CN102153198B - Granular sludge sewage treatment device capable of controlling diameter and density of granules - Google Patents
Granular sludge sewage treatment device capable of controlling diameter and density of granules Download PDFInfo
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- CN102153198B CN102153198B CN201010575664A CN201010575664A CN102153198B CN 102153198 B CN102153198 B CN 102153198B CN 201010575664 A CN201010575664 A CN 201010575664A CN 201010575664 A CN201010575664 A CN 201010575664A CN 102153198 B CN102153198 B CN 102153198B
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Abstract
The invention discloses a granular sludge sewage treatment device capable of controlling diameter and density of granules. The device comprises an inner barrel and an outer barrel which are concentric; an aeration device is arranged in an annular space between the inner barrel and the outer barrel; the aeration device is fixed on a pedestal through a supporting pile of the aeration device; the inner barrel wall of the inner barrel is connected with a cylindrical cyclone cylinder; the lower end of the cyclone cylinder is connected with a wall through pipe, the wall through pipe passes through the walls of the inner barrel and the outer barrel, and the side wall of the cyclone cylinder is provided with an overflow hole; and a water inlet funnel is fixed at the upper barrel port of the inner barrel, the water inlet funnel is connected with a spiral thin bent pipe, and the outlet of the thin bent pipe is tightly attached to the inside wall of the cyclone cylinder. On the basis of ensuring good outlet water quality, the device successfully realizes human control and selection of the diameter and the density of the aerobic sludge granules, and realizes proper solid-liquid separation; in addition, through the device, the initial granule forming speed is high, and the sludge load is balanced; the oxygenation efficiency is improved by gas-liquid separation; and the device has the advantages of energy conservation and high efficiency.
Description
Technical field
The invention belongs to sewage treatment area, relate to a kind of waste disposal plant, be specifically related to the granule sludge waste disposal plant of a kind of may command grain diameter and density.
Background technology
The aerobic particle mud sewage treatment process has obtained increasing environmental engineering scholar's concern since eighties of last century is in the news the end of the nineties.The sedimentation effect that has very strong anti-load impact ability, mud owing to aerobic particle mud is good, can shorten the sludge settling time greatly, dwindles the floor space of sewage work, reduces construction costs, is described as WWT new technology of future generation.Yet the long-term stability of aerobic particle mud is to limit the bottleneck that this technology popularization is used.Its major cause is that aerobic particle mud particle diameter in culturing process is difficult to control, because the increase of particle diameter can cause the loose of grain pattern, influences the settling property and the effluent quality of mud, disintegrates until mud granule.
At present; Academia has carried out useful exploration to the control of granule sludge; Main method comprises: (1) is in sequencing batch reactor; Shorten flooding time, make the mikrobe of granule interior also can obtain enough matrix in the short period of time, avoid the hydrolysis of granule interior mikrobe owing to lacking matrix; (2) microbial population through mikrobe means enrichment slow growth in sludge system is like the autotrophy nitrifier etc.These methods can be alleviated the disintegration of granule sludge to a certain extent, but still realize the long-term stability of granule sludge.
The basic functional principle of rotational flow separation is based on the centrifugal settling effect; After treating that isolating two phase mixed solutions get into separator with certain pressure from swirler-upper periphery tangential, produce intensive and rotatablely move, because the density difference between solid-liquid two phases; Suffered cf-; Entad buoyancy and fluid drag force is also inequality, and heavier solid particulate is discharged through the swirler-underflow opening. and most of clear liquid is then discharged through overflow weir, thereby realizes isolating purpose.
Nowadays cyclone technique is in water treatment field, has been widely used in one-level and handled, and like the cyclone sediment pond etc., but also directly is not used for the report of biological treatment process at present.
Summary of the invention
In order to overcome the deficiency of above-mentioned prior art; The object of the present invention is to provide the granule sludge waste disposal plant of a kind of may command grain diameter and density, it can realize the division in aeration zone and non-aeration district, and proposes effect through the gas of aerating apparatus; Realize that mixed solution is got into the eddy flow district and then got into the non-aeration district again by the aeration zone; Last suction function through aerating apparatus again gets into the aeration zone again, wherein, strengthens artificial control and the selection that shearing force realizes the prilling of aerobic sludge and realizes the aerobic sludge grain diameter through the swirler-device; And gas, the triphasic appropriateness separation of solid, liquid have been realized; Make reaction unit reach better treatment effect, through dissolved oxygen from the aeration zone, the Gradient distribution of the concentration of gas delivery district, eddy flow district and non-aeration district dissolved oxygen, can improve the aeration zone oxygen-transfer efficiency; Reduce the aeration zone, have certain energy-conservation effect.
To achieve these goals, the technical scheme of the present invention's employing is:
The granule sludge waste disposal plant of a kind of may command grain diameter and density comprises concentric inner core 10 and urceolus 11, and the lower edge of inner core 10 is higher than the lower edge of urceolus 11; The upper edge of inner core 10 is lower than the upper edge of urceolus 11, and urceolus 11 uprightly is fixed on the pedestal 21, and water outlet 7 is arranged on the sidewall of urceolus 11; Inner core 10 is fixed on the pedestal 21 through inner core supporting pile 14, in the annular space between inner core 10 and urceolus 11 aerating apparatus 12 is set, and aerating apparatus 12 is fixed on the pedestal 21 through aerating apparatus supporting pile 15; Aerating apparatus 12 connects inlet pipe 13; Inlet pipe 13 is led to pedestal 21 outsides, also has spoil disposal and blow-down pipe 16 on the pedestal 21, and the upper edge of the inner tube wall of inner core 10 and swirler-cylindrical shell 8 cylindraceous is tightly connected; The lower end of swirler-cylindrical shell 8 connects wears wall pipe 9; Wear the barrel that wall pipe 9 passes inner core 10 and urceolus 11, have overflow weir 6 on the sidewall of swirler-cylindrical shell 8, the last nozzle of inner core 10 is fixed with influent hopper 3; Influent hopper 3 connects spiral helicine thin bend pipe 4, and the inner side-wall of swirler-cylindrical shell 8 is close in the outlet of thin bend pipe 4.Said aerating apparatus 12 is micro-pore aeration, flexible pipe aeration or core aerating apparatus.Ventpipe 2 is arranged on the sidewall of inner core 10, be arranged in the annular space between inner core 10 and the urceolus 11, be higher than 0～0.6 times of inner diameter of steel flue in inner core 10 lower edges.
Said swirler-cylindrical shell 8, thin bend pipe 4, influent hopper 3 and wear wall pipe 9 and form the swirler-devices.The present invention compared with prior art has the following advantages:
(1) the artificial control and the selection of realization aerobic sludge grain diameter: after mixed solution gets into the swirler-device; Thin bend pipe guiding mixed solution is close to the oblique inflow down of inner core inwall, and the particle of big particle diameter and big density takes the lead under action of centrifugal force to the inwall migration, rebuffed sedimentation in the swirler-device; The big particle diameter of awl section enrichment is regularly discharged by wearing the wall pipe with big density particle in the bottom; Particle diameter smaller particles or flco, the overflow weir that is provided with from swirler-device top gets into the non-aeration district, wears wall pipe diameter more than or equal to thin bend pipe diameter; Realize the solid-liquid separation of appropriateness, and then realized the control of particle diameter and density.
(2) realize mixed solution circulating in reaction unit: aerating apparatus is fixed on the pedestal, in the annulus between inner core and urceolus, and a little more than the lower edge of inner core; Change the water body density in aeration zone and non-aeration district through aeration, and then change pressure, make the pressure of the pressure of aeration zone less than the non-aeration district; Thereby the outflow of the liquid in non-aeration district reaches the effect of suction, after the reaction unit water inlet; Be able to behind the mixed solution aeration of aeration zone expand, water level is able to promote, and mixed solution is proposed the effect overflow through gas and advanced the influent hopper of taper and get into the swirler-cylindrical shell; And realize the separation of gas at this; After realizing separating of grain diameter and density through the swirler-device, mixed solution and final entering non-aeration district, thus accomplished mixed solution circulating in reactor drum.
(3) realized gas, the triphasic appropriateness separation of solid, liquid: the influent hopper that is fixed in the inner core upper edge forms gas-liquid separation zone before mixed solution gets into swirler-; The effect of collecting rectification is played in this zone, and the air water mixed solution that aeration gas is carried into reaches the effect of appropriate gas-liquid separation in this zone; One ventpipe is set on the swirler-barrel, makes the further gas-liquid separation of mixed solution that gets into swirler-, make the top of swirler-WS remain atmospheric pressure, and then guaranteed the steady operation condition of swirler-.
(4) effluent quality is good: through realizing the division of aeration zone and non-aeration district functional area, make the entire reaction device have the effect of good synchronous nitration and denitrification, realized good effluent quality.
(5) oxygen-transfer efficiency is high: because the Metabolic activity of mikrobe; The concentration of dissolved oxygen is reduced by aeration zone, gas delivery district, eddy flow district and non-aeration district successively; Dissolved oxygen almost exhausts when mud is back to the aeration zone; Thereby improved the concentration gradient of aeration zone, and then improved the oxygen-transfer efficiency in this district.
(6) two-way choice, it is fast that particle forms speed: water outlet is opened when carrying out water outlet, and the liquid level of aeration zone can at first descend; Owing to the reason that is communicated with; The liquid level in non-aeration district descends thereupon, and the water in non-aeration district is effluented to the aeration zone by the bottom, can make sedimentary sludge blanket that certain expansion takes place; Thereby make the relatively poor mud generation come-up of sedimentation function of sludge blanket top be able to discharge with water outlet; Thereby changed traditional mode that only relies on the unidirectional selection of setting the shorter ST, formed a kind of two-way choice mode, quickened particulate and form.
(7) sludge loading is balanced: the upper inner cylinder water inlet; Making into, water need pass sludge blanket entering aeration zone; Quickened mixing of mud and water inlet, simultaneously by the non-aeration district to aeration zone, from inside to outside the water intake mode of radial pattern, better guaranteed the harmony of sludge loading.
Description of drawings
Fig. 1 utilizes structural representation of the present invention.
Fig. 2 is 2000 times of electromicroscopic photographs of the interior mud granule of reaction unit among the embodiment.
Fig. 3 is 12000 times of electromicroscopic photographs of the interior mud granule of reaction unit among the embodiment.
Fig. 4 is the water quality data of reaction unit operation water outlet after 50 days among the embodiment, and X-coordinate is working time, and ordinate zou is the COD clearance.
Fig. 5 is the water quality data of reaction unit operation water outlet after 50 days among the embodiment, and X-coordinate is working time, and ordinate zou is an ammonia nitrogen removal frank.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is explained further details.
Shown in accompanying drawing, the present invention is the granule sludge waste disposal plant of a kind of may command grain diameter and density, comprises concentric inner core 10 and urceolus 11; The lower edge of inner core 10 is higher than the lower edge of urceolus 11, and the upper edge of inner core 10 is lower than the upper edge of urceolus 11, and urceolus 11 uprightly is fixed on the pedestal 21; Water outlet 7 is arranged on the sidewall of urceolus 11, and inner core 10 is fixed on the pedestal 21 through inner core supporting pile 14, in the annular space between inner core 10 and urceolus 11 aerating apparatus 12 is set; Aerating apparatus 12 is fixed on the pedestal 21 through aerating apparatus supporting pile 15, and aerating apparatus 12 connects inlet pipe 13, and inlet pipe 13 is led to pedestal 21 outsides; Also have spoil disposal and blow-down pipe 16 on the pedestal 21, a circle draw-in groove 5 is set on the inner side-wall of inner core 10, the upper edge of swirler-cylindrical shell 8 has outside horizontal sides; This horizontal sides is fastened in the draw-in groove 5, guarantees that the upper edge of swirler-cylindrical shell 8 combines closely with the inner side-wall of inner core 10, also can be through the mode of other flexible connection; The lower end of swirler-cylindrical shell 8 connects wears wall pipe 9; Wear the barrel that wall pipe 9 passes inner core 10 and urceolus 11, have overflow weir 6 on the sidewall of swirler-cylindrical shell 8, the last nozzle of inner core 10 is fixed with influent hopper 3; Influent hopper 3 connects spiral helicine thin bend pipe 4, and the inner side-wall of swirler-cylindrical shell 8 is close in the outlet of thin bend pipe 4.Said aerating apparatus 12 is micro-pore aeration, flexible pipe aeration, core aeration or efflux aerator, guarantees that gas can not get into inner core 10, and can reach good suction castering action, makes the bottom that the deposition of mud can not take place.Ventpipe 2 is arranged on the sidewall of inner core 10, be arranged in the annular space between inner core 10 and the urceolus 11, be higher than 0～0.6 times of inner diameter of steel flue in inner core 10 lower edges.
Said swirler-cylindrical shell 8, thin bend pipe 4, influent hopper 3 and wear wall pipe 9 and form the swirler-devices.Annular space between inner core 10 and the urceolus 11 is aeration zone 19; Swirler-cylindrical shell and space between the inner core 10 below 8 is non-aeration district 20; The space that swirler-cylindrical shell 8, influent hopper 3 and inner core 10 surround is eddy flow district 18, is rectification gas-liquid separation zone 17 in the influent hopper 3.
More excellent step design; The height of urceolus 11 and diameter ratio are 15: 1～5: 1, and the lower edge of inner core 10 is higher than the inner diameter of steel flue of 0.3～1.2 times of the lower edge of urceolus 11, and the upper edge of inner core 10 is lower than the inner diameter of steel flue of upper edge more than 1 times or 1 times of urceolus 11; Aerating apparatus 12 is arranged in the annular space between inner core 10 and the urceolus 11; Be higher than 0～0.6 times of inner diameter of steel flue in inner core 10 lower edges, the diameter of swirler-cylindrical shell 8 is 0.2～0.9 times of inner core 10 diameters, and the length of swirler-cylindrical shell 8 is 0.7～2 times of diameter; Swirler-cylindrical shell 8 is inverted taper shape with wearing wall pipe 9 junctions, and its cone angle is 5 °～60 °.
Best a kind of selection, the height of urceolus 11 is 600cm, the barrel dliameter of urceolus 11 is 120cm; The barrel dliameter of inner core 10 is 65cm, and the lower edge of inner core 10 is higher than the lower edge 30cm of urceolus 11, and the upper edge of inner core 10 is lower than the upper edge 100cm of urceolus 11; In the aeration zone 19 and be higher than inner core 10 lower edge 25cm aerating apparatus 12 is set; The length of swirler-device cavity is 75cm, and swirler-cylindrical shell 8 is 45 ° with wearing wall pipe 9 junction cone angles, and the barrel dliameter of swirler-cylindrical shell 8 is 50cm; The caliber of thin bend pipe 4 is 8cm, and flowing into angle and sea line angle is 30 °.
Aerating apparatus 12 changes the density of the water body in aeration zone 19 and non-aeration district 20 through aeration, and then changes pressure, makes the pressure of the pressure of aeration zone 19 less than non-aeration district 20; Thereby the outflow of the liquid in non-aeration district 20 reaches the effect of suction, after the reaction unit water inlet; Water level is controlled at influent hopper 3 upper edges and substructure height 0.8～0.95 times; Be able to behind the 19 mixed solution aerations of aeration zone expand, water level is able to promote, and mixed solution is carried effect entering influent hopper 3 through gas and got into the swirler-device again; And realize the separation of gas at this; After realizing separating of grain diameter and density through the swirler-device, mixed solution and final entering non-aeration district 20, thus accomplished mixed solution circulating in reactor drum.
Particle in the mixed solution is according to different-grain diameter, different densities, and the cf-that is produced is different, after getting into the eddy flow district; The particle of big particle diameter and big density takes the lead in moving to inwall; Rebuffed sedimentation in the eddy flow district in the enrichment of awl pars infrasegmentalis, is regularly discharged by the wall pipe 9 of wearing that the awl pars infrasegmentalis connects; Wear wall pipe 9 diameters and get 0.15～1 times of flow-out hole diameter, particle diameter is that particle and the density of 50～1500um is 1.01～1.20g/cm
3Particle or flco, the overflow weir 6 that is provided with from swirler-cylindrical shell 8 tops goes out to flow into non-aeration district 20, overflow weir 6 diameters are realized the solid-liquid separation of appropriateness more than or equal to thin bend pipe 4 diameters, and then have realized the control of particle diameter and density.
Open when carrying out water outlet through the water outlet on the urceolus 11 7, can discharge a part and set the flco (this is traditional unidirectional selection) that is not precipitated in the ST below the water outlet 7, in addition; The liquid level of aeration zone 19 can at first descend; Because be communicated with, the liquid level in non-aeration district 20 descends thereupon, the water in non-aeration district 20 is effluented to aeration zone 19 by the bottom; Certain flow velocity that effluents can be discharged the density and the less flco of particle diameter that are precipitated to water outlet below 7 with water outlet; And then changed the mode of traditional unidirectional selection, and form a kind of two-way choice mode, quicken particulate at initial operating stage and form.
Through realizing the division of aeration zone and non-aeration district functional area, make the entire reaction device have the effect of good synchronous nitration and denitrification, realized good effluent quality; Meanwhile; Because the Metabolic activity of mikrobe, the concentration of dissolved oxygen is reduced by aeration zone, gas delivery district, eddy flow district and non-aeration district successively, and dissolved oxygen almost exhausts when mud is back to the aeration zone; Thereby improved the concentration gradient of aeration zone, and then improved the oxygen-transfer efficiency in this district.
During use; Make sewage from water-in 1 through influent hopper 3 accesss to plant, water-in 1 can be arranged on influent hopper 3 directly over, sewage gets into eddy flow districts 18 through influent hopper 3 earlier; Overflow weir 6 through swirler-cylindrical shell 8 sidewalls enters into non-aeration district 20 then; Pass sludge blanket from the bottom radial pattern of inner core 10 again and enter into aeration zone 19, quicken muddy water and mix balanced load; Along with continuous water inlet, water level constantly rises in the device, and flooding time was controlled at 1 to 30 minute.The upper limb that reaches influent hopper 3 when water level in the device and pedestal 21 distances 80%～95% the time, stop into water, begin aeration, the water level of intaking can be controlled with liquidometer.At this moment, the mixed solution of aeration zone 19 expands under the effect of aeration, when influent hopper 3 edges were overflow in the mixed solution expansion; Mixed solution gets into rectification gas-liquid separation zone 17, carries out gas-liquid separation at this, makes the gas of trying one's best few get into the swirler-device; Subsequently under action of gravity by thin bend pipe 4 drainages to eddy flow district 18 because thin bend pipe is close to barrel, flows and form eddy flow thereby on swirler-cylindrical shell 8 limit walls, form the tangential; Because mud granule is different with density of liquid; Thereby need bear different centrifugal forces, need the mud of getting rid of, sedimentation takes place when being rebuffed owing to receive bigger cf-to the migration of limit wall; The liquid that density is less and the mud of small particle size are owing to receive relatively little cf-; Can upwards enter into non-aeration district 20 by eddy flow from overflow weir 6 outflows; Reach solid-liquid separation; The effect (at the reactor drum initial operating stage, the increasing shearing force is mainly played in eddy flow district 18, promotes granuloplastic effect) that particle diameter is selected and controlled.
Meanwhile, the mixed solution in the aeration zone 19 is carried under the effect at the gas of gas, and the pressure of aeration zone 19 makes that less than the pressure in the non-aeration district 20 mixed solution in the non-aeration district 20 is sucked into aeration zone 19, makes reactor drum form successive and circulates.Not formed vacuum in order making in the inner core 10 after the suction, to be guaranteed the mobile smooth and easy of liquid, on inner core 10, be provided with ventpipe 2, and the gas that partly gets into eddy flow district 18 is discharged, further strengthened the effect of gas-liquid separation.
Whole aeration period was controlled at 2 to 8 hours, when reacting completely, stopped aeration; Precipitate after 2～60 minutes, water outlet 7 is opened and is carried out water outlet, and this moment, the liquid level of 10 of urceolus 11 and inner cores can at first descend; Because be communicated with, the liquid level of inner core 10 descends thereupon, the water of inner core 10 is effluented between urceolus 11 and inner core 10 by the bottom; Can make sedimentary sludge blanket that certain expansion takes place, thereby make the relatively poor mud generation secondary of sedimentation function of sludge blanket top select to be able to discharge, strengthen the controlled step of microbial biomass in the reactor drum with water outlet; At the reaction unit initial operating stage, more help particulate and form.
A concrete application of above-mentioned optimal selection, reaction unit adopts the returned sluge of Sewage Plant to inoculate, water inlet COD1200mg/L; Ammonia nitrogen 120mg/L, each loop cycle are 4 hours, adopt the intermittent cyclic formula operation of water inlet-aeration-deposition-water outlet; Wherein intake 2 minutes; Precipitate 8 minutes, water outlet 2 minutes, be aeration time remaining time; Move the 15th day and begin to form particle, particle size is at 0.15～0.35mm; Reactor drum runs to the 50th day, prilling almost completely in the reaction unit, and grain diameter maintains between 0.15～0.50mm all the time; Particle diameter control is good, realizes that small size particleization and particulate circularity on average can reach 0.9, and Fig. 2 is 2000 times of electromicroscopic photographs of mud granule in the reactor drum; Fig. 3 is 12000 times of electromicroscopic photographs of mud granule in the reactor drum; Show among the figure that mud granule is closely knit, smooth surface, bacterial number is many.Fig. 4 and Fig. 5 can find that for the water quality data of operation water outlet after 50 days the clearance of COD on average reaches more than 93%, and ammonia nitrogen removal frank on average reaches 60%-70%, has good effluent quality.
The present invention is through the design of swirler-device and special sludge discharge way; And the reasonable placement of aerating apparatus; Successfully overcome the restive problem of mud granule particle diameter, and realized replacing continuously of aerobic-anaerobic functional zone, made reactor drum have the function of synchronous nitration and denitrification; Improve the stability of effluent quality and mud granule, and greatly reduced the energy consumption of traditional aerobic treatment process.
Claims (9)
1. the granule sludge waste disposal plant of may command grain diameter and density is characterized in that, comprises that two ends connect and concentric inner core (10) and urceolus (11); The lower edge of inner core (10) is higher than the lower edge of urceolus (11), and the upper edge of inner core (10) is lower than the upper edge of urceolus (11), and urceolus (11) uprightly is fixed on the pedestal (21); Water outlet (7) is arranged on the sidewall of urceolus (11), and inner core (10) is fixed on the pedestal (21) through inner core supporting pile (14), in the annular space between inner core (10) and urceolus (11) aerating apparatus (12) is set; Aerating apparatus (12) is fixed on the pedestal (21) through aerating apparatus supporting pile (15), and aerating apparatus (12) is arranged in the annular space between inner core (10) and the urceolus (11), is higher than 0～0.6 times of inner diameter of steel flue in inner core (10) lower edge; Aerating apparatus (12) connects inlet pipe (13); Inlet pipe (13) is led to pedestal (21) outside, and pedestal (21) is gone up also has spoil disposal and blow-down pipe (16), and the upper edge with swirler-cylindrical shell cylindraceous (8) on the inner tube wall of inner core (10) is tightly connected; The lower end of swirler-cylindrical shell (8) connects wears wall pipe (9); Wear the barrel that wall pipe (9) passes inner core (10) and urceolus (11), have overflow weir (6) on the sidewall of swirler-cylindrical shell (8), the last nozzle of inner core (10) is fixed with influent hopper (3); Influent hopper (3) connects spiral helicine thin bend pipe (4); The inner side-wall of swirler-cylindrical shell (8) is close in the outlet of thin bend pipe (4), and the particle in the mixed solution is according to different-grain diameter, different densities, and the cf-that is produced is different; After getting into the eddy flow district; The particle of big particle diameter and big density takes the lead in to the inwall migration, and the sedimentation of in the eddy flow district, being rebuffed is in the enrichment of awl pars infrasegmentalis; The wall pipe (9) of wearing by the awl pars infrasegmentalis connects is regularly discharged, and particle diameter is that particle and the density of 50～1500 μ m is 1.01～1.20g/cm
3Particle or flco, the overflow weir (6) that is provided with from swirler-cylindrical shell (8) top goes out to flow into non-aeration district (20), overflow weir (6) diameter is more than or equal to thin bend pipe (4) diameter, thereby realized the control of particle diameter and density.
2. the granule sludge waste disposal plant of a kind of may command grain diameter according to claim 1 and density is characterized in that said aerating apparatus (12) is micro porous aeration head, aeration flexible pipe, core or efflux aerator.
3. the granule sludge waste disposal plant of a kind of may command grain diameter according to claim 1 and density is characterized in that, ventpipe (2) is arranged on the sidewall of inner core (10).
4. the granule sludge waste disposal plant of a kind of may command grain diameter according to claim 1 and density is characterized in that the height of urceolus (11) and diameter ratio are 15:1～5:1.
5. the granule sludge waste disposal plant of a kind of may command grain diameter according to claim 1 and density is characterized in that, the length of described swirler-cylindrical shell (8) is 0.7～2 times of its diameter.
6. the granule sludge waste disposal plant of a kind of may command grain diameter according to claim 1 and density is characterized in that, swirler-cylindrical shell (8) is inverted taper shape with wearing wall pipe (9) junction, and its cone angle is 5 °～60 °.
7. the granule sludge waste disposal plant of a kind of may command grain diameter according to claim 1 and density; It is characterized in that; The lower edge of inner core (10) is higher than the inner diameter of steel flue of 0.3～1.2 times of the lower edge of urceolus (11), and the upper edge of inner core (10) is lower than the inner diameter of steel flue of upper edge more than 1 times or 1 times of urceolus (11).
8. the granule sludge waste disposal plant of a kind of may command grain diameter according to claim 1 and density is characterized in that, the diameter of swirler-cylindrical shell (8) is 0.2～0.9 times of inner core (10) diameter.
9. the granule sludge waste disposal plant of a kind of may command grain diameter according to claim 1 and density is characterized in that, the diameter of wearing wall pipe (9) is 0.15～1 times of overflow weir (6) diameter.
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| BR112015012248B8 (en) * | 2012-11-27 | 2022-11-29 | Maureen Oshaughnessy | METHOD AND APPARATUS FOR SELECTING AND RETAINING SOLIDS WITH SUPERIOR SEDIMENTATION CHARACTERISTICS |
| CN105084454A (en) * | 2014-05-08 | 2015-11-25 | 帕克环保技术(上海)有限公司 | On-line calcium remoal device for anaerobic granular sludge |
| CN107857363A (en) * | 2017-09-13 | 2018-03-30 | 北京城市排水集团有限责任公司 | Particle and the device and its application method of floc sludge are sorted using cyclone separator |
| CN109928501A (en) * | 2019-04-09 | 2019-06-25 | 东华大学 | A kind of high-performance bio fluidized-bed reactor |
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| JP昭57-78993A 1982.05.17 |
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