CN101065188A - Material solubiliser reactor for hydrolysis and/or wet fermentation and waste treatment plant with such a solubiliser and reactor - Google Patents
Material solubiliser reactor for hydrolysis and/or wet fermentation and waste treatment plant with such a solubiliser and reactor Download PDFInfo
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- CN101065188A CN101065188A CNA2005800249992A CN200580024999A CN101065188A CN 101065188 A CN101065188 A CN 101065188A CN A2005800249992 A CNA2005800249992 A CN A2005800249992A CN 200580024999 A CN200580024999 A CN 200580024999A CN 101065188 A CN101065188 A CN 101065188A
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- 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
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- 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
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- 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
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Abstract
To provide an arm device for bedsides which fixes the angle between arms regardless of a torque which is applied to the connected section between the arms to hold the posture of the arms. For this arm device 1 for bedsides, a base 2, a first arm 10, a second arm 20 and a head mount 30 are connected by first to third turning shafts 13, 23 and 33. A first electromagnetic valve 80 is provided in a bypass 45 which communicates two liquid chambers 44a and 44b of a doubly acting type first hydraulic cylinder 40 provided between base 2 and the first arm 10. A second electromagnetic valve 90 is provided in a bypass 55 which communicates two liquid chambers 54a and 54b of a doubly acting type second hydraulic cylinder 50 provided between the first arm 10 and the second arm 20. The first electromagnetic valve 80 and the second electromagnetic valve 90 are operated by buttons 85 and 95 which are arranged on the head mount 30, and thus, the posture of the arm device 1 is changed.
Description
Technical field
The present invention relates to a kind of according to the described method that is used for handling the rubbish that contains organic principle of claim 1 preamble, a kind of according to the described material dissolution device, a kind of that is used at diluent liquid dissolving rubbish organic principle of claim 5 or 19 preambles according to claim 28 or described reactor and a kind of refuse treatment plant that comprises this material dissolution device and/or reactor that is used to implement hydrolysis and/or wet method macerate of 36 preambles.
Background technology
Along with the categorised collection of Europe implementation organic domestic waste, the importance of mechanical biological processing (MBA) household garbage is growing.The decomposition of microorganisms biological material wherein, exists difference between aerobic and anaerobe.Aerobic decomposition finally forms end product carbon dioxide and water and is called rotten.Anaerobic digestion is typically fermentation, wherein forms methane, ammonia and hydrogen sulfide as end product.
Known method has the distinct methods step that is used for garbage disposal according to the character of garbage mixture.Yet provide each method equipment very expensive separately.
DE 196 48 731 A1 have introduced a kind of aerobic method, wherein, the organic principle of rubbish distillate is for example burned in the removal of impurity of percolation filter wash-in and after with filter residue and drying or heap.
Diafiltration for example can be carried out in the box diafiltration equipment of foundation WO 97/27158 A1.Fact proved coming is the test of adopting according to the distillation diafiltration equipment of DE 101 42 906 A1, and wherein, diafiltration is carried out in the distillation zone of process water.
From the discharge water of the high organic content of percolation filter discharging is that anaerobic digestion is transported to biogas facility, and wherein, organic moiety is decomposed by methane bacteria and can be transported to the biogas combustion apparatus for the energy generation.Fact proved that the above-mentioned aerobic treatment of refuse in percolation filter has competitiveness and occupy more and more important position the anaerobism method.
EP 0 192 900 B1 have introduced a kind of so-called Valorga method-wherein, and fermentation is carried out from the fermentor of following feeding at one.Rubbish embolism shape to be processed be transported to the discharge gate that is arranged on below the radially external charging aperture.The conveying of rubbish is by being undertaken by being arranged on the biogas that gas nozzle on a plurality of fan-shaped section of fermentor sprays into compression, and wherein, each fan-shaped section can be controlled separately, flows to keep rubbish embolism shape between charging aperture and discharge gate.
EP 0 476 217 A1 disclose a kind of heatable fermentor, and wherein, delivered fresh and rot are transported to fermentor and the rot that produces is transported to the rot discharge gate by agitator as bacterial inoculum.Also can add inoculum like this in the Valorga method according to EP 0 192 900 B1 introduction in front.
EP 0 794 247 A1 disclose a kind of fermentor, wherein, the fermentate the inside of packing into are provided with in the swing roller of helix.By this helix fermentate embolism shape is transported to the rot discharge gate from charging aperture.This conveying can be undertaken by rotating and reverse of cylinder, wherein just changes, and the conveying of fermentate on being longer than oppositely on the time of delivery on the fermentate discharge gate direction just, thus reach the fermentate time of staying of predesignating.
In above-mentioned known method, handle greater than 25% garbage drying than higher dried material content (TS).
When handling flowable wet refuse, for example use so-called material dissolution device (pulper) according to DE 197 04 065 A1, wherein, rubbish employing diluent liquid is diluted and is stirred and fragmentation by blender, thereby formation suspension and organic principle are dissolved in the diluent liquid.In this disclosed solution, mix and undertaken by agitator, its blade constitutes like this, makes partly to constitute perpendicular flow in the material dissolution device.The shortcoming of this solution is, on the one hand for the geometry that constitutes the stirring vane complexity needs very high device technique spending, and on the other hand these blades because the floating thing and the impurity that contain in the suspension are subjected to very strong wearing and tearing.
Because rubbish to be processed also to contain not be the heavy burder and the impurity of insignificant ratio, so particularly adopt the solution (EP 0 794 247 A1, EP 0 476 217A1, DE 197 04 065 A1, DE 196 24 268 A1) of mechanical conveying equipment to produce quite serious wearing and tearing, because employed conveying equipment and other built-in fittings can be owing to the deposit that contains impurity/heavy burder damages.
Summary of the invention
Therefore purpose of the present invention is, a kind of unified approach that is used to handle the rubbish that contains organic principle is provided.The present invention also aims to be provided at the material dissolution device and reactor and a kind of corresponding therewith refuse treatment plant that use in this method.
This purpose by a kind of method with claim 1 feature, a kind of material dissolution device with claim 5 or 19 features, a kind ofly have the reactor of claim 28 or 36 features and be achieved by a kind of refuse treatment plant with claim 41 feature.
According to preferable methods of the present invention have mechanical treatment rubbish, in the material dissolution device, dissolve organic principle, hydrolysis contains biological suspension and ferments in the fermentation level from what the material dissolution device was discharged in reactor, during wherein, with hydrolysis or the process water that obtains in the fermentor circulate as recirculated water.According to the present invention, depend on the granularity of the garbage mixture of mechanical treatment, be chosen in the material dissolution device and/or the reactor that will use on the equipment.The advantage of doing like this is, the method that different garbage mixtures is used is identical and only environment division material dissolution device and reactor depend on the rubbish granularity and select.Preferably " limit granularity " is about 80mm.
What have advantage is that hydrolysis is attached to corresponding enforcement wet method macerate with hydrolysis reactor or wet oxidation in the reactor.
For the biological suspensions that will discharge basically imports in the fermentor, can have the suitable separating step that separates with impurity, heavy burder, fibre material etc. from solid material.
According to the present invention, the organic principle of the about 80mm of maximum particle size dissolves in a kind of material dissolution device, it replaces known mechanical agitator and has pneumatic to a certain extent agitator, wherein, the gas of air mixes by the suspension in the material dissolution device by importing preferably, and organic moiety is transferred in the dilution water as solution, produces suspension by it in the material dissolution device and flows.
The device technique spending that in fact this pneumatic solution does not have wearing and tearing also can be starkly lower than in the traditional solution situation realizes.Situation shows that organic principle can dissolve in the obvious shorter time in than the design of adopting mechanical agitator.
What mixing can be further improved is that nozzle of air supply is the parts of pneumatic pump, can be periodically or the conveying that circulates continuously at the material dissolution internal tank by its suspension.In this regard, also gas can be imported the bottom of material dissolution container, thereby the impurity/heavy burder that accumulates in the there mixes with gas also.
This pneumatic pump preferably has interior pipe, on the end section of its underpart, be provided with have nozzle of air supply can be by suspension circulation or through-flow nozzle plate and be configured on the end section at an upper portion thereof in the discharge gate of the suspension carried in the pipe.
In a kind of embodiment of special efficient operation, with discharge gate shock plate is set apart, the mixed material of being carried by pneumatic pump also decomposes with this plate of high speed impact.Meanwhile organic moiety changes water over to.Inert material particle and grit sink and can discharge.The fibre material that suspension contains and solid material part discharges from the organic principle that stops rubbing each other during this conveyings of shock plate and add.
In a kind of preferred embodiment, shock plate to small part limits exhaust chamber, the gas that circulates by its discharge.
What have advantage under the situation of bulk container volume is that a plurality of pneumatic pumps are set in the material dissolution container.
What have advantage especially according to the present invention is that interior pipe double braid covering constitutes, wherein, nozzle of air supply then or be arranged on inner cylinder indoor or be arranged in the doughnut and separately other chambers be used to hold heat medium, thereby interior pipe plays the effect of heat exchanger simultaneously, remains on the process temperature by its suspension.
Mixing can further improvedly be to be provided for the guide plate of water conservancy diversion on the excircle of interior pipe.Because these guide plates are fixedly installed in the material dissolution container, so its wearing and tearing are minimum.
Under the purposes situation of determining, what have advantage is that a plurality of material dissolution containers can series operation.
Be used for the rubbish organic principle foundation material dissolution device of the present invention at the minimum about 80mm of granularity of determining of diluent liquid dissolving, have at least one mechanical agitator according to the present invention, its adjacent separately mixing component has opposite throughput direction.The advantage of doing like this is that the mixture that is in the material dissolution device is carried between mixing component back and forth, thereby can improve abrasive wear and improve organic dissolving with this.
Mixing component is preferably disposed on the tumbler, and its blade angle of climb is separately approximately with 180 ° of displacements.The quantity of moving blade can be selected arbitrarily, but preferred even number, for example 6 moving blades.
Moving blade can be distributed to the discharge gate of the impurity/heavy burder of separation equably always from the feed gate of rubbish on tumbler.
It is contemplated that equally the material dissolution utensil has a plurality of parallel tumblers, wherein, tangent zone of each self-forming of the moving blade of each tumbler.
In a kind of special embodiment, in the zone of outlet, can be provided for the inlet duct of impurity/heavy burder eddy flow.In this regard, the gas of input can circulate, thereby reduces required gas flow.
The material dissolution container can have the rectangle moulding on the vertical section, wherein, its length L 1 is equivalent to four times height h1 at least.
According to the present invention, use a kind of reactor at hydrolysis and/or wet method macerate during from the suspension of the rubbish of the about 80mm of maximum particle size, have and be used for the mechanical mixer that mixed material is mixed and have conduit around blender.In this regard, blender is controlled like this, mixed material can be extracted by conduit from reactor top side direction reactor bottom side, wherein, form the annular flow that rises in the outside of conduit.
For optimizing hydrolysis or wet method macerate, conduit has the axial lengthening position that is used to change its length or height.Therefore corresponding swedged a plurality of conduits, for example 3 conduits can be set in reactor.
The required oxygen of hydrolysis or wet method macerate can near and/or the regional interior apparatus of oxygen supply supply of blender by the bottom.
Can have mensuration O for regulating the oxygen amount that to carry
2The O of content
2Probe, thus depend on these signals, can regulate like this axial location and/or the mixed material minute surface of axial lengthening position, conduit, it is best that it is preferably produced, just 100% coefficient of oxygen utilization almost.
Physical dimension ratio for example if any:
Duct height H1 corresponding to the 8-10 of conduit diameter d1 doubly,
The effective diameter d2 of reactor, just internal diameter corresponding to the 4-6 of conduit diameter d1 doubly,
Reactor bottom to the distance from bottom H2 of conduit doubly corresponding to the 1-2 of conduit diameter d1,
Distance between mixed material minute surface and the conduit corresponding to the 2-3 of conduit diameter d1 doubly,
Variable height displacement H4 between mixed material minute surface and the conduit is 0.5-2 a times of conduit diameter d1,
The upflow velocity v1 that circulates moves between 0.1m/s and 0.8m/s,
Conduit diameter d1 is between 0.5m and the 1.5m according to mixed material composition and dry matter ratio.
Cooling medium by the circulation conduit can prevent effectively that mixed material is overheated.
Can connect in principle a plurality of hydrolysis or wet method macerate are set.
Be used for handling the foundation that the contains organic matter suspension reactor of being carried of the present invention that obtains from the garbage mixture of the about 80mm of minimum particle size, as the inlet duct that is used for the mixing arrangement that mixed material mixes is had the preferred oxygen of gas.
Air inlet is preferably undertaken by near a large amount of nozzles of air supply the reactor bottom and can be regulated by surveying the gas probe.
Preferred gas can circulate by pump.
For raising mixes, the waste gas that forms in the reactor can be transported near the mixed material in motor bottom by air blast equally.
The refuse treatment plant of equipment material dissolution device preferably has the solid material treating apparatus, is used to separate and wash the impurity/heavy burder of discharging from the material dissolution device.
Can also have the level of separation according to refuse treatment plant of the present invention, be used for fiber or similar material are separated with the decomposition suspension of discharging from the material dissolution device.This separation level preferably has washing facility and dehydrating press, can purify the fiber/floating thing that is separated and be transported to other application apparatus by it.
Refuse treatment plant and fibre material separator are additional can equip sand washer, is used for washing the fine sand that still is contained in behind the defibre material in the remaining suspension liquid (dilution water).
The dilution water that contains organic principle preferably is transported to fermentor, and method is that these organic principles are converted to biogas and/or are transported to wet method macerate or wet oxidation as mixing water.
The dilution water that discharges from organic principle returns the material dissolution device then again, and wherein, superfluous water can be transported to effluent purifying device.
The solid material part that is transported to the material dissolution device preferably drops to bottom line by preposition solid material treating apparatus.
Situation shows, processing time is by being reduced to from common 61 days about 29 days according to treatment facility of the present invention, method be with the decomposition suspension of material dissolution device at least as shunting through hydrolysis and discharge fiber and solid material subsequently, wherein, solid material is at least as shunting process wet method macerate or wet oxidation to obtain the mixed material of oxidation.
During hydrolysis the aerobic acidifying of the suspension of material dissolution device and will be still undecomposed organic material decompose equally, thereby can be transported to the fermentor of additional materials.
At least one shunting of the solid material that decomposes can be carried out drying and compression equally in the separation equipment of hydrolysis postposition, be used to make the moulded parts of gasification or combustion apparatus.Compress under the situation that is preferably in low pressure and adds adhesive and carry out, this adhesive is until carry out the effect that bond is played in roasting in gasification or combustion apparatus.Adhesive can for example be produced by the plastics itself that separate when garbage disposal or provide.
For gasification, moulded parts must keep " gasification is stable " under the roasting state, that is to say that moulding remains to gasification always.
In a kind of embodiment of treatment facility, the suspension of handling during hydrolysis is delivered directly to fermentor.These waste water still can have very high solid material part because when fermentation, produce the waste water of discharging then, so can not mix with dilution water or recirculated water.But can reach mixing thus, be about to solid material and on separation equipment, from waste water, obtain substantially separating, thereby make waste water not contain solid material.The solid material of dehydration can carry out the wet method macerate then, wherein, a shunting of no solid material waste water can be mixed into suspension with solid material again for optimizing and revising solid material content.
In the another kind of embodiment of treatment facility, solid material enters wet method macerate or wet oxidation from hydrolysis.In this regard, breathe and nitride is discharged as ammonia by the decomposable oxide of the non-anaerobism of oxygen supply.
The mixed material of wet oxidation rear oxidation can be transported to have the solid material separator, the separation equipment of solid material screening and washing facility and dehydrating press.In this regard, the waste water that produces in the solid material separator uses and/or is transported to effluent purifying device as the dilution water of material dissolution device.The former synthetic that forms in the dehydrating press can directly be handled.
Preferably when the wet method macerate, carry the mixing water that when recirculated water mixes with the waste water of fermentor, forms to mixed material.
The oxidation mixture material that produces when the wet method macerate can be used to produce former synthetic and waste water by separation equipment.In this regard, waste water can mix with dilution water and/or be transported in the effluent purifying device.Former synthetic can carry out the back dipping and carry out drying and/or directly processing.
The waste gas that forms when hydrolysis and wet method macerate can be transported to air washer to discharge ammonia.
Treatment facility has according to material dissolution device of the present invention and agitator air and for hydrolysis and/or be used for the wet method macerate and have according to reactor of the present invention and mechanical agitator in particular for the garbage mixture of the about 80mm of mechanical treatment maximum particle size.
Be the garbage mixture of the about 80mm of mechanical treatment minimum particle size, preferably use according to material dissolution device of the present invention and mechanical agitator and for hydrolysis and/or be used for the wet method macerate and use foundation reactor of the present invention and mechanical agitator.The latter also can use aspect littler granularity." limit granularity " can depend on institute's rubbish to be processed and change, and alleged 80mm is for giving an example.
What have advantage is to carry out cleaning of mixed material at least in the reactor of wet oxidation under corresponding work mode situation in reactor.
Ammonia in the waste gas that forms during for release hydrolysis and wet oxidation, the air washer of growth ammonia inside can having.
Other have the theme that further constitutes other dependent claims of advantage the present invention.
Description of drawings
Below by accompanying drawing to a preferred embodiment of the present invention will be described in detail.Wherein:
Fig. 1 illustrates according to the present invention and is used for the material dissolution device schematic diagram of basic granularity less than the 80mm garbage mixture;
Fig. 2 illustrates the schematic cross-sectional of Fig. 1 material dissolution device;
Fig. 3, Fig. 4 illustrate material dissolution device alternate embodiments;
Fig. 5-7 illustrates the schematic diagram of Fig. 1 material dissolution device different operating state;
Fig. 8 illustrates a kind of scheme of Fig. 1 material dissolution device;
Fig. 9 illustrates the material dissolution device of refuse treatment plant and Fig. 1;
Fig. 9 a illustrates a kind of selectable working condition of Fig. 9 to be simplified and enlarged drawing (also with reference to Figure 19);
Fig. 9 b illustrates the another kind of selectable working condition of Fig. 9 to be simplified and enlarged drawing (also with reference to Figure 19);
Figure 10 illustrates the detail drawing of Fig. 9 hydrolysis and wet method macerate;
Figure 11 illustrates the material dissolution device of Fig. 1 according to two parallel connections of the present invention;
Figure 12 illustrates and is used for a kind of vertical section according to the present invention selectable material dissolution device of basic granularity greater than the 80mm garbage mixture;
Figure 13 a-13d illustrates the cross section for example of Figure 12 material dissolution device;
Figure 14 illustrates being connected in series of Figure 12 material dissolution device;
Figure 15 illustrates and is used for hydrolysis or the basic granularity of the wet method macerate vertical section less than the reactor preferred embodiment of 80mm garbage mixture;
Figure 16 illustrates the cross section of another preferred embodiment of reactor that is used for hydrolysis or wet method macerate;
A plurality of reactors was connected in series when Figure 17 illustrated hydrolysis;
A plurality of reactors was connected in series when Figure 18 illustrated the wet method macerate;
Figure 19 illustrates the simplified flow chart according to refuse treatment plant of the present invention;
Figure 20 illustrates a kind of hydrolysis reactor that is used for basic granularity greater than the 80mm garbage mixture;
Figure 21 illustrates and a kind ofly is used for basic granularity greater than the selectable wet method macerate of 80mm garbage mixture reactor;
Figure 22 illustrates the detailed feed separation equipment of Figure 19;
Figure 23 illustrates the detailed separation equipment of Figure 19; And
Figure 24 illustrates the detailed flow chart of Figure 19.
The specific embodiment
Fig. 1 illustrates the basic structure of material dissolution device 1, in this material dissolution device, the inoculation material of being carried 2, preferably the organic principle of rubbish for example dissolves in the dilution water 4 in diluent liquid, thereby has the mixture 8 with about 5-10% dried material content in the material dissolution device 1.The garbage mixture that preferably is transported to material dissolution device 1 has the granularity of the most about 80mm.Rubbish 2 and dilution water 4 are transported to material dissolution container 6 by feed gate 10 separately.Bottom 12 tapers of material dissolution container constitute and connect with discharge gate 16 on outlet 14, can discharge the impurity/heavy burder 18 that is deposited on the conical lower portion 12 by this gate.In the zone of conical lower portion 12, constitute another discharge gate 16, discharge containing organic suspension 20 and handling of material dissolution device 1 in, decomposing by this gate, in circulation, pass through feed gate 10 then and carry again as dilution water 4 according to Fig. 9.
In the inside of material dissolution container 6 pneumatic pump 24 is set, by its-as following also to introduce in detail-mixture 8 mixes in the inside of material dissolution container.In the embodiment shown in fig. 1, pipe 26 in pneumatic pump 24 has, it has the nozzle plate 27 with a large amount of nozzles of air supply 28 with the 6 coaxial settings of material dissolution container and on its underlying charging aperture shown in Fig. 1, preferably the gas of air can spray in the interior pipe by these nozzles.Nozzle plate 27 can be by suspension 8 circulation.Nozzle of air supply 28 is by compressed air piping 30 and can be connected with intermediate-pressure accumulator or air accumulator 34 by the control valve 32 of plant control unit control, and the latter is charged to for example pressure of 3-8bar by air compressor 36.This compressor carries air 40-that is to say by exhaust chamber 42 suction of suction channel 38 from material dissolution container 6 tops 22, this conveying air 40 circulates equally and the corresponding control by control valve 32 from air accumulator 34, spray into by compressed air piping 30 and nozzle of air supply 28 in the pipe 26.
By conversion equipment and/or metering device 66 along air compressor 36 following currents, air accumulator 34 can utilize control valve, pulsation conversion just.In this regard, to feed bypass pipe 154 pressurizations in the compressed air piping 30 along control valve 36 following currents.In this case, mixture 8 blast pressure that can be equivalent to 1.5 times of pressure gauge height circulates.
Therefore have conversion/metering device 66 in compressed air piping 30, admission line 156 extends in the outlet 14 of material dissolution device 1 from this device.Impurity and heavy burder also can and mix along with compressed air motion thus, thereby discharge the organic matter that adheres to and transfer in the mixture 8.
Fig. 2 schematically illustrates the pneumatic pump 24 of the cross section of material dissolution container 6 together with the center setting, and wherein, interior pipe 26 has the double braid covering 46 that is flow through by so-called heat medium.In this regard, nozzle of air supply 28 be arranged on by interior pipe 26 around the inside of cylinder chamber.
In a kind of selectable scheme of foundation Fig. 3, nozzle of air supply 28 also can be arranged on by double braid covering 46 around doughnut in, thereby heat medium flows through the cylindrical chamber at center.
Under the very large situation of vessel volume, have advantage be in material dissolution container 6, can be provided with a plurality of, for example three pneumatic pump 24a, 24b, 24c.
Discharge gate top at interior pipe 26 is provided with shock plate 44 apart, and it is to lower part restriction exhaust chamber 42 and can be by carrying air 40 circulation in the side.
For suspension 8 is heated to process temperature, interior pipe 26 has double braid covering 46, wherein, import heat medium in the doughnut that forms, thereby interior pipe 26 plays the effect of heat exchanger.The shell of material dissolution container 6 has heat insulation layer.
Be the dissolving material, the inoculation material 2 in the input material dissolution container 6 is at first adjusted to the dried material content TS of about 5-10% by the dilution water in the delivery cycle 4.By control compressed air is sprayed into by nozzle of air supply 26 subsequently control valve 32.In an illustrated embodiment, the operation of preferred a kind of pulsating in this regard, wherein, pulsation for example is at interval about 5-10 second.Process temperature is adjusted between 50-70 ℃ by the heat medium that flows in the double braid covering 46 in this regard.Form compressed air bubble 50 by the pulse inside of each comfortable pneumatic pump 24 of this compressed air, the piston that it is similar to piston pump is 12 suction mixture/suspension 8 from the bottom like that, flow 48 thereby form suspension upwards in the inside of interior pipe 26.This suspension that is aspirated is then to hit shock plate 44 at a high speed in the scope between can 10-20m/s, wherein, and by impacting and frictional energy carries out the machinery decomposition and organic principle is dissolved in the dilution water 4.
The inert material particle that rubbish contains, grit, impurity/heavy burder etc. obtain dissolving and deposit to conical lower portion 12.In addition, fibre material obtains discharging and entering in the suspension, wherein, by the shearing force that produces film and other solid portions is removed from the organic components of adhering to.Impurity/the heavy burder that produces is discharged by discharge gate 16 on material dissolution container 6 bottoms 12 and outlet 14.Situation shows, adopts according to material dissolution device of the present invention, and organic principle can obviously dissolve more fast and with device technique spending still less than the situation that adopts the traditional material dissolution device that wherein uses mechanical agitator or similar agitator.
Now the function of pneumatic pump 24 is elaborated once more by accompanying drawing 5-7.
Fig. 5 illustrates the material dissolution container 6 under the charging inactive state, wherein, inoculation material 2 is adjusted to the dried material content of alleged 5-10% by adding dilution water 4 in this container.The horizontal plane 54 of mixtures of materials is adjusted in this regard like this, make its be in pipe 26 top discharge gates in the pneumatic pump 24 below.By the pneumatic circulation of introducing by Fig. 1, flowing by the suspension that makes progress 48 sucks suspension and gets rid of to shock plate 44 and flow downward in by interior pipe 24 and the doughnut by the shell restriction of material dissolution container 6 again then.The suspension part of upwards carrying is size like this, and the horizontal plane 54 of material dissolution container 6 inside is descended with degree Δ h shown in Figure 6.When air sprayed into end, after just each comfortable compressed air pulsation finished, the horizontal plane 54 of column of suspension in interior pipe 26 inner declines (referring to Fig. 7) and doughnut 56 rose again, circulates and can begin until the basic status of adjusting to Fig. 5-next air inlet.The above-mentioned impact of flowing and passing through suspension impact plate 44 by material dissolution container 6 inside, suspension produces extremely strong mixing, thereby the organic principle of inoculation material 2 is very fast and dissolve with high efficiency, in addition fibre material and impurity/heavy burder deposition.Because this strong mixing to material dissolution container 6 inside needs moving component in fact anything but, minimize so compare with the tradition dissolving according to the wearing and tearing of material dissolution device 1 of the present invention.
What mixing can be further improved is, has built-in fitting according to Fig. 8 in doughnut 56, for example downward-sloping guide plate 58, and their are inevitable by downward suspension flow (Fig. 6) circulation, thereby produce further shearing force in suspension.Because these guide plates 58 fixedly install, so its wearing and tearing minimize equally.In an illustrated embodiment, guide plate 58 is arranged alternately on the inner periphery shell of material dissolution container 6 and on the shell of interior pipe 26, thereby the waveform shown in producing in doughnut 56 flows.Self-evident, replace guide plate 58 and also can use other built-in fittings or filling member.
Fig. 9 illustrates a kind of refuse treatment plant, wherein uses the above-mentioned material dissolution device 1 according to Fig. 1.
In this refuse treatment plant, connect several steps that are used for the separating solids material in the front of material dissolution device 1.In this regard, rubbish 60 to be processed at first-when needing after fragmentation-be transported in an illustrated embodiment the screening plant 62 that constitutes as rotary screen.The screenings 64 of granularity between 80-200mm is then by material preselector or conversion and/or metering device 66 or directly get rid of or separate by an additional step.In an illustrated embodiment, can a shunting or all solids materials flow be transported to screening plant 68, on this equipment, screenings 64 be separated into the light material 72 of heavy burder/impurity 70 and pollution, it is discharged respectively by conversion and/or metering device 66.
Be rich in organic screenings 78 and can be transported to mixing apparatus 74 by conversion and/or metering device 66, the dilution water 4 that utilizes denitrogenation on this equipment is with its dilution and be processed into the suspension 76 of solid material content 5%-15% by blender 268.
Impurity/the heavy burder 18 that produces in the material dissolution device 1 is discharged by discharge gate 16 and is transported to wash mill 80 from material dissolution device 1, wherein, and the organic principle that they adhere to by working water 82 purifications of being carried purifying area 106 in.Heavy burder/the impurity 84 that purified is transported to ferrous metal separator 86 and nonferrous metal separator 88 then, thereby materials flow 84 correspondingly is divided into iron content part 90, nonferrous metal part 92 and other materials 94.
Be transported to the fibre material separator 98 that also constitutes from wash mill 80 jointly by discharge gate 16 decomposition suspension 20 of from material dissolution device 1, discharging and the working water of polluting 96 as rotary screen.In this fibre material separator 98, fiber separates with the water 102 that contains organic principle with floating thing 100.Fiber/floating thing 100 purifies by the working water 82 that interpolation is transported to washing facility purifying area 106 on solid material screening and washing facility 104.This purification process can also add supported thus, promptly carries the recirculated water 108 that is branched off into dilution water 4 cycle of treatment to purifying area 106.
Two wash mills 80,104 utilize the screw conveyer that is obliquely installed to constitute in the embodiment that is introduced separately, and the materials flow separately that purify is transported to discharging by solid material discharge gate 110 at last in the lump of purifying area 106 by them.In purifying area 106, each self-separation of organic principle and solid material.Under the situation that needs purify very by force, this purification is implemented by working water 82 basically, this purification is being required can strengthen recirculated water 108 parts under the lower situation.
Purified and solid that the solid material discharge gate by wash mill 104 110 is discharged and fibre material 112 then dehydrating press 114 in dehydration and the solid material 116 of dehydration is transported to hot re-use device or be used for after the macerate again of heap.
The water that contains decomposing organic matter 118 that produces in the dehydrating press 114 mixes with the organic washings 120 that contain that discharge from purifying area 106 subsequently.This materials flow contains the part fine sand, and it is separated in sand washer 122.For this materials flow also transports from organic water 102 of containing of fibre material separator 98.In sand washer, fine sand part 124 is separated by the effect of agitator 126, purifies the organic principle that adheres to by sand removing hole 123 discharges and by adding working water 82.The fine sand 124 of preliminary clearning is transported to fine sand wash mill 128 then, and its basic structure is corresponding with wash mill 80,104, thereby repeats no more.The fine sand 130 that purified can be carried then and be used for underground and Reuse of materials device road construction.
The recirculated water 132 of the high organic content that exists after the washed-out sand is intermediate storage and by pump 136 or be transported to fermentor 138 or be delivered directly to heat exchanger 140 as recirculated water 132 in intermediate storage 134 then, is heated to process temperature by heat medium 142 and imports in the material dissolution devices 1 by feed gate 10 as dilution water 4 then in this heat exchanger.Heat medium 142 also can be used for the heating of pneumatic pump 24 double braid coverings.
According to the process process, the organic principle that is transported to the water of fermentor 138 converts biogas (methane gas) 144 to by methanation.
The recirculated water 132 that the organic waste water 146 of removal that fermentation level back exists exists when needing then mixes to be incorporated in the heat exchanger 140 and is heated to process temperature.In waste water 150 discharges and importing sewer that unwanted superfluous water 147 in the circulation are transported to waste water purification device 148 and will purify.A shunting of the waste water 150 that purified is transported to wash mill 80,104,128 and sand washer 122 as working water 82, thereby the working water circulation also comes to an end.
What the organic principle that the suspension 20 that decomposes contains can separate from rubbish more rapidly is, the suspension 20 by conversion and/or metering device 66 material dissolution devices 1 at first be transported to aerobic hydrolysis or acidifying level 162 and after 1-4 days processing time fibre material separator 98 and sand washer 122 in from solid material release suspension 20.To be stored in the intermediate storage 13 as the recirculated water 132 of high organic content and be transported to fermentor 138 through the suspension 21 of such processing subsequently.
After 3-10 days the time of staying, the mixed material 23 of discharge oxidation and denitrogenation also discharges from solid material in separation equipment 168 in wet method macerate 164.Meanwhile the waste water 170 of the almost solids-free material of Xing Chenging is transported to material dissolution device 1 and/or is transported to effluent purifying device 148 by conversion and/or metering device 66 as dilution water 4 then.The former synthetic 212 that forms is handled.
The waste gas that forms when hydrolysis 162 and during wet method macerate 164 discharges ammonia jointly in acid air washing machine 172.
Can low-down device technique spending separate organic principle and remaining materials flow is divided into part-streams recycling or that can heap by above-mentioned refuse treatment plant.
According to Fig. 9, equally can conversion separating apparatus under working condition 98,104,114,122,128 and the suspension 21 that will in hydrolysis 162, handle be delivered directly to fermentor 138, wherein, from the waste water 132 of high organic content and treated suspension 21, produce slurry compositions 133 by conversion equipment and/or metering device 66.The waste water 146 that fermentor 138 contains solid material is transported to wet method macerate or wet method synthetic 164 by conversion equipment and/or metering device 66 as fermentate.
The mixed material 23 of wet method macerate 162 rear oxidations carries out feed separation according to Fig. 9 a for the separating solids material utilizes filter 206, sand washer 122 and dehydrating press 208.The waste water 170 of the no solid material that obtains when feed separation uses as dilution water or recirculated water 4.The solid material 212 that separates when feed separation can carry out macerate 214 again, and wherein, the dried product 216 that produces in the macerate 214 wherein separates surplus material 224 through screening 218 with synthetic 212.Surplus material for example is transported to the material re-use device.
If after fermentor 138 main supply hydrolysis 162, contain the suspension 21 of solid material, contain the circulation that the waste water 146 of solid material can only enter dilution water 4 so, and as shown in Figure 9 with Fig. 9 b in amplify shown in, solid has utilized solid material separator 98, solid material screening and washing facility 104 and rearmounted dehydrating press 114 to separate in separation equipment with fibre material before this.The adjusting of waste water 146 or control are undertaken by conversion and/or metering device 66.In fermentor 138 fermentation and in separation equipment 98,104,114 separated solids material 116 be transported to wet method macerate 164, wherein, the rotten water of extruding in separation equipment 98,104,114 171 is reused for solid material 116 as shunting at least and mixes, to adjust desirable dry-matter content in the wet method macerate 164.For example, dry-matter content can be between 5-15%.Unnecessary rotten water 171 adds to the waste water 170 of wet method macerate 164 as recirculated water and therefore can be used as dilution water 4 for example flows to material dissolution device 1.
According to the present invention, containing the result that the ultimate density of the waste water 146 of solid material produces in separation equipment 98,104,114 from fermentor 138 is, return the solid material of extruding 116 by rotten water 171 to the small part of no solid material, can best adjust the solid material content in the wet method macerate 164 and obviously reduce the size of wet method macerate reactor 192 and the unnecessary rotten water 171 of no solid material can be imported in the circulation of dilution waters 4.
Figure 10 illustrates the flow chart that adopts hydrolysis 162, wet method macerate 164, separation equipment 168 and acid air washing machine 172.
The suspension 20 and the such organic material that decomposes that utilize hydrolysis 162 aerobic acidifyings to decompose can use it equally for fermentation in fermentor 138.From the decomposable material of non-anaerobism, separate attaching particles and dirt.
Flow to reactor 174 near the bottom of decomposition suspension 20 on air-blast device 178 of material dissolution device 1.By importing oxygen and mixing after the processing time that is incorporated in 1-4 days as near the extraction of treated suspension 21 from mixed material minute surface 186 by 176 pairs of mixed materials of operation agitator.
In wet method macerate 164, the decomposable organic matter of non-anaerobism is breathed and nitride is discharged as ammonia.Therefore in wet method macerate 164, recirculated water 132,133,4 is carried out denitrogenation and prevent to destroy biological in the fermentor 138 and hinder that gases produce and the ammonia concentration of decomposition efficiency rise by air feed.
Wet method macerate 164 mainly has reactor 192, and the inside is provided for agitator 194 (referring to Figure 12) that mixed material 23 is mixed.Near the bottom of reactor 192, have the air-blast device 196 that is used to send oxygen, supply with oxygen by the apparatus of oxygen supply identical 180 with hydrolysis 162.On mixed material minute surface 198, be formed for collecting the exhaust air chamber 200 that forms waste gas 202.
For avoiding mixed material overheated when the wet method macerate 164, has cooling unit 182.Cooling unit 182 with immerse mixed material interior feed 184 with return 204 and be connected.Be the cooling and mixing material,, can discharge the unnecessary heat in the mixed material thus by feeding 184 and return 204 and carry cooling agents.
In macerate 214 again, the former synthetic 212 of dehydration is processed into the separable dried product 216 of dry-matter content 75%-85%.Be separator 218 after the macerate 214 again, the inert material 222 that generation is used to store on this device also is transported to the material re-use device with remaining material 224.
The waste gas 188,200 that to collect in the exhaust air chamber 190,202 of hydrolysis reactor 174 and wet method macerate 192 is transported to the mixer 226 of acid air washer 172 and discharges ammonia there.Under the situation of adding hydrochloric acid or sulfuric acid 228, can obtain sal-ammoniac or sulfate 230 as commodity.In this regard, in the bottom section of mixer 226, assemble water-acidic mixture 232, utilize circulating pump 236 to extract and spray into again, thereby can produce surface reaction with waste gas 188,200 in top side from mixer 226 by spray equipment 234.According to the degree of treatment of water-acidic mixture 232, a part is extracted as the sal-ammoniac of finished market product or sulfate 230 by conversion and/or metering device 66 at circulation time.The discharge air 238 that forms denitrogenation in this process can discharge odoring substance in the purification level 240 of postposition, be discharged in the atmosphere as the process air 242 that purifies.
Figure 11 illustrates a kind of scheme of material dissolution device, can almost move continuously by it.In this embodiment, two or more material dissolution container 6 front and back connect, and wherein, each container has unshowned pneumatic pump among Figure 10.
Figure 12 illustrates a kind of basic structure of selectable material dissolution device 1.1, and wherein, the organic principle of the inoculation material of being carried 2 and/or the screenings 78 of screening plant 62 dissolve in dilution water 4.Preferably the material dissolution device 1.1 according to Figure 12 is used to handle bulk rubbish, and is used to handle single batch biologic garbage according to the material dissolution device 1 of Fig. 1.In this regard, the granularity of the garbage mixture of being carried (after mechanical treatment) preferably is at least 80mm.Mixture 8 is diluted to the dry-matter content of about 1-15% in material dissolution device 1.1.Material dissolution device 1.1 has material dissolution container 6, and it is essentially the rectangular shape of " keeping flat " with length L 1 and height h1 on the vertical section.This height length is than preferably satisfying h1: L1 〉=1: 4.
Rubbish 278 and dilution water 4 are separately by being transported to material dissolution container 6 according to the feed gate 10 in this diagram left-hand end section.Constitute conical lower portion 12 in the illustrated right-hand end section according to Figure 12 at material dissolution container 6, it feeds has in the outlet 14 of discharge gate 16, can discharge the impurity/heavy burder 18 that is deposited on the bottom 12 by this discharge gate.Another discharge gate 16 of formation on conical lower portion 12 is discharged the organic suspension 20 that contains that decomposes by it in material dissolution device 1, the above-mentioned Fig. 9 of foundation handles and carries again by feed gate 10 as dilution water 4 then.
In the inner space of material dissolution container 6, setting has the agitator 270 of Motor Drive tumbler 272, tumbler also is provided with a large amount of moving blade 276a, b, c, 278a, b, c in the above by whole length L 1 extension of material decomposition container 6 basically.The rotating vane 276,278 of preferred even number.Shown embodiment illustrates six moving blades 276,278 for example, but also it is contemplated that other quantity.
Moving blade 276,278 has approximately separately with 180 ° of blade angle of climbs of displacement each other, thereby moving blade 276a, 278a and 276b, 278b and 276c, 278c have opposite separately throughput direction.Therefore mixture 8 accumulates between moving blade 276a, 278a and 276b, 278b and 276c, the 278c, forms eddy current 280a, 280b that abrasive wear carries, 280c thus and organic matter is carried out the transition to dissolving.Between moving blade 278a, 276b and 278b, 276c, form simultaneously reverse eddy current 282a, 282b, separated from one another and so help abrasive wear equally and support organic matter to carry out the transition to dissolving by their mixtures.Impurity/heavy burder 18 sinks in mixture 8 and for example is transported to conical lower portion 12 and therefore is transported to discharge gate 16 by conveying worm 284.
For making part complete and its decomposition attached to the organic matter on impurity/heavy burder 18, has inlet duct, by its will be preferably compressed air by admission line 156 and air compressor 36 pulsatings, just intermittently or continuously send in the outlet 14, impurity/heavy burder 18 rises to mixture minute surface 286 always and maintains a certain distance h2 thus.Distance h 2 can be selected by the amount and the Strength Changes of air inlet.The entire inner space of material dissolution container 6 preferably is full of mixture 8, wherein, on the top section relative with bottom 12 chimney 288 is set, and mixture 8 inside rises.Formation exhaust air chamber 240 above the mixture minute surface 286 in chimney 288, it is connected with air compressor 36 by suction channel 38, thus the compressed air of inlet duct 52 can circulate.
In addition, the working water 82 of waste water purification device 148 and the recirculated water 108 that is branched off into dilution water 4 cycle of treatment import in the material dissolution containers 6 in the zone of outlet 14, leave material dissolution container 6 thereby impurity/heavy burder 18 can be used as the solid material that purifies or clean.
Be to adjust process temperatures best in the material dissolution container 6, this container can to small part by double braid covering 46 around, carry heat medium 142 by it.Can have the heat insulation layer 47 that surrounds material dissolution vessel 6 and double braid covering 46 in addition.
Figure 13 a-d illustrates the shape of cross section for example of the material dissolution device 1.1 among Figure 12.In this regard, the 290 expression moving blades 276,278 of the circle shown in the dotted line utilize the circular trace of its blade point description.
It is contemplated that according to Figure 13 a that like this material dissolution container 6 utilizes a circular cross section or utilizes two parallel vertical walls 292,294 to constitute according to Figure 13 b, they interconnect by semicircular base wall 295.Material dissolution container 6 can particularly constitute as hexagon according to Figure 13 c as polygon equally, and wherein, the horizontal expansion of base wall 295 is shorter than relative top wall 297.In Figure 13 d, material dissolution container 6 utilizes the rectangular cross section with the vertical wall 292,294 of circular arc to realize, wherein, the tumbler 274,296 of two parallel distributions is set in the inner space of material dissolution container 6, circular trace of its blade each self-described of point 290,298, they form one tangent regional 302 jointly.
Can connect a plurality of material dissolution devices 1.1 successively according to Figure 14, wherein, supply with the suspension 22 that in preposition material dissolution container 6a, produces to the material dissolution container 6n of postposition.Air inlet is preferably undertaken by shared air compressor 36.Impurity/the heavy burder 18 of discharging is preferably by shared conveyer 304, and for example conveying worm is transported to wash mill 80 and therefore is transported to other process steps according to Fig. 9.As selection, can in the purifying area 106 of wash mill 80, import recirculated water 108 to Fig. 9.
Figure 15 illustrates a kind of preferred embodiment that is used for the hydrolysis reactor 174 of the about 80mm garbage mixture of maximum particle size.The wet method macerate reactor 192 that is used for this granularity is identical with hydrolysis reactor 174 structures basically, thereby the explanation of back also is applicable to this reactor 192 or is applicable to wet method macerate 164.
The reactor 174 of hydrolysis 162 has the agitator 176 of adjustable transmission power, preferably blade agitators in inside.Agitator 176 by the conduit 244 of double braid covering around, this conduit end face and reactor bottom 246 and reactor head 248 at a distance of and preferably immerse in the mixed material fully.Agitator 176 is controlled like this, made its generation circulate 250, wherein, mixed material is carried by conduit 244 from the top down and is constituted the band shape that rises in the outside of conduit 244 in Figure 15 and flows 252.
Conduit 244 has doughnut 166 between wall and the outer wall within it, and this chamber and the top of unshowned cooling unit feed 184 and returns 204 with the bottom and be connected.Under the situation of control cooling unit, doughnut 166 is flow through by cooling agent, can prevent that thus mixed material is overheated.
Have apparatus of oxygen supply 180, it can be selected by near regional interior arm 254,256,258 oxygen supplys in mixed material in agitator 176 bottoms or upper and lower.Arm 254,256,258 can have a large amount of nozzles of air supply and raise bias voltage and inlet throttle by valve 262.Hydrolysis 162 required oxygen both can be used as liquid industrial oxygen, O just＞95%
2Exist, also can be as the oxygen that concentrates, O just＞95% on the air resolving device
2Handle.Under the few situation of mixed material charging, the surrounding air in the atmosphere can be sent in the reactor 174 equally.
In the top area of reactor 174, the exhaust air chamber 190 of the waste gas 188 that forms when being formed for being collected in hydrolysis 162.Exhaust air chamber 190 is by 186 restrictions of mixed material minute surface.Waste gas 188 can be discharged into acid air washer 172 by the pipeline 262 in the reactor head 248.
Top side by conduit 244 is adjustable axial elongated portion 264 vertically, can suck again by agitator 176 in company with banded 252 oxygen supplys that move upward of flowing, thus realization institute oxygen supply 100% utilization rate almost.
Coefficient of oxygen utilization can be by the O in the pipeline 262
2 Probe 266 is regulated by oxygen and the adjustment elongated portion 264 determining to send into.But coefficient of oxygen utilization also can by whole conduit 244 move axially and/or by changing mixed material minute surface 186 optimizations.
Propose to optimize the optimum condition of coefficient of oxygen utilization below for example:
Duct height H1 is corresponding to 8-10 times of conduit diameter d1.
The effective diameter d2 of reactor 174, just internal diameter is corresponding to 4-6 times of conduit diameter d1.
Distance between mixed material minute surface 186 and the conduit 244 is corresponding to 2-3 times of conduit diameter d1.
Variable height displacement H4 between mixed material minute surface 186 and the conduit 244 is 0.5-2 a times of conduit diameter d1.
The upflow velocity v1 of circulation 250 is between 0.1m/s and 0.8m/s.
Conduit diameter d1 is between 0.5m and the 1.5m according to mixed material composition and dried material ratio.
According to Figure 16, also have a plurality of above-mentioned conduits 244 in the reactor 174.For example can three conduit 244a, 244b, 244c be set each other in triangle.
According to Figure 17 and 18,, it is contemplated that series connection a plurality of reactors 174 or 192 for optimizing hydrolysis 162 or wet method macerate 164.In this regard, mixed material 23,23a, the 23b to handled material 21,21a, 21b or oxidation carries out again hydrolysis 162a, 162b or wet method macerate 164a, 164b.But reactor 174 or 192 also can parallel running.
Figure 19 schematically illustrates second flow chart that is used for the rubbish that contains organic principle is carried out garbage disposal.Reference numeral with according to the corresponding selection of the flow chart of Fig. 9, thereby repeat common device and materials flow are repeated no more for avoiding.
When garbage disposal begins, with rubbish 60 to be processed for example at first be transported to the screening plant 62 that constitutes as rotary screen.Rubbish 60 preferably has the dry-matter content of 45-60%.The screenings 64 that forms can or directly be handled or is transported to screening plant 68 as shunting at least, screenings 64 is separated into impurity/heavy burder 70 and pollutes light material 72, then with its each self-cleaning.
Be rich in organic screenings 78 and can be transported to mixing apparatus 74 as shunting at least, on this equipment, it is utilized the Partial flow dilution of denitrogenation dilution water 4 and be processed into the suspension 76 of solid material matter content 5-15% by blender 268.In addition, from suspension 76, isolate for example impurity such as image-tape, rope and electric wire 160 and discharge by the mechanical device of mixing apparatus 74.To be transported to the feed gate 10 of material dissolution device 1 or 1.1 through the suspension 76 of such processing and discharge coarse impurities 160.
Impurity/heavy burder 18 that material dissolution device 1,1.1 contains is discharged and is transported to wash mill 80 from material dissolution container 6 by discharge gate 16, will purify by the working water 82 of being carried in purifying area 106 attached to the organic principle on impurity/heavy burder 18 on this device.Impurity/the heavy burder 84 that purified like this can be transported to ferrous metal separator 86 and nonferrous metal separator 88 then, thereby the materials flow of impurity/heavy burder 84 is divided into iron content part 90 and nonferrous metal part 92 and unclassified stores 94.
The decomposition suspension 20 of discharging from material dissolution device 1,1.1 by discharge gate 16 is hydrolyzed 162 or 162.1.Preferably in hydrolysis 162,162.1, adjust to the dry-matter content of 5-15%.The waste gas 188 that hydrolysis 162,162.1 contains nitride is transported to acid air washer 172 for carrying out denitrogenation, and subsequently being to remove denitrogenation waste gas from odoring substance through purifying level 240 backs, is discharged in the atmosphere as the process air 240 that purifies.
The suspension 21 that to handle in hydrolysis 162,162.1 is transported to feed separation equipment 300, and the liquid 132 of high content of organics is separated with suspension 21 essentially no organic solid materials 116.When this feed separation 300, produce the purification fine sand 130 that can from process, extract as byproduct to a certain extent.
In fermentor, under the effect of methane bacteria, from the recirculated water 132 of high organic content, obtain biogas 144.Meanwhile produce the waste water 146 of discharging, the rotten water 159 that it can be used as discharge flows to wet oxidation 164,164.1.164,164.1 unwanted waste water 146 materials flows can be used as superfluous water 174 and are transported to effluent purifying device 148 to wet oxidation.
Figure 19 illustrates in addition, the solid material 116 of dehydration is being transported to compression device 312 as shunting at least after super-dry 311, be used to make the fuel that can on gasification or combustion apparatus 317, carry out heat/material re-use device, wherein, the adhesive of handling on liquefying plant 313 and/or processing and metering device 314 315 uses as adhesive and is transported to compression device 312.
Introduce hydrolysis 162.1, wet oxidation 164.1, feed separation equipment 300, separation equipment 168 and compression below in detail.
In the hydrolysis 162.1 as in the hydrolysis 162 that utilizes reactor according to Figure 15, the suspension 20 that decomposes is roughly purified and decomposes organic material like this, make it can be for the use of in fermentor 138, fermenting.In addition, the decomposable material of non-anaerobism is separated with dirt with attaching particles.
According to Figure 20, mixed material to the about 80mm of minimum particle size is hydrolyzed 162.1 basically in reactor 174, this reactor 246 has the inlet duct 178 that is used for oxygen supply near the bottom, what constitute the zigzag shape rising thus in mixed material flows 252, by it mixed material is mixed.Correspondingly do not need mechanical agitator.Air inlet can pulsating or is carried out continuously.
Supply with from the suspension 20 of material dissolution device 1,1.11 and extract in each reactor region in the middle of comfortable of suspension 21 of hydrolysis and carry out to reactor 174.
Oxygen that sprays into and the waste gas 188 that produces when hydrolysis 162.1 accumulate in the exhaust air chamber 190 above the mixed material minute surface 186.Because part oxygen passes through CO when hydrolysis 162
2Breathe, deactivation just, institute thinks that the best apparatus of oxygen supply 180 of regulating has O in reactor head 248
2 Measuring probe 266.
Be to strengthen the mixing of mixed material hydrolysis reactor 174 in, at least one shunting of waste gas 188 can and have big flow nozzle and is arranged on top arm 306 pulsatings of inlet duct 178 jet pipes 254 or sprays in the mixed material continuously according to the diagram of Figure 20 by suction channel 38, air compressor 36, admission line 136.What the waste gas 188 same formation zigzag shapes that spray into rose flows 308, and it is superimposed as one total mobile 310 with the oxygen flow 252 that sprays into.
The waste gas 188 that does not spray into mixed material is transported to acid air washer 172 and carries out denitrogenation as by Figure 19 by the agency of.
The dry-matter content of preferred mixture material is that the mixed material temperature in 5-15% and the reactor 174 is 70 ℃.Enough dissolved fats of this temperature or fatty compound.For can constant maintenance 70 ℃, the cooling liquid that has by refrigeration unit 182 flows through heat insulation layer 47.
In wet method macerate or wet oxidation 164.1, as foundation Figure 15 utilized in the wet method macerate 164 of wet method macerate reactor, the decomposable organic matter of non-anaerobism was breathed and nitride is discharged as ammonia.In oxidation 164.1, also therefore prevent to destroy fermentor 138 interior ammonia concentration biological and generation of obstruction gas and decomposition efficiency by 132,133,4 denitrogenations of air inlet recirculated water and rise.
To the wet oxidation 164.1 of the about 80mm mixed material of minimum particle size according to Figure 21 basically with the reactor 174 corresponding reactors 192 of hydrolysis 162.1 in carry out.But this reactor 192 also has near the inlet duct 178 of pulsating and the intermitten operation bottom, is used for the oxygen supply in the reactor 192 and mixed material mixed.Has above-mentioned O for regulating apparatus of oxygen supply 180
2 Measuring probe 266.
The waste gas 200 that forms at wet oxidation 164.1 equally can be by return mechanism at least as the flow divided pulsating formula or intermittently spray in the mixed material again.The waste gas 200 that does not return is transported to acid air washer 172 according to Figure 19 and carries out denitrogenation.
Has the steady temperature that heat insulation layer 74 and cooling unit 182 are used to regulate mixed material in addition.
Materials flow 20,21 when in addition, the conveying of the mixed material 23 of the solid material 116 of dehydration and the rotten water 159 of fermentor 138 and oxidation is with hydrolysis 162.1 in feed separation 200 is the same to be carried out in the intermediate reactor section.Be preferably in the dry-matter content of adjusting 5-15% in the reactor 192.The rotten water of being carried 159 uses mainly as dilution water.
The main distinction between hydrolysis reactor 174 and the wet oxidation reactor 192 is, carries more oxygen in wet oxidation 164.1 in mixed material, so that the substance transfer that will not carry out the transition to as yet in the solution arrives in this solution and to the compounding substances denitrogenation.The advantage of doing like this is, can cancel as the macerate again 214 in foundation Fig. 9 and Figure 10 flow chart, can also be significantly reduced to this thus.
Except the decomposable organic matter of non-anaerobism breathe and nitride as the ammonia discharge, in wet oxidation 164,164.1, can in reactor 192, carry out cleaning of mixed material according to control mode equally.In this regard, not only be in the solid material 116 in the mixed material, and the waste water 146 that also has fermentor 138 to contain and do not contain solid material can clean all.The waste water of compression device can utilize wet oxidation 164,164.1 to clean equally.
Provide this possibility by cleaning in the wet oxidation 164,164.1, promptly the mixture of solid material that no matter cleans (synthetic) or solid material and process water or waste water or pure procedure water or special-purpose waste water all can directly utilize on agricultural.
Preferably cleaning when wet oxidation 164,164.1 beginnings of wet oxidation 164,164.1 o'clock carried out, because utilize high temperature at that time that the microorganism utilizability of organic substance is improved.But also it is contemplated that when wet oxidation 164,164.1 finishes and implement to clean.
The time that cleans is depended on temperature at that time, thereby observes different cleaning the time according to temperature.For example, the desired efficient that cleans of German biologic garbage regulation will reach down more than time of one hour at 70 ℃.Must the corresponding prolongation time of staying under the lower temperature situation.
Clean is very important concerning will supplying with agriculture all biological former materials that utilize again particularly.Particularly biological and green rubbish, agricultural waste and energy plant, kitchen and dining room rubbish, defecation scum and dedicated process water and the waste water that belong to this type of.Come the biological products in the whole rubbish also to belong to this type of in Europe.
Figure 22 illustrates the schematic construction of feed separation equipment 300.The suspension of handling in the hydrolysis 162,162.1 21 is transported to the fibre material separator 98 that for example constitutes as rotary screen jointly with the pollution working water 96 in the wash mill 80.In addition, the working water of obtaining on effluent purifying device 148 82 can be used as dilution and is transported to fibre material separator 98.In fibre material separator 98, fiber is separated with the water 102 that contains organic principle with floating thing 100.
Fiber and floating thing 100 purify in purifying area 106 by the shunting of adding working water 82 on solid material screening and washing facility 104.This purification process can be supported thus, promptly by the purifying area 106 additional recirculated waters 108 that were branched off into dilution water 4 circulations before heat exchanger 140 of carrying.In purifying area 106, the organic principle of fiber and floating thing 100 separates with it.Very strong if desired purification is purifying area 106 additional transportation work water 82 so.Under the low situation about purifying of intensity, can strengthen the part of recirculated water 108.
Through the solid that purifies and discharge by the fibre material discharge gate 110 of washing facility 104 with fibre material 112 dewaters dehydrating press 114 in and the solid material 116 that dewaters is carried out wet oxidation 164,164.1.
The organic water 118 that contains that produces in dehydration extruder 114 mixes and is transported to sand washer 122 jointly with the organic washings 120 that contain from purifying area 106 discharges.Contain organic water 102 and can be transported to sand washer 122 equally.In sand washer 122, fine sand part 124 is passed through the effect separation of agitator 126 and will be dissolved by adding working water 82 attached to the organic principle on the fine sand part 124.The fine sand 124 of preliminary clearning is transported to fine sand wash mill 128 then like this, and its basic structure is with corresponding according to the wash mill 80 or 104 of Figure 19.The fine sand 130 that purified can be transported to the material re-use device in underground and the road construction then.
The liquid 132 of the high content of organics that when washed-out sand, produces as by Figure 19 by the agency of in intermediate storage 134 intermediate storage and be transported to fermentor 138 and/or use as recirculated water 132.
According to Figure 23, oxidation mixture material 23 working water 82 of wet oxidation 164,164.1 and be transported to fibrous matter separator 98 jointly on separation equipment 168 from the mixing water 121 of solid material screening and washing facility 104 and dehydrating press 114, with the waste water 170 that obtains no solid material, this waste water is transported to effluent purifying device 148 and/or uses as the dilution water 4 of material dissolution device 1,1.1 as introducing by Figure 19.
The washings 120 that contain organic water 118 and solid material screening and washing facility 104 that squeeze out in dehydration extruder 114 are transported to fibre material separator 98 jointly as mixing water 121.
According to Figure 24,, solid material 116 is carried out drying 311 being gasification among Figure 19 or combustion apparatus 317 when making the compression of fuel.The dry mixed material 311.1 of the best 15%-25% water content that forms after dry 311 is transported to compression device 312, particularly has agglomerate or the pelletizing device or the plodder of integrated blender or extruder.Compression is preferably under low pressure carried out, and wherein, is the adhesives that dry mixed material 311.1 adds as adhesive, so as will under low pressure to produce for example remain to roasting 317 as agglomerate and this moulded parts 312.1 of pelletizing always.In low pressure with add adhesive and compress the advantage that has for 315 times and be, reduce and be used to the part of appliance making the energy spending of moulded parts 317 and reduce compression device 312 for example as the wearing and tearing of blender.Utilize the compression 312 of adhesive 315 therefore to need the electric current of about 20kW also to produce approximately according to the present invention
The wearing and tearing cost, during being used for making the conventional compression of 1Mg moulded parts, then produce from rubbish 100kW electric current and
The wearing and tearing cost, produce thus approximately
Totle drilling cost/Mg.
Adhesive 315 preferably obtains from the screenings 72 that is produced, and it about 80% is formed and converted to the injected plastics material 313.1 of viscous by extruding or heat/chemical action on liquefying plant 313 by plastics.
For the adhesive 316 that does not have or plastic material 72 operational situations seldom, also can adopt to provide for example image-stone mortar or starch by handling and metering device 314 adds on the compression device 312 as organic or inorganic bond 314.1.In this case, preferred organic starch is for example as potato starch, because this starch lime white opposite can noresidue burn and release electricity and/or heat energy 317.1 lower with cost certainly.Lime white can be used as slag or mineral matter 317.2 is handled.
According to the quality of fuel requirements that will carry in subtend gasification or the combustion apparatus 317, compression device 312 completely or partially can be changed and materials flow 72 and 311.1 is delivered directly to hot re-use device 317.
A kind of method that contains organic principle rubbish that is used to handle is disclosed, wherein, in the unified method step, depend on the granularity of garbage mixture, use different material dissolution devices in diluent liquid, to dissolve organic principle and implement hydrolysis and/or wet method macerate, also disclose the material dissolution device and the reactor that are suitable for different reactors.A kind of suitable refuse treatment plant is disclosed in addition.
Reference numeral
1 material dissolution device
1.1 material dissolution device
2 inoculation materials
4 dilution waters
6 material dissolution containers
8 mixtures
10 feed gates
12 bottoms
14 outlets
16 discharge gates
18 impurity/heavy burder
20 suspension that decompose
21 suspension (hydrolysis) of processing
The suspension (hydrolysis) that 21a processes
The suspension (hydrolysis) that 21b processes
22 tops
The mixed material of 23 oxidations (wet method macerate)
The mixed material of 23a oxidation (wet method macerate)
The mixed material of 23b oxidation (wet method macerate)
24 pneumatic pumps
26 inner tubes
27 nozzle plates
28 nozzles of air supply
30 compressed air pipings
32 control valves
34 air accumulators
36 air compressors
38 suction channels
40 carry air
42 exhaust air chambers
44 shock plates
46 double braid coverings
47 heat insulation layers
48 suspension that make progress flow
50 compressed air bubbles
52 compressed air
54 horizontal planes
56 doughnuts
58 guide plates
60 rubbish
62 screening plants
64 screenings
66 conversion equipments and/or metering device
68 screening plants
70 heavy burders/impurity
72 gently expect
74 mixing apparatus
76 suspension
78 screenings
80 wash mills
82 working water
84 heavy burders that purify
86 ferrous metal separators
88 nonferrous metal separators
90 ferrous metal parts
92 nonferrous metal parts
94 unclassified stores
96 working water of polluting
98 fibre material separators
100 fibers/floating thing
102 contain the water of organic principle
Screening of 104 solid materials and washing facility
106 purifying areas
108 recirculated waters
110 solid material discharge gates
112 solid/the fibre materials that purify
114 dehydrating presses
The solid material of 116 dehydrations
118 contain the water of dissolved organic matter
120 washings
121 mixing waters
122 sand washers
123 grit floss holes
The fine sand of 124 preliminary clearning
126 agitators
128 fine sand wash mills
130 fine sands that purify
The recirculated water of 132 high organic contents
133 mixing suspensions
134 intermediate storages
136 pumps
138 fermentors
140 heat exchangers
142 heat mediums
144 biogas
146 waste water of discharging
147 superfluous waters
148 effluent purifying devices
150 waste water that purify
152 gate valves
154 bypass pipes
156 admission lines
158 mixing waters
159 rotten water
160 impurity
162 hydrolysis or acidifying level
162a hydrolysis or acidifying level
162b hydrolysis or acidifying level
164 wet method macerates
164a wet method macerate
164b wet method macerate
166 doughnuts
168 separation equipments
The waste water of 170 no solid materials
172 acid air washers
174 reactors
176 agitators
178 inlet ducts
180 apparatuss of oxygen supply
182 cooling units
184 feed
186 mixed material minute surfaces
188 waste gas
190 exhaust air chambers
192 reactors
194 agitators
196 inlet ducts
198 mixed material minute surfaces
200 waste gas
202 exhaust air chambers
204 return
206 filters
208 dehydrating presses
210 extruding slurries
212 former synthetics
214 macerates again
216 dried products
218 separators
220 solids and fibre material
222 inert materials
224 materials
226 mixers
228 hydrochloric acid or sulfuric acid
230 sal-ammoniacs or sulfate
232 water-acidic mixture
234 spray equipments
236 circulating pumps
238 air of discharging
240 purify level
242 process air
244 conduits
The 244a conduit
The 244b conduit
The 244c conduit
246 reactor bottoms
248 reactor head
250 circulate
252 flow
254 arms
256 arms
258 arms
260 valves
262 pipelines
264 elongated portion
266 O
2Probe
268 blenders
270 agitators
272 tumblers
The 276a moving blade
The 276b moving blade
The 276c moving blade
The 278a moving blade
The 278b moving blade
The 278c moving blade
The 280a eddy current
The 280b eddy current
The 280c eddy current
The reverse eddy current of 282a
The reverse eddy current of 282b
The reverse eddy current of 282c
284 conveying worms
286 mixture minute surfaces
288 chimneys
290 circular traces
292 vertical walls
294 vertical walls
295 base wall
296 tumblers
297 top walls
298 circular traces
300 feed separation equipment
302 tangent districts
304 conveyers
306 arms
308 flow
310 always flow
311 dryings
311.1 dry mixed material
312 compression devices
312.1 moulded parts (agglomerate, pelletizing)
313 liquefying plants
313.1 spray material
314 handle and metering device
314.1 adhesive
315 spontaneous adhesives
316 adhesives that add
317 burnings, equipment for gasification
317.1 electricity and heat energy
317.2 mineral matter/slag
Claims (62)
1. be used to handle the method for the rubbish that contains organic principle, have following steps:
The rubbish mechanical treatment is become garbage mixture,
Dissolving organic principle in material dissolution device (1,1.1),
Hydrolysis in reactor (174) (162,162.1) contains organic suspension (20) from what material dissolution device (1,1.1) was discharged, and
At the suspension (21) of fermentation level (138) fermentation hydrolysis, wherein,
During with hydrolysis or the process water that the time obtains of fermentation circulate as recirculated water (4), and
Depend on granularity, select to be used for the material dissolution device (1,1.1) and the reactor (174) of hydrolysis (162,162.1) through the garbage mixture of mechanical treatment.
2. by the described method of claim 1, wherein, when the about 80mm of granularity, change material dissolution device (1,1.1) and reactor (162,162.1).
3. by claim 1 or 2 described methods, wherein, hydrolysis (162,162.1) can connect wet method macerate or wet oxidation (164,164.1) afterwards at least indirectly.
4. by one of claim 1-3 described method, wherein, have separating step, be used for impurity, heavy burder, fibre material etc. are separated with the biological suspensions (132) that is transported to fermentation level (138).
5. material dissolution device, in by the described method of one of claim 1-4, be used for determining for example organic principle of the rubbish of 80mm of granularity in diluent liquid dissolving maximum, has material dissolution container (6), the inside is provided for mixing arrangement that rubbish and dilution water are mixed, wherein, contain organic suspension (20) by suspension floss hole (16) discharging, it is characterized in that, mixing arrangement has at least one nozzle of air supply (28), gas, preferably like this to suspension (8) pressurization, dissolve or be distributed in the diluent liquid by the shearing force that organic principle is produced by gas by it for air.
6. by the described material dissolution device of claim 5, wherein, nozzle of air supply (28) is the parts of pneumatic pump (24), and suspension (8) can be periodically in material dissolution container (6) inside by it or the conveying that circulates continuously.
7. by the described material dissolution device of claim 6, wherein, the pulsation spacing is greater than 3 seconds, preferably between 5 to 10 seconds.
8. by claim 6 or 7 described material dissolution devices, wherein, pneumatic pump (24) has interior pipe (26), on the charging aperture of its underpart, be provided with and have a large amount of nozzles of air supply (28) and can be, and have the discharge gate that is used for the suspension carried in the interior pipe (26) on its upper end section by suspension (8) circulation or through-flow nozzle plate (27).
9. by the described material dissolution device of claim 8, wherein, shock plate (44) is set apart with the discharge gate of interior pipe (26).
10. by the described material dissolution device of claim 9, wherein, shock plate (44) is to small part restriction exhaust chamber (42).
11., wherein, a plurality of pneumatic pumps (24a, 24b, 24c) are set in the material dissolution container (6) by one of claim 6-10 described material dissolution device.
12. by the described material dissolution device of one of claim 8-11, wherein, interior pipe (26) double braid covering constitutes, and nozzle of air supply (28) is arranged in the indoor or doughnut of inner cylinder, and other chambers are flow through by heat medium (142) separately.
13. by the described material dissolution device of one of claim 5-12, wherein, gas circulates and is extracted out from material dissolution container (6) and/or utilized applied pressure and turn back to nozzle of air supply (28) from holder (34) by pump (36).
14., wherein, in by interior pipe (26) and doughnut (56), be provided for the guide plate (58) of water conservancy diversion by the outer circle wall restriction of material dissolution container (6) by the described material dissolution device of one of claim 8-13.
15. by one of claim 5-14 described material dissolution device, wherein, a plurality of material dissolution containers (6a, 6b ... 6n) series connection, and suspension from the first material dissolution container (6a) flow to the rearmounted material dissolution container that connects (6b ... 6n).
16., have the outlet (14) that is used for impurity/heavy burder (18) by one of claim 5-15 described material dissolution device.
17., wherein, have the interface that is used for air inlet and mixed precipitation impurity/heavy burder (18) in the outlet (14) by one of claim 5-16 described material dissolution device.
18. by one of claim 5-17 described material dissolution device, wherein, diluent liquid (4) circulates.
19. material dissolution device, be used for minimum determining that granularity for example is the organic principle of 80mm and rubbish in diluent liquid, dissolving by the described method of one of claim 1-4, has material dissolution container (6), the inside is provided with at least one agitator (270) that is used for rubbish and dilution water are mixed into suspension, wherein, contain organic suspension (20) by discharge gate (16) discharging, it is characterized in that, agitator (270) has a large amount of adjacent mixing components (276,278), and they have opposite throughput direction separately.
20. by the described material dissolution device of claim 19, wherein, mixing component (276,278) constitutes as moving blade (276,278), and they are arranged on the shared tumbler (272), and adjacent moving blade (276,278) has the about 180 ° blade angle of climb of deflection.
21. by the described material dissolution device of claim 20, wherein, moving blade (276,278) is arranged on the tumbler (272) equably from the discharge gate (16) of charging aperture (10) up to impurity/heavy burder (18).
22., wherein, select the moving blade (276,278) of even number by claim 20 or 21 described material dissolution devices.
23. by one of claim 20-22 described material dissolution device, wherein, have two revolving parts (274,296), they utilize its moving blade (276,278) to form tangent zone (302).
24., wherein, in the zone of impurity/heavy burder (18) outlet (14), can import gas, preferably compressed air by one of claim 19-23 described material dissolution device.
25. by the described material dissolution device of claim 24, wherein, gas circulates and is extracted out from material dissolution container (6) and turned back in this container by pump (36).
26. by one of claim 19-25 described material dissolution device, wherein, a plurality of material dissolution containers (6a ... 6n) series connection, and suspension (20) flow in the rearmounted material dissolution container (6n) that connects from the first material dissolution container (6a).
27. by the described material dissolution device of one of claim 19-26, wherein, material dissolution container (6) has substantial rectangular on the vertical section moulding, its height-length compares corresponding to equation h1: L1 〉=1: 4.
28. reactor, be used for determining that in the maximum of handling conveying by the described method of one of claim 1-4 granularity for example is the mixed material of 80mm, have material loading and discharge gate and have and be used for mechanical mixer (176) that mixed material is mixed, it is characterized in that, blender (716) by conduit (244) around, wherein, under the situation of control blender (176), mixed material can pass through conduit (244) extracted and formed in the outside of conduit (244) rising from reactor top side direction reactor bottom side annular flow (252).
29. by the described reactor of claim 28, wherein, conduit (244) has the axial lengthening position (264) that is used to change its length or height.
30. by claim 28 or 29 described reactors, wherein, have the apparatus of oxygen supply (180) that is used for delivering oxygen in mixed material, wherein, carry and near the bottom of blender (176) and/or in the upper area, carry out selectively.
31. by the described reactor of claim 30, wherein, have and be used to regulate the O that send the oxygen amount
2Probe can be regulated the axial location and/or the mixed material minute surface (186) of axial lengthening position (264), conduit (244) like this by it, and it is best that it is preferably produced, just 100% coefficient of oxygen utilization almost.
32. by one of claim 28-31 described reactor, wherein have the interior pipe (244) of double braid covering, be used to carry the cooling medium of cooling and mixing material.
33., wherein, three conduits (244a, 244b, 244c) are set in reactor (174) by one of claim 28-32 described reactor.
34. by one of claim 28-33 described reactor, wherein, reactor can use when hydrolysis (162) and/or wet method macerate (164).
35. by the described reactor of one of claim 28-34, wherein, reactor preferably separately or combination have following physical dimension,
-duct height H1 corresponding to the 8-10 of conduit diameter d1 doubly,
The effective diameter d2 of-reactor (174), just internal diameter corresponding to the 4-6 of conduit diameter d1 doubly,
-reactor bottom (246) to the distance from bottom H2 of conduit (244) doubly corresponding to the 1-2 of conduit diameter d1,
Distance between-mixed material minute surface (186) and the conduit (244) corresponding to the 2-3 of conduit diameter d1 doubly,
The unique H4 of variable height between-mixed material minute surface (186) and the conduit (244) is 0.5-2 a times of conduit diameter d1,
-circulate (250) upflow velocity v1 between 0.1m/s and 0.8m/s,
-conduit diameter d1 is according to mixed material composition and dry matter ratio, between 0.5m and 1.5m.
36. reactor, being used for handle minimum definite granularity by the described method of one of claim 1-4 for example is the mixed material of the conveying of 80mm, have material loading and discharge gate and have and be used for mixing arrangement that mixed material is mixed, it is characterized in that mixing arrangement is by being used to carry the preferably inlet duct of oxygen (178) formation of gas.
37., wherein, near the bottom of reactor (174,192), a large amount of nozzles of air supply are set by the described reactor of claim 36.
38. by claim 36 or 37 described reactors, wherein, gas circulates and is extracted out from material dissolution container (6) and turned back in this container by pump (36).
39., wherein, have the survey gas probe (266) that is used to regulate the delivery of oxygen amount of wanting by claim 36, one of 37 or 38 described reactors.
40. by one of claim 36-39 described reactor, wherein, the waste gas (188,200) that produces in reactor (174,192) can be transported to by air blast (36) near the preferred mixed material the bottom.
41. refuse treatment plant, in by the described method of one of claim 1-4, use, have by the described material dissolution device of one of aforementioned claim, at the organic principle of this material dissolution device the inside dissolving rubbish, this refuse treatment plant have be used for fibre material with from material dissolution device (1) discharge, contain the separation level that organic decomposition suspension (20) separates.
42. by the described refuse treatment plant of claim 41, have solid material treating apparatus (80,86,88), be used for separating and washing the solid material (18) of discharging from material dissolution container (6).
43. by claim 41 or 42 described refuse treatment plants, wherein, separate level and have the fibre material separator (98) that is used for defibre material, floating thing or similar material and the washing facility (104) that is used for these materials (100) and dehydrating press (114).
44. by claim 41,42 or 43 described refuse treatment plants, have sand washer (142), be used for separating the fine sand contained (130) with washes.
45. by the described refuse treatment plant of one of claim 41-44, have fermentor (138), be used for converting the organic principle of the water (132) of high organic content to biogas.
46. by the described refuse treatment plant of claim 45, have effluent purifying device (148), be used to purify the superfluous water that the fermentation back produces.
47. by one of claim 41-46 described refuse treatment plant, wherein, the suspension (20) that decomposes in the material dissolution device (1) is at least as shunting through hydrolysis (162,162.1).
48. by the described refuse treatment plant of claim 47, wherein, the suspension of handling in the hydrolysis (162) (21) is through fibre material separator (98).
49. by the described refuse treatment plant of claim 47, wherein, the suspension of handling in the hydrolysis (162,162.1) (21) is delivered directly to fermentor (138).
50. by the described refuse treatment plant of claim 49, wherein, the waste water (146) that produces in the fermentor (138) is transported to separation equipment (98,104,114) and the rotten water (171) of the no solid material that meanwhile will separate mixes with dilution water (4).
51. by the described refuse treatment plant of claim 50, wherein, will not have the shunting of solid material corruption water (171) and mixes with dewatered solid material (116) and be transported to wet method macerate (164,164.1) from separation equipment (98,104,114).
52. by the described refuse treatment plant of claim 48, wherein, at least one of the dewatered solid material (116) that separation equipment (98,104,114) is produced afterwards divided fluidized drying, and is compressed into the moulded parts of gasification or combustion apparatus (317) in the compression device (312) that moves under preferred lower pressure under the situation of mixed adhesive (315,316).
53. by the described refuse treatment plant of claim 52, wherein, the adhesive gasification stably keeps moulded parts, until in gasification or combustion apparatus (317), carrying out roasting, and when garbage disposal, use by the adhesive (315) of separating plastic generation itself and/or the adhesive (316) that provides.
54., wherein, go up the solid material (116) of generation at least as shunting by the mixed material (23) of wet method macerate (164,164.1) to obtain oxidation at dehydrating press (114) by the described refuse treatment plant of claim 48.
55., wherein, can carry the mixing water (158) that forms when mixing at the recirculated water (132) and the waste water (146) of fermentor (138) to wet method macerate (164,164.1) by the described refuse treatment plant of claim 54.
56. by the described refuse treatment plant of claim 55, wherein, the oxidation mixture material (23) of wet method macerate (164,164.1) passes through separation equipment (168), and the waste water that forms in separation equipment (168) can be flowed to dilution water (4) and/or effluent purifying device (148).
57. by the described refuse treatment plant of claim 56, wherein, separation equipment (168) has solid material separator (98), solid material screening and washing facility (104) and dehydrating press (114).
58. by the described refuse treatment plant of claim 57, wherein, the former synthetic (212) that forms in separation equipment (168) is by being used for dry back dipping (212) and/or can directly handling.
59., wherein, when hydrolysis (162,162.1) and/or wet method macerate (164,164.1), use by the described reactor of claim 1-40 (174) by one of claim 41-58 described refuse treatment plant.
60. by the described refuse treatment plant of claim 59, wherein, front and back and/or a plurality of reactors of connection parallel to each other (174), thus manifold hydrolysis (162,162a, 162b) and/or wet method macerate (164,164a, 164b) produced.
61., wherein, the waste gas (188,200) that forms can be transported to the air washer (172) that is used to discharge ammonia in reactor (174,192) by claim 59 or 60 described refuse treatment plants.
62. by one of claim 54-61 described refuse treatment plant, wherein, the reactor (192) of wet method macerate (164.1) can move so at least, and it is cleaned mixed material.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102004027260 | 2004-06-03 | ||
| DE102004027260.3 | 2004-06-03 | ||
| DE102004050503.9 | 2004-10-15 |
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| Publication Number | Publication Date |
|---|---|
| CN101065188A true CN101065188A (en) | 2007-10-31 |
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ID=38965649
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2005800249992A Pending CN101065188A (en) | 2004-06-03 | 2005-06-03 | Material solubiliser reactor for hydrolysis and/or wet fermentation and waste treatment plant with such a solubiliser and reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101065188A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102671917A (en) * | 2012-05-21 | 2012-09-19 | 宁波开诚生态技术有限公司 | Integral loading acidifying machine |
| CN104284730A (en) * | 2012-03-27 | 2015-01-14 | 苏伊士环境集团 | Method for treating waste, in particular household refuse, and unit for implementing same |
| CN104769095A (en) * | 2012-08-13 | 2015-07-08 | 米歇尔·博诺姆 | Method and device for continuous dry methanation |
| CN112605096A (en) * | 2020-11-27 | 2021-04-06 | 飞潮(上海)环境技术有限公司 | Method for circularly enriching soluble chloride solution |
| CN116688782A (en) * | 2023-08-04 | 2023-09-05 | 河北农业大学 | Agricultural is with liquid manure pesticide mixing arrangement |
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2005
- 2005-06-03 CN CNA2005800249992A patent/CN101065188A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104284730A (en) * | 2012-03-27 | 2015-01-14 | 苏伊士环境集团 | Method for treating waste, in particular household refuse, and unit for implementing same |
| CN104284730B (en) * | 2012-03-27 | 2016-11-23 | 苏伊士环境集团 | The processing method of waste material, particularly house refuse, and apparatus for carrying out the method |
| US9943858B2 (en) | 2012-03-27 | 2018-04-17 | Suez Environment | Method for treating waste, in particular household refuse, and unit for implementing same |
| CN102671917A (en) * | 2012-05-21 | 2012-09-19 | 宁波开诚生态技术有限公司 | Integral loading acidifying machine |
| CN104769095A (en) * | 2012-08-13 | 2015-07-08 | 米歇尔·博诺姆 | Method and device for continuous dry methanation |
| CN112605096A (en) * | 2020-11-27 | 2021-04-06 | 飞潮(上海)环境技术有限公司 | Method for circularly enriching soluble chloride solution |
| CN116688782A (en) * | 2023-08-04 | 2023-09-05 | 河北农业大学 | Agricultural is with liquid manure pesticide mixing arrangement |
| CN116688782B (en) * | 2023-08-04 | 2023-10-03 | 河北农业大学 | Agricultural is with liquid manure pesticide mixing arrangement |
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Open date: 20071031 |