WO2003020450A1 - Verfahren zum aufbereiten von abfallstoffen und aufbereitungsanlage - Google Patents
Verfahren zum aufbereiten von abfallstoffen und aufbereitungsanlage Download PDFInfo
- Publication number
- WO2003020450A1 WO2003020450A1 PCT/EP2002/009855 EP0209855W WO03020450A1 WO 2003020450 A1 WO2003020450 A1 WO 2003020450A1 EP 0209855 W EP0209855 W EP 0209855W WO 03020450 A1 WO03020450 A1 WO 03020450A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- boiling
- reactor
- water
- waste
- plant according
- Prior art date
Links
- 239000002699 waste material Substances 0.000 title claims abstract description 99
- 238000000034 method Methods 0.000 title claims abstract description 83
- 238000012545 processing Methods 0.000 title claims abstract description 34
- 238000009835 boiling Methods 0.000 claims abstract description 116
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 68
- 239000012528 membrane Substances 0.000 claims abstract description 6
- 239000000463 material Substances 0.000 claims description 51
- 238000000605 extraction Methods 0.000 claims description 38
- 238000001035 drying Methods 0.000 claims description 37
- 238000010438 heat treatment Methods 0.000 claims description 27
- 238000011282 treatment Methods 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 22
- 238000003756 stirring Methods 0.000 claims description 16
- 238000000855 fermentation Methods 0.000 claims description 13
- 230000004151 fermentation Effects 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 238000004065 wastewater treatment Methods 0.000 claims description 8
- 238000005406 washing Methods 0.000 claims description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- 239000000470 constituent Substances 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 238000006073 displacement reaction Methods 0.000 claims description 3
- 230000002441 reversible effect Effects 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims 2
- 230000006378 damage Effects 0.000 claims 1
- 230000002093 peripheral effect Effects 0.000 claims 1
- 239000010813 municipal solid waste Substances 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 22
- 210000004027 cell Anatomy 0.000 description 17
- 239000000203 mixture Substances 0.000 description 17
- 239000000725 suspension Substances 0.000 description 16
- 238000004519 manufacturing process Methods 0.000 description 10
- 239000000126 substance Substances 0.000 description 10
- 238000004064 recycling Methods 0.000 description 9
- 230000007062 hydrolysis Effects 0.000 description 8
- 238000006460 hydrolysis reaction Methods 0.000 description 8
- 239000004615 ingredient Substances 0.000 description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- 150000001875 compounds Chemical class 0.000 description 7
- 238000002485 combustion reaction Methods 0.000 description 6
- 239000000446 fuel Substances 0.000 description 6
- 230000020169 heat generation Effects 0.000 description 6
- 239000005416 organic matter Substances 0.000 description 6
- 238000012546 transfer Methods 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000029087 digestion Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 229920005610 lignin Polymers 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 239000010822 slaughterhouse waste Substances 0.000 description 4
- 239000010802 sludge Substances 0.000 description 4
- 230000006641 stabilisation Effects 0.000 description 4
- 238000011105 stabilization Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 229920002678 cellulose Polymers 0.000 description 3
- 239000001913 cellulose Substances 0.000 description 3
- 239000010815 organic waste Substances 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000005325 percolation Methods 0.000 description 3
- 239000004033 plastic Substances 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 239000000654 additive Substances 0.000 description 2
- 238000004887 air purification Methods 0.000 description 2
- 230000000035 biogenic effect Effects 0.000 description 2
- 210000000170 cell membrane Anatomy 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000009264 composting Methods 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 230000020477 pH reduction Effects 0.000 description 2
- 235000011837 pasties Nutrition 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- 238000004056 waste incineration Methods 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 102000029797 Prion Human genes 0.000 description 1
- 108091000054 Prion Proteins 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000008953 bacterial degradation Effects 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000000872 buffer Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 230000002925 chemical effect Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000007791 dehumidification Methods 0.000 description 1
- 238000004332 deodorization Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000011982 device technology Methods 0.000 description 1
- 201000010099 disease Diseases 0.000 description 1
- 208000037265 diseases, disorders, signs and symptoms Diseases 0.000 description 1
- 239000005446 dissolved organic matter Substances 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000011081 inoculation Methods 0.000 description 1
- 239000010806 kitchen waste Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000005360 mashing Methods 0.000 description 1
- 235000012054 meals Nutrition 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000010327 methods by industry Methods 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- 150000002830 nitrogen compounds Chemical class 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000002985 plastic film Substances 0.000 description 1
- 229920006255 plastic film Polymers 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011012 sanitization Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000003307 slaughter Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000007669 thermal treatment Methods 0.000 description 1
- 238000001291 vacuum drying Methods 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- 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
- B03B9/06—General arrangement of separating plant, e.g. flow sheets specially adapted for refuse
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L5/00—Solid fuels
- C10L5/40—Solid fuels essentially based on materials of non-mineral origin
- C10L5/46—Solid fuels essentially based on materials of non-mineral origin on sewage, house, or town refuse
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
- F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2900/00—Special features of, or arrangements for incinerators
- F23G2900/50208—Biologic treatment before burning, e.g. biogas generation
-
- 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
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
-
- 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
-
- 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
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Definitions
- the invention relates to a method for processing waste materials according to the preamble of patent claim 1 and a residual waste treatment system according to the preamble of the independent patent claim 13.
- Waste Act applies in principle to every waste owner as well as to bodies subject to disposal, such as cities and cleaning companies.
- the Waste Act and the Federal Emission Protection Ordinance (BIMSCHV) stipulate that the waste is to be collected, transported, temporarily stored and treated in such a way that the possibilities of waste recycling are not impeded.
- municipalities have a material or an energy recovery available.
- Material recycling is the processing of waste into a secondary raw material, which is then used for energy purposes.
- the latter alternative is currently the most frequently used type of waste recycling.
- the problem with this thermal recycling is that the limit values specified by the legislator, particularly in the flue gas, must be observed, so that considerable plant-technical expenses are incurred must be undertaken to meet the legal requirements.
- conventional waste incineration plants are under public discussion, so that efforts are being made in the municipalities to recycle the waste.
- DE 196 48 731 AI describes a waste treatment process in which organic constituents of a waste fraction are washed out in a percolator and the biologically stabilized residue is burned after drying. This combustion takes place in a conventional waste incineration plant, so that the same problems exist with regard to the exhaust gases as with the thermal recycling described at the beginning.
- DE 199 09 328 AI discloses a method for processing residual waste in which it is fed to aerobic hydrolysis.
- the fraction to be biologically stabilized is charged with air and a washout liquid (water) in a reactor. Due to the action of atmospheric oxygen and the humidity that is set at the same time, the mixture of substances is heated aerobically, thermophilically, so that the bio-cells are broken open and the released ones organic substances are transported away by the washing liquid.
- the mixture of substances is conveyed through the reactor transversely to the air and to the washout liquid by means of a conveyor / agitator.
- This aerobic hydrolysis showed excellent results in the first test plants, whereby with a comparatively low expenditure on equipment, a substitute fuel can be produced which is not elutable, is not breathable and is characterized by a high calorific value.
- This substitute fuel can, for example, be supplied to gasification, the resulting gas then being used energetically or materially in power plants and cement plants or in the production of methanol or as a reducing agent in steel plants.
- the invention has for its object a method for processing waste and a
- waste is thermally stabilized in a reactor which is operated under vacuum, for example in the boiling range of water. Operation in a vacuum produces practically no exhaust gases, and the residues can be handled and stored hygienically and hygienically as a product.
- the decomposition of the organic cells by the biological digestion can be significantly accelerated compared to the conventional percolation processes described at the outset, so that only a fraction of the previously usual material throughput times is required. This makes it possible to make the reactor much more compact, with the reactor volume according to the first preliminary tests being only about 5% of a previous percolator with the same throughput.
- the membranes of the water-bearing cell structures are explosively destroyed by the thermal loading of the organic components of the residual waste in the boiling range of water, and the organically highly contaminated cell water released in this way can be removed from the reactor. Due to the heating and vacuum in the reactor, the ingredients are hygienized and can be handled in a medically safe manner.
- the reactor is operated as a boiling extractor, with the residual waste heated to the boiling temperature being subjected to a washout liquid, so that the organically laden constituents of the residual waste are washed out.
- a boiling extractor also expels nitrogen present in residual waste as ammonia. The expulsion of ammonia reduces the nitrogen pollution of the residual waste in such a way that no subsequent denitrification has to be carried out in subsequent process steps, for example the treatment of organically contaminated washing liquid in a biogas plant.
- the proportion of organic matter in the residual waste can be further reduced if boiling extraction is followed by boiling drying, in which the thermally stabilized residual waste present after the boiling extraction is fed to a reactor according to the invention, but then no washout liquid is fed in, but only thermal stabilization by heating of the pre-stabilized residual waste to the boiling range under vacuum.
- the effectiveness of the process is further increased if the boiling drying and / or the boiling extraction is preceded by preheating, so that less heating energy has to be supplied to the reactor to heat the residual waste to the boiling temperature.
- thermo stabilization With a suitable composition of the residual waste, it can also be sufficient to carry out the thermal stabilization solely by boiling extraction or by boiling drying, a preheating stage preferably being carried out in each case.
- This preheating is preferably carried out by an aerobic rotting process.
- aerobic heating results in a biologically produced hydrolysis which biochemically accelerates cell disruption and thereby increases the washout rate in the case of a subsequent extraction or the water removal in the case of subsequent drying.
- the vapors obtained after the boiling extractor or the boiling dryer are cooled and thus condensed by means of a condenser or an equivalent device, so that the process can be carried out essentially without exhaust air, apart from slight leakage air.
- the leakage air that may be generated can be burned in a burner with minimal process engineering effort or be further processed, for example in an exhaust air purification system.
- the organic contaminated washout liquid obtained after the boiling extraction can be fed to a biogas plant.
- Fermentation water removed in the biogas plant is preferably returned to the boiling reactor as recycle or process water.
- the biogas generated can be used to generate process heat in the reactor or to generate electrical energy, so that the system can be operated essentially self-sufficiently.
- the warm dry material present after the boiling drying is fed to an air-free cooling drying, so that the so that the warm dehumidification is dehumidified again.
- the basic module of the residual waste treatment system consists in principle of a heatable, vacuum-operated reactor which is designed with residual waste or material entry and a material discharge as well as a stirring device for conveying the residual waste and for introducing shear forces.
- This reactor can be operated as a boiling extractor and - without a washing out liquid - as a boiling dryer when washing out liquid is supplied.
- the stirring device of the reactor is preferably designed in such a way that its stirring elements scrapes off the material adhering to the inner circumferential walls of the reactor during one revolution, so that caking on the wall surfaces is avoided. Due to the effect of the stirring device, the material is moved along the heated inner circumferential surface wall and transported from the material entry to the material discharge - and possibly in the opposite direction.
- the stirring device is preferably designed in the form of a screw, and the screw can be designed with or without a central shaft.
- the drive of the stirring device is preferably carried out with a reversible direction of action, so that the conveying direction is reversible.
- the stirring device is particularly good if the stirrer is heatable.
- the residual waste and the wash-out liquid are fed in through a common material input.
- the reactor can be made very compact if it is provided with two sections, in each of which a stirrer is arranged. These two sections can be connected to one another via a suitable material feed or a material feed back, so that the material can be conveyed in the circuit.
- the thermally stabilized waste fraction is fed to a press, the organic constituents contained in the press water being converted in a biogas plant.
- a burner, a gas turbine or a gas engine, for example, can be used as the energy generator for heating the reactor, which works with the aforementioned material flows, for example the biogas occurring in the biogas plant, the organically polluted exhaust air occurring in the boiling reactor or the exhaust air resulting from the dewatering of the waste is fed for residue-free combustion.
- Figure 1 is a process diagram of a basic module for processing residual waste with a boiling extraction
- FIG. 2 shows a basic module of the method according to the invention for processing residual waste with boiling drying
- FIGS. 1 and 2 shows a reactor for use in a method according to FIGS. 1 and 2;
- Figure 4 shows an embodiment of the reactor of Figure 1
- Figures 5, 6, 7 schematic diagrams for interconnecting reactor sections for a boiling extraction / boiling drying and
- Figure 8 is a basic diagram of a method for processing residual waste with a boiling extraction and subsequent boiling drying.
- Figure 1 shows a basic diagram of a minimum equipment for carrying out a boiling extraction process for the treatment of organically contaminated waste materials such as.
- the organically contaminated substances 1 are fed to a reactor 2 and diluted with fresh water or circulating liquid 6.
- the suspension 74 of waste and liquid is mixed and transported with a stirring device 8.
- the heat is supplied to achieve the boiling temperature via a jacket heater 4.
- tensioned steam 38 can also be carried directly into the suspension 74 and / or by an upstream heating stage, which is not shown here.
- this residual waste consists of short-chain compounds, which are mostly absorbed on the surface. If the hot process water flows around this surface, then primarily insoluble compounds are hydrolyzed and washed out. The odor-intensive components of organic waste and the hydrolysis products are relatively readily water-soluble and can be washed out with the wash-out liquid. Such an extraction achieves a reduction in the organic matter and a deodorization of the residual waste.
- the process heat treatment takes place via a heat generation system 26 with which the heat energy 28 is generated in the form of hot water, pressurized hot water, thermal oil or steam 38.
- self-generated biogas can be used in the process, and / or other fossil fuels or electrical energy can also be used.
- the negative pressure keeps the boiling point well below 100 ° C and the jacket temperature 4 is adjusted to a temperature level depending on the suspension 74, so that no caking occurs on the heating surfaces so that the heat transfer into the suspension 74 takes place without losses can.
- ingredients such as. B. plastic parts and plastic films already at heating jacket or surface temperature 4 to 80 ° C begin to plasticize and to cover the heat transfer surfaces and the stirring device 8 with a viscous layer.
- the negative pressure is produced by a vacuum generator 4 (shown here as a vacuum pump) which lowers the boiling point in the boiling extractor 2 to ⁇ 60 ° C. by means of the negative pressure generated, preferably ⁇ 80 mbar.
- the ingredients leaving via vapors 48 are cooled in a vapor condenser 66 by cooling 16 below the dew point and the exhaust gases 54 are separated from the condensate 68.
- the vacuum generator 40 can, as required nis, be arranged before or after the vapor condenser 66.
- the exhaust gases 54 occurring at the vapor condenser contain leakage air and inert gas mixtures from the heated suspension 74 and residual gas quantities from circulating water 6 of a biogas plant described in more detail below.
- the resulting exhaust gas quantities are less than 1.0 m ⁇ and are therefore extremely low, so that one can practically speak of an exhaust-air-free process.
- the heating-up time in the boiling reactor 2 differs and can also be significantly shortened by preheating the additives 1 and the process water 6 outside the boiling reactor 2.
- the suspension 74 is discharged and the thermally stabilized substrate / water mixture 10 is fed to a dewatering device 14 (shown here as a classifying press).
- a dewatering device 14 shown here as a classifying press
- the solid Substance / press cake 22 separated from the process water 18 enriched with organic matter.
- the press cake 22 can then be fed to further process steps, such as. B. composting, biological drying or an echo-thermal drying as shown as an example in Figure 2.
- the actual extraction process depends on the input material and takes on average between a few minutes and over an hour.
- the suspension 74 is hygienized by the effect of temperature over an hour and, after dewatering 14 and drying 42 (FIG. 2), can be handled, stored and subjected to further work steps without any human medical problems.
- the process water 8 is advantageously removed in a biogas plant 20 (FIG. 8) in which the organic component is converted to biogas 24 by means of methane bacteria, which is then fed to the heat generation plant 26 for energy generation and the excess gas for further utilization 103 (FIG. 8) for heat and electricity generation becomes.
- the freed fermentation water 32 leaves the biogas plant 20 and is fed back to the boiling extractor 2 as process water / circulation water 6.
- the vapor condensates 68 contained a large part of the nitrogen compounds which can inhibit the biological anaerobic degradation process in the fermenter 20. Therefore, the vapor condensates 68 are treated together with the excess water 34 directly in a wastewater treatment 36 (FIG. 8) and then passed into the sewage system as cleaned wastewater 105 or partially supplied to the boiling extraction process 2 as process water / process water 6. By reducing the embroidery Substance in front of the biogas plant 20, the fermentation process no longer requires a nitrogen sink.
- a method is thus presented in which in a reactor 2 organically contaminated substances 1 are mixed and transported with water 6 by agitators 8 and the action of heat 4 in the range of the boiling point of water with vacuum application disintegrates the suspension 74 in such a way that cell membranes are produced within a few minutes destroyed, lignin and cellulose compounds broken up and made available to an anaerobic fermentation process in a biogas plant 20, so that the starting material 10 is thermally hygienized and, after a dewatering step 14 and subsequent drying 42 (FIG. 2), handled, processed and stored human-medically as a harmless mixture of substances can be.
- the treatment time in the reactor is 2 max. 2 h with a circulation water quantity of 10001 / kg residual waste, and the conversion to biogas in fermenter 20 is max. 5 days.
- the gas production is approx. 150 Nm 3 / lMg residual waste.
- the methane content is 70%.
- the amount of exhaust air is approx. 1.0 m 3 / lMg residual waste.
- the energy expenditure is approx. 5% of the energy yield with drying 15%.
- the treatment time in the reactor is at least 2 days with a circulation water volume of 30001 / lMg residual waste and the conversion to biogas in the fermenter is a maximum of 5 days. Pulp connections are not broken down.
- the gas production is approx. 70Nm 3 / lMg residual waste.
- the methane content is 70%.
- the amount of exhaust air per 1 mg of residual waste is approx. 1000m 3 .
- the treatment time in the gas reactor is at least 20 days with a circulation amount of inoculation sludge of 20% of the total content. 25 3 drum / room volumes are required for each IMg of residual waste. Pulp and lignin compounds are partially broken down after a journey time of 18 to 30 days.
- the gas production is approx. 100 Nm / lMg residual waste.
- the methane content is 55-60%.
- the amount of exhaust air per IMg. Residual waste is approximately 8000 m. Energy expenditure approx. 30% of the energy yield.
- FIG. 2 shows a minimum of equipment for carrying out a vacuum boiling drying process for drying, stabilizing and sanitizing substances such as:
- the moist material 1, 22, 60 is introduced into a boiling dryer 42 and moved, mixed and transported with a stirring device 8.
- the heat supply to achieve the boiling temperature takes place via the jacket heater 4.
- the process heat treatment takes place again via the heat generation system 26 with which the heat energy 28 is generated in the form of hot water, pressurized hot water, thermal oil or steam.
- the self-generated biogas from the boiling extraction process can be used as the energy carrier 24, and / or other fossil fuels or electrical energy can also be used.
- the boiling point is kept clearly below 100 ° C. by means of negative pressure and the jacket temperature 4, depending on the moist material 1, 22, 60, is set to a temperature level such that no caking occurs on the heating surfaces, so that the heat transfer can take place without losses is entered into the moist material 1, 22, 60.
- the operation of the boiling dryer 42 corresponds essentially to the operation of the boiling boiler shown in FIG. tractor 2 with the exception that no process water 6 is supplied.
- the boiling dryer 42 reference is made to the corresponding explanations for the boiling extractor 2.
- the heating-up time in the boiling dryer 42 differs and can also be significantly shortened by preheating the moist material 1, 22, 60 outside the boiling dryer 42 (device not shown). After heating to the operating temperature, the actual drying process takes between 1.5 and 3 hours, depending on the humidity of the moist material 1, 22, 60.
- the dry product 50 Due to the effect of temperature at more than 90 ° C. for a holding time of one hour, the dry product 50 is then hygienized and can be handled, stored and subjected to further work steps without any medical considerations.
- the dry product 50 leaves the boiling dryer 42 with an outlet temperature of approximately 60 to 80 ° C.
- the warm dry material 50 can be temporarily stored or further treated by means of the symbolically represented mass flow deflection 62. However, if a lower material temperature is desired for the subsequent further treatment, the warm dry material 50 is fed to a cooling dryer 52.
- the cooling dryer 52 consists of a sealed housing with an internal perforated conveyor belt 56 with which the dry material 50 (cake) is conveyed from the inlet to the outlet.
- the exhaust air 78 loaded with heat and residual moisture from the dry material 50 is cooled and dehumidified in a cooler / condenser 66.
- the condensate 68 is the
- Waste water treatment ( Figure 8) fed.
- the cooled and dehumidified drying air 80 is passed through the perforated conveyor belt 56 and the material cake 50.
- the cooled dry material 72 leaves the cooling dryer 52 via a lock and discharge device, not shown.
- the air circuit 78, 80 is closed, there are practically no exhaust air quantities or exhaust gases.
- FIG. 3 shows a basic module 90 of a reactor which can be used as a boiling extractor 2 or as a boiling dryer 42.
- this basic module 90 both functions can be like
- Boiling extraction 2 and boiling drying 42 are carried out.
- the core piece is the soulless funding and
- Circulation spiral 82 which also takes over the stirrer function 8. With this circulation spiral 82, the content
- the heating surface 4 is kept free of caking, and thus the heat transfer from the heating medium 28 into the moist material to be heated or into the suspension 74 is ensured.
- the circulation spiral 82 is moved by at least one drive 96 and a special sealing bush 98 prevents leakage air from entering.
- the aggregate materials 1, 6, 22, 60 are fed in via the inlet slide or the lock 84, and the product 10, 50 is discharged via the outlet slide or the lock 88 after the throughput time has ended.
- the vacuum set by means of the pumps 40, 44 sets the boiling point in the boiling extractor 2 or boiling dryer 42 to clearly ⁇ 100 ° C. and the vapors 46, 48 leave the reactor 2, 42 via a steam dome / vapor outlet 94 (90).
- steam 38 can be blown in in addition to the jacket heater 92, 4.
- FIG. 4 shows an embodiment with an agitator 106 with a central axis and overlapping agitator blades 107 which keep the heating surfaces 92 of the reactor free of caking with the aid of the abrasive moist material 76 or the suspension 74 during the rotation due to the propeller-like arrangement.
- the agitator 106 can also be heated by a heating medium 28 with agitator blades 107 similar to the already known autoclaves for producing animal meal from slaughterhouse waste or in disk dryers for drying sludge (not shown here in the drawing).
- a device for carrying out two processes is presented above, such as: the boiling extraction according to FIG. 1, the boiling drying according to FIG. 2.
- Steps are carried out in two separate process containers 2, 42, since the processes boiling extraction 2 and
- Boiling drying 42 different retention and treatment have dewatering times and an intermediate dewatering step 14 reduces the evaporation energy expenditure energetically and temporally.
- FIGS. 5 to 6 show arrangement examples for boiling extraction 2 and boiling drying 42.
- FIG. 5 shows a reactor 90 which is filled 84 and discharged 88 discontinuously.
- the ingredient 74, 76 to be treated is moved back and forth by the drive 96 with the agitator 106 (arrow 100) until the process is complete.
- This arrangement and mode of operation is particularly suitable for small and individual systems in which, for. B. two to three passes can be made in one day shift.
- FIG. 6 shows an arrangement of a plurality of reactor stages or reactor sections connected in series, in which the individual batches are continuously loaded 84, treated and unloaded 88. So that the vacuum is maintained during the displacement processes 102, the stages are separated from one another by slides or locks.
- the individual reactor sections can be connected in series in any number 90.1 - 90.m.
- FIG. 7 shows an arrangement in which the ingredient 74, 76 to be treated circulates in a closed circuit.
- two reactor sections 90.1, 90.2 arranged approximately parallel are connected to one another via displacement components 104.
- the two reactor sections 90.1, 90.2 each have an agitator 106 with a drive 96, the conveying direction in the two sections 90.1, 90.2 being carried out in the opposite direction (arrow 102).
- the sliding components 104 are provided, by means of which the respectively adjacent end sections of the sections 90.1, 90.2 are connected to one another, so that the circuit shown is obtained.
- the material to be processed is fed in via the material inlet 84 and removed from the reactor via the material outlet 88.
- this is a discontinuous operation, but in which the uniform rotation (with the filling level useful for the process) causes the ingredients to be conveyed through the devices (90.1, 90.2, 104).
- the arrangement shown in Figure 7 is suitable for the throughput of large quantities, which, for. B. can be run in several shifts and can be practically operated in continuous operation when using at least three devices with the appropriate volume buffers.
- FIG. 8 shows a combination of the boiling extraction process according to FIG. 1 and the downstream boiling drying process according to FIG. 2 in connection with a biogas plant 20, a wastewater treatment plant 36 and an exhaust air treatment plant 30.
- Residual waste or other organically contaminated waste materials 1 can either be supplied to the boiling extraction 2 or directly to the boiling dryer 42 for drying.
- Pasty or liquid sludges 60 can be ner 42 are fed directly or as a mixture 62 with the press cake 22 and residual waste 1 as additives or as a single component.
- the vapors 48, 46 obtained at the boiling dryer and at the boiling extractor 2 are fed via the vacuum generators 40 to a cooler / condenser 66, in which the vapors 48, 66 are condensed out and separated from the exhaust gas 54.
- the condensate 68 is fed to a wastewater treatment plant 36.
- the resulting exhaust gases are mixed into an exhaust air purification system 30 or for post-combustion of the burner supply air for the heat generation system 26.
- the organically highly contaminated press water 18 from the extraction 2 is fed to the biogas plant 20 for removal and biogas generation 24.
- the biogas 24 can then use other energy, such as a thermal power plant for electricity generation are supplied.
- the de-fermented fermentation water 32 from the biogas plant 20 is fed back into the extraction 2 as process water / circulation liquid as a wash-out liquid 6.
- the excess water 34 from the biogas plant (fermentation) 20 is treated in the wastewater treatment 36 together with the broth condensate 68 and conducted as cleaned wastewater 105 into the sewage system or a receiving water.
- the input streams 1, 60, 22, which are contaminated with organic matter before being introduced into the reactors (extractor, dryer) 90 in an intensive rotting box (feed container) 108 by gassing with air 110 or with technical oxygen 111 to be preset to the desired operating temperature for a short time by means of biologically produced aerobic heating.
- Biologically produced hydrolysis occurs simultaneously with the aerobic heating (Acidification), in which biochemical digestion and increasing the biochemical availability in the subsequent treatment steps in the reactors 90 significantly increase the washout rate in extraction 2 and the water removal in drying 42.
- exhaust air flow 54 to be treated can be kept as small as possible, gassing with technically enriched oxygen 111 is particularly suitable.
- the exhaust air 54 is drawn off from the feed containers (rotting boxes) 108 and the above-described exhaust air treatments 30, 26 for removal or combustion fed.
- the water-carrying cells of the membranes are torn open by the action of vacuum 46, 48 and heating 4, 26, 28, so that the cell water, as in the vacuum boiling extraction process (FIG. 1) in the boiling extractor 2, is available within a few minutes for washing out the organic components 18 and is converted into biogas 24 in a biogas plant 20.
- the cell disruption begins from the second day of treatment and, depending on the material composition, has reached the highest possible disruption rate between the third and fifth day.
- the highly polluted exhaust air flow is approximately 3000 m 3 per 1000 kg of product 74, 76.
- the thermal energy expenditure amounts to at least 280 kWh and the electrical energy expenditure additionally 24 kWh.
- cooling medium generator 18 organically highly contaminated process water
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Electrical Discharge Machining, Electrochemical Machining, And Combined Machining (AREA)
- Chemical And Physical Treatments For Wood And The Like (AREA)
- Analysing Materials By The Use Of Radiation (AREA)
- Fertilizers (AREA)
- Treatment Of Sludge (AREA)
- Mixers Of The Rotary Stirring Type (AREA)
- Degasification And Air Bubble Elimination (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
Claims
Priority Applications (15)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
HU0401993A HUP0401993A2 (hu) | 2001-09-03 | 2002-09-03 | Eljárás és berendezés szerves tartalmú hulladék kezelésére |
SI200220028A SI21496A (sl) | 2001-09-03 | 2002-09-03 | Postopek in naprava za predelavo odpadkov |
KR10-2004-7003212A KR20040041598A (ko) | 2001-09-03 | 2002-09-03 | 폐기물 처리 방법 및 그에 대응하는 처리 설비 |
DE50203294T DE50203294D1 (de) | 2001-09-03 | 2002-09-03 | Verfahren zum aufbereiten von abfallstoffen und aufbereitungsanlage |
JP2003524746A JP2005501701A (ja) | 2001-09-03 | 2002-09-03 | 廃棄物質を処理する方法、およびその方法に対応した処理プラント |
EA200400397A EA005332B1 (ru) | 2001-09-03 | 2002-09-03 | Способ и установка для переработки отходов |
EP02776975A EP1432535B1 (de) | 2001-09-03 | 2002-09-03 | Verfahren zum aufbereiten von abfallstoffen und aufbereitungsanlage |
NZ531619A NZ531619A (en) | 2001-09-03 | 2002-09-03 | Method for processing waste products and corresponding processing plant |
US10/488,722 US20040237859A1 (en) | 2001-09-03 | 2002-09-03 | Method for processing waste products and corresponding processing plant |
AT02776975T ATE296688T1 (de) | 2001-09-03 | 2002-09-03 | Verfahren zum aufbereiten von abfallstoffen und aufbereitungsanlage |
CA002469382A CA2469382C (en) | 2001-09-03 | 2002-09-03 | Processing waste using boiling water temperature and vacuum |
BR0212303-7A BR0212303A (pt) | 2001-09-03 | 2002-09-03 | Método para o processamento de substâncias de refugo, e fábrica de processamento |
AU2002339481A AU2002339481B2 (en) | 2001-09-03 | 2002-09-03 | Method for processing waste products and corresponding processing plant |
HR20040204A HRP20040204A2 (en) | 2001-09-03 | 2004-03-02 | Method for processing waste products and corresponding processing plant |
NO20041318A NO20041318L (no) | 2001-09-03 | 2004-03-30 | Fremgangsmate for bearbeiding av avfallsstoffer, samt korresponderende bearbeidingsanlegg |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10142906.1 | 2001-09-03 | ||
DE10142906A DE10142906A1 (de) | 2001-09-03 | 2001-09-03 | Verfahren zum Aufbereiten von Restmüll und Restmüllaufbereitungsanlage |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2003020450A1 true WO2003020450A1 (de) | 2003-03-13 |
Family
ID=7697400
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2002/009855 WO2003020450A1 (de) | 2001-09-03 | 2002-09-03 | Verfahren zum aufbereiten von abfallstoffen und aufbereitungsanlage |
Country Status (24)
Country | Link |
---|---|
US (1) | US20040237859A1 (de) |
EP (1) | EP1432535B1 (de) |
JP (1) | JP2005501701A (de) |
KR (1) | KR20040041598A (de) |
CN (1) | CN1240492C (de) |
AT (1) | ATE296688T1 (de) |
AU (1) | AU2002339481B2 (de) |
BR (1) | BR0212303A (de) |
CA (1) | CA2469382C (de) |
DE (2) | DE10142906A1 (de) |
EA (1) | EA005332B1 (de) |
ES (1) | ES2242071T3 (de) |
HR (1) | HRP20040204A2 (de) |
HU (1) | HUP0401993A2 (de) |
LT (1) | LT5179B (de) |
LV (1) | LV13162B (de) |
NO (1) | NO20041318L (de) |
NZ (1) | NZ531619A (de) |
PL (1) | PL368854A1 (de) |
PT (1) | PT1432535E (de) |
SI (1) | SI21496A (de) |
WO (1) | WO2003020450A1 (de) |
YU (1) | YU19204A (de) |
ZA (1) | ZA200401568B (de) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102008030653B4 (de) * | 2007-12-30 | 2012-02-23 | Archea Biogastechnologie Gmbh | Verfahren und Anlage zur Steigerung der Biogasausbeute eines Substrats |
WO2012172329A3 (en) * | 2011-06-17 | 2013-10-24 | Aerothermal Group Limited | Apparatus and process for treating waste |
CN105705895A (zh) * | 2013-08-07 | 2016-06-22 | 张贤智 | 食物垃圾真空干燥处理系统 |
Families Citing this family (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7396457B2 (en) * | 2006-06-27 | 2008-07-08 | Hyosung Corporation | Apparatus and method for recovering acetic acid and catalyst in process for preparation of 2,6-naphthalenedicarboxylic acid |
JP2009241072A (ja) * | 2006-07-26 | 2009-10-22 | Miike Iron Works Co Ltd | 固形化処理装置 |
DE102007056840A1 (de) * | 2007-11-26 | 2009-05-28 | Eltaga Licensing Gmbh | Verfahren und Vorrichtung zur Herstellung eines fertig aufbereiteten Gärsubstrats zur Biogaserzeugung |
PT2275525E (pt) * | 2009-07-13 | 2013-05-24 | Kompoferm Gmbh | Equipamento e procedimento para recuperação de biogás |
DE102010017334A1 (de) * | 2010-06-11 | 2011-12-15 | Mkr Metzger Gmbh Recyclingsysteme | Verfahren zur Behandlung von organischen Rückständen aus anaeroben Prozessen |
US8329455B2 (en) | 2011-07-08 | 2012-12-11 | Aikan North America, Inc. | Systems and methods for digestion of solid waste |
KR101176765B1 (ko) * | 2012-03-05 | 2012-08-28 | 유성종 | 폐기물 열처리 장치 |
FR3021237B1 (fr) * | 2014-05-23 | 2020-07-10 | Finance Developpement Environnement Charreyre - Fidec | Procede et installation de traitement d'un melange de dechets a deux cycles de compostage |
TWI574751B (zh) * | 2015-06-18 | 2017-03-21 | Shi Li-Ju | Energy Saving Purification System for High Temperature Organic Liquid |
US11215360B2 (en) * | 2015-08-18 | 2022-01-04 | Glock Ökoenergie Gmbh | Method and device for drying wood chips |
WO2018167370A1 (en) * | 2017-03-15 | 2018-09-20 | Biogts Oy | Hygienisation unit and method for hygienising raw material fed to a biogas reactor |
US10645950B2 (en) | 2017-05-01 | 2020-05-12 | Usarium Inc. | Methods of manufacturing products from material comprising oilcake, compositions produced from materials comprising processed oilcake, and systems for processing oilcake |
RU2650068C9 (ru) * | 2017-07-03 | 2018-05-30 | Андрей Владимирович Редькин | Система термического обеззараживания твердых медицинских отходов |
KR102254637B1 (ko) * | 2019-04-23 | 2021-05-21 | 비엔지코리아(주) | 유기성 잔재 폐자원의 혼합 연소 처리장치 |
US11839225B2 (en) | 2021-07-14 | 2023-12-12 | Usarium Inc. | Method for manufacturing alternative meat from liquid spent brewers' yeast |
CN113441535A (zh) * | 2021-08-13 | 2021-09-28 | 北京嘉博文生物科技有限公司 | 一种有机垃圾生物处理机尾气切换排放装置 |
KR102528460B1 (ko) * | 2023-01-11 | 2023-05-04 | 주식회사 에스빌드 | 재활용 코르크를 이용한 친환경 코르크 칩 생산시스템, 그 시스템에 의한 코르크 칩 제조방법 및 그 방법으로 제조되는 친환경 코르크 칩 |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6244199B1 (en) * | 1996-10-22 | 2001-06-12 | Traidec S.A. | Plant for thermolysis and energetic upgrading of waste products |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4765257A (en) * | 1987-12-02 | 1988-08-23 | Cf Systems Corporation | Apparatus and method for waste disposal |
US4977839A (en) * | 1988-01-14 | 1990-12-18 | Chemical Waste Management, Inc. | Process and apparatus for separating organic contaminants from contaminated inert materials |
ES2097528T3 (es) * | 1992-08-10 | 1997-04-01 | Protec Partner Umwelttech | Procedimiento y dispositivo para el tratamiento biologico de aguas residuales con carga organica y de residuos organicos. |
DE4234385A1 (de) * | 1992-10-06 | 1994-04-07 | Formex Trading Gmbh | Verfahren zur Pyrolyse von organischen Stoffen |
US5380445A (en) * | 1993-10-22 | 1995-01-10 | Midwest Research Institute | Pretreatment of microbial sludges |
US6112675A (en) * | 1996-04-08 | 2000-09-05 | Foster Wheeler Environmental Corporation | Process and apparatus for treating process streams from a system for separating constituents from contaminated material |
DE19648731A1 (de) | 1996-11-25 | 1998-05-28 | Herhof Umwelttechnik Gmbh | Verfahren und Vorrichtung zur Behandlung von Restabfall |
DE19807539C2 (de) | 1998-01-30 | 2000-11-16 | Horst Anders | Verfahren zur thermischen Behandlung von Abfällen |
DE19909328B4 (de) | 1998-11-06 | 2004-09-23 | Christian Widmer | Abfallverwertungsverfahren |
-
2001
- 2001-09-03 DE DE10142906A patent/DE10142906A1/de not_active Withdrawn
-
2002
- 2002-09-03 CA CA002469382A patent/CA2469382C/en not_active Expired - Fee Related
- 2002-09-03 AU AU2002339481A patent/AU2002339481B2/en not_active Expired - Fee Related
- 2002-09-03 PL PL02368854A patent/PL368854A1/xx unknown
- 2002-09-03 DE DE50203294T patent/DE50203294D1/de not_active Expired - Fee Related
- 2002-09-03 HU HU0401993A patent/HUP0401993A2/hu unknown
- 2002-09-03 NZ NZ531619A patent/NZ531619A/en unknown
- 2002-09-03 CN CNB028172256A patent/CN1240492C/zh not_active Expired - Fee Related
- 2002-09-03 US US10/488,722 patent/US20040237859A1/en not_active Abandoned
- 2002-09-03 JP JP2003524746A patent/JP2005501701A/ja active Pending
- 2002-09-03 PT PT02776975T patent/PT1432535E/pt unknown
- 2002-09-03 BR BR0212303-7A patent/BR0212303A/pt not_active IP Right Cessation
- 2002-09-03 WO PCT/EP2002/009855 patent/WO2003020450A1/de active IP Right Grant
- 2002-09-03 EP EP02776975A patent/EP1432535B1/de not_active Expired - Lifetime
- 2002-09-03 EA EA200400397A patent/EA005332B1/ru not_active IP Right Cessation
- 2002-09-03 YU YU19204A patent/YU19204A/sh unknown
- 2002-09-03 ES ES02776975T patent/ES2242071T3/es not_active Expired - Lifetime
- 2002-09-03 SI SI200220028A patent/SI21496A/sl not_active IP Right Cessation
- 2002-09-03 KR KR10-2004-7003212A patent/KR20040041598A/ko not_active Application Discontinuation
- 2002-09-03 AT AT02776975T patent/ATE296688T1/de not_active IP Right Cessation
-
2004
- 2004-02-26 ZA ZA200401568A patent/ZA200401568B/en unknown
- 2004-03-02 LV LVP-04-27A patent/LV13162B/en unknown
- 2004-03-02 HR HR20040204A patent/HRP20040204A2/hr not_active Application Discontinuation
- 2004-03-30 NO NO20041318A patent/NO20041318L/no not_active Application Discontinuation
- 2004-04-01 LT LT2004031A patent/LT5179B/lt not_active IP Right Cessation
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6244199B1 (en) * | 1996-10-22 | 2001-06-12 | Traidec S.A. | Plant for thermolysis and energetic upgrading of waste products |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102008030653B4 (de) * | 2007-12-30 | 2012-02-23 | Archea Biogastechnologie Gmbh | Verfahren und Anlage zur Steigerung der Biogasausbeute eines Substrats |
WO2012172329A3 (en) * | 2011-06-17 | 2013-10-24 | Aerothermal Group Limited | Apparatus and process for treating waste |
CN105705895A (zh) * | 2013-08-07 | 2016-06-22 | 张贤智 | 食物垃圾真空干燥处理系统 |
Also Published As
Publication number | Publication date |
---|---|
HUP0401993A2 (hu) | 2005-02-28 |
LT5179B (lt) | 2004-11-25 |
EP1432535A1 (de) | 2004-06-30 |
NO20041318L (no) | 2004-03-30 |
ATE296688T1 (de) | 2005-06-15 |
EA005332B1 (ru) | 2005-02-24 |
CN1240492C (zh) | 2006-02-08 |
EP1432535B1 (de) | 2005-06-01 |
CN1551806A (zh) | 2004-12-01 |
CA2469382A1 (en) | 2003-03-13 |
US20040237859A1 (en) | 2004-12-02 |
KR20040041598A (ko) | 2004-05-17 |
JP2005501701A (ja) | 2005-01-20 |
YU19204A (sh) | 2005-09-19 |
PT1432535E (pt) | 2005-09-30 |
AU2002339481B2 (en) | 2008-06-26 |
LT2004031A (en) | 2004-08-25 |
NZ531619A (en) | 2007-11-30 |
HRP20040204A2 (en) | 2004-08-31 |
DE50203294D1 (de) | 2005-07-07 |
ES2242071T3 (es) | 2005-11-01 |
CA2469382C (en) | 2008-03-25 |
EA200400397A1 (ru) | 2004-08-26 |
SI21496A (sl) | 2004-12-31 |
DE10142906A1 (de) | 2003-03-20 |
LV13162B (en) | 2004-07-20 |
BR0212303A (pt) | 2004-10-13 |
PL368854A1 (en) | 2005-04-04 |
ZA200401568B (en) | 2004-10-21 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP1432535A1 (de) | Verfahren zum aufbereiten von abfallstoffen und aufbereitungsanlage | |
US4872998A (en) | Apparatus and process for forming uniform, pelletizable sludge product | |
DD251569A5 (de) | Verfahren zur rueckgewinnung von verwertbarem gas aus muell | |
EP1127034A1 (de) | Verfahren und vorrichtung zur aufbereitung eines organik enthaltenden stoffgemisches | |
EP2891633B1 (de) | Vorrichtung und Verfahren zur thermischen Hydrolyse von organischer Masse | |
DE102010005253B4 (de) | Verfahren und Vorrichtung zum Behandeln und/oder Aufbereiten von flüssigem Gärrest aus einem Nachgärer und/oder Fermenter einer Biogasanlage | |
EP0254024B1 (de) | Verfahren zum Konvertieren von Klärschlamm-Filterkuchen durch Pyrolyse zu Öl, Gas und Koks und Anlage zur Durchführung des Verfahrens | |
DE4308920A1 (de) | Vorrichtung zur Behandlung von Bioabfällen oder dergleichen | |
EP1078698B1 (de) | Verfahren und Vorrichtung zur thermolytischen Aufarbeitung von polymer- und zellulosehaltigen Stoffen, insbesondere Shredderleichtgut | |
WO2006089766A1 (de) | Verfahren und reaktor zur biologischen aufbereitung von organik enthaltenden abfallstoffen | |
DE19946299C2 (de) | Verfahren und Vorrichtung zur gemeinsamen Vergärung von kohlenhydrat-, fett- und eiweisshaltigen Bioabfällen, cellulosereichen Bioabfällen, Faulschlamm aus Kläranlagen sowie Papierschlamm und Molke | |
JP3484634B2 (ja) | 殺菌・発酵処理システム | |
EP0803568A1 (de) | Vergärungsanlage und ein mit dieser Anlage durchführbares mehrstufiges Verfahren | |
EP0958332B1 (de) | Verfahren und vorrichtung zum verarbeiten von biologischen reststoffen, insbesondere klärschlamm | |
DE102006009165A1 (de) | Verfahren und Reaktor zur biologischen Aufbereitung von Organik enthaltenden Abfallstoffen | |
DE19617218C2 (de) | Verfahren und Vorrichtung zum Verarbeiten von biologischen Reststoffen, insbesondere Klärschlamm | |
EP1603839A2 (de) | Verfahren und hybridreaktor zur restmüllaufbereitung | |
DE4114386A1 (de) | Verfahren zur abwasserreinigung | |
WO2001056715A1 (de) | Aufbereitungsverfahren | |
DE19724049A1 (de) | Verfahren und Anlage zur Behandlung von Klärschlämmen oder Schlämmen ähnlicher Konsistenz | |
DE3928325A1 (de) | Verfahren zum trocknen und/oder verbrennen von klaerschlamm | |
EP2631581A2 (de) | Trocknungsvorrichtung für eine Biogasanlage und ein Verfahren zum Trocknen eines Flüssigproduktes mit einer solchen Trocknungsvorrichtung | |
AT401022B (de) | Verfahren zur erzeugung von biogas und kompost und einrichtung zur durchführung des verfahrens | |
EP0252069A2 (de) | Vorrichtung zur Behandlung von Abfallschlämmen | |
DE10207518A1 (de) | Verfahren und Vorrichtung zur Eindickung von Gärgut aus der Vergärung von Abfällen |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 1200400178 Country of ref document: VN Ref document number: P-192/04 Country of ref document: YU |
|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ OM PH PL PT RO RU SD SE SG SI SK SL TJ TM TN TR TT TZ UA UG US UZ VN YU ZA ZM ZW Kind code of ref document: A1 Designated state(s): AE AG AL AM AT AU AZ BA BB BG BY BZ CA CH CN CO CR CU CZ DE DM DZ EC EE ES FI GB GD GE GH HR HU ID IL IN IS JP KE KG KP KR LC LK LR LS LT LU LV MA MD MG MN MW MX MZ NO NZ OM PH PL PT RU SD SE SG SI SK SL TJ TM TN TR TZ UA UG US UZ VN YU ZA ZM |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR IE IT LU MC NL PT SE SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG Kind code of ref document: A1 Designated state(s): GH GM KE LS MW MZ SD SL SZ UG ZM ZW AM AZ BY KG KZ RU TJ TM AT BE BG CH CY CZ DK EE ES FI FR GB GR IE IT LU MC PT SE SK TR BF BJ CF CG CI GA GN GQ GW ML MR NE SN TD TG |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
DFPE | Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101) | ||
WWE | Wipo information: entry into national phase |
Ref document number: 2004/01568 Country of ref document: ZA Ref document number: 200401568 Country of ref document: ZA |
|
WWE | Wipo information: entry into national phase |
Ref document number: 1-2004-500283 Country of ref document: PH Ref document number: 145/MUMNP/2004 Country of ref document: IN |
|
WWE | Wipo information: entry into national phase |
Ref document number: 200220028 Country of ref document: SI Ref document number: 2469382 Country of ref document: CA |
|
ENP | Entry into the national phase |
Ref document number: 2004 200400192 Country of ref document: RO Kind code of ref document: A |
|
WWE | Wipo information: entry into national phase |
Ref document number: P20040204A Country of ref document: HR Ref document number: 200420040027 Country of ref document: LV |
|
WWE | Wipo information: entry into national phase |
Ref document number: 10488722 Country of ref document: US Ref document number: 20028172256 Country of ref document: CN Ref document number: 2003524746 Country of ref document: JP Ref document number: 1020047003212 Country of ref document: KR |
|
WWE | Wipo information: entry into national phase |
Ref document number: 531619 Country of ref document: NZ |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2002339481 Country of ref document: AU |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2002776975 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2004031 Country of ref document: LT |
|
WWE | Wipo information: entry into national phase |
Ref document number: 200400397 Country of ref document: EA |
|
REG | Reference to national code |
Ref country code: DE Ref legal event code: 8642 |
|
WWP | Wipo information: published in national office |
Ref document number: 2002776975 Country of ref document: EP |
|
WWP | Wipo information: published in national office |
Ref document number: 2004031 Country of ref document: LT |
|
WWG | Wipo information: grant in national office |
Ref document number: 2004031 Country of ref document: LT |
|
WWG | Wipo information: grant in national office |
Ref document number: 2002776975 Country of ref document: EP |