secondary gas line.
  • Another secondary gas supply in the form of air heated in the fluidized bed cooler 34 was carried out via line 39 in an amount of 1900 Nm 3 / h. The latter air flow was at a temperature of 500 ° C.
  • the combustion temperature was 850 ° C and above the top secondary gas line an average suspension density of 30 kg / m 3 .
  • the exhaust gas from the fluidized bed reactor was freed from the solids discharged in the downstream recycle cyclone 22, dusted in the downstream cyclone separator 29 and finally introduced into the waste heat boiler 30.
  • the temperature of the exhaust gases was reduced from 850 ° C. to 140 ° C. 3.6 t / h of superheated steam of 45 bar and 480 ° C. were generated.
  • the gas was then introduced into the separator 31 and freed from further ash there. Finally, it was fed to the chimney at a temperature of 140 ° C. via line 32.
  • 660 kg / h of ash and an additional 247 kg / h of sulfated desulfurizing agent were obtained.
  • the ash quantity of 660 kg / h corresponds to the total ash production in the combustion stage.
  • the gasification circulating fluidized bed of gasification residue was removed via line 18 and fed to the fluidized bed reactor 21 via line 20 together with the loaded desulphurizing agent discharged via line 11 and the filter residue discharged via line 43.
  • the total feed rate was 2068 kg / h.
  • the fluidized bed reactor 21 was further supplied with air via the fluidizing gas line 24 3075Nm 3 / h air and secondary gas line 25 7325Nm 3 / h.
  • Another secondary gas supply in the form of air heated in the fluidized bed cooler 34 was carried out via line 39 in an amount of 1900 Nm 3 / h. The latter air flow was at a temperature of 500 ° C.
  • the combustion temperature was 850 ° C and above the uppermost secondary gas line an average suspension density of 30 kg / m 3 .
  • the exhaust gas from the fluidized bed reactor was freed from the solids discharged in the downstream recycle cyclone 22, dusted in the downstream cyclone separator 29 and finally introduced into the waste heat boiler 30.
  • the temperature of the exhaust gases was reduced from 850 ° C. to 140 ° C. 4.4 t / h of superheated steam of 45 bar and 480 ° C. were generated.
  • the gas was then introduced into the separator 31 and freed from further ash there. Finally, it was fed to the chimney at a temperature of 140 ° C. via line 32.
  • 660 kg / h of ash and an additional 247 kg / h of sulfated desulfurizing agent were obtained.
  • the ash quantity of 660 kg / h corresponds to the total ash production in the combustion stage.
  • the heat transfer salt heated up to 420 ° C.
  • the ashes cooled in the cooler 34 to 400 ° C. were returned to the fluidized bed reactor 21 via line 40 to absorb the heat of combustion.
  • the fluidized bed cooler 34 which has four separate cooling chambers, was in turn fluidized with 1900 Nm 3 / h of air, which heated up to a mixing temperature of 500 ° C. As already mentioned above, it was fed via line 39 to the fluidized bed reactor 21 as secondary gas.
  • the energy parts which were used according to this example were divided as follows:
  • Example 2 was varied insofar as the energy generation in the combustion stage was increased by additional coal combustion without any change within the gasification stage.
  • the one led over the fluidized bed cooler 34 Increase the amount of solids to 73 t / h. 760 kg / h of ash and 284 kg / h of sulfated desulfurizing agent were obtained. Based on the total amount of coal added, the harnessed energy was divided as follows:

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Carbon And Carbon Compounds (AREA)
EP82200261A 1981-04-07 1982-03-02 Verfahren zur gleichzeitigen Erzeugung von Brenngas und Prozesswärme aus kohlenstoffhaltigen Materialien Expired EP0062363B1 (de)

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DE3113993A DE3113993A1 (de) 1981-04-07 1981-04-07 Verfahren zur gleichzeitigen erzeugung von brenngas und prozesswaerme aus kohlenstoffhaltigen materialien

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Families Citing this family (106)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6117199A (en) * 1982-04-26 2000-09-12 Foster Wheeler Energia Oy Method and apparatus for gasifying solid carbonaceous material
DE3300867A1 (de) * 1983-01-13 1984-07-19 Mannesmann AG, 4000 Düsseldorf Verfahren zur erzeugung von stahl durch einschmelzen von eisenschwamm im lichtbogenofen
DE3310220A1 (de) * 1983-03-22 1984-09-27 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum vergasen fester brennstoffe im wanderbett und im wirbelbett
DE3428782A1 (de) * 1984-08-04 1986-02-13 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur erzeugung von eisenschwamm
DE3439600A1 (de) * 1984-10-30 1986-05-07 Carbon Gas Technologie GmbH, 4030 Ratingen Verfahren zur erzeugung von schwefelarmem gas aus feingemahlenen kohlenstoffhaltigen feststoffen
US4676177A (en) * 1985-10-09 1987-06-30 A. Ahlstrom Corporation Method of generating energy from low-grade alkaline fuels
EP0220342A1 (de) * 1985-11-01 1987-05-06 Metallgesellschaft Ag Verfahren zum Behandeln von wasserhaltigem Kondensat
DE3673362D1 (de) * 1985-12-27 1990-09-13 Shell Int Research Oxydation von flugasche.
DE3612888A1 (de) * 1986-04-17 1987-10-29 Metallgesellschaft Ag Kombinierter gas-/dampfturbinen-prozess
AT392079B (de) * 1988-03-11 1991-01-25 Voest Alpine Ind Anlagen Verfahren zum druckvergasen von kohle fuer den betrieb eines kraftwerkes
US4880439A (en) * 1988-05-05 1989-11-14 Texaco Inc. High temperature desulfurization of synthesis gas
DE3929926A1 (de) * 1989-09-08 1991-03-21 Metallgesellschaft Ag Verfahren zum behandeln der gase aus der vergasung fester, feinkoerniger brennstoffe
EP0468357B1 (en) * 1990-07-23 1993-11-24 Mitsubishi Jukogyo Kabushiki Kaisha Gasifying combustion method and gasifying power generation method
FR2669099B1 (fr) * 1990-11-13 1994-03-18 Stein Industrie Procede et dispositif de combustion de materiaux carbones divises.
US5403366A (en) * 1993-06-17 1995-04-04 Texaco Inc. Partial oxidation process for producing a stream of hot purified gas
US5375408A (en) * 1993-07-06 1994-12-27 Foster Wheeler Development Corporation Combined-cycle power generation system using a coal-fired gasifier
CA2127394A1 (en) * 1993-07-12 1995-01-13 William Martin Campbell Transport gasifier
US5447702A (en) * 1993-07-12 1995-09-05 The M. W. Kellogg Company Fluid bed desulfurization
WO1996006147A1 (en) * 1994-08-23 1996-02-29 Foster Wheeler Energia Oy Method of operating a fluidized bed reactor system, and system
CH690790A5 (de) * 1995-01-10 2001-01-15 Von Roll Umwelttechnik Ag Verfahren zur thermischen Behandlung von Abfallmaterial.
DE19503438A1 (de) * 1995-02-03 1996-08-08 Metallgesellschaft Ag Verfahren zum Vergasen von brennbare Bestandteile enthaltendem Material in der zirkulierenden Wirbelschicht
FI110266B (fi) * 1999-01-25 2002-12-31 Valtion Teknillinen Menetelmä hiilipitoisen polttoaineen kaasuttamiseksi leijukerroskaasuttimessa
EP1198541A1 (en) * 1999-05-14 2002-04-24 Kemestrie Inc. Process and apparatus for gasification of refuse
ES2183662B1 (es) * 1999-05-14 2003-12-16 Kemestrie Inc Recipiente de reaccion de gasificacion y procedimiento correspondiente
ES2190689B1 (es) * 2000-03-15 2004-10-16 Luis M. Santi De Azcoitia Y Villanueva Procedimiento de obtencion de gas combustible a partir de materiales combustibles.
US20050084434A1 (en) * 2003-10-20 2005-04-21 Enviroserve Associates, L.L.C. Scrubbing systems and methods for coal fired combustion units
DE102004030370B3 (de) * 2004-06-23 2005-12-15 Kirchner, Hans Walter, Dipl.-Ing. Verfahren zur Abkühlung und Entteerung von Brenngas aus Biomassevergasungen
FI120162B (fi) * 2005-02-17 2009-07-15 Foster Wheeler Energia Oy Leijupetikattilalaitos ja menetelmä rikkipitoisen polttoaineen polttamiseksi leijupetikattilalaitoksessa
US8114176B2 (en) * 2005-10-12 2012-02-14 Great Point Energy, Inc. Catalytic steam gasification of petroleum coke to methane
AU2006201957B2 (en) * 2006-05-10 2008-06-05 Outotec Oyj Process and plant for producing char and fuel gas
US7922782B2 (en) * 2006-06-01 2011-04-12 Greatpoint Energy, Inc. Catalytic steam gasification process with recovery and recycle of alkali metal compounds
AU2008282518B2 (en) * 2007-08-02 2012-03-01 Greatpoint Energy, Inc. Catalyst-loaded coal compositions, methods of making and use
US20090090056A1 (en) * 2007-10-09 2009-04-09 Greatpoint Energy, Inc. Compositions for Catalytic Gasification of a Petroleum Coke
WO2009048723A2 (en) * 2007-10-09 2009-04-16 Greatpoint Energy, Inc. Compositions for catalytic gasification of a petroleum coke and process for conversion thereof to methane
US9371487B2 (en) 2007-12-12 2016-06-21 Outotec Oyj Process and plant for producing char and fuel gas
CN101910371B (zh) * 2007-12-28 2014-04-02 格雷特波因特能源公司 用于制备合成气衍生产物的方法
US20090165382A1 (en) * 2007-12-28 2009-07-02 Greatpoint Energy, Inc. Catalytic Gasification Process with Recovery of Alkali Metal from Char
WO2009086407A2 (en) 2007-12-28 2009-07-09 Greatpoint Energy, Inc. Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock
US20090165384A1 (en) * 2007-12-28 2009-07-02 Greatpoint Energy, Inc. Continuous Process for Converting Carbonaceous Feedstock into Gaseous Products
WO2009086361A2 (en) * 2007-12-28 2009-07-09 Greatpoint Energy, Inc. Catalytic gasification process with recovery of alkali metal from char
WO2009086383A2 (en) * 2007-12-28 2009-07-09 Greatpoint Energy, Inc. Catalytic gasification process with recovery of alkali metal from char
WO2009086372A1 (en) * 2007-12-28 2009-07-09 Greatpoint Energy, Inc. Carbonaceous fuels and processes for making and using them
WO2009086366A1 (en) * 2007-12-28 2009-07-09 Greatpoint Energy, Inc. Processes for making synthesis gas and syngas-derived products
US20090165380A1 (en) * 2007-12-28 2009-07-02 Greatpoint Energy, Inc. Petroleum Coke Compositions for Catalytic Gasification
CN101910373B (zh) * 2007-12-28 2013-07-24 格雷特波因特能源公司 从焦炭中回收碱金属的催化气化方法
WO2009086363A1 (en) * 2007-12-28 2009-07-09 Greatpoint Energy, Inc. Coal compositions for catalytic gasification and process for its preparation
AU2008345189B2 (en) * 2007-12-28 2011-09-22 Greatpoint Energy, Inc. Petroleum coke compositions for catalytic gasification
US20090220406A1 (en) * 2008-02-29 2009-09-03 Greatpoint Energy, Inc. Selective Removal and Recovery of Acid Gases from Gasification Products
WO2009111342A2 (en) * 2008-02-29 2009-09-11 Greatpoint Energy, Inc Carbonaceous fines recycle
US7926750B2 (en) * 2008-02-29 2011-04-19 Greatpoint Energy, Inc. Compactor feeder
WO2009111330A1 (en) * 2008-02-29 2009-09-11 Greatpoint Energy, Inc. Processes for making adsorbents and processes for removing contaminants from fluids using them
US8286901B2 (en) * 2008-02-29 2012-10-16 Greatpoint Energy, Inc. Coal compositions for catalytic gasification
US8114177B2 (en) * 2008-02-29 2012-02-14 Greatpoint Energy, Inc. Co-feed of biomass as source of makeup catalysts for catalytic coal gasification
US8366795B2 (en) * 2008-02-29 2013-02-05 Greatpoint Energy, Inc. Catalytic gasification particulate compositions
WO2009111332A2 (en) * 2008-02-29 2009-09-11 Greatpoint Energy, Inc. Reduced carbon footprint steam generation processes
US8297542B2 (en) * 2008-02-29 2012-10-30 Greatpoint Energy, Inc. Coal compositions for catalytic gasification
US20090217575A1 (en) * 2008-02-29 2009-09-03 Greatpoint Energy, Inc. Biomass Char Compositions for Catalytic Gasification
WO2009111331A2 (en) * 2008-02-29 2009-09-11 Greatpoint Energy, Inc. Steam generation processes utilizing biomass feedstocks
WO2009124017A2 (en) * 2008-04-01 2009-10-08 Greatpoint Energy, Inc. Processes for the separation of methane from a gas stream
CA2718536C (en) * 2008-04-01 2014-06-03 Greatpoint Energy, Inc. Sour shift process for the removal of carbon monoxide from a gas stream
CN102076828A (zh) * 2008-06-27 2011-05-25 格雷特波因特能源公司 用于合成气制备的四列催化气化体系
CN102112585B (zh) * 2008-06-27 2013-12-04 格雷特波因特能源公司 用于sng生产的三列催化气化系统
CA2729003C (en) * 2008-06-27 2014-08-12 Francis S. Lau Two-train catalytic gasification systems
US20090324461A1 (en) * 2008-06-27 2009-12-31 Greatpoint Energy, Inc. Four-Train Catalytic Gasification Systems
WO2009158583A2 (en) * 2008-06-27 2009-12-30 Greatpoint Energy, Inc. Four-train catalytic gasification systems
WO2010033850A2 (en) 2008-09-19 2010-03-25 Greatpoint Energy, Inc. Processes for gasification of a carbonaceous feedstock
CN102159687B (zh) * 2008-09-19 2016-06-08 格雷特波因特能源公司 使用炭甲烷化催化剂的气化方法
EP2326699A2 (en) 2008-09-19 2011-06-01 Greatpoint Energy, Inc. Processes for gasification of a carbonaceous feedstock
WO2010033848A2 (en) * 2008-09-19 2010-03-25 Greatpoint Energy, Inc. Processes for gasification of a carbonaceous feedstock
WO2010048493A2 (en) 2008-10-23 2010-04-29 Greatpoint Energy, Inc. Processes for gasification of a carbonaceous feedstock
CN102272267A (zh) 2008-12-30 2011-12-07 格雷特波因特能源公司 制备催化的碳质微粒的方法
EP2370549A1 (en) * 2008-12-30 2011-10-05 Greatpoint Energy, Inc. Processes for preparing a catalyzed coal particulate
KR101468768B1 (ko) 2009-05-13 2014-12-04 그레이트포인트 에너지, 인크. 탄소질 공급원료의 히드로메탄화 방법
CN102459525B (zh) * 2009-05-13 2016-09-21 格雷特波因特能源公司 进行含碳原料的加氢甲烷化的方法
US8268899B2 (en) * 2009-05-13 2012-09-18 Greatpoint Energy, Inc. Processes for hydromethanation of a carbonaceous feedstock
WO2010141629A1 (en) * 2009-06-02 2010-12-09 Thermochem Recovery International, Inc. Gasifier having integrated fuel cell power generation system
US20110031439A1 (en) * 2009-08-06 2011-02-10 Greatpoint Energy, Inc. Processes for hydromethanation of a carbonaceous feedstock
CN102667057B (zh) * 2009-10-19 2014-10-22 格雷特波因特能源公司 整合的强化采油方法
AU2010310849B2 (en) * 2009-10-19 2013-05-02 Greatpoint Energy, Inc. Integrated enhanced oil recovery process
AU2010339953A1 (en) * 2009-12-17 2012-07-05 Greatpoint Energy, Inc. Integrated enhanced oil recovery process injecting nitrogen
WO2011084580A2 (en) * 2009-12-17 2011-07-14 Greatpoint Energy, Inc. Integrated enhanced oil recovery process
US8669013B2 (en) 2010-02-23 2014-03-11 Greatpoint Energy, Inc. Integrated hydromethanation fuel cell power generation
US8652696B2 (en) * 2010-03-08 2014-02-18 Greatpoint Energy, Inc. Integrated hydromethanation fuel cell power generation
EP2563883A1 (en) 2010-04-26 2013-03-06 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with vanadium recovery
US20110265697A1 (en) * 2010-04-29 2011-11-03 Foster Wheeler North America Corp. Circulating Fluidized Bed Combustor and a Method of Operating a Circulating Fluidized Bed Combustor
JP5559428B2 (ja) 2010-05-28 2014-07-23 グレイトポイント・エナジー・インコーポレイテッド 液体重質炭化水素フィードストックのガス状生成物への変換
KR101424941B1 (ko) 2010-08-18 2014-08-01 그레이트포인트 에너지, 인크. 탄소질 공급원료의 히드로메탄화
KR101543136B1 (ko) 2010-11-01 2015-08-07 그레이트포인트 에너지, 인크. 탄소질 공급원료의 히드로메탄화
CA2827916C (en) 2011-02-23 2016-06-21 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with nickel recovery
FI124422B (fi) * 2011-03-14 2014-08-29 Valmet Power Oy Menetelmä tuhkan käsittelemiseksi ja tuhkan käsittelylaitos
DE102011100490A1 (de) 2011-05-04 2012-11-08 Outotec Oyj Verfahren und Anlage zur Erzeugung und Weiterbehandlung von Brenngas
CN103582693A (zh) 2011-06-03 2014-02-12 格雷特波因特能源公司 碳质原料的加氢甲烷化
WO2012168945A1 (en) * 2011-06-10 2012-12-13 Bharat Petroleum Corporation Limited Process for co-gasification of two or more carbonaceous feedstocks and apparatus thereof
US9012524B2 (en) 2011-10-06 2015-04-21 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US20140065559A1 (en) * 2012-09-06 2014-03-06 Alstom Technology Ltd. Pressurized oxy-combustion power boiler and power plant and method of operating the same
KR101646890B1 (ko) 2012-10-01 2016-08-12 그레이트포인트 에너지, 인크. 응집된 미립자 저등급 석탄 공급원료 및 그의 용도
US9328920B2 (en) 2012-10-01 2016-05-03 Greatpoint Energy, Inc. Use of contaminated low-rank coal for combustion
WO2014055349A1 (en) 2012-10-01 2014-04-10 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9034058B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
FI125951B (en) * 2012-12-20 2016-04-29 Amec Foster Wheeler En Oy A method for adjusting a circulating fluidized bed gasifier
CN103742899B (zh) * 2014-01-23 2016-05-04 上海锅炉厂有限公司 一种富氧燃烧循环流化床多联产系统及工艺
US10464872B1 (en) 2018-07-31 2019-11-05 Greatpoint Energy, Inc. Catalytic gasification to produce methanol
US10344231B1 (en) 2018-10-26 2019-07-09 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization
US10435637B1 (en) 2018-12-18 2019-10-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization and power generation
US10618818B1 (en) 2019-03-22 2020-04-14 Sure Champion Investment Limited Catalytic gasification to produce ammonia and urea
FR3130944B1 (fr) * 2021-12-17 2023-12-15 Ifp Energies Now Installation et procede de combustion en boucle comportant un reacteur air cyclonique

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2588075A (en) * 1945-12-18 1952-03-04 Standard Oil Dev Co Method for gasifying carbonaceous fuels
GB665077A (en) * 1949-01-03 1952-01-16 Standard Oil Dev Co Improvements in or relating to the production of water gas
US3807090A (en) * 1970-12-02 1974-04-30 Exxon Research Engineering Co Purifications of fuels
GB1542862A (en) * 1975-02-14 1979-03-28 Exxon Research Engineering Co Combustion or part-combustion in fluidized beds
SE7503313L (sv) * 1975-03-21 1976-09-22 Stora Kopparbergs Bergslags Ab Sett for omvandling av kolhaltiga material innehallande svavel till i huvudsak svavelfri brennbar gas samt anordning for genomforande av settet
US4165717A (en) * 1975-09-05 1979-08-28 Metallgesellschaft Aktiengesellschaft Process for burning carbonaceous materials
US4069304A (en) * 1975-12-31 1978-01-17 Trw Hydrogen production by catalytic coal gasification
DE2624302A1 (de) * 1976-05-31 1977-12-22 Metallgesellschaft Ag Verfahren zur durchfuehrung exothermer prozesse
JPS5354202A (en) * 1976-10-27 1978-05-17 Ube Ind Ltd Gasification of coal or its mixture with heavy liquid hydrocarbon influidized beds and gasifying furnaces
DE2729764A1 (de) * 1977-07-01 1979-01-04 Davy Bamag Gmbh Verfahren zur vergasung von kohlenstoffhaltigem material
JPS5851989B2 (ja) * 1977-11-01 1983-11-19 工業技術院長 石炭類のガス化方法
DE2836175A1 (de) * 1978-08-18 1980-02-28 Metallgesellschaft Ag Verfahren zum vergasen fester, feinkoerniger brennstoffe

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US4444568A (en) 1984-04-24
AR227714A1 (es) 1982-11-30
JPH0466919B2 (cs) 1992-10-26
FI821104A0 (fi) 1982-03-30
IE52546B1 (en) 1987-12-09
IE820796L (en) 1982-10-07
FI73724B (fi) 1987-07-31
AU545446B2 (en) 1985-07-11
DE3113993A1 (de) 1982-11-11
NO155545C (no) 1987-04-15
MX159901A (es) 1989-09-29
EP0062363A1 (de) 1982-10-13
GR75461B (cs) 1984-07-20
ATE17866T1 (de) 1986-02-15
NO155545B (no) 1987-01-05
FI821104L (fi) 1982-10-08
DE3268909D1 (en) 1986-03-20
BR8201974A (pt) 1983-03-15
ES511221A0 (es) 1983-06-01
CS250214B2 (en) 1987-04-16
ZA822345B (en) 1983-11-30
FI73724C (fi) 1987-11-09
NO821072L (no) 1982-10-08
IN152949B (cs) 1984-05-05
NZ199930A (en) 1985-07-31
CA1179846A (en) 1984-12-27
JPS57179290A (en) 1982-11-04
AU8238982A (en) 1982-10-14
ES8306785A1 (es) 1983-06-01

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