WO2000069995A1 - Process and apparatus for the gasification of carbonaceous material - Google Patents
Process and apparatus for the gasification of carbonaceous material Download PDFInfo
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- WO2000069995A1 WO2000069995A1 PCT/FI2000/000435 FI0000435W WO0069995A1 WO 2000069995 A1 WO2000069995 A1 WO 2000069995A1 FI 0000435 W FI0000435 W FI 0000435W WO 0069995 A1 WO0069995 A1 WO 0069995A1
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- gas
- scrubber
- dry scrubber
- gasification
- process according
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Classifications
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- 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
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- 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
-
- 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
- C10J2300/0903—Feed preparation
- C10J2300/0909—Drying
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
-
- 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
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
- C10J2300/092—Wood, cellulose
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1621—Compression of synthesis gas
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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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1643—Conversion of synthesis gas to energy
- C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
-
- 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
- C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis gas
Definitions
- the present invention relates to a process according to the preamble of Claim 1 for the gasification of a starting material made up of a carbonaceous material.
- the starting material is gasified at an elevated temperature in the presence of oxygen.
- the condensable compounds are separated from the gases obtained from the gasification, and the product gases thus obtained are recovered.
- the invention also relates to an apparatus according to the preamble of Claim 12, the apparatus comprising a gasification unit and, connected to the gasification unit, a unit for the removal of condensable compounds.
- Thermochemical gasification is a process wherein by a partial oxidation by elevating the temperature a carbonaceous raw material, such as biomass or coal, is converted to gaseous substances.
- a carbonaceous raw material such as biomass or coal
- gasification reactors for ex- ample, solid-bed, fluidized-bed, moving-bed and rotary-bed reactors.
- cyclone and vortex reactors there are known, for example, cyclone and vortex reactors.
- the product gas obtained from the process contains carbon monoxide, carbon dioxide, hydrogen, methane, a small amount of higher hydrocarbons, water, nitrogen (if air is the oxidizing medium), as well as carbon, ashes, tars and oils.
- the calorific value of the gas produced by gasification is approximately 2 - 6 MJ/m 3 n, and it is suitable for limited transfer in a pipe and for synthesis gas, for example, for the production of ammonia, methanol and fuel.
- tars heavy hydrocarbons
- tars is generally meant a mixture of organic compounds containing both lower molar mass compounds, such as benzene, and heavy poly- aromatic hydrocarbons.
- light tars are usually regarded mixtures having boiling points of 80 - 350 °C (from benzene to pyrene), and heavy tars for their part are compounds having boiling points higher than approximately 300 °C (chrysene, coronene, etc.).
- Tars in particular light tar components, constitute on the one hand an apparatus- technology problem through the soiling of pipes and blowers and on the other hand an environmental problem, if an attempt is made to remove the tars from the gas, for example, according to the conventional technology by wet scrubbing.
- Wet scrubbing additionally indicate that the degree of separation of the fine tar mist remains poor.
- the object of the present invention is to eliminate the disadvantages associated with the prior art and to provide a process for the production of a gas substantially free of incondensable compounds ("tar-free") by oxidative gasification of carbonaceous starting materials.
- the invention is based on the idea that the gas produced in the gasifier is fed into a scrubbing unit (dry scrubber) operating according to the fluidized-bed principle and serving as a tar-removal device.
- dry scrubber the gases are contacted with the bed material of the fluidized bed.
- the interior temperature of the dry scrubber is maintained at a level lower than the condensation temperature of the condensable substances, preferably at approximately 160 °C at maximum, in which case the tarry compounds are condensed in the dry scrubber into the bed material, and the product gases are purified.
- the (tar) compounds condensed into the bed material are returned with the bed material to the gasifier, where they are broken up into light gases.
- the apparatus according to the invention comprises a dry scrubber operating according to the fluidized-bed principle, wherein the gasifier gases can be brought into contact with a solid material in the form of a circulating bed.
- the apparatus can be used for producing a nearly tar-free gas, which is suitable for the production of both heat and in particular electricity (e.g. diesel electric power plants, boiler plants, connection to a large power plant).
- the gas can also be used as synthesis gas, for example, for the preparation of methanol.
- Trial runs have shown that the separation of tars in the dry scrubber is so effective that no signs of tarring of the dry scrubber have been observable even after gasification runs of more than 30 hours.
- the sight glasses of the apparatus are completely clear, and tar is not observable on the metal surfaces, either.
- the sawdust samples taken from the dry scrubber have been loose, readily flowing.
- the tars have been converted to light gases.
- the gasification apparatus is made up of a gasifier and, linked with it, a scrubbing unit for the condensing compounds, the unit comprising a dry scrubber operating according to the fluidized-bed principle.
- a gasifier and, linked with it, a scrubbing unit for the condensing compounds, the unit comprising a dry scrubber operating according to the fluidized-bed principle.
- the gasifier or the dry scrubber is a device operating according to the circulating fluidized bed principle, preferably both of them.
- device operating according to the fluidized-bed principle is generally meant a device having a bed which contains a solid material and which is maintained in a fluid state by directing into it a flowing material, such as gas.
- circulating fluidized bed unit for its part is meant in the present invention a multiple-phase flow apparatus made up of gas distribution nozzles, a riser, a cyclone separator, and a straight, uncontrolled return duct, wherein a significant proportion of the particles of the fluidized bed travel via the riser to the cyclone, from where they are returned to the lower section of the riser.
- a carbonaceous starting material is gasified at a temperature above 600 °C, most preferably approximately 700 - 1000 °C, by using an understoichiometric amount of air, in which case the starting substance as such breaks up into gases.
- a gas mixture is obtained which contains at least carbon monoxide and hydrogen, and often also carbon dioxide.
- air is used for oxidation, considerable amounts of nitrogen are also present in the gas mixture.
- it may contain small amounts of light hydrocarbons, such as methane, ethane, propane and n-butane.
- the gas is suitable, for example, for synthesis gas for the preparation of ammonia, methanol and fuel and, as was pointed out above, for the production of heat and electricity.
- the gasifier can be described with the words "thermochemical cracker”. Fluidized- bed units known per se can be used as the gasifier. However, as was stated above, preferably a circulating fluidized bed gasifier is used, in which case an apparatus option having an annular riser and in the center of it a cylindrical dipleg is deemed to be especially preferable.
- the apparatus comprises, for example, a circulating-bed fluid-flow gasifier, in which the fluidization space is made up of a space annular in cross-section between two cylinders or cones one inside the other, in which space the starting material is gasified at an elevated temperature, possibly in the presence of a separate solid. Such a solid may have catalytic properties.
- the solids are separated from the gasifier gases by means of a multi-inlet cyclone positioned directly on top of the annular duct. Owing to this structure, the residence time of gasification can be shortened, since the solids can be separated from the reaction gas stream with the multi-inlet cyclone faster and more effectively than with single-inlet cyclones. From the cyclone the solids can be returned via the space, annular in cross-section, formed by the two cylinders or cones, one inside the other, and serving as the return duct for the solids, i.e. the dip- leg, possibly to a regenerator section. If a separate bed material is not used, the starting material is recycled to the riser without regeneration.
- the gas mixture obtained from the gasifier also contains carbonaceous condensable compounds, which can be called tars.
- the gas mixture is directed according to a preferred embodiment of the invention to a dry scrubber operating according to the circulating fluidized bed principle, wherein they are contacted with the bed material in order to condense the con- densable compounds into the solids of the bed.
- dry scrubber in this context a device wherein the separation of the condensable compounds of the gases from the gases is carried out by means of a dry or moist solid medium.
- the dry scrubber comprises a circulating fluidized bed reactor, which serves at the same time as the dryer of the starting material and as the scrubber of the gasifier gases.
- the solid bed material used in the scrubber is a dryable material which will be gasified later in the process, such as biomass and refuse.
- a riser which comprises a dry scrubber operating according to the circulating fluidized bed principle, the dry scrubber comprising a riser wherein the exit gases of the gasifier can be contacted with the bed material.
- the interior temperature of the dry scrubber is maintained at a temperature lower than the condensation temperature of the condensable materials in order to condense these compounds into the biomass.
- the gas arriving from the gasifier the gas having already partially cooled (to approximately 300-400 °C), and the mass flow from the tar scrubber meet, aerosols are formed at the moment of impinging. Within a certain temperature range the aerosols remain in the tar scrubber on the surface of the biomass and circulate together with the mass stream. Thus the tars are in practice in a state of equilibrium and circulate between the scrubber and the gasifier.
- the residence time of the starting substance in the scrubber is several minutes. The tar-free gases obtained from the dry scrubber are recovered.
- a scrubber operating according to the circulating fluidized bed principle is preferable to, for example, a bubbling bluid- ized bed unit (BFB).
- BFB bubbling bluid- ized bed unit
- the advantages of the CFB are based on fluid-technology advantages.
- the fluid-technology operating window in the CFB gas velocity, particle size distribution
- BFB bubbling fluidized bed type apparatus
- the gas is in the form of large bubbles, and as a consequence of this the transfer of material between the gas and the particles is poorer than in CFB.
- It is a further advantage of CFB that particles having a large specific surface area are concentrated in the scrubber substantially better than in BFB.
- CFB dry scrubber may operate both as endothermal and as exothermal, in which case with very wet raw materials it can evaporate a considerable amount of water.
- the fluid technology flexibility of CFB is a crucially important prerequisite for the full-scale use of the heat exchange surfaces in the scrubber with all types of materials.
- the circulating bed used in the dry scrubber is the starting material to be gasified, in which case a moist biomass is dried in the dry scrubber before it is fed to gasifica- tion.
- the material to be gasified may contain at the same time both coarse and fine fractions, since a portion of the bed material will, nevertheless, remain in place and the finer fraction will circulate along with the gases.
- the temperature in the dry scrubber is maintained at ⁇ 160 °C, preferably at 80 - 120 °C, and especially preferably at approximately 90 - 110 °C.
- the tar scrubber according to a preferred embodiment of the invention is recuperative by its operating principle, i.e. its temperature is regulated by indirect heat exchange (by indirect heating or cooling).
- the scrubber serves as a drying scrubber when, for example, a slurry is being treated with steam, and as a cooling scrubber when, for example, a dry sawdust is being treated.
- heat is introduced into the dry scrub- ber if its interior temperature drops substantially below the condensation temperature of the gases and, respectively, heat is removed from the dry scrubber if its interior temperature rises substantially above the condensation temperature of the gases.
- the heat-exchange surface is located inside the tar scrubber, whereby a more effective heat exchange is produced than if the surface were outside.
- the fluidization gas used is, at least in the main, post-scrubber gas.
- Post-scrubber gas comprises at least in part the gases obtained from the gasification, which gases are combined with the circulating gas stream of the dry scrubber. There is namely produced in the dry scrubber a significant circulating gas return stream, which is directed to the lower section of the scrubber via the return duct.
- the function of the circulating gas is to produce fluidization conditions, and constant conditions are aimed at in the circulation gas stream. In this case the scrubber is controlled by controlling the temperature difference.
- the scrubber preferably comprises an elongate reactor mantle having three sections, i.e. a lower section, a riser section and an upper section, which has a cyclone for separating solids from the gases.
- the cyclone may be a conventional single-inlet cyclone or a multi-inlet cyclone.
- the cyclone has a separation chamber for the separation of solids from the gases, a gas outlet pipe connected to the separation chamber, and a solids dipleg connected to the riser for returning to the riser the solids separated from the gases.
- the riser of the dry scrubber and/or the dipleg of the cy- clone are/is preferably connected to the feed connection of the gasification unit in order to feed the bed material from the dry scrubber to the gasifier.
- a gas recycling duct which may be arranged outside the reactor mantle.
- the outlet connection for the gaseous exit material of the gasification unit may be connected to this gas recycling line.
- the conical lower section of the scrubber there are separate feed connections for the starting material to be dried and, respectively, for the tar- containing product gas to be purified.
- the lower section further has withdrawal connections, i.e. outlet connections, for the dried biomass.
- a grate which serves as a distribution plate for the circulating gas.
- the riser duct section has, fitted inside the reactor mantle, at least one riser pipe. Around the pipe there is a heat-exchange mantle to provide indirect heat exchange.
- the riser may have several parallel pipes (e.g. 2 - 15) in order to increase the heat-exchange surface.
- the starting material such as biomass or refuse fractions
- an outside bed material or a catalyst acting in the manner of a bed material for example, a fluidized-bed cracking catalyst.
- Bed materials usable in this case are various silicate materials (sand) and similar fine materials withstanding heat sufficiently well.
- the advantages of gasification with- out a foreign fluid material include the elimination of the erosion problem and the reduction of the internal consumption. In this case there are also not formed any dust emissions causing additional problems in terms of gas purification.
- the costs of investment and operation are reduced, the risk of sintration caused by a foreign fluid material is eliminated, whereby a higher concentration of coke in the gasifier is achieved and, consequently, the quality of the gas is improved.
- biomass starting materials are preferably selected from among the forest industry residues and thinning residues; agricultural residues such as straw, residues from olive thinning or collection; energy plants such as willow and energy hay, Miscan- thus and peat.
- the refuse is preferably organic, solid or liquid, and it is selected from among refuse derived fuel (RDF), sawmill waste, plywood, furniture and other residues of the mechanical forest industry; waste plastic; and waste slurries (including industrial and community effluents).
- RDF refuse derived fuel
- sawmill waste plywood, furniture and other residues of the mechanical forest industry
- waste plastic waste plastic
- waste slurries including industrial and community effluents
- Especially advantageous starting materials include wood chips, wood shavings, sawdust, peat, lumbering residues and chips, community refuse, briquettes, straw, and energy plants.
- inventions to be mentioned include the gasification of so-called opportunity fuel type fuel batches. These include fuel batches, not always available, containing large amounts of volatile compounds. Some examples are thinning wood, snag wood chips, REF, RDF, automobile tires and other waste rubber and plastic, timber offcuts from building sites, wood from demolishing, etc.
- the gas obtained from these starting substances can be used to replace the principal fuel, such as carbon, of the principal process.
- the proportion of product gas of the total fuel is typically small. In this case, any incidentally available fuel batches can be exploited at only a marginal conversion cost. Investment in a turbine/generator/converter is thus not needed.
- the gasification apparatus in this application serves as a kind of 'waste grinder' by means of which the said starting materials can be disposed of advantageously.
- the fact that the gases are nearly devoid of tar promotes the transfer of chemical heat from this sidestream process to the principal process. It also reduces the maintenance costs.
- the ash of the secondary fuel in this manner also remains separate from the ash of the principal fuel.
- the product gas is used as fuel for smallish spark-ignition gas engines and as additional fuel for largish heavy oil diesel en- gines.
- the starting materials selected for the gasifier are primarily wood-based biomass fractions.
- the use of the gasifier as a producer of synthesis gas is also possible.
- the gasifier feed is again wood-based biomass.
- the gases obtained from the process and the apparatus do not contain condensable compounds (they are "tar-free"), which means that they do not contain substantial amounts of hydrocarbon compounds which have, in terms of the use of the gases, a detrimentally high saturated-state vapor pressure at above 200 °C.
- concentration of such compounds in the gases is lower than 0.1 % by volume, in particularly lower than 0.01 % by volume.
- the material to be gasified is fed into the dry scrubber 2 via the grav- ity pipe 4 so that a significant amount of oxygen cannot pass into the dry scrubber via the feed devices.
- the control of the feed of the material to be gasified is most preferably carried out by control of the rotation speed of the feed screw by means of the inverter 3.
- the material to be gasified comes into contact with the tarry gas coming from the gasifier 5, whereupon the tars are condensed into the material to be gasified.
- the energy balance of the dry scrubber in general needs to be controlled by either direct or indirect cooling or heating in order for the temperature to be maintained within the desired operating window (70-120 °C). Since direct cooling has several disadvantages, the riser of the dry scrubber is made up of a plurality of parallel pipes 8, inside which the gas and the material to be gasified rise upwards and outside which there flows a heating or cooling liquid or gas. The said space thus constitutes a heat-exchange mantle.
- the lower section 10 of the riser is a continu- ous, usually upwardly expanding cone.
- the upper section of the dry scrubber is made up of a cyclone 11 above the heat exchange section. The material to be gasified, separated in the cyclone, is returned to the lower section of the dry scrubber.
- the gasifier 5 is preferably a light- structured CFB reactor made from refractory steel and equipped with a multi-inlet cyclone and a simple return duct.
- the operating temperature of the gasifier is 700-900 °C, suitable for refractory steels. Especially if the gasification is carried out without an abrasive circulating material, ceramic abrasion shields are not needed.
- the gasification air or oxygen-enriched gas mixture is introduced into the lower section of the gasifier via the grate plate, and the gasification air flow is controlled according to the gasifier temperature so that if the temperature tends to rise above the upper limit, the air flow is reduced and vice versa.
- the material to be gasified which has accumulated tar compounds in the dry scrubber 2, is fed via the feed connection 13 into the gasifier 5, preferably with the help of a smallish (not shown) intermediate silo and a screw feeder 6.
- the rotation speed of the feeding screw 6 is controlled by means of the inverter 7.
- a portion of the gasification air is directed to between the screw and the gasifier.
- the starting of the plant is carried out so that the storage silo 1 for the material to be gasified is filled, the circulation gas blower is started, and the feeding of the mate- rial to be gasified into the dry scrubber is started.
- the starting igniter of the gasifier is ignited.
- the temperature in the gasifier has exceeded the minimum limit (approximately 600 °C)
- the feeding of the material to be gasifier into the gasifier is started and the starting igniter power is reduced as the stream of material to be gasified increases.
- the starting igniter is switched off, and the shifting to the gasifying run is carried out by rapidly increasing the feeding in of material to be gasified.
- Gas is removed from the gasifier 5 via the outlet connection 14, and the gas stream is connected to the recycle line 12 of the dryer, i.e. the return pipe, from which it travels via the feed con- nection 9' to the dryer.
- the gases produce the required fluidization gas flow.
- the separation of solids and tar from the gases takes place in the manner described above, and the product gases are removed via the outlet connection and are recovered.
- the storage capacity of the dry scrubber 2 is sufficient for controlling, in a rapid change of power, primarily the stream of material to be gasified fed into the gasifier, and the stream fed into the dry scrubber follows with a delay, taking its control quantity from the pressure difference of the riser of the dry scrubber.
- the stopping of the plant is carried out by first discontinuing the feeding of gasification air into the gasifier, and when the temperature in the gasifier has begun to decrease, the feeding in of material to be gasified is discontinued. At this time the temperature in the dry scrubber also begins to decrease, whereupon the feeding of material to be gasified into the dry scrubber can be discontinued. Last, the circulation gas blower is stopped and any valves possibly causing air leaks are closed.
- a gasification apparatus was constructed which comprised a scrubber and a gasifier connected to it.
- Cyclone a coaxial multi-inlet cyclone having a height of approximately 1 m and having 16 inlets on the cyclone circumference and a blade height of 40 mm.
- the cyclone had a 110 mm diameter central pipe upwards.
- the return duct had natural circulation, the diameter of the return duct was 85 mm, and its height was 2000 mm.
- the riser duct comprised 6 parallel riser pipes the diameters of which were 85 mm and which were arranged inside a pipe mantle having a diameter of 320 mm and a height of 2000 mm.
- the height of the upper section of the scrubber was 1000 mm, and in its lower section the pipe mantle was conical and equipped with feeding and outlet connections.
- the grate at the bottom of the scrubber had a nozzle having a diameter of 100 mm.
- the circulating fluidized bed gasifier was an uncooled, steel-structured CFB reactor capable of being used with both over- and understoichiometric air feed.
- the most important parts of the gasifier were: A coaxial multi-inlet cyclone having a height of 500 mm, 16 tangential inlets on the cyclone circumference and a blade height of 100 mm.
- the cyclone had a 110 mm diameter central pipe downwards.
- the circulation flow had been arranged as natural circulation in an annular return duct (d u ⁇ 50 mm, d s 100 mm) having a height of 1200 mm.
- the outer diameter of the riser duct was 300 mm and height 2000 mm.
- the thermal losses in the gasifier were for both runs approximately 3.9 kW, and the thermal losses of the dryer and the circulation gas duct were estimated at 2.1 kW in total.
- the separation of tars in the dry scrubber succeeded very well. In the steady state the tars did not cause problems of process or apparatus technology.
- the CFB gasification of sawdust without a foreign fluidization material succeeded well.
- the apparatus can be used for producing from biomasses a tar-free, high quality gas with a low calorific value, which gas is a technically suitable fuel, for example, for boilers, furnaces, piston engines and gas turbines.
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP00927281A EP1187893B1 (en) | 1999-05-14 | 2000-05-12 | Process for the gasification of carbonaceous material |
AT00927281T ATE289345T1 (en) | 1999-05-14 | 2000-05-12 | METHOD FOR GASIFICATION OF CARBON-CONTAINING MATERIAL |
AU45715/00A AU4571500A (en) | 1999-05-14 | 2000-05-12 | Process and apparatus for the gasification of carbonaceous material |
DE60018181T DE60018181T2 (en) | 1999-05-14 | 2000-05-12 | METHOD FOR GASIFYING CARBON-CONTAINING MATERIAL |
CA002372195A CA2372195A1 (en) | 1999-05-14 | 2000-05-12 | Process and apparatus for the gasification of carbonaceous material |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FI991107 | 1999-05-14 | ||
FI991107A FI112665B (en) | 1999-05-14 | 1999-05-14 | Process and plant for gasification of carbonaceous material |
Publications (1)
Publication Number | Publication Date |
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WO2000069995A1 true WO2000069995A1 (en) | 2000-11-23 |
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Application Number | Title | Priority Date | Filing Date |
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PCT/FI2000/000435 WO2000069995A1 (en) | 1999-05-14 | 2000-05-12 | Process and apparatus for the gasification of carbonaceous material |
Country Status (8)
Country | Link |
---|---|
EP (1) | EP1187893B1 (en) |
AT (1) | ATE289345T1 (en) |
AU (1) | AU4571500A (en) |
CA (1) | CA2372195A1 (en) |
DE (1) | DE60018181T2 (en) |
ES (1) | ES2235873T3 (en) |
FI (1) | FI112665B (en) |
WO (1) | WO2000069995A1 (en) |
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CN102559284A (en) * | 2012-01-16 | 2012-07-11 | 贝洪毅 | Large-scale biomass gasification and destructive distillation gas making engineering purification system |
CN102977929A (en) * | 2012-10-11 | 2013-03-20 | 田原宇 | Household garbage coupling fluidized bed hierarchical pyrolytic gasifier |
CN105820827A (en) * | 2016-05-19 | 2016-08-03 | 北京神雾环境能源科技集团股份有限公司 | System for generating synthesis gas through coal pyrolysis and cracking tube cracking |
CN105820828A (en) * | 2016-05-19 | 2016-08-03 | 北京神雾环境能源科技集团股份有限公司 | System for generating synthesis gas through coal pyrolysis and catalytic cracking |
CN105838399A (en) * | 2016-05-19 | 2016-08-10 | 北京神雾环境能源科技集团股份有限公司 | Biomass pyrolysis and cracking tube cracking system |
US10011792B2 (en) | 2010-08-16 | 2018-07-03 | Nikhil Manubhai Patel | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
CN109126642A (en) * | 2016-04-15 | 2019-01-04 | 四川省雷波明信化工有限公司 | A kind of combustion method for fluidized bed |
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KR100590973B1 (en) | 2000-02-29 | 2006-06-19 | 미츠비시 쥬고교 가부시키가이샤 | Apparatus for methanol synthesis using gas produced by gasifying biomass and the using method thereof |
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WO1986001822A1 (en) * | 1984-09-14 | 1986-03-27 | A. Ahlstrom Corporation | Method for cleaning gases containing condensable components |
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- 1999-05-14 FI FI991107A patent/FI112665B/en not_active IP Right Cessation
-
2000
- 2000-05-12 CA CA002372195A patent/CA2372195A1/en not_active Abandoned
- 2000-05-12 DE DE60018181T patent/DE60018181T2/en not_active Expired - Lifetime
- 2000-05-12 ES ES00927281T patent/ES2235873T3/en not_active Expired - Lifetime
- 2000-05-12 AT AT00927281T patent/ATE289345T1/en not_active IP Right Cessation
- 2000-05-12 AU AU45715/00A patent/AU4571500A/en not_active Abandoned
- 2000-05-12 WO PCT/FI2000/000435 patent/WO2000069995A1/en active IP Right Grant
- 2000-05-12 EP EP00927281A patent/EP1187893B1/en not_active Expired - Lifetime
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US4198212A (en) * | 1977-05-24 | 1980-04-15 | The Lummus Company | Coal gasification effluent treatment |
DE3340204A1 (en) * | 1983-11-07 | 1985-05-15 | Klöckner-Humboldt-Deutz AG, 5000 Köln | METHOD AND DEVICE FOR PURIFYING HOT GAS WITH HEAT RECOVERY |
WO1986001822A1 (en) * | 1984-09-14 | 1986-03-27 | A. Ahlstrom Corporation | Method for cleaning gases containing condensable components |
US5032143A (en) * | 1987-05-08 | 1991-07-16 | A. Ahlstrom Corporation | Method and apparatus for treating process gases |
US5213587A (en) * | 1987-10-02 | 1993-05-25 | Studsvik Ab | Refining of raw gas |
DE19612346A1 (en) * | 1996-03-28 | 1997-10-02 | Ver Verwertung Und Entsorgung | Combined solid fuel drying and gaseous fuel treatment process |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10011792B2 (en) | 2010-08-16 | 2018-07-03 | Nikhil Manubhai Patel | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
US10550343B2 (en) | 2010-08-16 | 2020-02-04 | Nikhil Manubhai Patel | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
US11220641B2 (en) | 2010-08-16 | 2022-01-11 | Nikhil Manubhai Patel | Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge |
CN102559284A (en) * | 2012-01-16 | 2012-07-11 | 贝洪毅 | Large-scale biomass gasification and destructive distillation gas making engineering purification system |
CN102977929A (en) * | 2012-10-11 | 2013-03-20 | 田原宇 | Household garbage coupling fluidized bed hierarchical pyrolytic gasifier |
CN109126642A (en) * | 2016-04-15 | 2019-01-04 | 四川省雷波明信化工有限公司 | A kind of combustion method for fluidized bed |
CN109126642B (en) * | 2016-04-15 | 2021-09-21 | 雷波明信实业发展有限公司 | Combustion method for fluidized bed |
CN105820827A (en) * | 2016-05-19 | 2016-08-03 | 北京神雾环境能源科技集团股份有限公司 | System for generating synthesis gas through coal pyrolysis and cracking tube cracking |
CN105820828A (en) * | 2016-05-19 | 2016-08-03 | 北京神雾环境能源科技集团股份有限公司 | System for generating synthesis gas through coal pyrolysis and catalytic cracking |
CN105838399A (en) * | 2016-05-19 | 2016-08-10 | 北京神雾环境能源科技集团股份有限公司 | Biomass pyrolysis and cracking tube cracking system |
Also Published As
Publication number | Publication date |
---|---|
DE60018181T2 (en) | 2006-02-16 |
EP1187893A1 (en) | 2002-03-20 |
CA2372195A1 (en) | 2000-11-23 |
FI991107A (en) | 2000-11-15 |
ES2235873T3 (en) | 2005-07-16 |
ATE289345T1 (en) | 2005-03-15 |
AU4571500A (en) | 2000-12-05 |
FI991107A0 (en) | 1999-05-14 |
EP1187893B1 (en) | 2005-02-16 |
DE60018181D1 (en) | 2005-03-24 |
FI112665B (en) | 2003-12-31 |
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