CN108558128B - Co-flocculation air-float anaerobic bioreactor and method thereof - Google Patents
Co-flocculation air-float anaerobic bioreactor and method thereof Download PDFInfo
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- CN108558128B CN108558128B CN201810205481.8A CN201810205481A CN108558128B CN 108558128 B CN108558128 B CN 108558128B CN 201810205481 A CN201810205481 A CN 201810205481A CN 108558128 B CN108558128 B CN 108558128B
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- 238000005189 flocculation Methods 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 83
- 230000016615 flocculation Effects 0.000 claims abstract description 42
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000003814 drug Substances 0.000 claims abstract description 21
- 239000002893 slag Substances 0.000 claims abstract description 21
- 239000010802 sludge Substances 0.000 claims abstract description 19
- 238000007790 scraping Methods 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 70
- 239000007788 liquid Substances 0.000 claims description 31
- 239000002351 wastewater Substances 0.000 claims description 24
- 238000005188 flotation Methods 0.000 claims description 17
- 239000012295 chemical reaction liquid Substances 0.000 claims description 9
- 230000009467 reduction Effects 0.000 claims description 6
- 244000005700 microbiome Species 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 3
- 238000005191 phase separation Methods 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 239000008394 flocculating agent Substances 0.000 claims description 2
- 239000011259 mixed solution Substances 0.000 claims 2
- 229940079593 drug Drugs 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 11
- 238000007334 copolymerization reaction Methods 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000012071 phase Substances 0.000 description 11
- 239000007789 gas Substances 0.000 description 10
- 239000002245 particle Substances 0.000 description 7
- 238000007599 discharging Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000009264 composting Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000001687 destabilization Effects 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 244000144977 poultry Species 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000003307 slaughter Methods 0.000 description 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2866—Particular arrangements for anaerobic reactors
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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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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses a co-flocculation air-floatation anaerobic bioreactor and a method thereof. The co-flocculation air-floatation anaerobic bioreactor mainly comprises a biological reaction zone, a dosing mixing zone and a flocculation air-floatation zone, wherein the biological reaction zone is provided with a sludge discharge pipe, a three-phase separator and a lifting pipe, the dosing mixing zone is provided with a medicine dissolving tank, a flow control valve and a jet device, and the flocculation air-floatation zone is provided with a direct-current vortex reaction tank, a flow reducing chamber, a slag scraping machine, a slag collecting tank, a flow reducing pipe and a gas collecting chamber. The invention combines anaerobic biological reaction and co-flocculation air floatation process, utilizes marsh gas generated by anaerobic biological reaction to carry out air floatation removal on particulate matters, and simultaneously generates co-polymerization adhesion effect, thus having the characteristics of good effluent quality, medicament saving, high efficiency and low energy consumption.
Description
Technical Field
The invention belongs to the field of environmental protection equipment, and particularly relates to a co-flocculation air-floatation anaerobic bioreactor and a method thereof.
Background
The anaerobic bioreactor is a device for converting organic matters in wastewater into methane by utilizing anaerobic microorganisms, thereby realizing water quality purification. The anaerobic bioreactor has the main advantages that: oxygen supply is not needed, biogas energy is produced, residual sludge is less, and the nutrition requirement is low, so that the anaerobic bioreactor has wide application in the field of treating high-concentration organic wastewater. Through years of development, anaerobic bioreactors have various configurations, undergo three-stage development processes, and the first generation anaerobic bioreactors are mainly represented by traditional anaerobic digestion tanks; the second generation anaerobic bioreactor is mainly represented by an upflow sludge blanket reactor (UASB) and an anaerobic biological filter (AF); the third generation anaerobic bioreactor is mainly represented by an anaerobic granular sludge blanket reactor (EGSB) and an internal circulation reactor (IC). To the third generation anaerobic bioreactor, the organic volume load can reach 20kg COD.m -3 ·d -1 The above method can achieve good removal rate.
High-concentration complex wastewater (such as livestock and poultry raising wastewater, slaughter wastewater, papermaking wastewater and the like) contains a large amount of granular organic pollutants, the organic pollutants are completely removed and need to undergo hydrolysis-fermentation-methanogenesis processes, and the hydrolysis of granular substances is the speed-limiting step of the whole process. Therefore, in the treatment of high-concentration complex wastewater, anaerobic bioreactors often only operate at low loads, with their treatment potential completely suppressed, in order to ensure a certain pollutant removal rate. Anaerobic bioreactors efficiently treat high-concentration complex wastewater, and first, must efficiently remove particulate matter. In the wastewater treatment engineering, an air floatation device is usually arranged to remove particulate matters, but the engineering complexity is increased, and the capital investment is increased. For the thin cultivation industry, the effluent water treatment needs to reach the discharge standard at low cost, so that the development of the anaerobic bioreactor with the air floatation function has important practical significance.
The adhesion of particles and bubbles is the key of the air floatation process, if tiny biogas bubbles are adhered with micro-flocculation particles when coagulant is added and the reaction stage of colloid destabilization and agglomeration is carried out, then the micro-biogas bubbles are grown together in the floating process, and the micro-biogas bubbles are adhered and aggregated with other particles or micro-flocculation particles to form gas-carrying floccules, so that copolymerization adhesion phenomena of inter-particle wrapping and intermediate bubble bridging are formed. The invention combines anaerobic biological reaction and copolymerization adhesion, and has advancement and practicability.
Disclosure of Invention
The invention aims to solve the problems in the prior art and provides a co-flocculation air-floatation anaerobic bioreactor.
The co-flocculation air-floatation anaerobic bioreactor comprises a water inlet area, a biological reaction area, a water outlet area, a dosing mixing area and a flocculation air-floatation area which are arranged from bottom to top; the water inlet area is internally provided with a water inlet pipe and a water distributor communicated with one end of the water inlet pipe, and the bottom of the water inlet area is connected with a mud pipe; the upper part of the biological reaction zone is provided with a three-phase separator, and the three-phase separator is connected with a lifting pipe; an effluent weir is arranged in the effluent area; the medicine adding mixing area is provided with a medicine dissolving tank, a flow control valve and a jet device, the medicine dissolving tank is communicated with a throat pipe of the jet device through a pipeline with the flow control valve, and an inlet of the jet device is communicated with a lifting pipe; the flocculation air flotation area is internally provided with a direct-current vortex reaction tank and a flow-reducing chamber, the direct-current vortex reaction tank is of a continuous two-section structure, the lower section is of an inverted cone shape, the upper section is of a straight cylinder shape, the direct-current vortex reaction tank is coaxially arranged along the center of the flocculation air flotation area, the flow-reducing chamber is formed by clamping the outer wall of the direct-current vortex reaction tank and the inner wall of the flocculation air flotation area, the bottom of the direct-current vortex reaction tank is communicated with the outlet of a jet device, the bottom of the flow-reducing chamber is provided with a flow-reducing pipe, and the flow-reducing pipe is communicated with a water distributor; a slag scraping machine is arranged at the liquid level of the flow reducing chamber, and a slag collecting groove is arranged around the outside of the flow reducing chamber and used for collecting scum scraped by the slag scraping machine; the top of the down-flow chamber and the slag collecting tank are provided with a closed space to form a gas collecting chamber for collecting the gas produced by the reactor, and the gas collecting chamber is provided with an exhaust pipe.
On the basis of the scheme, the following preferable modes can be adopted for each component:
the volume ratio of the biological reaction area to the flocculation air floatation area is 50-100:1. The height-diameter ratio of the biological reaction area is 5-10. The ratio of the cross-sectional area of the bioreactor to the cross-sectional area of the riser is greater than 2500:1 and the riser diameter is no greater than 50mm. The volume ratio of the direct-current vortex reaction tank to the flow-down chamber in the flocculation air floatation area is 1:2. The inlet at the bottom of the direct-current vortex reaction tank in the flocculation air-floating zone is provided with a guide vane structure. The bottom cone angle of the direct-current vortex reaction tank in the flocculation air floatation area is 30-45 degrees, and the ratio of the height of the inverted cone to the height of the circular straight cylinder of the direct-current vortex reaction tank is 1-2:1. The biological reaction zone is filled with a granular sludge bed layer.
A method for treating wastewater by co-flocculation air-flotation anaerobic organisms by utilizing the reactor comprises the following steps: the wastewater enters a water distributor through a water inlet pipe, and the water distributor uniformly distributes the wastewater on the section of a water inlet area of the reactor so that the wastewater enters a biological reaction area; in the biological reaction zone, wastewater flows through a granular sludge bed layer, soluble organic matters are converted into methane through the action of microorganisms, granular matters move upwards from pores of the granular sludge bed layer, three-phase separation is carried out at a three-phase separator of the biological reaction zone, separated reaction liquid partially enters a water outlet weir in a water outlet zone from the biological reaction zone and is discharged out of the reactor, and mixed liquid consisting of methane, reaction liquid and solid which is not separated enters a riser from a collector of the three-phase separator and then enters a dosing mixing zone through the riser; in the dosing mixing area, the mixed liquid enters the ejector and then is ejected from the nozzle to enter the throat, flocculating agent liquid medicine in the medicine dissolving tank is reversely absorbed by utilizing pressure drop in a mixing chamber at the front end of the throat, and the mixed liquid after dosing enters the flocculation air floatation area through the throat; in the flocculation air-floating zone, the mixed liquid enters a direct-current vortex reaction tank through a guide vane structure inlet, water flow is mixed in an inverted cone-shaped cylinder part to realize primary reaction, then enters a straight cylinder part, and the water flow is gradually relaxed along with the diameter expansion to realize the growth of flocs; floating the flocs wrapped with the bubbles to the liquid surface to form scum, removing the scum by a scum scraping machine, collecting the scum in a slag collecting tank, allowing methane escaping from the liquid surface to enter a gas collecting chamber, and returning the degassed reaction liquid from a flow reducing chamber to a water distributor through a flow reducing pipe to form the internal circulation of the mixed liquid; the sludge in the reactor is periodically discharged from the sludge discharge pipe. The dosage of the flocculant can be regulated by a flow control valve.
The invention has the advantages that: 1) Flocculation and air floatation are carried out in a flocculation air floatation area simultaneously, so that a copolymerization adhesion effect is generated, the medicament is saved, the treatment time is short, and the scum stability is good; 2) The large height-diameter ratio of the biological reaction zone is beneficial to increasing the rising flow rate, so that the granular substances are not precipitated in the biological reaction zone but enter the flocculation air floatation zone along with the mixed liquid, and the removal of the granular substances is enhanced; 3) The ejector is used as a dosing device in the dosing mixing area, and the flow control valve is matched, so that power can be saved, and the mixing is complete; 4) The direct-current vortex reaction tank in the flocculation air floatation area has the characteristic of small pressure drop, and the pressure of the mixed liquid is not increased any more; 5) The mixing intensity of partial water flow of the conical cylinder of the direct-current vortex reaction tank in the flocculation air floatation area corresponds to the rapid stirring process in the flocculation experiment; the water flow of the straight cylinder part is relaxed and corresponds to the slow stirring process in the flocculation experiment, the flocs float to the liquid surface and are immediately removed by a slag scraping machine, and the scum generating process is stable and quick to remove; 6) The scum with large energy density formed by the particles in the wastewater can be used for composting and recycling energy, and the particles in the effluent are less, and the effluent quality is good.
Drawings
FIG. 1 is a schematic diagram of the functional area of a co-flocculation air-flotation anaerobic bioreactor;
FIG. 2 is a schematic diagram of a co-flocculation air-flotation anaerobic bioreactor;
in fig. 1: a water inlet area I, a biological reaction area II, a water outlet area III, a dosing mixing area IV and a flocculation air floatation area V;
in fig. 2: the device comprises a water inlet pipe 1, a water distributor 2, a mud discharging pipe 3, a three-phase separator 4, a lifting pipe 5, a water outlet weir 6, a medicine dissolving tank 7, a flow control valve 8, a jet device 9, a direct-current vortex reaction tank 10, a downflow chamber 11, a slag scraping machine 12, a slag collecting tank 13, a downflow pipe 14 and a gas collecting chamber 15.
Detailed Description
The invention is further illustrated and described below with reference to the drawings and detailed description.
As shown in the attached drawings 1 and 2, the co-flocculation air-floatation anaerobic bioreactor comprises a water inlet area I, a biological reaction area II, a dosing mixing area IV and a flocculation air-floatation area V which are sequentially connected from bottom to top, and a water outlet area III is arranged above the biological reaction area II. The water inlet area I, the biological reaction area II and the water outlet area III are sequentially connected to form a cylindrical reactor main body, and the bottom of the water inlet area I is in a funnel shape. The water inlet area I is internally provided with a water inlet pipe 1 and a water distributor 2 communicated with one end of the water inlet pipe 1, the bottom of the water inlet area I is connected with a mud discharging pipe 3, and a control valve can be arranged on the mud discharging pipe 3. The biological reaction zone II is filled with a granular sludge bed layer. The upper part of the biological reaction zone II is provided with a three-phase separator 4, and the outlet of a gas phase collector of the three-phase separator 4 is connected with a riser 5. The liquid phase channel of the three-phase separator 4 is communicated with a water outlet area III, and a water outlet weir 6 is arranged in the water outlet area III. The medicine adding mixing area IV is provided with a medicine dissolving tank 7, a flow control valve 8 and an ejector 9, a mixing chamber is arranged in the ejector 9, an inlet of the ejector 9 extends into the mixing chamber, the tail end of a pipeline at the inlet is in a nozzle shape, the mixing chamber is also connected with a throat, and when water flow is sprayed into the mixing chamber, the water flow continuously enters the throat, and negative pressure is generated based on a Venturi effect. The medicine dissolving tank 7 is used for storing flocculant liquid medicine and is communicated with a mixing chamber at the front end of a throat pipe of the ejector 9 through a pipeline with a flow control valve 8. The inlet of the ejector 9 is communicated with the riser 5. The flocculation air-floating zone V is provided with a direct-current vortex reaction tank 10 and a flow-down chamber 11, the direct-current vortex reaction tank 10 is of a continuous two-section structure, the lower section is of an inverted cone-shaped cylinder shape, the upper section is of a cylindrical straight cylinder shape, when water flow enters the lower section, turbulent flow is formed to be vigorously mixed due to the fact that the diameter is continuously increased, water flow tends to be stable after entering the upper section, and flocs are gradually agglomerated and grown in the collision contact process. The straight-flow type vortex reaction tank 10 is coaxially arranged along the center of the flocculation air-floating zone V, the flow-down chamber 11 is formed by clamping the outer wall of the straight-flow type vortex reaction tank 10 and the inner wall of the flocculation air-floating zone V, the straight-flow type vortex reaction tank 10 is annularly arranged outside the straight-flow type vortex reaction tank 10, water overflowed from the straight-flow type vortex reaction tank 10 can enter the flow-down chamber 11, and the flocculation is carried by bubbles to rise to the liquid level. The bottom of the direct-current vortex reaction tank 10 is communicated with the outlet of the ejector 9, the bottom of the downflow chamber 11 is provided with a downflow pipe 14, and the downflow pipe 14 is communicated with the water distributor 2 to form a circulation loop. A slag scraper 12 is arranged at the liquid level of the flow-down chamber 11, and a slag collecting groove 13 is arranged around the outside of the flow-down chamber 11 and used for collecting scum scraped by the slag scraper 12; the top of the downflow chamber 11 and the slag collecting groove 13 are provided with a closed space to form a gas collecting chamber 15 for collecting the gas produced by the reactor, and the gas collecting chamber 15 is provided with an exhaust pipe.
The parameters of the various components in the reactor can be set as follows: the volume ratio of the biological reaction zone II to the flocculation air floatation zone V is 50-100:1. The height-diameter ratio (H/D) of the biological reaction zone II is 5-10. The ratio of the cross-sectional area of the biological reaction zone II to the cross-sectional area of the riser 5 is greater than 2500:1, and the diameter of the riser 5 is not greater than 50mm. The volume ratio of the direct-current vortex reaction tank 10 to the flow reduction chamber 11 in the flocculation air flotation zone V is 1:2. The bottom inlet of the direct-current vortex reaction tank 10 in the flocculation air-floating zone V is provided with a guide vane structure. The cone angle of the bottom of the direct-current vortex reaction tank 10 in the flocculation air-floating zone V is 30-45 degrees, and the ratio of the height of the inverted cone-shaped cylinder to the height of the circular straight cylinder of the direct-current vortex reaction tank 10 is 1-2:1.
The method for treating wastewater by co-flocculation air floatation anaerobic organisms based on the reactor comprises the following steps: the wastewater enters a water distributor 2 through a water inlet pipe 1, and the water distributor 2 uniformly distributes the wastewater on the section of a water inlet area I of the reactor so that the wastewater enters a biological reaction area II; in the biological reaction zone II, wastewater flows through a granular sludge bed layer, soluble organic matters are converted into methane through the action of microorganisms, granular matters move upwards from pores of the granular sludge bed layer, three-phase separation is carried out at a three-phase separator 4 of the biological reaction zone II, separated reaction liquid enters a water outlet weir 6 in a water outlet zone III from the biological reaction zone II to be discharged out of the reactor, and mixed liquid consisting of methane, reaction liquid and solid which is not separated enters a riser 5 from a collector of the three-phase separator 4 and then enters a dosing mixing zone IV through the riser 5; in the dosing mixing zone IV, mixed liquid enters a jet device 9 and then is ejected from a nozzle to enter a throat, flocculant liquid medicine in a medicine dissolving tank 7 is sucked in a mixing chamber at the front end of the throat by utilizing pressure drop, and the dosage of flocculant is regulated by a flow control valve 8; the mixed liquid after adding the medicine enters a flocculation air floatation zone V through a throat pipe; in the flocculation air-floating zone V, the mixed liquid enters a direct-current vortex reaction tank 10 through a guide vane structure inlet, water flow is vigorously mixed in an inverted cone-shaped cylinder part to realize primary reaction, then enters a straight cylinder part, and the water flow is gradually relaxed along with the diameter expansion to realize the growth of flocs; the flocs wrapped with bubbles float to the liquid surface to form scum, the scum is removed by a scum scraping machine 12 and then is collected in a slag collecting groove 13, methane which escapes from the liquid surface enters a gas collecting chamber 15, and the degassed reaction liquid returns to the water distributor 2 from a flow reducing chamber 11 through a flow reducing pipe 14 to form the internal circulation of mixed liquid; the sludge in the reactor is periodically discharged from the sludge discharge pipe 3.
The key point of the present invention for realizing the co-flocculation air floatation process is that the height ratio of the conical cylinder part and the straight cylinder part in the direct-flow vortex reaction tank in the flocculation air floatation zone is enhanced by controlling the height ratio of the conical cylinder part and the straight cylinder part in the direct-flow vortex reaction tank. The reactor is operated under high load to increase the cross-sectional area of the bio-reaction zone or decrease the cross-sectional area of the riser to obtain liquid lifting power.
Claims (8)
1. A co-flocculation air-float anaerobic bioreactor, which is characterized in that: comprises a water inlet area (I), a biological reaction area (II), a water outlet area (III), a dosing mixing area (IV) and a flocculation air floatation area (V) which are arranged from bottom to top; a water inlet pipe (1) and a water distributor (2) communicated with one end of the water inlet pipe (1) are arranged in the water inlet area (I), and the bottom of the water inlet area (I) is connected with a mud pipe (3); the upper part of the biological reaction zone (II) is provided with a three-phase separator (4), and the three-phase separator (4) is connected with a lifting pipe (5); an effluent weir (6) is arranged in the effluent area (III); the medicine adding mixing area (IV) is provided with a medicine dissolving tank (7), a flow control valve (8) and a jet device (9), the medicine dissolving tank (7) is communicated with a throat pipe of the jet device (9) through a pipeline with the flow control valve (8), and an inlet of the jet device (9) is communicated with the lifting pipe (5); the flocculation air flotation zone (V) is internally provided with a direct-current vortex reaction tank (10) and a flow reduction chamber (11), the direct-current vortex reaction tank (10) is of a continuous two-section structure, the lower section is of an inverted cone-shaped cylinder shape, the upper section is of a cylinder shape, the direct-current vortex reaction tank (10) is coaxially arranged along the center of the flocculation air flotation zone (V), the flow reduction chamber (11) is formed by clamping the outer wall of the direct-current vortex reaction tank (10) and the inner wall of the flocculation air flotation zone (V), the bottom of the direct-current vortex reaction tank (10) is communicated with the outlet of a jet device (9), the bottom of the flow reduction chamber (11) is provided with a flow reduction pipe (14), and the flow reduction pipe (14) is communicated with the water distributor (2); a slag scraping machine (12) is arranged at the liquid level of the flow reducing chamber (11), and a slag collecting groove (13) is arranged outside the flow reducing chamber (11) in a surrounding manner and is used for collecting scum scraped by the slag scraping machine (12); the top of the flow-down chamber (11) and the slag collecting groove (13) are provided with a closed space to form a gas collecting chamber (15) for collecting the gas produced by the reactor, and the gas collecting chamber (15) is provided with an exhaust pipe;
the volume ratio of the biological reaction area (II) to the flocculation air floatation area (V) is 50-100:1; the height-to-diameter ratio of the biological reaction zone (II) is 5-10.
2. A co-flocculation air flotation anaerobic bioreactor according to claim 1, wherein the ratio of the cross-sectional area of the biological reaction zone (ii) to the cross-sectional area of the riser (5) is greater than 2500:1 and the riser (5) diameter is no greater than 50mm.
3. A co-flocculation air flotation anaerobic bioreactor according to claim 1, wherein the ratio of the volume of the direct flow vortex reaction tank (10) to the volume of the down flow chamber (11) in the flocculation air flotation zone (v) is 1:2.
4. A co-flocculation air-flotation anaerobic bioreactor as claimed in claim 1, wherein the inlet at the bottom of the direct-current vortex reaction tank (10) in the flocculation air-flotation zone (v) is provided with a guide vane structure.
5. The co-flocculation air-floatation anaerobic bioreactor according to claim 1, wherein the bottom cone angle of the direct-current vortex reaction tank (10) in the flocculation air-floatation zone (V) is 30-45 degrees, and the ratio of the inverted cone height of the direct-current vortex reaction tank (10) to the height of the circular straight cylinder is 1-2:1.
6. A co-flocculation air flotation anaerobic bioreactor according to claim 1, wherein the biological reaction zone (ii) is filled with a bed of granular sludge.
7. A method for treating wastewater by utilizing co-flocculation air flotation anaerobic organisms of the reactor according to claim 1, which is characterized in that the wastewater enters a water distributor (2) through a water inlet pipe (1), and the water distributor (2) uniformly distributes the wastewater on the section of a water inlet area (I) of the reactor so that the wastewater enters a biological reaction area (II); in the biological reaction zone (II), wastewater flows through a granular sludge bed layer, soluble organic matters are converted into methane through the action of microorganisms, granular matters move upwards from pores of the granular sludge bed layer, three-phase separation is carried out at a three-phase separator (4) of the biological reaction zone (II), separated reaction liquid part enters an effluent weir (6) in a water outlet zone (III) from the biological reaction zone (II) to be discharged out of the reactor, and mixed liquid consisting of methane, reaction liquid and solid which is not separated enters a riser (5) from a collector of the three-phase separator (4) and then enters a dosing mixing zone (IV) through the riser (5); in the dosing mixing zone (IV), the mixed solution enters a jet ejector (9) and then is ejected from a nozzle to enter a throat, the flocculating agent liquid medicine in a drug dissolving tank (7) is sucked back by utilizing pressure drop in a mixing chamber at the front end of the throat, and the mixed solution after dosing enters a flocculation air floatation zone (V) through the throat; in the flocculation air-floating zone (V), the mixed liquid enters a direct-current vortex reaction tank (10) through a guide vane structure inlet, water flow is mixed in an inverted cone-shaped cylinder part to realize primary reaction, then enters a straight cylinder part, and the water flow is gradually relaxed along with the diameter expansion to realize the growth of flocs; the flocs wrapped with bubbles float to the liquid surface to form scum, the scum is collected in a slag collecting groove (13) after being removed by a slag scraping machine (12), methane which escapes from the liquid surface enters a gas collecting chamber (15), and the degassed reaction liquid returns to the water distributor (2) from a flow reducing chamber (11) through a flow reducing pipe (14) to form the internal circulation of the mixed liquid; the sludge in the reactor is periodically discharged from the sludge discharge pipe (3).
8. A method according to claim 7, characterized in that the dosage of flocculant is regulated by means of a flow control valve (8).
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