WO2007093429A2 - Procédé et dispositif de production de gaz à partir de matière contenant du carbone - Google Patents

Procédé et dispositif de production de gaz à partir de matière contenant du carbone Download PDF

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Publication number
WO2007093429A2
WO2007093429A2 PCT/EP2007/001347 EP2007001347W WO2007093429A2 WO 2007093429 A2 WO2007093429 A2 WO 2007093429A2 EP 2007001347 W EP2007001347 W EP 2007001347W WO 2007093429 A2 WO2007093429 A2 WO 2007093429A2
Authority
WO
WIPO (PCT)
Prior art keywords
pyrolysis
carbonaceous material
gasification
unit
scraping
Prior art date
Application number
PCT/EP2007/001347
Other languages
German (de)
English (en)
Other versions
WO2007093429A3 (fr
Inventor
Jörg KEMPER
Frank Lohmann
Original Assignee
Native Power Solutions Gmbh & Co. Kg
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Native Power Solutions Gmbh & Co. Kg filed Critical Native Power Solutions Gmbh & Co. Kg
Publication of WO2007093429A2 publication Critical patent/WO2007093429A2/fr
Publication of WO2007093429A3 publication Critical patent/WO2007093429A3/fr

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Classifications

    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B19/00—Heating of coke ovens by electrical means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
    • C10J2300/1238—Heating the gasifier by electromagnetic waves, e.g. microwaves by plasma
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the present invention relates to a method and apparatus for producing CO and H 2 -containing gas from carbonaceous material.
  • the gasification generally takes place in several steps: the drying / heating in preparation, the pyrolysis and the gasification, namely the reaction of the pyrolysis products by oxidation and reduction.
  • the resulting gas contains i.a. Hydrogen, carbon monoxide and methane, which can serve as fuel.
  • the composition of the resulting gas depends on the reaction gas used and the temperature at which the gasification takes place. At higher temperatures, the concentration of hydrogen and carbon monoxide increases and decreases the concentration of methane.
  • From DE 32 33 774 A1 discloses a method and a plant for gasification of carbonaceous material to a mainly consisting of CO and H 2 gas mixture are known in which the carbonaceous material is input in particulate form in a shaft furnace to a predetermined level.
  • the shaft furnace has plasma torches on the ground.
  • CO 2 or H 2 O is supplied.
  • the carbonaceous material is subjected to a high temperature under oxidizing conditions.
  • the volatiles are then released and react with the oxidizer.
  • the non-volatile part is, however, coked.
  • Oxidizer that has not reacted with the volatiles may react further down in the shaft furnace with the coke produced and additionally form CO and possibly H 2 O. Upwardly escaping CO 2 and H 2 O can react with the carbonaceous material falling down to CO and H 2 .
  • the gas leaving the shaft furnace has a maximum temperature of 1500 ° C. The temperature on the surface of the granular material in the shaft furnace can reach approximately 2000 ° C.
  • An object of the present invention is to provide a method and an apparatus in which the carbonaceous material is treated for gasification.
  • a method for gasifying carbonaceous material to CO and H 2 containing gas comprising the steps of: at least partially pyrolizing the carbonaceous material; Gasification of the pyrolysis products and / or of the carbonaceous material, wherein the pyrolysis products and / or the carbonaceous material are comminuted after the pyrolysis and simultaneously brought to the process temperature for the gasification.
  • Crushing increases the surface area of the material to be gasified, resulting in a significant acceleration of the gasification process, such as bringing to gasification process temperature during crushing.
  • the overall energy balance is improved. Because unlike the crushing of the starting material before the pyrolysis, for which quite a lot of energy is required, the solid pyrolysis products, which are mostly coal, with relatively little effort and reduce energy. More preferably, the pyrolyzed carbonaceous material is comminuted immediately after pyrolysis and brought to process temperature for gasification before it is appreciably cooled to further improve the overall energy balance.
  • the gasification can take place auto- or allothermic.
  • the gasification is preferably carried out with the aid of external heat input. It is particularly preferred to provide the external heat input by a plasma, for example an inert gas plasma or oxygen plasma. Because with the help of a plasma can easily reach temperatures, which is guaranteed that even residues of tar or harmful compounds split and in in particular CO and H 2 are converted.
  • a plasma for example an inert gas plasma or oxygen plasma.
  • the use of steam plasma has proved to be particularly advantageous: It consists of O, H, OH, O 2 , H 2 and H 2 O radicals which are very good with the pyrolysis products and possibly not yet pyrolyzed carbonaceous material.
  • the enthalpy density of water vapor plasma is very high. These properties lead to an acceleration of the
  • the pyrolysis is carried out by means of microwave irradiation and heating.
  • microwave irradiation and heating By coupling energy via microwaves into the carbonaceous material, it is achieved that the carbonaceous material is completely penetrated with little effort and heated rapidly from the inside to the outside.
  • Moisture-containing carbonaceous material also achieves sufficient drying and conversion of the moisture to water vapor, which is then available as an oxidizing agent during gasification. Since the carbonaceous material is heated from the inside to the outside, combustion is suppressed, and instead the carbonaceous material is pyrolytically split into volatile carbon compounds and non-volatile carbon compounds with shorter carbon chains.
  • Conventional heating means may be used to preheat the carbonaceous material from outside to inside or reheat it after or parallel to microwave irradiation.
  • the heat input from the inside to the outside and from the outside to the inside reduces the time required for as complete pyrolysis as possible and overall improves the energy balance of the entire process.
  • the pyrolysis products serve below as starting materials for the gasification, which is faster and more efficient due to the already at least partially carried out pyrolysis.
  • An important advantage is that it can be used particularly well in small-scale systems for decentralized energy supply. Because of the pretreatment by means of microwaves, for example, even household waste or biomass in the form of garden waste can be used without expensive prior treatment. Namely, the drying and heating as well as the pyrolysis are achieved largely or completely by the microwave irradiation. Also, a heating unit to support pyrolysis can be provided with only a small footprint. It has proven to be advantageous to densify the carbonaceous material before and / or during and / or after microwave irradiation. The compaction leads to a more efficient energy input by microwave irradiation and / or thermal radiation and is preferably carried out before the microwave irradiation and / or optionally before the heat radiation. As a result, as complete as possible pyrolysis of the carbonaceous material is achieved by the microwave irradiation.
  • the object is achieved by a device for gasifying carbonaceous material to CO and H 2 -containing gas with a pyrolysis station and a gasification reactor in which a comminution unit is arranged in the gasification reactor, which comminutes the nonvolatile pyrolysis products. If carbonaceous material should not be completely pyrolyzed, this too is crushed by means of the comminution unit.
  • the arrangement of the comminution unit in the gasification reactor has the significant advantage that the material to be gasified is heated on the one hand by contact with the comminution unit, since the comminution unit has by its arrangement within the gasification reactor substantially the same temperature as the ambient temperature inside the gasification reactor, for Others can be exposed to the material to be gasified at the moment of its comminution of the ambient temperature inside the gasification reactor and because of its enlarged by the crushing surface immediately assumes the ambient temperature.
  • the gasification reactor has at least one heat source with the aid of which the gasification of the comminuted pyrolysis products and of the comminuted carbonaceous material, if it has not been completely pyrolyzed, takes place.
  • the gasification can also take place autothermally, so that the heat source can also be dispensed with.
  • the pyrolysis station is designed as a microwave station with heating unit in order to split the carbonaceous material into pyrolysis products as efficiently as possible and if necessary to dry and / or to heat them.
  • the pyrolysis station has a compression unit.
  • the compression unit may be connected upstream of or integrated in the pyrolysis station.
  • the integration into the pyrolysis station is particularly suitable when irradiated simultaneously with microwaves and heated by radiant heat as well as to be compacted.
  • the compaction unit allows a more compact design of the pyrolysis station, which can be thermally insulated with less effort.
  • the shredding unit is designed as a scraping unit that scrapes off the surface of the pyrolysis products and / or the carbonaceous material that is emerging from the microwave station.
  • the scraping unit releases the gasification process temperature to the fresh scraping point of the scraped off material by direct contact. In this way the energy input into the material particles is accelerated.
  • the scraper creates a cracked surface, which further enlarges the gasification surface.
  • the scraping unit is designed as an arrangement of blades which can be guided past the pyrolysis products and / or the carbonaceous material.
  • the scraping unit is designed as a rotatable scraping part which has perforations on the side facing the exiting pyrolysis products and / or the carbonaceous material.
  • the edges of the apertures scrape particles from the non-volatile materials which pass through the apertures into the reactor.
  • the exit from the pyrolysis station is designed as a tube and projects the rotating scraping part into the tube.
  • the scraper is arranged axially displaceable in the pipe direction.
  • the scraping part of ceramic to ensure a long life even at high gasification temperatures.
  • the at least one heat source is at least one plasma torch, more preferably at least one steam plasma torch.
  • plasma torches can reach sufficiently high temperatures that also toxic and undesirable compounds in CO and H2 are split.
  • the plasma also provides necessary oxidizing agent.
  • the plasma torch is on
  • Shredder directed to bring the shredder and crushed by them material to a high temperature so that the gasification can begin even during the crushing.
  • Figure 1 is a perspective view of a first embodiment of a device for gas generation
  • Figure 2 is a horizontal section through the device of Figure 1;
  • Figure 3 is a vertical section in the longitudinal direction through the device of Figure 1 in a simplified view
  • Figure 4 is a vertical section perpendicular to the longitudinal direction through the device of Figure 1 in a simplified view
  • Figure 5 is a schematic detail view of a first embodiment of a scraping unit
  • Figures 6a, b is a schematic detail view of a second embodiment of a scraping unit from the side and in plan view;
  • Figure 7 is a horizontal section through a device as in Figures 1 to 4 with the scraping unit of Figures 6a, b;
  • Figures 8a, b is a schematic representation of a particular embodiment of the scraping unit of Figures 6a, b;
  • FIG. 9 schematically shows the material flow of a gasification:
  • Figure 10 is a perspective view of a second embodiment of a
  • FIG. 11 shows a horizontal section through a device as in FIG. 10 with the scraping unit from FIGS. 6a, b;
  • Figure 12 is a vertical section perpendicular to the longitudinal direction through the
  • FIG. 13 shows a vertical section through the device from FIG. 10 at the level of the pyrolysis furnace for the pyrolysis.
  • the starting material may be industrial or household waste or biomass based on renewable raw materials, such as garden waste, wood chips, preferably a grain size of about 6-20 mm, sawdust, pellets, peel, husks or straw. Even fossil fuels can be gasified in the gas generator.
  • the carbonaceous material is filled through the hopper 100.
  • the carbonaceous material 2 can already be preheated there to about 60 ° -80 ° C (see also reference 201, Figure 9).
  • the carbonaceous material 2 is conveyed further into a reactor 6.
  • the carbonaceous material 2 is heated to about 400-500 0 C. This is done predominantly by microwaves generated in the microwave generator 31 and a heater 62 which utilizes the waste heat of the primary reactor 4 in which the gasification is taking place, or externally energized, eg as an electric furnace, or a combination of internal and external energy.
  • the heater 62 is connected to the reactor 6 and connected upstream of the microwave generator 31.
  • the carbonaceous material 2 is passed through a crimping part 61 surrounded by the heater 62.
  • the Quetschteil is conical, with being Cross section tapered in the conveying direction. As a result, the carbonaceous material 2 is compressed airtight before the microwave zone 32.
  • the carbonaceous material 2 is heated from the outside inwards. Due to the microwave radiation in the microwave station 3, the carbonaceous material 2 is penetrated and heated from the inside to the outside. This combination of supplied radiant heat and microwave irradiation leads to the best possible heat input into the carbonaceous material 2.
  • the carbonaceous material 2 Due to the heat input, the carbonaceous material 2 is also dried. This is particularly advantageous in non-pretreated starting materials such as industrial or domestic waste or garden waste, but also generally in biomass from renewable resources.
  • the gas generator 1 is therefore insensitive to even greater fluctuations in the moisture content of the carbonaceous material 2.
  • the moisture exits as water vapor from the carbonaceous material 2 and serves as an oxidizing agent in the gasification process.
  • the high heat input in particular into the interior of the carbonaceous material 2 by the microwave irradiation, triggers the pyrolysis of the carbonaceous material 2.
  • pyrolysis i.a. the longer-chain molecules of the carbonaceous material 2 are split into shorter molecules. Volatile and non-volatile pyrolysis products form, which are used as starting materials for the subsequent gasification.
  • the carbonaceous material 2 is passed through a feed tube 33, so that the entire carbonaceous material 2 is guided through the microwave zone 32. Especially if pellets or similar
  • Biomaterial be used as starting material 2 the molecular structures are virtually broken by the microwave irradiation, whereby the pyrolysis proceeds more efficiently.
  • the airtight compression in the pinch part 61 in front of the microwave zone 32 ensures that as far as possible no nitrogen from the ambient air enters, which would reduce the calorific value of the generated CO and H 2 containing gas.
  • the dimensioning of the microwave generator 31 depends in particular on the extent of the microwave zone 32, the density of the carbonaceous material 2 and the desired temperature.
  • the choice of frequency may be limited by government regulations. For example, in Germany only the frequencies 24.25GHz, 5.8GHz, 2.45GHz and exceptionally 915MHz are allowed for microwave heating.
  • a microwave generator can also be used two, three or more, which can form either a coherent microwave zone or multiple separate microwave zones.
  • the feed tube 33 leads into the gasification reactor 4, into which also a plasma burner 5 opens and in which the gasification takes place.
  • the feed tube 33 passes through a sieve drum 42 arranged in the gasification reactor 4.
  • the sieve drum 42 is rotatably mounted about its longitudinal axis and is rotated via the drive 106.
  • the longitudinal axis of the screen drum 42 is parallel to the feed tube 33.
  • Screen drum pockets 43 are arranged on the circumferential wall of the screen drum 42 (see in particular FIG. 4).
  • a scraper unit 7, here in the form of five blades 71 which are carried along with the screen drum 42, while passing the exit of the feed tube 33 and the surface of the exiting material, i. the nonvolatile pyrolysis products 21 and possibly not yet fully reacted pyrolytically
  • the hot gas stream 23 of the plasma burner 5 opens into the gasification reactor 4. Therefore, the scraped off particles 25 are exposed directly to the hot gas stream 23.
  • the blades 71 of the scraping unit 7 constantly pass through the hot gas stream 23, so that they also have the process temperature of about 950 ° -1050 ° C and leave the direct contact with scraping this temperature to the supplied pyrolysis products 21 and possibly the carbonaceous material 2 , As a result, the particles 25 in the shortest possible time to process temperature and can be gasified.
  • the temperature of 950 cC and more in the gasification zone ensures that even harmful carbon compounds and tar are completely gasified and also the content of CO and H 2 in the gasification product is as high as possible.
  • Turbulences prevail in the hot gas stream, leading to a rapid mixing of the scraped off particles with the remaining reactor contents, ie with the reactants for lead the gasification.
  • the gasification takes place faster and more intensively, whereby the overall efficiency is increased.
  • Particles 25, which sink in the reactor interior and remove from the hot gas stream 23, are collected by the screen drum 42 in their compartments 43, transported back to the hot gas stream and poured there in the hot gas stream, so that they are better available again for gasification.
  • the entire reactor contents are constantly circulated, which further promotes gasification.
  • FIGS. 6a, b A further embodiment of a scraping unit is shown in detail in FIGS. 6a, b and as part of the gas generator in FIG. It is a rotating scraper 72, which is arranged at the outlet of the feed tube 33.
  • the scraping part 72 consists of a ceramic disk with windows 75 arranged on the front side.
  • the rotating scraping part 72 is driven via a shaft 73. Due to the rotational movement of the non-volatile pyrolysis 21 particles 25 are scraped off. These fly through the frontal windows 75 from the feed tube 75 into the hot gas stream 23 of the
  • Plasma torch 5 Since the volatile pyrolysis products as well as the water vapor already formed during drying also have to escape through the windows 75 from the feed tube 33, intensive gasification already takes place in the region of the windows 75, which act like small reactor chambers. As a result, the overall efficiency of the gas generator 1 is further increased.
  • FIGS. 8a, b A particular embodiment of a rotating scraping part is shown in FIGS. 8a, b.
  • the rotating scraping part 72 ' has radially arranged windows 74 in addition to the windows arranged on the front side. It rotates in the feed tube 33 and is driven as above via the shaft 73.
  • the drive 105 of the rotating scraping member 72 ' consists essentially of a drive bushing 81, which is rotatably mounted in a housing (not shown).
  • the rotational movement takes place in the present example, a sprocket 87.
  • a gear, a toothed belt, a V-belt or the like can be used.
  • the shaft 73 is guided radially in the drive bush 81, but can move axially.
  • a driving star 82 At the right end of the shaft 73 is positively and / or positively secured a driving star 82 and secured by screw 86.
  • the driving star 82 engages in circularly arranged grooves in the drive bushing 81.
  • the rotational movement of the drive bush 81 transmits to the shaft 73.
  • the driving star 82 can move within the grooves.
  • the axial movement is to the right by a rear Travel limit 83, which is bolted to the drive sleeve 81, limited.
  • a rear Travel limit 83 which is bolted to the drive sleeve 81, limited.
  • a spring 84 to the end of the grooves in the drive bushing 81 is possible.
  • FIG. 8a shows the normal operation of the rotating scraping part 72 '.
  • the follower 82 is located at the rear travel limit 83 and the radial windows 74 are covered by the walls of the delivery tube 33.
  • Nonvolatile pyrolysis products 21 can now escape from the feed tube 33 through the windows 74 and prevent their clogging.
  • the axial position of the driving star 82 can be defined and thus counteracted via a control of the input variables "speed of the scraper” and "speed of material supply” the risk of clogging.
  • the displacement measurement of the driving star 82 allows a determination of the state of wear of the rotating blade part 72.
  • Plasma torch 5 in the present example is a steam plasma torch.
  • the composition of the steam plasma promotes the gasification process very strongly, which consists of the radicals O, H, OH, O 2 , H 2 and H 2 O at a mean temperature in the range of 4000 0 C and peak values in the core of the plasma flame of approx. 12000 0 C.
  • the enthalpy density of water vapor is very high and the thermal efficiency of water vapor sources is 70% -90%.
  • water vapor is readily available. Water vapor plasma therefore not only has an accelerating effect on the gasification process, but is also advantageous for economic reasons.
  • reactor contents of the plasma flame 51 are supplied via line 41 (FIG. 3). There, the gasification takes place particularly intense. In addition, this leads to a circulation of the reactor contents, since the plasma flame 51 supplied mixture of gas and particles 25 enters as hot gas stream 23 back into the reactor interior and there leads to turbulence and improved heat transfer to the newly supplied particles 25.
  • the mixture of gas and particles also hits the scraping device 7 and the surface of the supplied pyrolysis products 21, possibly also of the carbonaceous material 2, and heats them to the process temperature. Subsequently, it flows into the lateral upper region of the screening drum 42 and mixes with the material constantly conveyed up through the screening drum. This will maintain a continuous gasification process. This gasification process also speeds up the gasification process.
  • the gasification reactor 4 can be dimensioned significantly smaller, with the result that the insulation losses are greatly reduced and the overall efficiency can be significantly increased.
  • the size of the gas generator can be so greatly reduced that in addition to systems in the power range of about 100 kW e i (net) and more small systems for residential use in the power range of about 2-4 kW e ⁇ (net) are possible.
  • the ash 24 produced during the gasification is screened off through the sieve drum 42 and falls into the lowermost region of the gasification reactor 4.
  • the remaining gasification products 23 are withdrawn via the lower reactor region by means of a slight negative pressure by means of a blower 128 from the reactor interior to a filter unit 112.
  • the ceramic filter cartridges 113 serve as dust filters and have the advantage that the gas generated can be filtered without prior cooling, ie at about 700 ° -800 ° C.
  • the generated hot gas for power generation could be fed directly to a hot gas engine or even to a pore burner.
  • the hot gas is passed via a line 122 to another station 120, which has the function of a gas-water heat exchanger and / or a scrubber. This allows the hot gas to cool to below 50 0 C and clean.
  • the heat can be used by the warmed up cooling water, which is fed via the input 1 16 and the output 118 is derived, is fed by means of a pump 126 in the building technology or forwarded to an external heat exchanger. The heat can also be used for preheating the carbonaceous material. 2 use.
  • the cooled clean gas is withdrawn by means of the blower 128 via a negative pressure from the system and removed for further use in an external gas storage or a combined heat and power plant.
  • the second apparatus for producing gas shown in FIG. 10 differs from the first apparatus shown in FIG. 1, in particular with regard to the design of the pyrolysis station. While in the first device, the material to be pyrolyzed after compaction is first heated with the aid of the heater from outside to inside, before it is irradiated with microwaves to heat it from the inside out (see also Figures 2 and 3), is in the second device, the material to be pyrolyzed first irradiated with microwaves of the microwave generator 31 to reach the inside of the pyrolysis, and then by a heater, in this example, a porous furnace 63, out to bring the material also from the outside to the pyrolysis temperature ,
  • FIG. 13 shows a vertical section through the device from FIG. 10 at the level of the porous burner 63.
  • the microwave station is combined with three porous burners 63 which adjoin the microwave generator 31 and around the feed tube 33 are arranged in the region of the lower circumference, so that the radiant heat 66 radiates onto the feed tube 33.
  • the pore burner 63 may be fired with syngas generated in the gas generator and containing CO 2 and H 2 , which is supplied via the synthesis gas ports 64.
  • the synthesis gas is burned together with air or oxygen in the pore area of the pore burners 63 to generate thermal energy.
  • the resulting exhaust gases exit through the discharge outlet 65 and can be used for preheating other components.
  • the pore area is generally formed of ceramic foam or other high temperature resistant structure.
  • Particularly advantageous for pore burners is their very high power density of about 1000 kW / m 2 .
  • high temperatures of up to about 1400 ° C can be achieved.
  • Further advantages are high heating rates and good controllability of the oven temperature. Since pore burners allow very high gas temperatures, gas generated during the gasification process can be supplied to them immediately without prior cooling, if necessary after dust filtration.
  • the porous burner 63 achieves a heat input that is six times higher than that of a conventional gas burner.
  • the use of a pore burner in combination with microwave pyrolysis improves the overall energy balance of the pore burner Gas burner with still small footprint and is therefore particularly suitable for gas generators, which are sized for home use.
  • the feed tube 33 for feeding the pyrolyzed material and the plasma torch 5 are arranged relative to one another such that the hot gas flow generated by the plasma flame 51 is not only laterally but frontally on the scraper unit 72 (see also Figures 6a, b) meets to heat the scraper unit 72 even better.
  • the scraper unit 72 transfers its temperature to the material to be shredded. Due to the frontal orientation of the hot gas stream 23 on the scraper unit 72, it is also better achieved that the hot gas stream in the front windows 75 of the scraper unit 72 also directly heats the material to be shredded to the process temperature for the gasification.
  • the drum 45 is not designed as a sieve drum, but only as a drum 45 with drum compartments 43 (see Figure 12) to bring not yet gasified particles 25 back into the hot gas stream.
  • the few ash 24 can exit via the end faces of the drum 45 and be discharged via the ash outlet 114.
  • the non-perforated drum 45 has the additional advantage of more efficient thermal insulation of the interior of the gasification reactor 4.
  • the plasma flame 51 is arranged in the second device in a diffuser 52 provided with openings 53 (see FIG. 11).
  • the volatile and solid pyrolysis products come together with the radicals generated there, with which they react to CO and H 2 .
  • they are heated very rapidly in the plasma very rapidly, so that a sudden volume expansion takes place, which leads to a local negative pressure.
  • the openings 53 are on this local vacuum another Pyrolysis products are sucked into the water vapor plasma flame 51, so that a constant flow of hot gas is maintained.
  • the space requirement is further reduced in the second device.
  • the second apparatus for producing gas from FIGS. 10 to 13 can also be executed with the scraping unit 72 'as in FIGS. 8a, b or also with blade 71 as in FIG. 4 or another scraping unit.
  • the generated hot gas can be further used as described above.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Procédé de gazéification de matière contenant du carbone (2) en gaz contenant du CO et du H2 (23), qui consiste d'abord à pyrolyser la matière contenant du cabrone (2), puis à la broyer pour augmenter le rendement, avant de la gazéifier. A cet effet, une unité de broyage conçue de préférence sous forme d'unité à racloirs (71) est située à la sortie (33) du poste de pyrolyse débouchant dans le réacteur de gazéification, la matière contenant du carbone pyrolysée étant amenée à la température de processus pour la gazéification lors du broyage.
PCT/EP2007/001347 2006-02-17 2007-02-16 Procédé et dispositif de production de gaz à partir de matière contenant du carbone WO2007093429A2 (fr)

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DE102006007457A DE102006007457B4 (de) 2006-02-17 2006-02-17 Verfahren und Vorrichtung zum Erzeugen von Gas aus kohlenstoffhaltigem Material
DE102006007457.2 2006-02-17

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WO2007093429A2 true WO2007093429A2 (fr) 2007-08-23
WO2007093429A3 WO2007093429A3 (fr) 2008-05-29

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AT516178A4 (de) * 2014-09-16 2016-03-15 Ame Handelsgesellschaft M B H Verfahren und Vorrichtung zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen
AT518474A1 (de) * 2016-04-12 2017-10-15 Ame Handelsgesellschaft M B H Verfahren zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen

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DE202012101259U1 (de) 2011-04-06 2012-07-11 Behzad Sahabi Transportable Vorrichtung zur Reinigung von belastetem Ausgangsmaterial

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US3449213A (en) * 1964-08-04 1969-06-10 Edward M Knapp Pyrolysis of coal with microwave energy
DE3239352A1 (de) * 1982-10-23 1984-04-26 Krupp-Koppers Gmbh, 4300 Essen Vorrichtung zur trockenen kuehlung von heissem schuettgut, insbesondere von heissem koks
DE3433238C1 (de) * 1984-09-11 1986-01-09 Artur Richard 6000 Frankfurt Greul Verfahren zur Wirbelschichtvergasung vom Müll zusammen mit anderen Brennstoffen und Einrichtung zur Durchführung des Verfahrens
US5550312A (en) * 1991-11-29 1996-08-27 Noell-Dbi Energie-Und Entsorgungstechnik Gmbh Method of thermal utilization of waste materials
US5280757A (en) * 1992-04-13 1994-01-25 Carter George W Municipal solid waste disposal process
DE19528765A1 (de) * 1995-08-04 1997-02-06 Siemens Ag Austragseinrichtung für eine Schweltrommel für Abfall
DE19531340A1 (de) * 1995-08-25 1996-03-14 Bergk Erhard Dipl Ing Tu Verfahren und Vorrichtungen zur Ent-, Vergasung und Verwertung von Siedlungsabfall und anderen Abfallstoffen
DE19720331A1 (de) * 1997-05-15 1998-11-19 Clemens Dr Kiefer Verfahren und Vorrichtung zur Entgasung und Vergasung oder Verbrennung
DE19846805A1 (de) * 1998-10-10 2000-04-13 Clemens Kiefer Verfahren und Vorrichtung zur Vergasung und Verbrennung
US20030024806A1 (en) * 2001-07-16 2003-02-06 Foret Todd L. Plasma whirl reactor apparatus and methods of use
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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT516178A4 (de) * 2014-09-16 2016-03-15 Ame Handelsgesellschaft M B H Verfahren und Vorrichtung zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen
AT516178B1 (de) * 2014-09-16 2016-03-15 Ame Handelsgesellschaft M B H Verfahren und Vorrichtung zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen
AT518474A1 (de) * 2016-04-12 2017-10-15 Ame Handelsgesellschaft M B H Verfahren zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen
AT518474B1 (de) * 2016-04-12 2020-08-15 Ame Handelsgesellschaft M B H Verfahren zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen

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AR059537A1 (es) 2008-04-09
DE102006007457B4 (de) 2007-12-27
WO2007093429A3 (fr) 2008-05-29

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