[go: up one dir, main page]

EP1603839A2 - Procede et reacteur hybride pour traiter des dechets residuels - Google Patents

Procede et reacteur hybride pour traiter des dechets residuels

Info

Publication number
EP1603839A2
EP1603839A2 EP04721117A EP04721117A EP1603839A2 EP 1603839 A2 EP1603839 A2 EP 1603839A2 EP 04721117 A EP04721117 A EP 04721117A EP 04721117 A EP04721117 A EP 04721117A EP 1603839 A2 EP1603839 A2 EP 1603839A2
Authority
EP
European Patent Office
Prior art keywords
water
process water
treatment
percolation
up0107k
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.)
Withdrawn
Application number
EP04721117A
Other languages
German (de)
English (en)
Inventor
Christian Widmer
Martin Schmied
Thomas Engelhard
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.)
ISKA GmbH
Original Assignee
ISKA GmbH
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
Priority claimed from DE200410003458 external-priority patent/DE102004003458A1/de
Application filed by ISKA GmbH filed Critical ISKA GmbH
Publication of EP1603839A2 publication Critical patent/EP1603839A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • 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
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
    • C05F9/00—Fertilisers from household or town refuse
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
    • Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
    • Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
    • 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
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/40—Bio-organic fraction processing; Production of fertilisers from the organic fraction of waste or refuse

Definitions

  • the invention relates to a method and a hybrid reactor for processing waste materials, in particular residual waste, according to the preamble of claims 1 and 21, respectively.
  • the object of the invention is to create a method and a hybrid reactor for the treatment of waste materials, in which the treatment of the process water is simplified compared to conventional solutions.
  • the method includes a process water treatment step in which denitrification of the
  • This denitrification is preferably carried out in a stripper device with a stripper column into which air is blown in countercurrent to the injected process water and which is followed by a catalyst column for converting the ammonia gas into nitrogen.
  • Another alternative provides a stripper device with a stripper column, into which saturated steam is injected in countercurrent to the injected process water and which is followed by a cooler for condensing the emerging steam mixture.
  • the effectiveness of the process can be further improved if lye is added in front of the stripper devices. This lye raises the pH value of the process water and dissolves ammonia gas in the process water.
  • the proportion of solids in the process water can be further reduced by ultrafiltration.
  • a precipitation of chlorides, phosphates etc. can be assigned to this ultrafiltration.
  • the biological process water treatment is preferably carried out with the aid of a hybrid reactor which has a sludge discharge device on its bottom and a device on its head for destroying an emerging floating blanket.
  • Air or oxygen can be injected into the head of the reactor to desulfurize the biogas that is formed.
  • the hybrid reactor can be provided with a gas injection device, via which the sludge bed that is created is periodically pressurized.
  • the sand wash can be followed by a sand removal and precipitation device in order to filter off the remaining finest sand and not to carry out the precipitation of salts, inert substances, etc. in the hybrid reactor.
  • PCA physical chemical treatment
  • Hybrid reactors can contain reverse osmosis to separate turbid water, salts etc. from the process water.
  • FIG. 1 shows a basic diagram of a method for the aerobic treatment of residual waste with a percolation or pulper system
  • FIG. 2 shows a solid and water treatment in the case of percolation or pulping with subsequent separation steps
  • FIG. 3 shows a first exemplary embodiment of a PCA system
  • FIG. 3.1 shows a series connection of two stripper columns after the first PCA wastewater treatment
  • FIG. 4 shows a second exemplary embodiment of a PCA system
  • FIG. 5 shows a combination of the concepts according to FIGS. 3 and 4
  • FIG. 6 shows an overall view of a process scheme for residual waste treatment with a hybrid reactor
  • FIG. 7 shows a hybrid reactor with an upstream sand sedimentation and filling reactor
  • Figure 8 is a partial view of a process scheme for anaerobic residual waste treatment with a fermentation plant
  • Figure 9 shows a variant of the method shown in Figure 2.
  • the organically contaminated substances 1 are fed to a percolation system 4 or a pulper system 5 either via a direct feed 2 or via an upstream mechanical processing system 3.
  • the mechanical preparation 3 has the steps of sieving, sorting and crushing, the screen cut 3.1 being preferably fed to a percolation plant 4 with a grain size of 50 mm to 250 mm and preferably to a pulper plant 5 with a grain size> 250 mm. In the case of a sieve cut 3.1 with a maximum grain size of approximately 50 mm, this is preferably fed to a dry fermentation plant 6 (FIG. 8).
  • a sieve overflow 3.2 is provided for separating material with a high calorific value, such as foils, boxes and paper.
  • facilities 3.3 for sieving and sorting steps to remove contaminants, e.g. Machine parts, wooden beams, ferrous and non-ferrous metals, as well as inert materials and minerals in various grain sizes are provided. The separated solids are further processed depending on their properties
  • the metal-containing solids can be returned to the steel processing industry and the wood-like solids to the paper industry, and the mineral substances or minerals can be stored in a landfill for storage.
  • the percolation plant 4 can be a percolation plant according to the German patent application DE 196 48 731 AI, in which organic components of a waste fraction are washed out in a percolator and the residue is burned after drying, for example. Furthermore is shown a Kastenperkolationsstrom with a lying box-shaped or cylindrical 'percolator, for example in WO 97/27158, as well as a Siedeperkolationsstrom the German patent application DE 101 42 906 AI used, according to which a percolator in the boiling range of the process water is operated in accordance.
  • a rotatable mechanical agitator 4.1 is arranged for circulating and mixing a heap of ork. Wash-out water 9.4 is introduced into the head of the container 4.5, through which the organic substances are washed out of the pile and which is then drawn off at the foot of the container 4.5 as organically highly contaminated outlet water 4.3.
  • the outlet opening is arranged downstream of a sieve plate 4.2 to prevent the solids from escaping.
  • the solids 4.4 which have been freed from the organic matter, are removed from the container 4.5 via a discharge device and separation steps (FIGS. 2.9) are fed with a classifying press 10 and a sinking swimming separation 14.
  • the outlet water 4.3 is fed directly to the sinking swimming separation 14.
  • the mean dry matter content in tank 4.5 is determined by the amount of wash-out water 9.4 supplied and the organically highly contaminated outlet water 4.3, as well as the residence time in the tank 4.5
  • the pulper or fabric dissolving system 5 which can be used alternatively, has a pulper vessel 5.5 in which a fast-running agitator 5.1. is arranged to equalize the supplied organically contaminated substances 1.
  • the organic matter in the pile is diluted with wash-out water 9.4 supplied from the top and by shear forces of the agitator 5.1. brought into solution.
  • Large-area light materials 5.3 are discharged via an overhead mechanical discharge device 5.2 for further treatment 15.
  • the discharge device 5.2 is constructed similarly to a fork and is shown here as a sieve.
  • the dissolved organic matter is discharged with the solids 5.4 through a discharge device on the bottom and fed to the classifying press 10 and thus to the sinking float separation 14 which follows it.
  • the TS content in the pulper 5.5 is adjusted to 5% to 10% by the addition of the washout water 9.4.
  • the pulping and separation process in the pulper system 5 is about 1h to 3h.
  • the material flows 5.7 and 9.3 occurring in the classifying press 10 and the sinking swimming separation 14 are fed as a residual flow 5.7 to the further treatment 15 and the organically highly loaded liquid 9.3 freed from the solids of a biogas plant 9 according to the invention (FIGS. 1, 6, 7).
  • the liquid 9.3 charged with organic matter is fed to a biogas plant 9 (FIGS. 1, 6, 7) for anaerobic degradation.
  • the liquid 9.3 is deflated by converting the organic portion by means of methane bacteria and feeding it to a biogas combustion 8 via a gas generation line 7 for energy generation.
  • the fermentation water freed from the organic matter leaves the biogas plant 9 and is fed as washable water 9.4 to the washout processes 4, 5 as process water.
  • a partial flow 9.6 of the wash-out water 9.4 becomes an ultrafiltration 13 and / or a decanter and / or a belt press or a mechanical one
  • Solid-water mixture 16.1 is fed to the further treatment 15 as a press cake 16.2 and can partly as inoculation sludge 16.3 of the liquid loaded with organic matter
  • Press water 16 obtained in ultrafiltration 13 becomes a physically chemical one according to the invention
  • PCA plant Processing plant 21, 22, 23, 24 fed for denitrification.
  • the press water 16 is freed of nitrogen in the PCA system 21, 22, 23, 24. Material flows occur which either as salt-free water or permeate 23.5 of the liquid laden with organic matter 9.3 or as purified salt-free process water 23.6 of the
  • FIG. 2 schematically shows a process sequence in a percolation or pulper system 4, 5 with the subsequent separation steps 10, 14 from FIG. 1.
  • the course of the solid streams 4.4, 5.4 after the percolation system 4 and the pulper system 5 is the same.
  • the main difference is that the percolation plant 4 does not have to be followed by the sinking swimming separation 14 in order to feed the material flow 4.3 to the biogas plant 9, whereas in the pulpering plant 5 the sinking swimming separation 14 is necessary to filter out the pulp (solid) from the material flow 5.4.
  • the sinking swimming separation 14 is interposed for simplification in both methods.
  • the light materials 5.3 are further processed 15 and the solids 5.5 are also fed to the classifying press 10.
  • the wastewater 10.1 freed from coarse solids of the classifying press 10 is fed to a mixer 14.1.5, in which it is mixed with air by means of a blower 14.1.4 and then blown into a separation tank 14.1 of the sinking swimming separation 14 with a slight overpressure via a bottom-side blowing device 14.1.6 becomes.
  • a mixer 14.1.5 in which it is mixed with air by means of a blower 14.1.4 and then blown into a separation tank 14.1 of the sinking swimming separation 14 with a slight overpressure via a bottom-side blowing device 14.1.6 becomes.
  • the outlet water 4.3 of the percolator 4 which is loaded with organic matter, becomes the separation basin 14.1 on the head side. fed where it mixes with the wastewater 10.1 and from this water mixture float 14.1.1 and sediment 14.1.2 separate.
  • the floating materials 14.1.1 float up and form a floating material blanket.
  • the floating materials 14.1.1 are drawn off by an overhead mechanical device 14.1.3 and fed to the classifying press 10 via a delivery line 14.1.7 for additional dewatering.
  • the sediments 14.1.2 e.g. Sand, stones and metal parts sink in the separation basin 14.1 and are removed by a discharge and transport device 14.1.8. Depending on the intended use, they are processed further via a conveyor line 14.1.9
  • the sand for use as a building material for example for road construction, is freed from the organic matter by washing out according to the Z2 deposition ordinance.
  • the sediments or the sand-liquid mixture 14.1.2 are introduced into the top of the vessel via the delivery line 14.1.10 and by means of the purified operating water 23.6 of the PCA introduced via an introduction device 14.2.6. Plant 21, 22, 23, 24 washed.
  • air can be added to the process water 23.6 in the mixer 14.1.5 via a blower 14.1.4.
  • the air and the process water 23.6 can be introduced into the vessel continuously or discontinuously, and separately from one another.
  • the sand 14.2.2 sinks down into the vessel and the organic constituents 14.2.1 float on top and are discharged as an organic working water mixture 14.2.3.
  • the sand 14.2.9 freed from the organic matter is discharged on the bottom side via a discharge and conveying device 14.2.8 and used as a building material or added to the press cake 12 and subjected to further treatment 15.
  • the two liquid streams 14.1.11, 14.2.3 loaded with organic matter are introduced mixed on the head side via an inlet line 14.2.7.
  • the sieve stage 14.3 preferably has an internally coated drum or vibrating sieve 14.3.1 with a mesh size of approximately 0.5 mm to 1.5 mm, so that the fibers, residues and plastic particles contained in the liquid stream 14.2.7 are separated.
  • the resulting paste-like mass 14.2.10 is discharged and fed to the classifying press 10 for dewatering via a conveyor 14.2.4 and conveyor lines 14.2.5, 14,2,6.
  • the pasty mass 14.2.10 can be fed to the percolation system 4 again via conveyor lines 14.2.5, 14.2.11.
  • the organically highly contaminated liquid 9.3 of the sinking swimming separation 14 that passes through the sieve 14.3.1 and accumulates on the bottom is fed to the biogas plant 9 according to FIG. 1, the fermentation water freed from the organic matter being supplied to the biogas plant 9 as absorbable washout water 9.4 of the percolation plant 4 or is fed again to the pulper system 5 and, on the other hand, passes through the ultrafiltration 13 and the PCA system 21, 22, 23, 2 as partial stream 9.6.
  • FIG. 3 shows a preferred PCA system according to the invention in detail.
  • the press water 16 of the ultrafiltration 13 is heated to the necessary process temperature in a heat exchanger 17.
  • a lye 19 is added to the heated press water 18 to raise the pH so that ammonia is present in the press water 18 in dissolved form.
  • the mixed water 20 is in a stripper device 22 for separating ammonium gas from the water
  • the stripper device 22 has a stripper column 22.1, into which the mixed water 20 is introduced in an overhead region by means of a spray device 22.4.
  • the sprayed mixed water 20 flows in the stripper column 22.1. downwards, a packing 22.6 being introduced into the stripping column 22.1 to enlarge the exchange area.
  • the mixed water 22 is flowed through in countercurrent by the heated air 22.2 introduced via a supply air blower.
  • the air 22.2 is heated to the same temperature as the mixed water 20 via a heat exchanger 22.7.
  • the ammonium contained in the mixed water 20 is triggered by the counter-current and preheated air and leaves the stripper column 22.1 as the ammonia-laden exhaust air 22.3.
  • the water 22.5 freed from the ammonium collects at the bottom of the stripper column 22.1 and is fed to a reverse osmosis 23.
  • the pH of the mixed water 20 is advantageously raised to> 10 and the temperature of the mixed water 20 and the heated air 22.2 is set to 60 ° C.
  • the exhaust air 22.3 is fed to a catalyst column 22.8 in which the gaseous ammonia is broken down and reduced to atmospheric nitrogen and the hydrogen is oxidized to water.
  • the catalyst column 22.8 is preheated to the necessary operating temperature at the beginning by means of a heater 22.9. If there is sufficient ammonium in the exhaust air 22.3, the further process can proceed autothermally, i.e. The pollutants contained in the exhaust air 22.3 provide the necessary heat of reaction. This is achieved if the ammonium content in the press water 16 is approximately at least 2000 mg / 1
  • the exhaust air 22.3 leaves the catalyst column 22.8 as residual air saturated with water vapor and loaded with nitrogen 22.11.
  • the residual air 22.11 is cooled in a cooler or condenser 22.12 and then discharged into the environment as exhaust air 22.13 loaded with nitrogen N2.
  • a portion freed from ammonium leaves the catalyst column 22.8 as condensate 22.10, which is fed to the reverse osmosis 23.
  • the mixed water 20 loaded with ammonia is fed to the first stripper column 22.1 and, after a first cleaning step, is drawn off as water 22.5 freed from ammonia up to 90%.
  • This water is fed to the second stripping column 22.5 22 I 1 and there subjected to a further purification step via a pump 22.5.1.
  • the water 22.5 'freed of up to 99% of the ammonia then reaches the reverse osmosis 23.
  • the exhaust air 22.3, 22.3' laden with ammonia from the two stripper columns 22.1, 22.1 ' is fed to a catalyst column 22.8 described above.
  • FIG. 4 shows a basic diagram of a further exemplary embodiment of a PCA system 21 for the treatment of press water 16, which has an ammonium content of at most approximately 2000 mg / 1, a chloride content of approximately 5000 mg / 1 and a chemical oxygen demand (COD content) of approximately 2000 mg / 1.
  • the press water 16 of the ultrafiltration 13 is heated in a heat exchanger 17 and fed as a heated mixed water 20 to a stripper column 21.1 at the head end with the addition of an alkali 19 to raise the pH.
  • the mixed water 20 is sprayed via a spray device 21.4 in the stripper column 21.1 and moves downward, the material exchange area being enlarged via a packing 21.6.
  • saturated steam 21.2 is injected in the counterflow, which is generated, for example, by means of a steam generator or a waste steam generator 21.7. This evaporation makes it possible to reduce the ammonium in the mixed water 20 by up to 99%.
  • the ammonium is washed out of the mixed water 20 and the loaded exhaust steam
  • the concentrate 24.2 can also be dried, e.g. by evaporation in a vacuum boiling dryer, and then the further treatment 15 are fed.
  • the water 21.5 freed from the ammonia is withdrawn from the stripper column 21.1 at the bottom and fed to the above-mentioned reverse osmosis 23.
  • FIG. 5 shows a combination of the basic schemes of
  • the combination has two stripper devices 22, 21 connected in series.
  • heated air 21.2 is blown into the stripper column 21.1 and in the second stripper device 22, as is the case in FIG.
  • the exhaust air 22.3 loaded with ammonia from the first stripping column 22.1 is fed to a stripping catalyst 22.8.
  • the ammonia freed water 22.5 is mixed with the condensate 21.10 of the stripper catalyst 22.8 and fed as mixed water 20.1 to the stripper column 21.1 of the second stripper device 21 via a pump 22.5.1 of the stripper column.
  • the ammonia-laden waste steam 21.3 from the second stripper column 21.1 is, as described above, fed to the cooling device 24 and condensed there.
  • the ammonia-laden water 21.5 is fed to the reverse osmosis 23 in the above manner.
  • FIG. 6 shows a process diagram of a residual waste treatment with essentially a percolation system 4 or a pulper system 5 and a material separation and
  • the liquid 9.3 is fermented in fully mixed and one to two-stage stirred tank reactors, the organics being converted into biogas.
  • a mechanical stirring system or a gas injection circulation system is usually used as the agitator.
  • the residence time of the liquid 9.3 in such a stirred tank reactor is approximately 18 to 24 days.
  • the hybrid reactor 9 has an insulated cylindrical container 9.1. At the bottom, the pre-treated liquid 9.3 is injected over the cross-section of the container 9.1 via an injection device 9.3.3 in such a way that there is an approximate climbing speed of 2 m / h.
  • the organic constituents released from the injected liquid 9.3.2 by means of methane bacteria sink downward in the hybrid reactor 9 and form a sludge bed 9.2.1 there.
  • the sludge bed 9.2.1 serves as a fermentation stage and reaction bed for the precipitation of, for example, inert substances, chlorides and phosphates.
  • a discharge sludge 9.10 mixed with the precipitated inert substances and salts is removed from the container 9.1 via a sludge discharge device 9.8. discharged.
  • the precipitation is supported by a precipitant 9.7, which is added to the liquid 9.3 before entering the hybrid reactor 9.
  • the methane bacteria are arranged in a packing or a fixed bed 9.2 from a bed or block elements to increase the metabolism, ie to improve the decomposition of methane gas and to improve the cleaning of the liquid laden with organics 9.3.2.
  • the increase in material turnover is based primarily on an increase in the reaction areas and immobilization of the active bacterial sludge.
  • the reaction areas range from about 200 m 2 / m 3 to 300 m 2 / m 3 .
  • the sludge discharge device 9.8. has at least one moving floor device 9.8.1 with scraper elements and at least one screw conveyor 9.8.3.
  • the moving floor device 9.8.1 is shown as a piston rod of a hydraulic cylinder-piston unit 9.8.2 to which the scraper elements are attached. With each extension movement of the piston rod, ie in FIG. 6 a movement to the right, the discharge sludge 9.10 is conveyed to the screw conveyor 9.8.3. A drain of the screw conveyor 9.8.3 can be shut off via a valve 9.8.4.
  • the liquid freed from the organic constituents is withdrawn from the top of the container 9.1 and fed as the wash-out water 9.4 to the percolation system 4 or the pulper system 5, and as a partial stream 9.6 to the ultrafiltration 13 with subsequent PCA system 21, 22, 23, 24.
  • a horizontal agitator 9.11 is provided close below the surface of the injected liquid 9.3.2 collected in the container 9.1.
  • the horizontal agitator 9.11 can be replaced by a vertical agitator or the like.
  • a blower or a compressor 9.15 is injected periodically via a pipe 9.14 and gas injection nozzles 9.14.1 gas 9.14.2.
  • This gas is preferably taken from the biogas supplied for biogas combustion.
  • This gas injection has the effect that channel formation in the packed packing 9.2 is prevented and old, dead bacterial sludge is released from the packed packing 9.2 and, depending on the weight, floats as a floating substance 9.11.1 or is discharged as a sinking substance with the discharge sludge 9.10.
  • a partial stream 9. 6 is branched off from the washout water 9.4 and fed to the ultrafiltration 13.
  • the press water 16 with an ammonium content of approximately 1000 mg / 1 to 3000 mg / 1 is fed to the PCA system 21, 22, 23, 24, denitrified there as described above (FIGS. 3, 3.1. 4 and 5) and admixed with the loaded liquid 9.3 as the denitrated process water 23.6.
  • a solid-water mixture 16.1 obtained in the ultrafiltration 13 with a dry matter content of about 4% to 8% is fed to the further treatment 15 as a press cake 16.2 and / or as a vaccine sludge 16.3 for the hybrid reactor 9 also admixed with the liquid 9.3, which is highly loaded with organic matter.
  • the partial flow 9.6 serves as circulating water 9.5 for setting the operating temperature.
  • the circulation water 9.5 is heated in a heat exchanger 9.5.1 and mixed with the liquid 9.3 filled with organic matter.
  • FIG. 7 shows an alternative basic diagram of a method according to FIGS. 1 and 6 for the treatment of residual waste with a biogas plant 9 ′, which is preceded by a sand settling and precipitation reactor 25.
  • the upstream connection of such a reactor 25 has the advantage that the sand settling and precipitation process does not take place in the hybrid reactor 9 and thus the structurally complex sludge discharge device 9.8 can be dispensed with.
  • the sand settling time is about 1 hour and the precipitation time lasts a maximum of 5 minutes.
  • the size and geometry of the container 25.1 is designed for a stay of at least one hour.
  • the sand settling and precipitation reactor 25 has a cylindrical container 25.1 with a baffle 25.2 for forcibly guiding a liquid flow in the container 25.1.
  • the baffle 25.2 extends from a container ceiling in the direction of a bottom-side screw-like discharge device 25.4, a passage for the liquid flow being formed between the baffle 25.2 and the discharge device 25.4.
  • the liquid 9.3 loaded with organic matter is mixed with a precipitant 9.7 and fed to the container 25.1.
  • the liquid 9.3 flows around the baffle 25.2, the sand and the precipitated products, e.g. Collect chlorides and phosphate at the bottom of the container and be discharged by the discharge device 25.4 as discharge sludge 9.10.
  • the liquid 9.3.1 freed from the sand and the precipitated products is removed from the top of the container 25.1 and fed to the hybrid reactor 9 for further processing as described above.
  • a mixing device can also be used or this can be combined with the partition 25.2.
  • the mixing device can be particularly advantageous in the case of heavy metals, since these require a longer contact time.
  • a mixer can also be provided in the feed line to the container 25.1.
  • FIG. 8 shows an alternative to waste treatment with a percolation plant 4 or a pulper plant 5.
  • the method shown there is based on the use of a dry fermentation plant 6. Consequently, this process scheme does not have a hybrid reactor 9 according to the invention.
  • the fermentation system 6 has a fermentation tank for carrying out a fermentation process in the absence of air, i.e. anaerobic digestion.
  • a fermentation tank is e.g. for systems from the Swiss company Kompogas AG (www.kompogas.ch), the Austrian building materials and recycling association (BRV, www.brv.at), Dranko and the French company Valorga Int. SAS (www.steinmuller-valorga. Fr) is used.
  • the sieve cut or fresh waste 3.1 of the mechanical preparation 3 of the organically contaminated substances 1 is admixed with inoculum 6.4, which is taken from the fermentation process after inoculation with anaerobic bacteria, and after dilution with process water 10.2 with a pumping and conveying device 6.3 introduced into the fermentation tank via a feed line 6.5 at the top.
  • the fermenter content 6.7 is periodically circulated by an agitator 6.1 and transported by mechanical action to an outlet below.
  • the process heat is via an outer jacket heating and not shown
  • the fresh waste 3.1 is mixed with the inoculation 6.4. and process water 10.2. inoculated and diluted and entered and circulated into the fermentation tank by means of a pumping and conveying device 6.3 via the feed line 6.5.
  • the fermentation tank 6 at Dranko / Valorga is designed as a cylindrical standing element in steel or concrete construction and has no mechanical agitator in the interior.
  • the circulation takes place exclusively via the pumping and conveying device 6.3.
  • the circulation takes place via a gas injection system with injection lances 6.2 close to the bottom, via which the fermenter content 6.7 is subjected to pressure surges> 8 bar intermittently.
  • the process temperature is set via an outer jacket heating and a heat exchanger in the pumping and conveying device 6.3 or the feed line 6.5, as well as direct steam injection into the fresh waste 3.1.
  • the anaerobic biogas generation from the fermentation process according to the fermentation system 6 takes place in the fermentation tank, the resulting biogas being led overhead through the gas generation line 7 to the gas combustion 8.
  • This biogas with a methane content of around 55% to 65% can be used to generate heat and electricity via a combined heat and power plant.
  • the ferment content 6.7 leaves the fermentation tank as a fermentation cake 6.6 and is fed to at least two separation stages 10, 11 in order to produce a treatable wastewater.
  • the first separation stage is usually a classifying press 10, in which the press cake 12 is separated from the wastewater 10.1 contaminated with organic matter and is added to the further treatment 15.
  • the wastewater 10.1 usually has a dry matter content of> 12% and is fed to a second separation stage 11.
  • a partial flow of the waste water 10.1 is added to the fresh waste 3.1 as process water 10.2.
  • the second separation stage can also be a classifying press 11.
  • the press cake 12.1. the second separation stage 11 can also be added to the further treatment 15.
  • the waste water 11.1 of the second separation stage 11 is fed to an ultrafiltration 13 in the manner described at the beginning.
  • the solid-water mixture 16.1 from the ultrafiltration 13 is mixed as a press cake 16.2 with the press cake 12, 12.1 of the upstream separation stages 10, 11 and fed to the further treatment 15.
  • the mixture can have a dry matter content of 35% to 45%.
  • the press water 16 of the ultrafiltration 13 with a maximum TS content of 5% is supplied to the PCA system 21, 22, 23, 24 according to the invention for cleaning and denitrification (FIGS. 3, 3.1, 4, 5).
  • the organic is washed out in the case where clean sand 14.2.9 is required with process or municipal water 23.6.
  • the wastewater 9.3 from sieve stage 14.3, which has been cleaned of fibrous materials and sand and is loaded with organic matter, is used as washing water and is fed to the biogas reactor 9 for the production of biogas.
  • the organic process water mixture 14.2.3 is fed to the sieving stage or floating and fiber separation 14.3.
  • the liquid flow 14.2.3 loaded with organic matter and press water 14.3.3 returned via the delivery line 14.2.5 are fed to this stage 14.3 from a classifying press 14.3.2 arranged downstream of the sieving stage 14.3.
  • the proportion of the press water 14.3.3 supplied to the sieving stage 14.3 is in turn set via a flow deflector / mixer 14.1.12. This press water can alternatively or simultaneously also be fed to the washing stage 14.2 or the percolator 4 or the pulper system 5.
  • Gap sizes / sieve widths from 0.5 to 1.5 mm are freed of the fibers and mold materials.
  • This pasty mass 14.2.10 is dewatered via the above-mentioned classifying press 14.3.2 and optionally either captured separately via the fabric deflector 14.1.12 or fed to the further treatment 15.
  • the press water 14.3.3 is - as explained above - via the delivery lines 14.2.5, depending on the degree of contamination, optionally returned to the sieving stage 14.3., The washing stage 14.2 or the percolation 4 or pulper system 5.
  • Liquid 9.3 is then, as described, fed to the biogas plant 9 or partially returned to the washing stage.
  • PCA PCA

Landscapes

  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
  • Processing Of Solid Wastes (AREA)
  • Physical Water Treatments (AREA)
  • Treatment Of Sludge (AREA)

Abstract

La présente invention concerne un procédé pour traiter de façon mécanique et biologique des déchets, en particulier des déchets résiduels, le procédé comprenant un traitement physico-chimique (PCA) de détritruration d'une eau de traitement de laquelle ont été éliminés les composantes organiques. L'invention a également pour objet un réacteur hybride comprenant un lit fixe, un dispositif d'extraction de boue et un dispositif de destruction de la partie surnageante.
EP04721117A 2003-03-17 2004-03-17 Procede et reacteur hybride pour traiter des dechets residuels Withdrawn EP1603839A2 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE10311904 2003-03-17
DE10311904 2003-03-17
DE200410003458 DE102004003458A1 (de) 2003-03-17 2004-01-22 Verfahren und Hybridreaktor zur Restmüllaufbereitung
DE102004003458 2004-01-22
PCT/DE2004/000546 WO2004083125A2 (fr) 2003-03-17 2004-03-17 Procede et reacteur hybride pour traiter des dechets residuels

Publications (1)

Publication Number Publication Date
EP1603839A2 true EP1603839A2 (fr) 2005-12-14

Family

ID=33030902

Family Applications (1)

Application Number Title Priority Date Filing Date
EP04721117A Withdrawn EP1603839A2 (fr) 2003-03-17 2004-03-17 Procede et reacteur hybride pour traiter des dechets residuels

Country Status (5)

Country Link
US (1) US20060180547A1 (fr)
EP (1) EP1603839A2 (fr)
AU (1) AU2004222180A1 (fr)
CA (1) CA2519384A1 (fr)
WO (1) WO2004083125A2 (fr)

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102006058419A1 (de) * 2006-12-08 2008-06-26 Bilfinger Berger Umwelttechnik Gmbh Verfahren zur Perkolataufbereitung und Perkolataufbereitungsanlage
IT1393315B1 (it) * 2008-10-30 2012-04-20 Pianese Processo per la trasformazione dei rifiuti solidi urbani in materiali e/o conglomerati dalla quota inerte, in energia ottenuta dal biogas derivante da trattamento a freddo di bioconversione anaerobica della frazione organica ed in eventuale ammendante
CN101786094B (zh) * 2010-03-25 2011-02-09 河北省建筑材料工业设计研究院 生活垃圾与污水联合处理工艺
US10334870B2 (en) 2010-10-07 2019-07-02 Tropicana Products, Inc. Processing of whole fruits and vegetables, processing of side-stream ingredients of fruits and vegetables, and use of the processed fruits and vegetables in beverage and food products
JP6297069B2 (ja) 2013-02-15 2018-03-20 ペプシコ, インコーポレイテッドPepsiCo Inc. 栄養特性および官能特性を向上させるための共製品の飲料への含有およびその調製
JP6931816B2 (ja) * 2018-10-12 2021-09-08 株式会社石垣 可溶化装置一体型消化タンク
CN110790421A (zh) * 2019-10-15 2020-02-14 杭州中橙科技有限公司 一种高效污水处理池
IT202100009365A1 (it) * 2021-04-14 2022-10-14 Bridgestone Europe Nv Sa Pneumatico provvisto di una etichetta di identificazione temporanea
CN114993029B (zh) * 2022-05-11 2024-04-19 陕西泰臻节能环保科技有限公司 一种水性墨凹版印刷热泵加热回收机组

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5228995A (en) * 1992-04-23 1993-07-20 Stover Enos L Biochemically enhanced hybrid anaerobic reactor
DE4324410C1 (de) * 1993-07-21 1994-08-04 Enviro Consult Ingenieurgesell Verfahren zum Entfernen von Ammonium aus dem Zentratwasser einer biologischen Abwasserreinigungsanlage
DE19508785C2 (de) * 1994-03-10 1997-06-05 Mannesmann Ag Verfahren und Anlage zur Behandlung von Restmüll
JP3103027B2 (ja) * 1995-11-27 2000-10-23 株式会社荏原製作所 汚水中のアンモニアを用いる排ガスの処理方法と装置
GR1002461B (el) * 1995-12-29 1996-11-01 Βιομηχανικη αξιοποιηση των σκουπιδιων με πληρη ανακυκλωση υλικων και με αριστοποιηση στην παραγωγη προιοντων και ενεργειας.
DE19610056B4 (de) * 1996-03-14 2007-08-30 Linde Ag Verfahren und Vorrichtung zur Biogasgewinnung
DE19648731A1 (de) * 1996-11-25 1998-05-28 Herhof Umwelttechnik Gmbh Verfahren und Vorrichtung zur Behandlung von Restabfall
DE19725823B4 (de) * 1997-06-18 2004-07-08 Linde-Kca-Dresden Gmbh Verfahren zur Biogasgewinnung
DE10005149A1 (de) * 2000-02-07 2001-08-23 Daniel Friedli Trocknungsverfahren
US20050006295A1 (en) * 2003-02-10 2005-01-13 Upen Bharwada Water treatment system

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2004083125A2 *

Also Published As

Publication number Publication date
AU2004222180A1 (en) 2004-09-30
WO2004083125A2 (fr) 2004-09-30
WO2004083125A3 (fr) 2004-11-25
CA2519384A1 (fr) 2004-09-30
US20060180547A1 (en) 2006-08-17

Similar Documents

Publication Publication Date Title
DE2952794C2 (de) Verfahren und Vorrichtung zur Aufbereitung organischer Abfallmassen mit hohem Gehalt an Stickstoffverbindungen
DE69322132T2 (de) Verfahren und Anlage zur anaeroben Zersetzung von organischen Abfällen
DE69617458T2 (de) Vorrichtung und verfahren zum recycling und umwandeln von abfall
DE69937024T2 (de) Verfahren für die Methangärung von organischen Abfällen
DE69807899T2 (de) Methode zur abwasserreinigung mit einer zusätzlichen schlammbehandlung durch ozon
EP0229927A2 (fr) Procédé de séparation et de traitement de la partie organique d'ordures ménagères
DD251569A5 (de) Verfahren zur rueckgewinnung von verwertbarem gas aus muell
EP1687093B1 (fr) Procede et dispositif de traitement par voie humide et mecanique d'un melange de substances, en particulier de dechets de tous types
DD253607A5 (de) Verfahren zur entsorgung von klaerschlamm aus einer biologischen abwasserreinigungsanlage
DE2100521A1 (de) Verfahren zum Steuern der Temperatur in einer biologischen Abbauanlage, ins besondere in einer Abwasserklaranlage sowie Einrichtung zur Ausfuhrung des Verfahrens
DE3422959A1 (de) Verfahen zur biologischen reduktion von schwefeloxiden und oxydaton von organischen substanzen
EP1603839A2 (fr) Procede et reacteur hybride pour traiter des dechets residuels
EP0486578B1 (fr) Procede d'epuration et de traitement de produits contamines
DE102005026027A1 (de) Stofflöser, Reaktor für Hydrolyse und/oder Nassrotte und Abfallaufbereitungsanlage mit einem derartigen Stofflöser und Reaktor
EP1567454A2 (fr) Procede de purification des eaux usees avec production de boue en excedent et installation de purification des eaux usees correspondante
CH619675A5 (fr)
DE102006038450A1 (de) Verfahren und Vorrichtung zur Behandlung eines Stoffgemisches aus Abfällen
DE2335538B1 (de) Verfahren zur Beschleunigung und Intensivierung biologischer Abbauvorgaenge
DE2260616A1 (de) Verfahren zum verwerten von klaerschlamm aus abwasser-klaeranlagen in verbindung mit der beseitigung und aufarbeitung von haus-, gewerbe-, industrie-, landund forstwirtschaftsabfaellen
DE2111489A1 (de) Verfahren zur Aufbereitung von Wasser
EP0909586A1 (fr) Procédé et installation pour le traitement de déchets
EP2046689B8 (fr) Dispositif de purification préliminaire des eaux usées avec traitement ultérieur intégré des solides
DE102019007790A1 (de) Trennvorrichtungen und Trennverfahren zur Trennung biogener, halbsynthetischer und/oder synthetischer Stoffgemische in ihre festen, flüssigen und gasförmigen Anteile unter Wärmerückgewinnung
DE2315705A1 (de) Verfahren und vorrichtung zum umwandeln von haushalts-, landwirtschaftsund grosshandels-muell sowie von verrottbaren industrie- und gewerbe-abfaellen in klaerschlamm, wasser und gase
EP1064240A1 (fr) Procede et installation pour traiter des dechets

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20050922

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IT LI LU MC NL PL PT RO SE SI SK TR

AX Request for extension of the european patent

Extension state: AL LT LV MK

RAX Requested extension states of the european patent have changed

Extension state: MK

Payment date: 20050922

Extension state: AL

Payment date: 20050922

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20080520