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WO2008083703A1 - Procédé de séchage de déchets solides et / ou liquides - Google Patents

Procédé de séchage de déchets solides et / ou liquides Download PDF

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Publication number
WO2008083703A1
WO2008083703A1 PCT/EP2006/070243 EP2006070243W WO2008083703A1 WO 2008083703 A1 WO2008083703 A1 WO 2008083703A1 EP 2006070243 W EP2006070243 W EP 2006070243W WO 2008083703 A1 WO2008083703 A1 WO 2008083703A1
Authority
WO
WIPO (PCT)
Prior art keywords
waste
amount
drying
dried
determined
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/EP2006/070243
Other languages
German (de)
English (en)
Inventor
Jochen Zingelmann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
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 Individual filed Critical Individual
Priority to PCT/EP2006/070243 priority Critical patent/WO2008083703A1/fr
Publication of WO2008083703A1 publication Critical patent/WO2008083703A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/22—Controlling the drying process in dependence on liquid content of solid materials or objects
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B11/00—Machines or apparatus for drying solid materials or objects with movement which is non-progressive
    • F26B11/02—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles
    • F26B11/04—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles rotating about a horizontal or slightly-inclined axis
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B2200/00—Drying processes and machines for solid materials characterised by the specific requirements of the drying good
    • F26B2200/04—Garbage

Definitions

  • the invention relates to a method for drying solid and / or liquid waste, which method can be used in particular in the treatment and recycling of waste
  • the object of the invention is the drying process of solid and / or liquid Abfa I is open, as they occur in particular during the treatment and utilization ⁇ optimize.
  • the invention proposes a method for drying solid and / or liquid wastes, especially in the treatment and utilization of waste materials, wherein in the method, the amount and moisture of the waste to be dried are determined from These determined values, the amount of heat is determined, which is required to dry the waste to below a predetermined residual moisture, and according to the determined amount of heat, a drying plant for drying the amount of waste is controlled.
  • the amount and moisture of the waste to be dried is determined and the drying plant controlled so that the waste to be dried leave the drying plant with a predetermined or predetermined residual moisture.
  • the amount of heat eg the temperature and / or amount, ie throughput of drying air
  • the drying plant is controlled to dry the amount of waste.
  • the drying plant operates in continuous operation, so that the amount of waste material fed in per unit time and its moisture are determined.
  • the control of the drying a ⁇ lage takes place in such a way that such an amount of heat is supplied or such an amount of heat acts on the waste in the drying plant that the output of the drying plant amount of waste has the maximum allowable residual moisture level.
  • the drying process of the waste can be optimized by circulating or otherwise agitating the waste within the drying plant, thus increasing 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 carried out without contact.
  • the drying of the waste material takes place within the drying plant by drying air.
  • This drying air expediently flows opposite and / or transversely and / or at an angle therebetween to the transport direction of the waste to be dried within the drying plant.
  • the drying plant used is preferably a rotary drum drying plant which has internals which, on the one hand, store the waste Fabrics through the rotary drum! transport and on the other hand keep the Abfail für within the rotary drum in motion, in particular circulation movement.
  • the internals are expediently a web which protrudes helically in the manner of a screw conveyor from the inside of the rotary drum.
  • the amount of heat required for drying the amount of Abfaüstoffen is controlled by the flow rate and / or temperature of drying air and / or the Verweiizeit the amount of waste to be dried in the drying plant.
  • the erfi ⁇ dungswashe method may be integrated in a control and / or in a control unit of the drying plant.
  • the residual moisture content of the amount leaving the drying plant dried solids is determined and optionally fed via a control loop with the difference between the desired maximum residual moisture content (target residual moisture) and measured (actual) residual moisture and thus as a reference variable a controller.
  • drying method according to the invention can be in the treatment and recycling of waste materials, as described in the above-mentioned writings, especially dry after appropriate sorting and preprocessing organic waste prior to their Kompak- drying in the second drying stage.
  • the gasification of these dried in the manner according to the invention and then compacted organic Abfail für for the production of coke is more advantageous
  • Development of the invention associated with the production of activated carbon by the compacted waste materials are gasified to form gas, ash and coke in a gasification reactor, the coke and the ash are separated and the coke is further processed to activated carbon. It is expedient here if the separation of coke and ash takes place via a screening device in or at the discharge of the gasification reactor. For the production of activated carbon from the coke only the crushing of the coke is required if the activated carbon is to be in the form of bulk material.
  • 1 is a block diagram showing the individual process and Anlagenkompo ⁇ nents a method for substantially complete recovery of domestic and commercial waste and / or liquid predominantly organic waste,
  • Fig. 2 is a schematic representation of a Naturaliauf-drying plant with rotary drum and
  • Fig. 3 is a schematic representation of a gasification reactor with separate discharge of ash and coke.
  • material groups such as metal, glass, plastic, paper, cardboard, cardboard and / or composites of mixtures of these and other raw materials.
  • 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 pipe rotates about its longitudinal axis in a defined direction.
  • process-specific internals 12 screw conveyor
  • hot air 18 is blown into the drum, which extracts the material in the drum 10 water and easily volatiles.
  • 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 TrommeSsieb or on a conveyor belt 24, a slat curtain 26 o.dgi. Closure system prevents escape of hot air from the discharge end 28 of the dry drum 10.
  • fractionation of the dried waste material takes place, this end, a drum of an inner defined perforated drum which is continuously rotated about its longitudinal axis, and an outer closed-Senen drum, in which The sieved fine fraction falls into it and is transported out in the longitudinal direction with a conveyor belt.
  • the dust generated in the drum is sucked off and the exhaust air is cleaned via the biofilter.
  • Other screening methods and devices may 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.
  • an inclined conveyor with webs transverse to the direction on the belt.
  • 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 thrown off into separate shafts and recorded in, in particular, the same-level collection systems and neither as bulk material, loose, or as pressed bales fed to traditional recycling.
  • the non-sorted material is pre-shredded electro-mechanically in the further process sequence with a single and / or multi-shaft crushing system and at the same time freed by a particular multi-stage separation of metallic components.
  • a Mathba ⁇ dmagneten are the ferrous metals and deposited with a Wirbelstromabscheider the non-ferrous metals.
  • 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 e.g. under no. 1 described and shown in Fig, 2, the material is removed from the residual moisture.
  • Other drying methods 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 can be identical to that under no. 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 associated description in DE-A-103 46 892) consists of a tub of stainless steel with sloping bottom, at regular intervals nozzles with defined spray characteristics are incorporated in the bottom, by the compressed air for swirling which is directed to the masses to be floated.
  • ground water is up to the upper edge of a gutter, which is located at the opposite end to the material entry.
  • the material entry is made 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 flooded organic material collects in the gutter. 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 are fed to the central water treatment (see point 5 - ancillary equipment).
  • the remaining material in the stream consists predominantly of organic substances, they are fed to a process-specific equipped conveyor belt a homogenizing and Kompaktiermaschine.
  • the moisture content of the material is determined by means of a non-contact measuring method, and the throughput quantity is determined using a belt scale.
  • high-waste water e.g. Sewage sludge and / or other sludge
  • the adjustment of the material to the process-specific moisture required By metering high-waste water, e.g. Sewage sludge and / or other sludge, which is controlled by a process computer, the adjustment of the material to the process-specific moisture required, The admixture of the sludge via a controlled via the water content dosing, which extracts the material to be conveyed from a silo.
  • the material is fed to the feed chutes of the compacting plants.
  • a scraper above the belt controlled by a filling level indicator in the loading shaft, directs the material via a chute directly into the respective feed chute of the compacting plant.
  • the compacting machines operate on the principle of a twin-screw extruder and are equipped with process-specific tuned shafts, which homogeneously mix and compact the material. During this process, the estate heats up to over 150 ° C. Thus, the material is sanitized, homogenized and solidified in itself.
  • the briquettes are protected against the weather and very storable. They are biologically inactive and odorless! ,
  • the material strands emerging in this way are guided behind the fitting over a cooling section 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 conveyor belt and from there via a controlled scraper device to a vibrating chute, which leads directly into the lock of the carburettor.
  • the lock conveys the briquettes into the reactor, thereby ensuring the upper closure of the reactor, via openings in the upper reactor area, some of which lead to the interior of the reactor, and steam injection units. into the gasification zone, the necessary oxygen is introduced into the process.
  • the required steam is generated in the inner shell 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.
  • the material in the lower end of the carburetor rests on a conical part, which is closed at the bottom by a grate that is shaking and / or rotatable and thus allows the discharge of the ashes in the underlying collecting container.
  • the resulting coke can be drawn off via a chamber cooled with water on a steel conveyor belt through an altered lower part of the gasifier and then cooled by a lock from the gasifier. borrow.
  • the separation of the ash from the coke is carried out via a vibrating sieve, 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 and recirculated via a central water treatment plant adapted to the requirements of the process.
  • the gas is mixed with air in order to arrive at an optimized gas mixture for the chemical process in the energy recovery plant.
  • the individual elements of the gasification reactor 30, as shown in FIG. 3, include:
  • 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 coking outflow shaft 43 above the controlled spool 44 (when it is closed), selectively via the discharge with Siebaniage 45 can dissipate.
  • Siebaniage 45 it is no longer a burning of coke, but a separation of the coke from the ashes.
  • the coke remains above the sieve 45 in the discharge of the reactor 30, while the ash falls through the sieve through down and is discharged through the Aschenaustragsö réelle 46.
  • the coke is thus carried out separately in the gasification reactor 30, for 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, a bulk material).
  • the desired form for example, a bulk material.
  • there is a comminution of the coke which can be done in a nachgeschaiteten 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 eg FIGS. 5 to 9 with the associated 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, resulting in a quasi-modulatory 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, on the upper side walkable covered with grates and accessible by laterally welded steps,
  • LSA Light-weight separator
  • the separator consists of a PVC tube filled with a stainless steel wire mesh rolled up from a flat sheet. (Sketch 4, Fig. A) On the large surface of this fabric, the small dispersed droplets of light contained in the wastewater settle and combine into large drops, which can then be separated by their buoyancy.
  • 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 inlet and outlet are closed by caps.
  • the series connection of two such separators can reduce light materials below a concentration of significantly ⁇ 5.0 mg / l.
  • the inlet is brought to a medium height.
  • the overflow passes through the upper spigot into a settling chamber as described above.
  • the hot water should be pre-filtered e.g. take place over a gravel pit.
  • the exhaust air produced at different points in the system is laden with dust, volatile organic and inorganic substances.
  • the biofilter has to fulfill several functions: Adsorption of the entrained dust, Adsorption and metabolism of organic, partially odorous substances and inorganic odorous substances, regulation of the water content of the exhaust air.
  • 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.
  • Grates are installed in the container at a distance of 50 cm, thus enabling the multi-stage flow of air through the different floors of the fighter (minima! 4-fold cleaning).
  • 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.
  • a carrier for microbiology e.g. Oat straw, dried heather and / or other structurant material.
  • the microbiology is applied as a dispersion.
  • the exhaust air flows through the filter from a lower corner to the diametrically opposite upper corner.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

Procédé de séchage de déchets solides et / ou liquides, en particulier lors du traitement et de la valorisation de déchets, selon lequel la quantité et l'humidité des déchets à sécher sont déterminées. La quantité de chaleur nécessaire pour sécher les déchets jusqu'à une valeur inférieure à une valeur d'humidité résiduelle prédéfinie est calculée à partir de ces valeurs déterminées de quantité et d'humidité. Une installation de séchage destinée à sécher la quantité desdits déchets est commandée en fonction de la quantité de chaleur calculée.
PCT/EP2006/070243 2006-12-28 2006-12-28 Procédé de séchage de déchets solides et / ou liquides Ceased WO2008083703A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/EP2006/070243 WO2008083703A1 (fr) 2006-12-28 2006-12-28 Procédé de séchage de déchets solides et / ou liquides

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2006/070243 WO2008083703A1 (fr) 2006-12-28 2006-12-28 Procédé de séchage de déchets solides et / ou liquides

Publications (1)

Publication Number Publication Date
WO2008083703A1 true WO2008083703A1 (fr) 2008-07-17

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010029045A2 (fr) 2008-09-09 2010-03-18 Hans Werner Procédé et dispositif de séchage de biomasse
CN104110949A (zh) * 2014-08-12 2014-10-22 汪芳 盖盒式自传金银花晾晒机
CN104792130A (zh) * 2015-04-03 2015-07-22 王惠苗 一种通过螺杆调整的肥料颗粒干燥装置
EP3144617A1 (fr) * 2015-08-18 2017-03-22 Glock Gaston Procédé et dispositif destinés au séchage de copeaux de bois
CN107843080A (zh) * 2017-11-07 2018-03-27 太仓红码软件技术有限公司 一种智能调节干燥方式的物料干燥设备及其工作方法
CN111156804A (zh) * 2020-02-15 2020-05-15 温州市克微科技有限公司 一种垃圾干化预热装置
CN117168109A (zh) * 2023-11-02 2023-12-05 烟台枫林食品股份有限公司 花生红衣提取的原花青素粉烘干装置

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3905123A (en) * 1973-10-15 1975-09-16 Industrial Nucleonics Corp Method and apparatus for controlling a tobacco dryer
DE2747232A1 (de) * 1977-10-21 1979-04-26 Quester Fa Wilh Verfahren und vorrichtung zur durchfuehrung von behandlungsvorgaengen fuer schuettgueter u.dgl.
EP0073498A2 (fr) * 1981-08-28 1983-03-09 Nippon Steel Corporation Procédé de séchage du charbon à cokéfier
US4487577A (en) * 1982-10-27 1984-12-11 Lecorp, Inc. Adaptive control for thermal dryer
EP0632242A1 (fr) * 1993-07-02 1995-01-04 U. Ammann Maschinenfabrik AG Séchage et/ou chauffage de matériau en vrac
DE4435810A1 (de) * 1994-10-07 1996-04-11 Siemens Ag Verfahren zur Prozeßführung einer Trocknungsanlage und zugehörige Anordnung

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3905123A (en) * 1973-10-15 1975-09-16 Industrial Nucleonics Corp Method and apparatus for controlling a tobacco dryer
DE2747232A1 (de) * 1977-10-21 1979-04-26 Quester Fa Wilh Verfahren und vorrichtung zur durchfuehrung von behandlungsvorgaengen fuer schuettgueter u.dgl.
EP0073498A2 (fr) * 1981-08-28 1983-03-09 Nippon Steel Corporation Procédé de séchage du charbon à cokéfier
US4487577A (en) * 1982-10-27 1984-12-11 Lecorp, Inc. Adaptive control for thermal dryer
EP0632242A1 (fr) * 1993-07-02 1995-01-04 U. Ammann Maschinenfabrik AG Séchage et/ou chauffage de matériau en vrac
DE4435810A1 (de) * 1994-10-07 1996-04-11 Siemens Ag Verfahren zur Prozeßführung einer Trocknungsanlage und zugehörige Anordnung

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102008046299A1 (de) 2008-09-09 2010-06-10 Hans Werner Verfahren und Vorrichtung zum Trocknen von Biomasse
DE102008046299B4 (de) * 2008-09-09 2011-01-27 Hans Werner Verfahren und Vorrichtung zum Trocknen von Biomasse
WO2010029045A2 (fr) 2008-09-09 2010-03-18 Hans Werner Procédé et dispositif de séchage de biomasse
CN104110949B (zh) * 2014-08-12 2016-01-27 张春平 盖盒式自转金银花晾晒机
CN104110949A (zh) * 2014-08-12 2014-10-22 汪芳 盖盒式自传金银花晾晒机
CN104792130B (zh) * 2015-04-03 2016-12-21 青岛玉兰祥商务服务有限公司 一种通过螺杆调整的肥料颗粒干燥装置
CN104792130A (zh) * 2015-04-03 2015-07-22 王惠苗 一种通过螺杆调整的肥料颗粒干燥装置
EP3144617A1 (fr) * 2015-08-18 2017-03-22 Glock Gaston Procédé et dispositif destinés au séchage de copeaux de bois
CN107843080A (zh) * 2017-11-07 2018-03-27 太仓红码软件技术有限公司 一种智能调节干燥方式的物料干燥设备及其工作方法
CN107843080B (zh) * 2017-11-07 2019-08-16 福建省三明正元化工有限公司 一种智能调节干燥方式的物料干燥设备及其工作方法
CN111156804A (zh) * 2020-02-15 2020-05-15 温州市克微科技有限公司 一种垃圾干化预热装置
CN111156804B (zh) * 2020-02-15 2020-09-01 南京溧水高新创业投资管理有限公司 一种垃圾干化预热装置
CN117168109A (zh) * 2023-11-02 2023-12-05 烟台枫林食品股份有限公司 花生红衣提取的原花青素粉烘干装置
CN117168109B (zh) * 2023-11-02 2024-01-19 烟台枫林食品股份有限公司 花生红衣提取的原花青素粉烘干装置

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