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WO2008083704A1 - Procédé de production de charbon actif à partir de déchets organiques compactés - Google Patents

Procédé de production de charbon actif à partir de déchets organiques compactés Download PDF

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Publication number
WO2008083704A1
WO2008083704A1 PCT/EP2006/070245 EP2006070245W WO2008083704A1 WO 2008083704 A1 WO2008083704 A1 WO 2008083704A1 EP 2006070245 W EP2006070245 W EP 2006070245W WO 2008083704 A1 WO2008083704 A1 WO 2008083704A1
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WO
WIPO (PCT)
Prior art keywords
coke
activated carbon
waste
drying
waste materials
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2006/070245
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German (de)
English (en)
Inventor
Jochen Zingelmann
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Individual
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Individual
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Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to PCT/EP2006/070245 priority Critical patent/WO2008083704A1/fr
Publication of WO2008083704A1 publication Critical patent/WO2008083704A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/30—Active carbon
    • C01B32/312—Preparation
    • C01B32/318—Preparation characterised by the starting materials
    • C01B32/324—Preparation characterised by the starting materials from waste materials, e.g. tyres or spent sulfite pulp liquor

Definitions

  • the invention relates to a process for the production of activated carbon from compacted organic waste! Istoffen, whereby the method can be used in particular in connection with the treatment and utilization of wastes,
  • Processes and devices for processing and recycling waste liquor are known from DE-A-102 61 537, EP-A-I 434 003 and US-A-2004/0134395.
  • the organic wastes are extracted from a mixture of inorganic and organic wastes to be fed, after compaction, to a gasification process for the recovery of gases and ash.
  • the object of the invention is to provide a process for the production of activated carbon from kompaktêt ⁇ organic AbfaNstoffen, soft can find particular application in the treatment and recovery of Abfaüstoffen.
  • the invention proposes a process for the production of activated carbon from compacted organic wastes, especially in the treatment and recovery of waste, proposed in the method, the compacted AbfaNstoffe be gasified to form ash and coke in a gasification reactor, the Coke and ash are separated and - the coke is further processed to activated carbon.
  • aiso is proposed to remove the coke resulting from the gasification of the compacted organic wastes from the gasification reactor in order to use it as activated carbon. This is a fairly economical production of activated carbon. This activated carbon is produced, so to speak, as a waste product in the treatment and utilization of organic waste.
  • the separation of coke and ash takes place via a screening device in or at the discharge of the gasification reactor. It is also expedient if, for the production of activated carbon in bulk form, the coke discharged from the gasification reactor is comminuted directly or in a downstream system component or in the case of further processing.
  • the amount and moisture of the waste to be dried is determined and the drying plant is controlled so that the waste to be dried leave the drying plant with a pre-defined or predefinable residual moisture.
  • the amount of heat eg Temperature and / or amount, ie throughput of drying air
  • the drying plant is then controlled to dry the amount of waste.
  • the drying plant operates in continuous operation, so that the amount of waste material supplied per unit of time and its moisture are determined.
  • the control of the drying installation takes place in such a way that such an amount of heat is supplied or such an amount of heat acts on the waste materials present in the drying plant that the amount of waste discharged by the drying plant has the maximum permissible residual moisture level.
  • the drying process of the waste materials can be optimized by circulating or otherwise agitating the waste within the drying plant so as to increase the surface area of the waste within the drying plant, thus making the removal of moisture from the waste more effective.
  • the determination of the amount and the moisture of the waste to be dried is preferably without contact.
  • drying air flows expediently opposite and / or across and / or at an angle therebetween Hiegenden angle to the transport direction of the waste to be dried within the drying plant.
  • a drying system with rotary drum is preferably used on the drying installation, which has fixtures which, on the one hand, transport the waste materials through the rotary drum and, on the other hand, the waste within the rotating drum, in particular circulation movement hold.
  • the internals are expediently a web which protrudes helically from the inside of the rotary drum in the manner of a screw conveyor.
  • the amount of heat required for drying the amount of waste materials is controlled by the flow rate and / or temperature of drying air and / or the residence time of the amount of waste to be dried in the drying plant.
  • the drying process can be integrated in a control and / or in a control unit of the drying plant.
  • the residual moisture content of the Trocknungsaniage leaving dried waste is determined and optionally fed via a control loop with the difference between the desired maximum allowable residual moisture (Soil residual moisture) and measured (actual) residual moisture and thus as FUhrungsucc a controller.
  • 1 is a block diagram showing the individual process and plant components of a process for the substantially complete recovery of domestic and commercial waste and / or liquid predominantly organic waste
  • Fig. 2 is a schematic representation of a füriauf-drying plant with rotary drum and 3 shows a schematic representation of a gasification reactor with separate discharge of ash and coke,
  • the method described here by way of example for the complete recovery of domestic and commercial waste and / or liquid predominantly organic waste consists of process sections, each of which has a modular structure and thereby make it possible to adapt to different flow rates (see the general procedure in FIG. 1) Thanks to its modular design, it is also possible to operate the energetic stage locally away from the rest of the installation, thus making use of the advantages of decentralized energy generation. Special features of the process are the drying (pre- and post-drying) and the production of coke for use as activated carbon.
  • the material is fed to a silo after coarse crushing and iron deposition, which (for example with a puller) metered the material continuously into the further treatment.
  • the material stream to be treated is transferred to a drying drum 10.
  • This drum 10 consists of a metal tube with process-specific internals 12 (screw conveyor), which are able to transport the material in the longitudinal direction 14, while the metal tube rotates in a defined direction about its longitudinal axis.
  • process-specific internals 12 screw conveyor
  • hot air 18 is blown into the drum, which extracts the material in the drum 10 water and volatile substances.
  • the resulting residence time is calculated in the dryer, wherein the residence time through
  • the laden with water vapor, dust and volatile substances exhaust air 20 is fed to a (not shown in Fig. 2) biofilter and cleaned there (Description Section 5 - ancillary facilities).
  • the dried material falls from the drying drum 10 via a chute 22 in the subsequent drum screen or on a conveyor belt 24.
  • a drum screen consists of an inner, defined perforated drum, which is rotated continuously about its longitudinal axis, and an outer closed drum into which the screened fine fraction falls and is transported in the longitudinal direction with a conveyor belt. The one in the drumming! Any dust is sucked off and the exhaust air is cleaned via the biofilter. Other screening methods and devices can also be used.
  • the fine fraction is fed directly to the treatment.
  • the coarse fraction is, as far as possible dried and thus also deodorized and freed from the mineral and small parts, then transferred to the sorting belt.
  • the sorting belt for this purpose, serves an inclined conveyor with webs transverse to the direction of the tape.
  • the sorting process is carried out in steps, housed in one or more overhead cabins, manually and / or with automated systems.
  • the material is transported through the sorting cabs with conveyor belts.
  • the different material groups are discharged into separate manholes and recorded in, in particular, flush-catching collection systems, and used either as bulk goods, as loose or as pressed bales for traditional recycling.
  • the material which has not been sorted out is precompressed with a single- and / or multi-shaft comminution system and at the same time freed by a particularly multi-stage separation of metallic constituents.
  • the iron metals are separated by an overband magnet and the non-ferrous metals are separated by an eddy current separator.
  • the metallic constituents are separated from the process separately for ferrous and non-ferrous metals and recycled, as described under no. 1 described supplied.
  • a drying drum such as under no. 1 described and shown in Fig. 2, the material is removed from the residual moisture.
  • Other Trocknu ⁇ gsverfah- ren can also be used.
  • the air heating takes place via heat exchangers against hot water, which was obtained by heat extraction from the exhaust gas of the engines.
  • the exhaust air is the under. 1 named biofilter supplied.
  • This second screening stage may be identical to that described under Zi ff, 1, and differs only in the mesh size of the screen, which is about 50% of the first in this second screening stage.
  • the fine fraction which is composed essentially of mineral constituents, is supplied to a flotation in this process section.
  • the transverse transport of the fine fraction to the flotation is provided by belts.
  • the flotation (see, for example, Figures 3 and 4 with related description in DE-A-103 46 892) consists of a trough of stainless steel with sloping bottom. At regular intervals, nozzles with defined spray characteristics are installed in the bottom, through which compressed air is directed to swirl the masses to be floated.
  • the material entry takes place from the side where the floor is highest.
  • the injected compressed air and the supplied water at the end of the task Due to the slope of the soil, the injected compressed air and the supplied water at the end of the task, a flow of material to the bottom of the soil.
  • the sandy-gravelly material collects and is transported with a snail to one side.
  • the purified mineral fraction is conveyed through a second screw with sieve bottom from the plant and drained, it can be used as a building material.
  • the Crufa ⁇ gr ⁇ nne collected the flotated organic material It is discharged through a sieve belt and fed directly to the compaction.
  • the water from the gutter and the drainage water from the sieve auger are fed to the central water treatment (for description see point 5 - ancillary equipment).
  • the remaining material in the stream consists for the most part! from organic substances. They are fed to a process-specific equipped conveyor belt of a homogenizing and Kompaktierech.
  • the moisture content of the material is measured using a non-contact measuring method and the throughput quantity is determined with a belt scale.
  • high-waste water e.g. Sewage sludge and / or other sludge that is controlled by a process computer
  • the adjustment of the material to the process-specific moisture required The admixture of the sludge via a water content controlled metering device that extracts the material to be conveyed from a silo.
  • Abstrefer over the belt controlled by a level indicator in the task Schacht, directs the material via a chute directly into the respective feed chute of the compacting plant.
  • the compacting plants work on the principle of a twin-screw extruder and are equipped with process-specific tunings that homogeneously mix and compact the material.
  • the material heats up to more than 150 0 C.
  • This material is sanitized, homogenized and solidified.
  • the briquettes are protected against the weather for a long time. They are biologically inactive and odorless,
  • the material strands emerging in this way are guided over a cooling section behind the molded piece and, after hardening, cut to length mechanically and / or in an automatic process.
  • the properties of the briquettes correspond to the process-specific requirements for the following gasification process.
  • the briquettes are converted into an energetically or chemically usable, tar-free gas which is suitable both for cogeneration plants with gas engines and / or for fuel cells with specific catalysts or can be used as synthesis gas.
  • the gasification reactor used is a fixed-bed shaft gasifier. It is a descending gasification with low negative pressure in the range of about 100 to 300 mm Ws.
  • the briquettes are transported via a conveyor (trough chain conveyor, chain scraper, etc.) onto the distributor belt and from there via a controlled stripping device to a vibrating chute, which leads directly into the lock of the carburettor.
  • the lock conveys the briquettes into the reactor and ensures the upper closure of the reactor. Via openings in the upper reactor area, some of which lead into the interior of the reactor and the introduction of steam into the gasification zone, the necessary oxygen is introduced into the process.
  • a process-specific mixture of air and / or oxygen and / or steam which is tailored to the gasification substance, is used.
  • the steam needed is in the inner Mante! generated around the reactor core. Water is introduced into the jacket from the outside and from the bottom, which spontaneously evaporates due to the high temperature of the inner jacket (about 500 ° C.) and becomes superheated steam, which is then passed via pipes directly into the lower part of the gasification zone.
  • air and / or oxygen are also conducted to the center of the gasification zone through a pipe with a distributor device at the lower end. This achieves the most uniform possible temperature distribution in the gasification zone.
  • Air is introduced into the lower part of the carburetor core via a second series of air nozzles in order to melt off the lower part of the resulting coke bed by oxidation / gasification.
  • Carburetor rests on a kegelige part, which at the lower end by a Rust is completed, which is rutted and / or rotatable and thus allows the discharge of the ashes in the underlying collecting container.
  • the carburetor of the resulting coke can be withdrawn through a modified lower part of the carburetor of the resulting coke on a water-cooled chamber on a steel conveyor belt and then cooled by a lock from the carburetor to be recovered.
  • the separation of the ash from the coke is via a vibrating screen, the discharge of the ash via a screw with lock.
  • the coke can be used as activated coke.
  • the bottom of the container is conical, so that the ashes can be discharged via a screw with rotary valve.
  • An integral part of the system is a rapid cooling of the gas in a cooler and an intensive gas scrubbing with subsequent drying, which releases a gas that meets the process-specific requirements of gas utilization.
  • the cooling and washing water from this process is purified by a central, tailored to the requirements of the process Wasseraufbituitugsstrom and circulated.
  • the resulting contaminants from the water treatment are separated mechanically and / or automatically and the gasification material prior to the compacting, as described in sec. 2, fed again.
  • the gas is mixed with air in order to arrive at an optimized gas mixture for the chemical process in the energy recovery plant.
  • a gasification reactor 30, as can be used, for example, for the gasification of the compacted organic waste, is shown schematically in FIG. 3.
  • the peculiarity of the gasification reactor 30 shown in FIG. 3 is that the resulting coke, located in the lower part of the gasification reactor 30 and in particular in the coke bale 43 above the controlled spool 44 (when it is closed), selectively via the discharge drain with sieve 45 eats. So here it does not come to one more Combustion of the coke, but to a separation of the coke from the ash, The coke remains above the sieve 45 in the discharge of the reactor 30, while the ash falls down through the Siebaniage down and is discharged through the Aschenaustragsötechnisch 46.
  • the coke is thus carried out separately in the gasification reactor 30 in order to be fed to further processing for the purpose of producing activated carbon.
  • the coke already forms the activated carbon and only has to be processed in order to have the activated carbon in the desired form (for example as bulk material).
  • the desired form for example as bulk material.
  • there is a comminution of the coke which can be done in a downstream crushing plant.
  • the gas is used for energy.
  • the energetic utilization can take place in three different ways:
  • the polluted water produced in the process is transported to a central water treatment (see, for example, Figures 5-9 with related description in DE-A-103 46 892).
  • the WAB consists of a container of approx. 3.0 m in height which is specifically adapted to the project and subdivided into various chambers, each of which is equipped with process-specific adapted devices, thus creating a virtually modular structure.
  • the dividing walls between the individual modules have a nozzle of 0 100 mm in each case at a distance of 0.5 m and 1.5 m from the lower edge in the middle for attaching 100 mm PVC pipe or similar materials for the different process-specific discharges.
  • the plant is an open-topped container, which is preferably made of stainless steel, accessible on the upper side covered with grates and accessible by laterally welded steps,
  • Inlet chamber into which the wastewater is pumped, with measuring station for the process-specific necessary parameters
  • Settling chamber into which the water from the inlet chamber runs directly over the lower pipe socket, for sedimenting substances, such as sands and other mineral constituents
  • LSA Le ⁇ chtstoffabsche ⁇ der
  • the separator consists of a PVC tube filled with a stainless steel wire mesh rolled up from a flat sheet. (Sketch 4, Fig. A)
  • the outlet from the LSA takes place via the upper nozzle on which a PVC sheet, 90 °, is placed and connected to a pipe approx. 1.0 m long, pointing downwards (Diagram 4 Fig. B).
  • the unused inlets and outlets are closed by caps.
  • the series connection of two such separators can reduce light materials below a concentration of significantly ⁇ 5.0 mg / l.
  • Mixer and dosing device containing a stirrer and dosing equipment to remove water from the suspended matter and flocculants of suspended solids and many dissolved substances.
  • the inlet is brought to a medium height.
  • the overflow passes through the upper spigot into a settling chamber as described above,
  • the water After the passage of two settling chambers, the water is usable again. As process water, a previous filtration should take place eg via a gravel filter.
  • the exhaust air produced on different parts of the system is laden with dust, volatile organic and inorganic substances.
  • the biofilter has to fulfill several functions: - Adsorption of the entrained dust,
  • the biofilter is a cuboid container of approx. 600 x 250 x 250 cm, corresponding to a 20 "sea container, with two tight-fitting doors at one head end.
  • the condensation collects and is pumped to the WAB.
  • nozzles are attached to the roof of the container, through which water can be sprayed into the container together with nutrients.
  • microbiology for example, oat straw, dried heather and / or other structure-forming material can be used.
  • the microbiology is applied as a dispersion, the exhaust air flows through the filter from a lower corner to diametra) opposite upper corner,

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

Procédé de production de charbon actif à partir de déchets organiques compactés, en particulier lors du traitement et de la valorisation de déchets, selon lequel les déchets compactés sont gazéifiés dans un réacteur de gazéification, des cendres et du coke étant produits. Le coke et les cendres sont séparés l'un de l'autre et le coke est soumis à un nouveau traitement pour obtenir du charbon actif.
PCT/EP2006/070245 2006-12-28 2006-12-28 Procédé de production de charbon actif à partir de déchets organiques compactés Ceased WO2008083704A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/EP2006/070245 WO2008083704A1 (fr) 2006-12-28 2006-12-28 Procédé de production de charbon actif à partir de déchets organiques compactés

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2006/070245 WO2008083704A1 (fr) 2006-12-28 2006-12-28 Procédé de production de charbon actif à partir de déchets organiques compactés

Publications (1)

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WO2008083704A1 true WO2008083704A1 (fr) 2008-07-17

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Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB190422459A (en) * 1904-10-18 1904-11-24 Ferdinand Louis Josep Gregoire Improved Process and Apparatus for Loading Coke from Coke Furnaces into Trucks, and the Simultaneous Separation of Ashes and Small Coke therefrom
US4603119A (en) * 1984-05-16 1986-07-29 Alfons Karl Process for production of activated carbon from lignite coke
JPH05132306A (ja) * 1991-02-19 1993-05-28 Oomura Concrete Kk 高温ガス流による活性炭の製造方法および装置、並びに活性炭
JPH06227807A (ja) * 1993-02-02 1994-08-16 Kyodo Kumiai Ratesuto 粒状活性炭の製造方法
WO1998007655A1 (fr) * 1996-08-20 1998-02-26 BLüCHER GMBH Charbon actif granule issu de residus de distillation
WO2000000429A1 (fr) * 1998-06-29 2000-01-06 Katz, Raul Procede de preparation de charbon active a partir d'ordures menageres
WO2000071936A1 (fr) * 1999-05-25 2000-11-30 Mbr Technologies, Inc. Procede, methode et appareil d'activation rapide permettant de fabriquer du charbon actif en boulettes a partir de dechets carbones
JP2006001805A (ja) * 2004-06-18 2006-01-05 Takasago Ind Co Ltd 炭化物の製造方法

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB190422459A (en) * 1904-10-18 1904-11-24 Ferdinand Louis Josep Gregoire Improved Process and Apparatus for Loading Coke from Coke Furnaces into Trucks, and the Simultaneous Separation of Ashes and Small Coke therefrom
US4603119A (en) * 1984-05-16 1986-07-29 Alfons Karl Process for production of activated carbon from lignite coke
JPH05132306A (ja) * 1991-02-19 1993-05-28 Oomura Concrete Kk 高温ガス流による活性炭の製造方法および装置、並びに活性炭
JPH06227807A (ja) * 1993-02-02 1994-08-16 Kyodo Kumiai Ratesuto 粒状活性炭の製造方法
WO1998007655A1 (fr) * 1996-08-20 1998-02-26 BLüCHER GMBH Charbon actif granule issu de residus de distillation
WO2000000429A1 (fr) * 1998-06-29 2000-01-06 Katz, Raul Procede de preparation de charbon active a partir d'ordures menageres
WO2000071936A1 (fr) * 1999-05-25 2000-11-30 Mbr Technologies, Inc. Procede, methode et appareil d'activation rapide permettant de fabriquer du charbon actif en boulettes a partir de dechets carbones
JP2006001805A (ja) * 2004-06-18 2006-01-05 Takasago Ind Co Ltd 炭化物の製造方法

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