EP3439788B1 - Verfahren und anlage zur aufbereitung von asche aus müllverbrennungsanlagen - Google Patents

Verfahren und anlage zur aufbereitung von asche aus müllverbrennungsanlagen Download PDF

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Publication number
EP3439788B1
EP3439788B1 EP17715452.3A EP17715452A EP3439788B1 EP 3439788 B1 EP3439788 B1 EP 3439788B1 EP 17715452 A EP17715452 A EP 17715452A EP 3439788 B1 EP3439788 B1 EP 3439788B1
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EP
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Prior art keywords
fraction
ash
grain size
classifying device
installation
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EP17715452.3A
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German (de)
English (en)
French (fr)
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EP3439788A1 (de
Inventor
Manfred Klinkhammer
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Schauenburg Maschinen-Und Anlagen-Bau GmbH
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Schauenburg Maschinen-Und Anlagen-Bau GmbH
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Priority to PL17715452T priority Critical patent/PL3439788T3/pl
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B9/00—General arrangement of separating plant, e.g. flow sheets
    • B03B9/04—General arrangement of separating plant, e.g. flow sheets specially adapted for furnace residues, smeltings, or foundry slags
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J1/00—Removing ash, clinker, or slag from combustion chambers

Definitions

  • the invention relates to a method and a system for processing ash from waste incineration plants.
  • the ash is, in particular, domestic waste incineration ash (HMVA).
  • the aim is to separate the ashes in such a way that several parts (fractions) of the ashes are contaminated with different pollutants. While heavily polluted parts have to be disposed of costly, less heavily contaminated and possibly unpolluted parts can be recycled profitably. Of particular importance in the treatment of ashes is the extraction of ferrous and non-ferrous metals from the ashes, which are particularly profitable.
  • domestic waste incineration ash is processed in a wet classification process.
  • the ash is mixed with liquid.
  • Classification means a separation of a starting material consisting of particles with a given particle size distribution into several fractions of different particle size distribution.
  • the classification is used, for example, to separate the ashes in different proportions of pollutants.
  • a method for processing ash by wet classification in which the ash is first mixed with liquid in a mashing container and, after sieving a coarse fraction, is fed as a feed stream to a classification stage which has an upflow classifier and an upstream hydrocyclone.
  • the feed stream comprises a grain size distribution between 0 and 4 mm.
  • Very fine particles are separated in the hydrocyclone.
  • a residual fraction with a particle size between 0 mm and 0.25 mm is drawn off as a suspension on the top of the fluid bed produced in the upflow classifier.
  • a good fraction with a particle size range between 0.25 mm and 4 mm is drawn off at the bottom of the fluidized bed.
  • the good fraction can be landfilled without environmental requirements or, if necessary, also used economically.
  • the remaining fraction contains pollutants such as heavy metals. It must be disposed of in compliance with legal regulations.
  • a method for processing ash from waste incineration plants in which the classification stage also has an upflow classifier and an upstream hydrocyclone system.
  • the good fraction is drawn off at the bottom of the fluid bed and dewatered by means of a sieve device.
  • the sieve passage of the sieve device is returned to the hydrocyclone plant.
  • the invention is based on the object of treating ashes from waste incineration plants in a stable process in such a way that the added value and in particular the recovery of metal are optimized.
  • the invention is based on the knowledge that a treatment plant can be operated even more economically if the ash-water mixture is not only classified into a good fraction and a bad fraction, as in the prior art, but instead is classified again within the good fraction. So far went It is assumed that it is economically optimal to dispose of the polluted bad fraction and to send the pollutant-free good fraction to the processing plant.
  • the ferrous metals and especially the non-ferrous metals are economically interesting. However, it was found that the non-ferrous metals are not available in every grain size in an economically usable manner.
  • the classification into three stages into a coarse fraction, a medium fraction with a smaller maximum grain size and a fine fraction with a smaller maximum grain size again allows that according to the invention only the coarse fraction is fed to a treatment of metal contained in the coarse fraction.
  • the middle fraction is advantageously largely free of pollutants. The latter are found mainly in the fine fraction.
  • the maximum grain size of the middle fraction is 1.2 mm, preferably approximately 1.0 mm, and the maximum grain size of the fine fraction is 0.4 mm (or 400 ⁇ m), preferably approximately 0 , 25 mm (or 250 pm). While the middle fraction of the processing of metal is supplied in the prior art, this fraction is deliberately not used for metal extraction in the context of the invention. Surprisingly, it was found that the middle fraction contains only a few non-ferrous metals, which are separated using the method according to the invention can. This significantly increases the efficiency compared to known solutions.
  • the ash-water mixture is preferably made available in a grain size between 0 and a maximum of 5 mm.
  • a preferred embodiment of the invention is characterized in that the ash-water mixture is pumped into the classifying device without further treatment or is introduced into the classifying device in the free inlet.
  • a hydrocyclone is connected upstream of the upflow classifier. Contaminated sludge is separated in the cyclone. About 90% of the volume flow is separated with the sludge.
  • the ash-water mixture is pumped into the classifying device without further treatment or is fed into the classifying device in free flow, for example from the underflow of a classifying sieve, and classified there in three stages into three fractions of different grain sizes.
  • a hydrocyclone upstream of the classifying device is not required and preferably also not desired because it is advantageously the entire ash-water mixture introduced into the classifying device.
  • the classifying device is preferably a three-stage upstream classifier.
  • the ash-water mixture is passed to a baffle plate in the classifying device.
  • the coarse fraction is drawn off below the baffle plate. According to the invention, only this coarse fraction is fed to the preparation for the extraction of metal.
  • With upstream water, the middle fraction and the fine fraction are separated in two further classification stages.
  • a certain amount of water is required, which is made available by advantageously pumping the ash-water mixture into the classifying device in a defined amount without further treatment.
  • the ash-water mixture with a grain size between 0 and a maximum of 5 mm can already be delivered to the operator of the plant by a third party. However, only the ashes from the waste incineration plant are preferably made available by the third party.
  • the ash contains a grain size fraction of roughly 0 to 150 mm, possibly with larger components.
  • the ash is mixed with liquid in a mashing container and subsequently classified before the mixture is pumped into the classifying device. The classification before the pumping process can be done in several stages.
  • the coarse fraction is fed to the treatment for metal contained in the coarse fraction.
  • This is particularly non-ferrous metal, which means a special added value.
  • the coarse fraction is preferably first dewatered and then cleaned in a post-cleaning stage before it is fed to the treatment of metal contained in the coarse fraction. It has been found that the dewatering and subsequent post-cleaning further increase the efficiency, since the conventional iron and non-iron separators can probe the ferrous metals and the non-ferrous metals better, and also the salts contained in the mineral can be greatly reduced.
  • the method is preferably operated in a closed liquid circuit.
  • a closed circuit part of the liquid escapes from the system, for example due to liquid adhering to removed fractions or by evaporation. This part of the liquid must be reintroduced into the system.
  • make-up water is added to the circuit in the post-cleaning stage. The addition of the fresh make-up water to compensate for the lost water at this point has the additional advantage that the make-up water is supplied where it can also take on the task of reducing salts in the coarse fraction.
  • the foam formation is also due to the light substances contained in the fine fraction.
  • the light fabrics also contain, for example, unburned organic components. Due to their low specific weight, these light materials are included in the fine fraction, although they have a larger diameter than the fine fraction, which can be 3 to 5 mm.
  • a particularly advantageous embodiment of the invention is characterized in that light substances are removed from the fine fraction after the classifying device. The removal is preferably carried out immediately after the classifying device.
  • the fine fraction advantageously has a maximum particle size of 70 pm, advantageously 50 pm, in particular approximately 30 pm, or smaller. This proportion also enables a certain amount of foam to form. However, it was found that this foam is not stable, but decomposes after a short time without the aid of chemicals. In this respect, the foam formation has no influence on trouble-free continuous operation.
  • the remaining fine fraction is discarded.
  • the remaining fine fraction is on one before disposal
  • Vibration drainers are initially statically dewatered as far as possible and then transported away from them.
  • a sludge-liquid mixture is formed in the form of a filtrate, which is fed to a hydrocyclone stage, from which a fraction (underflow) is returned to static dewatering.
  • the overflow of the hydrocyclone stage is preferably conducted into at least one settling basin.
  • the fine fraction coming from the classifying device is again classified.
  • the resulting fine fraction has only a very low pollution.
  • this fraction contains surprisingly few foam-forming substances.
  • the fine fraction is passed into at least one settling basin with at least one setting chamber, in which the fine fraction can settle.
  • this fine fraction does not produce a stable foam that is disruptive to the process.
  • the liquid remaining in the settling basin met the discharge criteria for public wastewater with regard to heavy metals. This means that this liquid can be operated in its own circuit for a very long time, even with regard to salt criteria such as chlorides, by replenishing the necessary make-up water before the liquid in the basin has to be exchanged.
  • the fine sludge deposited from the fine fraction is advantageously pumped out with a thick matter pump.
  • an insert with guide walls is arranged in the settling basin, which tapers in the direction of the pump.
  • the guide walls can be perforated. They ensure that the fine sludge is fed to the pump so that it can remove the fine sludge as completely as possible.
  • the fine sludge is preferably drawn off via a time control. It has already been stated above that the quality of the liquid in the settling tank is surprisingly good. This is also attributed to the fact that the fine fraction originating from the classifying device is classified again and only the resulting fine fraction is passed into the settling tank. As stated above, the high water quality has a positive influence on the liquid circuit of the process.
  • the sedimentation tank also allows inexpensive disposal, since contaminated solids can be disposed of separately from the high proportion of solid-free water with a very small amount of water.
  • the classifying device is preferably designed and set up such that the maximum grain size of the middle fraction is 1.0 mm and the maximum grain size of the fine fraction is 0.25 mm.
  • a preferred embodiment of the invention is characterized in that the system comprises a pump for pumping the water-ash mixture or a free inlet for introducing the ash-water mixture into the classifying device, e.g. from the underflow of a classifying sieve and that the pump or the free inlet is in flow connection with the classifying device in such a way that the ash-water mixture is pumped or introduced into the classifying device without further treatment.
  • the ash is fed into a mashing container 2 via a conveyor belt 1 with a grain size distribution of 0 to 150 mm or smaller (preferably a maximum of 60 mm).
  • the ashes are mixed with liquid in the mashing container 2 and fed to a classification station 3 as an ash-water mixture.
  • the ash-water mixture is pre-classified into a fraction of approx. 5 to a maximum of 150 mm, which is sent for dry processing, and a fraction of approx. 0 mm to a maximum of 5 mm.
  • the grain size distribution is preferably between 0 and approximately 2 mm. This fraction is pumped as an ash-water mixture into a classifying device 5 by means of a pump 4, without the ash-water mixture being subjected to further treatment.
  • the entire volume flow of the ash-water mixture is preferably pumped into the classification device 5.
  • the ash-water mixture is preferably introduced into the classifying device 5 in a free inlet (without a pump). Then the volume flow required for the classifying device 5 is made available exclusively by the gravity of the ash-water mixture.
  • the classifying device 5 is a three-stage classifying device.
  • the classifying device 5 has a filler neck 6 which interacts with a baffle plate 7.
  • Figure 1 the classifying device is shown only roughly schematically and in Figure 2 explained in more detail.
  • a direct application of the ash-water mixture without further Treatment is particularly advantageous because both the speed and the amount of the volume flow can be used to classify the ash-water mixture into three fractions.
  • the ash-water mixture is classified in three stages into a coarse fraction 8, a medium fraction 9 with a smaller maximum grain size and a fine fraction 10 with a smaller maximum grain size.
  • the maximum grain size of the respective smaller fraction is therefore smaller than the minimum grain size of the larger fraction in each case, whereby it has previously been pointed out that, for technological reasons, there may be (minor) overlaps in the grain size ranges.
  • the grain size of the middle fraction 9 is at most 1.2 mm, preferably at most 1.0 mm.
  • the maximum grain size of the fine fraction 10 is 0.4 mm, preferably approximately 0.25 mm.
  • a preferred exemplary embodiment is characterized in that the fine fraction 10 has a particle size distribution of 0 to 0.25 mm, the middle fraction 9 has a particle size distribution of 0.25 to 1 mm and the coarse fraction has a particle size distribution of 1 to 2 mm.
  • the coarse fraction 8 is fed to a treatment of metal contained in the coarse fraction.
  • the coarse fraction is optionally dewatered in a dewater 11.
  • the dewatered coarse fraction is then cleaned in a post-cleaning stage 12.
  • make-up water is added to the liquid circuit of the overall system added as indicated by arrow 13.
  • the fresh make-up water 13 cleans the coarse fraction on the one hand and thereby increases the efficiency of the subsequent treatment for the extraction of metal.
  • the make-up water compensates for liquid that has escaped from the liquid circuit.
  • the metal is extracted in an iron separator 14 using, for example, an overband magnet and a nonferrous separator 15.
  • the nonferrous metal is collected in a container 16.
  • the rest of the coarse fraction is dumped (dump 17).
  • a coarse fraction 8, a middle fraction 9 and a fine fraction 10 are classified in the classification device 5 in three stages.
  • the middle fraction preferably has a maximum grain size of 1.2, in particular 1.0. Contrary to the state of the art, it is not used for metal extraction. Rather, it was recognized that the middle fraction 9 has no non-ferrous metals or only a very small proportion of non-ferrous metals. This proportion was regularly used in the prior art in metal extraction. According to the invention, however, only the coarse fraction 8 is fed to the metal preparation. This enables the system to be operated with a high degree of economy.
  • the middle fraction 9 is dewatered in a dewater 18 and placed on a heap 19. Since the material is largely free of pollutants, it can be used for building materials at a later date.
  • a recirculation 20 is preferably provided, via which liquid from the overflow of the hydrocyclone 21 to Level control of the pump sump below the swing dewater 18 is used.
  • the hydrocyclone ensures water pre-separation. At the same time, it serves to thicken the material in the lower reaches.
  • the fine fraction 10 has a maximum grain size of approximately 0.4 mm, in particular approximately 0.25 mm. This is sludge contaminated with pollutants.
  • the fine fraction it is technologically possible that even light materials with a diameter that is sometimes significantly larger but with a lower specific weight are discharged with the fine fraction.
  • the light materials are, for example, polystyrene or unburned organic material. These light materials are also responsible for unwanted foaming.
  • the classifying device 5 is preferably followed by a curved screen 22 with which the light materials can be separated.
  • the curved screen 22 is excellently suitable for separating the light materials, since it does not clog up even in continuous operation.
  • the light materials are collected in a container 23.
  • the fine fraction 10 is taken up in a pump sump 24 after removal of the light materials and pumped by means of a pump 25 to a hydrocyclone system 26, which in the present case is designed as a multi-cyclone system.
  • the fine fraction is classified into a remaining fine fraction 27 and very fine fraction 28.
  • the fine fraction preferably has a maximum grain size of 70 pm, advantageously 50 pm, in particular approximately 30 ⁇ m.
  • the remaining fine fraction 27 is dewatered in a dewaterer 29.
  • the drainage device 29 is preferably an oscillating drainage device. This works preferably at intervals.
  • a sludge-liquid mixture is created which is fed to a hydrocyclone stage 31 by means of a pump 30. This is set such that a fraction 32 of at least 20 pm, preferably at least 30 pm, is returned to the dewaterer 29.
  • the fine fraction 28 is passed into a settling basin 33, which has a plurality of settling chambers 34.
  • a settling basin 33 In the settling basin 33 there is also an insert 35 with guide walls which taper in the direction of a pump 36. Fine sludge settles in the settling basin.
  • the insert 35 with its tapered guide walls ensures that the fine sludge is advantageously fed to the pump 36.
  • the pump 36 is a thick matter pump which pumps the fine sludge to the dewater 29.
  • a liquid 37 remains which is removed from the settling basin and possibly pumped to a process water distributor 39 with the interposition of a clarifying tank 28.
  • the quality of the liquid 37 is so good that, on the one hand, it can be returned as process water to the liquid circuit of the overall system, and on the other hand, it can be disposed of cheaply without further treatment.
  • FIG. 2 shows the classifying device 5 schematically in an enlarged view. It is an upstream classifier.
  • the ash-water mixture is in the Filler neck 6 filled. Then it arrives on the baffle plate 7.
  • This technology requires a certain minimum flow rate of the ash-water mixture, which can be made available in a particularly advantageous manner by a task without further treatment.
  • Upflow water is poured into the classifying device through openings 40, which is directed against the filling direction of the ash-water mixture.
  • the classifying device is designed and set up in such a way that the coarse fraction 8 lowers against the flow direction of the upstream water and is withdrawn from the classifying device.
  • the remaining ash-water mixture passes into a second (rotating) stage 41 of the classifying device 5.
  • upstream water is filled in through openings 40, which is directed against the lowering movement of the middle fraction.
  • the middle fraction 9 is withdrawn from the second stage 41, as indicated by the arrow 9.
  • the fine fraction 10 is removed in a third stage 42. These are the finest particles with a maximum grain size of 0.4 mm and light materials.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
  • Processing Of Solid Wastes (AREA)
EP17715452.3A 2016-04-03 2017-04-03 Verfahren und anlage zur aufbereitung von asche aus müllverbrennungsanlagen Active EP3439788B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL17715452T PL3439788T3 (pl) 2016-04-03 2017-04-03 Sposób i instalacja do obróbki popiołów z instalacji do spalania odpadów

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016106054.2A DE102016106054A1 (de) 2016-04-03 2016-04-03 Verfahren und Anlage zur Aufbereitung von Asche aus Müllverbrennungsanlagen
PCT/EP2017/057846 WO2017174502A1 (de) 2016-04-03 2017-04-03 Verfahren und anlage zur aufbereitung von asche aus müllverbrennungsanlagen

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EP3439788A1 EP3439788A1 (de) 2019-02-13
EP3439788B1 true EP3439788B1 (de) 2020-01-01

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EP (1) EP3439788B1 (pl)
CN (1) CN108883419B (pl)
DE (1) DE102016106054A1 (pl)
PL (1) PL3439788T3 (pl)
RU (1) RU2721198C2 (pl)
WO (1) WO2017174502A1 (pl)

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DE10220813B4 (de) * 2002-03-14 2004-02-26 Schauenburg Maschinen- Und Anlagen-Bau Gmbh Verfahren zur Verwertung von Aschen mit hohem Kohlegehalt aus Kohlestaubfeuerungsanlagen
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UA100021C2 (uk) * 2009-12-29 2012-11-12 Государственное Предприятие "Украинский Научно-Технический Центр Металлургической Промышленности "Энергосталь" Виробничий комплекс для утилізації твердих побутових відходів
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Also Published As

Publication number Publication date
PL3439788T3 (pl) 2020-07-27
RU2018134763A (ru) 2020-04-07
RU2018134763A3 (pl) 2020-04-10
CN108883419B (zh) 2021-01-05
DE102016106054A1 (de) 2017-10-05
WO2017174502A1 (de) 2017-10-12
CN108883419A (zh) 2018-11-23
RU2721198C2 (ru) 2020-05-18
EP3439788A1 (de) 2019-02-13

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