EP1187893B1 - Procede pour gazeifier les matieres carbonees - Google Patents

Procede pour gazeifier les matieres carbonees Download PDF

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Publication number
EP1187893B1
EP1187893B1 EP00927281A EP00927281A EP1187893B1 EP 1187893 B1 EP1187893 B1 EP 1187893B1 EP 00927281 A EP00927281 A EP 00927281A EP 00927281 A EP00927281 A EP 00927281A EP 1187893 B1 EP1187893 B1 EP 1187893B1
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EP
European Patent Office
Prior art keywords
gas
dry scrubber
process according
scrubber
gasified
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EP00927281A
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German (de)
English (en)
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EP1187893A1 (fr
Inventor
Seppo Ruottu
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Fortum Oil Oy
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Fortum Oil Oy
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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
    • 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
    • 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
    • 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 example, 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 polyaromatic 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.
  • US 4198212 discloses a method of gasifying coal to produce a coal gasification effluent and a char residue.
  • the char residue is cooled by indirect heat transfer in a char bed, and the coal gasification effluent is passed through the cool char bed to effect cooling of the coal gasification effluent, with tars and oil present in the effluent being absorbed by the char bed.
  • the gasification effluent is cooled without fouling of heat transfer surfaces, and tars and oils are effectively removed therefrom.
  • 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. In the dry scrubber the gases are contacted with the bed material of the fluidized bed. The interior temperature of the dry.
  • the 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.
  • 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 dipleg, 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 condensable 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.
  • wet scrubbing the scrubbing of gases is carried out, as is known, by means of liquid.
  • 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.
  • 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 gasification.
  • 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 scrubber 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 cyclone 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 without 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.
  • Starting materials of many types can be used as the feed in the reactor system.
  • the common nominator of the materials used as starting materials is that they contain carbon or are carbonaceous. These materials can be divided into two principle groups: biomass and refuse.
  • the 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 engines.
  • the starting materials selected for the gasifier are primarily wood-based biomass fractions.
  • 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 gravity 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 continuous, 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 material to be gasified into the dry scrubber is started.
  • the pressure difference of the riser duct of the dry scrubber is at its setting value, 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 connection 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 ul 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.
  • Sawdust was gasified in the apparatus.
  • the moisture contents of the sawdust were determined by weighing and drying the samples in an oven at approximately 110 °C until the weight of the sample no longer changed. Samples of the gas were taken into bags, and the gas compositions were measured at Neste.
  • 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.

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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)
  • Processing Of Solid Wastes (AREA)
  • Industrial Gases (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Claims (15)

  1. Procédé pour la gazéification d'une matière carbonée, selon lequel procédé
    une matière carbonée est gazéifiée (5) à une température élevée afin de produire un gaz,
    des composés condensables sont séparés (2) du gaz, et
    le produit gazeux ainsi obtenu est récupéré,
    caractérisé en ce que
    afin de séparer les composés condensables, le gaz obtenu à partir des gazéificateurs est introduit dans un épurateur sec (2) fonctionnant selon le principe du lit fluidisé, dans lequel il est mis en contact avec la matière de lit du lit fluidisé, la température intérieure de l'épurateur sec étant maintenue à une température en dessous de la température de condensation des composés condensables afin de condenser ces composés dans la matière de lit,
    la matière de lit de l'épurateur sec (2) est au moins en partie constituée de la matière carbonée à gazéifier, et le gaz de fluidification utilisé dans l'épurateur sec (2) est au moins principalement le gaz de sortie de l'épurateur (2), une partie de celui-ci étant recyclée vers la section inférieure de l'épurateur.
  2. Procédé selon la revendication 1, caractérisé en ce que la matière de lit contenant les composés condensés est dirigée de l'épurateur sec (2) vers la gazéification (5).
  3. Procédé selon la revendication 1 ou 2, caractérisé en ce que l'épurateur sec (2) utilisé est un appareil fonctionnant selon le principe du lit fluidisé circulant.
  4. Procédé selon l'une quelconque des revendications ci-dessus, caractérisé en ce que les gaz obtenus à partir de la gazéification (5) sont combinés avec le courant gazeux de fluidification de l'épurateur sec (2).
  5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que la matière à gazéifier est séchée dans l'épurateur sec (2) avant d'être amenée à la gazéification (5).
  6. Procédé selon la revendication 5, caractérisé en ce que la température dans l'épurateur sec (2) est maintenue à < 160°C, de préférence à approximativement 80 à 120°C.
  7. Procédé selon la revendication 5 ou 6, caractérisé en ce que la température dans l'épurateur sec (2) est régulée par échange de chaleur indirect.
  8. Procédé selon la revendication 7, caractérisé en ce que de la chaleur est introduite dans l'épurateur sec (2) si sa température intérieure chute sensiblement en dessous de la température de condensation des gaz.
  9. Procédé selon la revendication 7, caractérisé en ce que de la chaleur est évacuée de l'épurateur sec (2) si sa température intérieure s'élève sensiblement au-dessus de la température de condensation des gaz.
  10. Procédé selon l'une quelconque des revendications ci-dessus, caractérisé en ce que la matière de départ carbonée est gazéifiée à une température de 600 à 1 000°C.
  11. Procédé selon l'une quelconque des revendications ci-dessus, caractérisé en ce qu'à partir d'une biomasse à gazéifier, il est produit un mélange gazeux contenant au moins du monoxyde de carbone et de l'hydrogène.
  12. Procédé selon l'une quelconque des revendications ci-dessus, caractérisé en ce que la substance de départ carbonée utilisée est une biomasse ou un déchet.
  13. Procédé selon la revendication 10, caractérisé en ce que du bois d'éclaircissement, des morceaux de déchet de déboisement, du REF (combustible de récupération), du RDF (combustible issu de déchêts), du plastique ou du caoutchouc de déchet, ou des rognures de site de construction est utilisé pour produire un gaz utilisable pour la production de chaleur et/ou d'électricité.
  14. Procédé selon la revendication 12, caractérisé en ce qu'une biomasse à base de bois est gazéifiée pour produire un gaz utilisable en tant que carburant pour des moteurs à gaz à allumage par étincelle et en tant que carburant supplémentaire pour des moteurs diesel à combustion d'huile lourde.
  15. Procédé selon la revendication 12, caractérisé en ce qu'une biomasse de bois à base de bois est gazéifiée pour produire un gaz de synthèse.
EP00927281A 1999-05-14 2000-05-12 Procede pour gazeifier les matieres carbonees Expired - Lifetime EP1187893B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FI991107 1999-05-14
FI991107A FI112665B (fi) 1999-05-14 1999-05-14 Menetelmä ja laitteisto hiilipitoisen materiaalin kaasuttamiseksi
PCT/FI2000/000435 WO2000069995A1 (fr) 1999-05-14 2000-05-12 Procede et appareil pour gazeifier les matieres carbonees

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EP1187893A1 EP1187893A1 (fr) 2002-03-20
EP1187893B1 true EP1187893B1 (fr) 2005-02-16

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EP (1) EP1187893B1 (fr)
AT (1) ATE289345T1 (fr)
AU (1) AU4571500A (fr)
CA (1) CA2372195A1 (fr)
DE (1) DE60018181T2 (fr)
ES (1) ES2235873T3 (fr)
FI (1) FI112665B (fr)
WO (1) WO2000069995A1 (fr)

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CN104987894A (zh) * 2015-07-08 2015-10-21 陕西延长石油（集团）有限责任公司 一种含焦油煤气中固体颗粒的排放装置及方法

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US6991769B2 (en) 2000-02-29 2006-01-31 Mitsubishi Heavy Industries, Ltd. Biomass gasifycation furnace and system for methanol synthesis using gas produced by gasifying biomass
DK2606105T3 (da) 2010-08-16 2023-01-23 Singularity Energy Tech Llc Sandwich-gasificeringsproces for højeffektiv konvertering af kulstofholdige brændstoffer med henblik på rensning af en syntesegas med nul restkulstofudladning
CN102086522A (zh) * 2010-12-20 2011-06-08 苏州竞立制氢设备有限公司 氢氧分离器洗涤装置
CN102559284B (zh) * 2012-01-16 2014-05-21 贝洪毅 大型生物质气化、干馏制气工程净化系统
CN102977929B (zh) * 2012-10-11 2014-05-07 田原宇 生活垃圾耦合流化床分级热解气化炉
CN108970553B (zh) * 2016-04-15 2021-09-21 雷波明信实业发展有限公司 一种流化床
CN105820827A (zh) * 2016-05-19 2016-08-03 北京神雾环境能源科技集团股份有限公司 一种煤热解和裂解管裂解产合成气系统
CN105838460A (zh) * 2016-05-19 2016-08-10 北京神雾环境能源科技集团股份有限公司 一种煤热解和裂解产气联合燃气发电系统
CN105838399A (zh) * 2016-05-19 2016-08-10 北京神雾环境能源科技集团股份有限公司 一种生物质热解和裂解管裂解系统
CN105778950A (zh) * 2016-05-19 2016-07-20 北京神雾环境能源科技集团股份有限公司 一种生物质热解和催化裂解系统
CN105838396A (zh) * 2016-05-19 2016-08-10 北京神雾环境能源科技集团股份有限公司 一种垃圾热解和裂解管裂解系统
CN105838395A (zh) * 2016-05-19 2016-08-10 北京神雾环境能源科技集团股份有限公司 一种垃圾热解和裂解系统
CN105820828A (zh) * 2016-05-19 2016-08-03 北京神雾环境能源科技集团股份有限公司 一种煤热解和催化裂解产合成气系统

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104987894A (zh) * 2015-07-08 2015-10-21 陕西延长石油（集团）有限责任公司 一种含焦油煤气中固体颗粒的排放装置及方法
CN104987894B (zh) * 2015-07-08 2019-01-18 陕西延长石油（集团）有限责任公司 一种含焦油煤气中固体颗粒的排放装置及方法

Also Published As

Publication number Publication date
ATE289345T1 (de) 2005-03-15
DE60018181D1 (de) 2005-03-24
FI991107A0 (fi) 1999-05-14
WO2000069995A1 (fr) 2000-11-23
DE60018181T2 (de) 2006-02-16
AU4571500A (en) 2000-12-05
FI991107A (fi) 2000-11-15
EP1187893A1 (fr) 2002-03-20
ES2235873T3 (es) 2005-07-16
FI112665B (fi) 2003-12-31
CA2372195A1 (fr) 2000-11-23

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