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EP0062363A1 - Procédé pour la production simultanée de gaz combustible et d'énergie thermique à partir de matières carbonacées - Google Patents

Procédé pour la production simultanée de gaz combustible et d'énergie thermique à partir de matières carbonacées Download PDF

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Publication number
EP0062363A1
EP0062363A1 EP82200261A EP82200261A EP0062363A1 EP 0062363 A1 EP0062363 A1 EP 0062363A1 EP 82200261 A EP82200261 A EP 82200261A EP 82200261 A EP82200261 A EP 82200261A EP 0062363 A1 EP0062363 A1 EP 0062363A1
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EP
European Patent Office
Prior art keywords
gas
fluidized bed
gasification
stage
combustion
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
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EP82200261A
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German (de)
English (en)
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EP0062363B1 (fr
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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Priority to AT82200261T priority Critical patent/ATE17866T1/de
Publication of EP0062363A1 publication Critical patent/EP0062363A1/fr
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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 method for the simultaneous generation of fuel gas and process heat from carbon-containing materials by gasification in a first fluidized bed stage and subsequent combustion of the combustible constituents remaining in the gasification in a second fluidized bed stage.
  • 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 and thus has enables short-term adaptation to the respective energy form requirement.
  • 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 low-quality coal, such as coal washing mountains, mud coal, coal with a high salt content. tiv. However, lignite and oil shale can also be used.
  • the principle of the circulating fluidized bed used in the gasification and combustion stage 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 - distribution states without 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 solid matter discharge into 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.
  • the carbonaceous material does not already have the amount of water vapor required for gasification itself in the form of moisture, it is necessary to add water vapor for the gasification reaction.
  • 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 method of operation does not rule out that the entry of subordinate amounts of water vapor can also take place together with the oxygen-containing secondary gas and the entry of subordinate amounts of oxygen-containing gases together with water vapor as the fluidizing gas.
  • the residence time of the gases in the gasification stage - calculated above the entry point of the carbon-containing material - is usually realized by entering the carbonaceous material at a higher level in the gasification stage. This results on the one hand in a gas richer in smoldering products with a correspondingly higher calorific value, and on the other hand it is ensured that the gas has practically no hydrocarbons with more than 6 carbon atoms.
  • the gas can be desulfurized using the usual desulfurizing agents.
  • a preferred embodiment consists in 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 ⁇ m and for this purpose an average suspension density of 0.1 to in the fluidized bed reactor 10 kg / m 3 , preferably 1 to 5 kg / m 3 , and 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 gas 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 desulfurization 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 combustible constituents not converted in the gasification stage are burned in a further circulating fluidized bed, and at the same time the by-products obtained during gas cleaning are removed in an environmentally friendly manner.
  • the loaded desulphurizing agents coming from the gas cleaning 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.
  • the other by-products, such as dust from gas dedusting and gas water, are also removed.
  • process heat is understood to be a heat transfer medium, the energy content of which can be used in various ways for carrying out processes. It can be gas for heating or - if it is an oxygen-containing gas - for the operation of various types of combustion devices.
  • the generation of saturated steam or superheated steam - likewise for heating, for example reactors - or for driving electrical generators or the heating of heat transfer salts, for example for heating tubular reactors or autoclaves, is particularly advantageous.
  • the combustion is carried out in two stages with oxygen-containing gases supplied at different levels.
  • Their advantage lies in " soft" combustion, in which local overheating phenomena are avoided and NO x 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 point has already been largely consumed.
  • an advantageous embodiment of the invention consists in creating an average suspension density of 15 to 100 kg / m 3 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 one Gas supply to remove cooling surfaces located within 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 the diameter to the 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.
  • any gas which does not impair the nature of the exhaust gas can be used as the fluidizing gas.
  • Inert gases such as recirculated flue gas (exhaust gas), nitrogen and water vapor, are suitable. With a view to intensifying the combustion process, however, it is advantageous to use oxygen-containing gas as the fluidizing gas.
  • 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 resulting, certain, average suspension 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.
  • the increased heat transfer at a practically constant combustion temperature there is the possibility of dissipating the amounts of heat generated with increased combustion output.
  • the increased oxygen requirement required due to the higher combustion capacity is here virtually automatically 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 expedient here - via one or more lances, e.g. by pneumatic blowing.
  • Another expedient, universally applicable design of the combustion process consists in creating an average suspension density of 10 to 40 kg / m3 above the upper gas supply by adjusting the amounts of fluidization and secondary gas, removing hot solids from the circulating fluidized bed and cooling in the fluidized state by direct and indirect heat exchange and return at least a partial flow of cooled solid to 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, for example, 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 regulated by recirculating 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 entry-cooled solid which is, for example, given to a pneumatic conveyor line or a floating exchanger stage, the solid which is subsequently 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 gas residence times and gas velocities are above the secondary gas Line at normal pressure and type of fluidization or secondary gas supply in accordance with the same parameters of the previously discussed embodiment.
  • 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 makes it possible to bind the heat of combustion to a comparatively small amount of coolant.
  • 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 at will in the combustion stage without influencing the fuel gas generation in the gasification stage.
  • Air or oxygen-enriched air or technically pure oxygen can be used as oxygen-containing gases in the process according to the invention.
  • 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, for example up to 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 fed 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 13, a filter device 14 and another 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, respectively Fluidizing gas or supplied as a secondary gas.
  • a separate addition of fuel and line 27 of desulfurizing agent is possible via line 26.
  • desulphurization agents, sludge and gas water are also introduced, which are introduced via lines 11 or 42 or 43.
  • 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.
  • the return line 23 becomes by means of line. 33 a partial stream of solid circulated via fluidized bed reactor 21, separating cyclone 22 and return line 23 was removed and cooled in the fluidized bed cooler 34.
  • the dust 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 fed via line 41 to the fluidized bed cooler 34 and heated there passes via line 39 as a secondary gas into the fluidized bed reactor 21.
  • Recooled solid is fed to the fluidized bed reactor 21 via line 40 to absorb the heat of combustion.
  • saturated steam of 45 bar was 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 m 3 N / h of fuel gas were discharged via line 44. The calorific value of the fuel gas generated was 10.6 MJ / m 3 N.
  • the gasification circulating fluidized bed of gasification residues was removed via line 18 and together with the loaded desulphurized via line 11 and the filter residue discharged via line 43 are fed via line 20 to the fluidized bed reactor 21 '.
  • the total feed rate was 1869 kg / h.
  • the fluidized bed reactor 21 was further supplied with 34 3400 m 3 N / h of air via the fluidizing gas line 24 and 4900 m 3 N / h of air via the secondary gas line 25.
  • 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 m3N / h.
  • the latter airflow was at a temperature of 500 ° C.
  • the combustion temperature in the fluidized bed reactor was 850 ° C.
  • 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 desulfurized gas emerged together with the loaded desulfurization agent at a temperature of 900 ° 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 a quantity of 1.52 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, 3400 m 3 N / h of fuel gas were removed via line 44. The calorific value of the fuel gas generated was 10.6 MJ / m 3 N.
  • the gasification circulating fluidized bed of gasification residue was removed via line 18 and, together with the loaded desulfurizing agent discharged via line 11 and filter residue discharged via line 43, was passed via line 20 to the fluidized bed reactor 21.
  • the total feed rate was 2068 kg / h.
  • the fluidized bed reactor 21 was further supplied with air via the fluidizing gas line 24 3075 m 3 N / h and air via secondary gas line 25 7325 m 3 N / 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 m 3 N / h.
  • the last-mentioned air stream had a temperature of 500 o C.
  • 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 fluidized bed cooler 34 which has four separate cooling chambers, was in turn fluidized with 1900 m 3 N / h of air, which heated up to a mixing temperature of 500 ° C. As already mentioned above, it was fed to the fluidized bed reactor 21 as a secondary gas via line 39.
  • the energy used according to this example was divided as follows:
  • Example 2 was varied in that the energy generation in the combustion stage was increased by additional coal combustion without any change within the gasification stage.
  • Example 2 changing operation were t / h steam at 45 bar and 480 o C and produced in the radiator 34 302 t / h heat transfer salt of 350 to 420 ° C heated in the waste heat boiler 30 5.7.
  • the amount of solids passed through the fluidized bed cooler 34 had to be increased to 73 t / h '. 760 kg / h of ash and 284 kg / h of sulfated desulfurization agent were obtained.

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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 Procédé pour la production simultanée de gaz combustible et d'énergie thermique à partir de matières carbonacées Expired EP0062363B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT82200261T ATE17866T1 (de) 1981-04-07 1982-03-02 Verfahren zur gleichzeitigen erzeugung von brenngas und prozesswaerme aus kohlenstoffhaltigen materialien.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3113993 1981-04-07
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EP0119648A3 (fr) * 1983-03-22 1985-07-10 Metallgesellschaft Ag Procédé pour gazéifier des combustibles solides en lit mouvant et lit fluidisé
EP0171097A1 (fr) * 1984-08-04 1986-02-12 Metallgesellschaft Ag Procédé de fabrication d'éponge de fer
EP0227196A3 (en) * 1985-12-27 1988-01-20 Shell Internationale Research Maatschappij B.V. Oxidation of flyash
EP0334833A1 (fr) * 1988-03-11 1989-09-27 VOEST-ALPINE INDUSTRIEANLAGENBAU GESELLSCHAFT m.b.H. Procédé pour la gazéification sous pression de charbon pour le fonctionnement d'une centrale énergétique
EP0468357A1 (fr) * 1990-07-23 1992-01-29 Mitsubishi Jukogyo Kabushiki Kaisha Méthode de combustion gaséifiante et méthode de production d'énergie par gaséification
FR2669099A1 (fr) * 1990-11-13 1992-05-15 Stein Industrie Procede et dispositif de combustion de materiaux carbones divises.
EP0634470A1 (fr) * 1993-07-12 1995-01-18 M. W. Kellogg Company Gazéificateur à lit entraîné
WO1996021824A1 (fr) * 1995-01-10 1996-07-18 Von Roll Umwelttechnik Ag Procede de traitement thermique de dechets
EP0725127A1 (fr) * 1995-02-03 1996-08-07 Metallgesellschaft Ag Procédé pour la gazéification de matériau contenant des substances combustibles dans une couche fluidisée circulante
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Cited By (21)

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Publication number Priority date Publication date Assignee Title
EP0117928A1 (fr) * 1983-01-13 1984-09-12 Metallgesellschaft Ag Procédé de fabrication d'acier par fusion d'éponge de fer dans un four à arc
EP0119648A3 (fr) * 1983-03-22 1985-07-10 Metallgesellschaft Ag Procédé pour gazéifier des combustibles solides en lit mouvant et lit fluidisé
EP0171097A1 (fr) * 1984-08-04 1986-02-12 Metallgesellschaft Ag Procédé de fabrication d'éponge de fer
EP0227196A3 (en) * 1985-12-27 1988-01-20 Shell Internationale Research Maatschappij B.V. Oxidation of flyash
EP0334833A1 (fr) * 1988-03-11 1989-09-27 VOEST-ALPINE INDUSTRIEANLAGENBAU GESELLSCHAFT m.b.H. Procédé pour la gazéification sous pression de charbon pour le fonctionnement d'une centrale énergétique
EP0468357A1 (fr) * 1990-07-23 1992-01-29 Mitsubishi Jukogyo Kabushiki Kaisha Méthode de combustion gaséifiante et méthode de production d'énergie par gaséification
US5224338A (en) * 1990-07-23 1993-07-06 Mitsubishi Jukogyo Kabushiki Kaisha Gasifying combustion method and gasifying power generation method
FR2669099A1 (fr) * 1990-11-13 1992-05-15 Stein Industrie Procede et dispositif de combustion de materiaux carbones divises.
EP0634470A1 (fr) * 1993-07-12 1995-01-18 M. W. Kellogg Company Gazéificateur à lit entraîné
CH690790A5 (de) * 1995-01-10 2001-01-15 Von Roll Umwelttechnik Ag Verfahren zur thermischen Behandlung von Abfallmaterial.
WO1996021824A1 (fr) * 1995-01-10 1996-07-18 Von Roll Umwelttechnik Ag Procede de traitement thermique de dechets
EP0725127A1 (fr) * 1995-02-03 1996-08-07 Metallgesellschaft Ag Procédé pour la gazéification de matériau contenant des substances combustibles dans une couche fluidisée circulante
WO2007128370A1 (fr) * 2006-05-10 2007-11-15 Outotec Oyj PROcÉdÉ ET INSTALLATION de production De CHARBON ET De GAZ COMBUSTIBLE
US9175226B2 (en) 2007-12-12 2015-11-03 Outotec Oyj Process and plant for producing char and fuel gas
US9371487B2 (en) 2007-12-12 2016-06-21 Outotec Oyj Process and plant for producing char and fuel gas
WO2011135518A3 (fr) * 2010-04-29 2013-04-04 Foster Wheeler North America Corp. Dispositif de combustion à lit fluidisé entraîné et procédé de commande d'un dispositif de combustion à lit fluidisé entraîné
EP2500401A1 (fr) * 2011-03-14 2012-09-19 Metso Power OY Procédé de traitement de cendres et installation de traitement de cendres
US8833278B2 (en) 2011-03-14 2014-09-16 Valmet Power Oy Method for processing ash, and an ash processing plant
DE102011100490A1 (de) 2011-05-04 2012-11-08 Outotec Oyj Verfahren und Anlage zur Erzeugung und Weiterbehandlung von Brenngas
WO2012150097A1 (fr) 2011-05-04 2012-11-08 Outotec Oyj Procédé et plante pour la production et le traitement ultérieur d'un gaz combustible
WO2014096524A1 (fr) * 2012-12-20 2014-06-26 Foster Wheeler Energia Oy Procédé et appareil pour réguler un gazéifieur

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US4444568A (en) 1984-04-24
NO821072L (no) 1982-10-08
DE3268909D1 (en) 1986-03-20
ZA822345B (en) 1983-11-30
CS250214B2 (en) 1987-04-16
AU545446B2 (en) 1985-07-11
JPS57179290A (en) 1982-11-04
ES8306785A1 (es) 1983-06-01
FI821104L (fi) 1982-10-08
MX159901A (es) 1989-09-29
JPH0466919B2 (fr) 1992-10-26
GR75461B (fr) 1984-07-20
FI821104A0 (fi) 1982-03-30
IE820796L (en) 1982-10-07
CA1179846A (fr) 1984-12-27
AU8238982A (en) 1982-10-14
EP0062363B1 (fr) 1986-02-05
IN152949B (fr) 1984-05-05
NO155545B (no) 1987-01-05
DE3113993A1 (de) 1982-11-11
AR227714A1 (es) 1982-11-30
ES511221A0 (es) 1983-06-01
NO155545C (no) 1987-04-15
IE52546B1 (en) 1987-12-09
NZ199930A (en) 1985-07-31
FI73724B (fi) 1987-07-31
BR8201974A (pt) 1983-03-15
ATE17866T1 (de) 1986-02-15
FI73724C (fi) 1987-11-09

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