CN210457831U - Device for treating high-concentration organic wastewater by Fenton-SMAD-BBR - Google Patents

Device for treating high-concentration organic wastewater by Fenton-SMAD-BBR Download PDF

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CN210457831U
CN210457831U CN201920967198.9U CN201920967198U CN210457831U CN 210457831 U CN210457831 U CN 210457831U CN 201920967198 U CN201920967198 U CN 201920967198U CN 210457831 U CN210457831 U CN 210457831U
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tank
sludge
zone
dosing
fenton
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柳超
钱彬杰
王莉元
肖传晶
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Qingdao University of Technology
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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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • C02F11/127—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering by centrifugation
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
    • 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
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/34—Organic compounds containing oxygen
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/02—Specific form of oxidant
    • C02F2305/026—Fenton's reagent
    • 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
    • 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
    • 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
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/301—Aerobic and anaerobic treatment in the same reactor
    • 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
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Treatment Of Sludge (AREA)

Abstract

The utility model discloses a device of high concentration organic waste water is handled to Fenton-SMAD-BBR, the device specifically includes the fragrant oxidation tower of integral type, from mixing formula anaerobic reactor, water conservancy diversion bioreactor, the equalizing basin, sludge thickening tank and centrifugal dehydrator, the fragrant oxidation tower supernatant outlet of integral type with from mixing formula anaerobic reactor inlet tube intercommunication, from mixing formula anaerobic reactor delivery port and water conservancy diversion bioreactor water inlet intercommunication, from mixing formula anaerobic reactor and water conservancy diversion bioreactor bottom sludge outlet all with sludge thickening tank one end intercommunication, centrifugal dehydrator is connected to the sludge thickening tank other end. Waste water carries out preliminary degradation through integral type fenton oxidation tower, has improved the biodegradability of waste water, then adopts SMAD and BBR combined process who carries out the improvement to current biochemical treatment process, reduces COD in the waste water, BOD and ammonia nitrogen, and both coordinate each other, and the synergism realizes the safe innocent treatment to organic waste water, and simple process is compact, has saved the capital construction area, convenient management and transportation.

Description

Device for treating high-concentration organic wastewater by Fenton-SMAD-BBR
Technical Field
The utility model belongs to the technical field of waste water treatment, concretely relates to device of effective degradation high concentration organic waste water has improved the biodegradability of waste water through fenton's oxidation, and waste water further improves waste water treatment's efficiency through modified biochemical reaction device (SMAD-BBR), and whole device area is little, and easy control is convenient for transport.
Background
With the rapid development of the chemical industry in China, a large amount of organic pollutants are generated in the chemical industry in the production process, and enter a water body through various ways, so that the water environment quality is deteriorated, and the life safety of human beings is threatened. The chemical wastewater has the characteristics of large water quality change, poor biodegradability, difficult degradation and the like, and is difficult to completely degrade organic matters in the wastewater by adopting general biochemical treatment, so the treatment effect is not ideal. Under normal conditions, proper pretreatment methods such as flocculation, micro-electrolysis, Fenton oxidation and other processes are adopted according to the water quality condition of actual wastewater, organic matters which are difficult to degrade in the wastewater are destroyed, the biodegradability of the wastewater is improved, and thenCombined with biological treatment processes, e.g. SBR, A/O, A2And O, and the like, and treating the wastewater. The Fenton oxidation method is to mix hydrogen peroxide and ferrous sulfate according to a certain proportion, generate hydroxyl radical (. OH) under the condition of proper pH, and utilize the strong oxidizing property of the hydroxyl radical to oxidize and decompose the organic matters which are difficult to be biochemically degraded in the wastewater into H nonselectively2O and CO2. The device disclosed in patent CN105621740B is generally adopted to current fenton oxidation unit, including the integrative pond of fenton reaction unit and coagulating sedimentation, and waste water gets into the integrative pond of coagulating sedimentation through the fenton oxidation unit under the effect of fenton reagent. Although the method has good treatment effect, the equipment occupies a large area and has high construction cost. In addition, in the process of treating organic wastewater by fenton oxidation, not only a large amount of chemical agents are consumed, but also a large amount of iron mud which is difficult to treat is generated, for this reason, in the practical application process, fenton oxidation and other biochemical treatment processes are often combined, for example, patent CN201310446135.6 discloses a method for treating high-salinity high-polymer wastewater by a combined fenton oxidation and biological process, which sequentially performs fenton oxidation, flocculation dephosphorization, hydrolytic acidification, anaerobic reaction, secondary chemical oxidation, primary aerobic treatment and secondary aerobic treatment on wastewater, the process is complicated, the management is complex, only a water storage system needs five stages, the occupied area of equipment is large, the movement is inconvenient, patent CN2012102755721 discloses a treatment method for high-concentration refractory organic wastewater, which sequentially performs coagulation air flotation, iron-carbon micro-electrolysis and ultraviolet fenton oxidation reactor on wastewater to pretreat the wastewater, so as to reduce refractory organic matters in the wastewater, increasing biodegradability, then passing through conventional A via waste water2The method has the advantages that the front-end pretreatment process is complex, a large amount of chemical agents are consumed, flocculation and precipitation are needed after treatment of the ultraviolet Fenton oxidation reactor, and meanwhile, the whole process has the defects of large floor area, difficulty in control and the like. Therefore, a high-concentration organic wastewater treatment device which occupies a small area and is convenient to move and manage is urgently needed at present.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the defects in the prior art, seek to design a high-concentration organic wastewater treatment method and a device thereof, and solve the problems of complex existing process, large equipment occupied area, heaviness, difficulty in moving and control management.
In order to realize above-mentioned purpose, the utility model relates to a Fenton-SMAD-BBR high concentration organic wastewater treatment device, specifically include the fragrant oxidation tower of integral type, from mixing formula anaerobic reactor (SMAD), water conservancy diversion bioreactor (BBR), the equalizing basin, sludge thickening tank and centrifugal dehydrator, the fragrant oxidation tower supernatant export of integral type with from mixing formula anaerobic reactor inlet tube intercommunication, from mixing formula anaerobic reactor delivery port and water conservancy diversion bioreactor water inlet intercommunication, from mixing formula anaerobic reactor and water conservancy diversion bioreactor bottom sludge outlet all with sludge thickening tank one end intercommunication, centrifugal dehydrator is connected to the sludge thickening tank other end.
The utility model relates to a Fenton oxidation tower of integral type (Fenton), which comprises a tank body, mechanical stirring device, the elevator pump, the sulphuric acid medicine groove, the sodium hydroxide medicine groove, the ferrous sulfate medicine groove, the hydrogen peroxide solution medicine groove, first delivery port, first sludge discharge port, a water inlet, sulphuric acid is thrown the medicine mouth, the sodium hydroxide is thrown the medicine mouth, ferrous sulfate is thrown the medicine mouth and the hydrogen peroxide solution is thrown the medicine mouth, the jar body is from the settling zone that reaction zone and the infundibulate barrel that constitute that the circular cylinder body constitutes downwards in proper order, mechanical stirring device fixed mounting is on jar body top cover, mechanical stirring device's stirring rod stretches into jar body cavity, set up first delivery port at jar body middle part, the infundibulate barrel bottom sets up first sludge discharge port, the sulphuric acid medicine groove is fixed respectively to set up in the external side of jar, the sodium hydroxide medicine groove, ferrous sulfate medicine groove and hydrogen peroxide solution medicine groove, the device comprises a sodium hydroxide dosing port, a ferrous sulfate dosing port and a hydrogen peroxide dosing port, wherein a sulfuric acid dosing tank is communicated with a sulfuric acid dosing port pipeline through a sulfuric acid dosing pump, the ferrous sulfate dosing tank is communicated with the ferrous sulfate dosing port pipeline through the ferrous sulfate dosing pump, the hydrogen peroxide dosing tank is communicated with the hydrogen peroxide dosing port pipeline through the hydrogen peroxide dosing pump, the sodium hydroxide dosing tank is communicated with the sodium hydroxide dosing port pipeline through the sodium hydroxide dosing pump, a water inlet is communicated with a lifting pump through a pipeline, and wastewater is pumped into a tank body.
Further, the angle α between the pipeline circumscribed by the first water outlet and the horizontal plane is 15 °.
To facilitate the settling process, the angle β at the junction of the circular cylinder and the funnel cylinder is 135 °.
Furthermore, the self-mixing anaerobic reactor comprises a reactor body, a periodically self-driven billow type lifting device and a constant temperature device, wherein the constant temperature control device is arranged in the reactor body and used for controlling the water temperature in the reactor body, one end of a water inlet pipe is fixed at the upper part of the reactor body, the other end of the water inlet pipe extends into the reactor body, a support frame is fixedly arranged at the bottom of the reactor body, a lifting pipe is fixed at the upper part of the support frame, a gas collecting ring is fixed on the lifting pipe, a gas collecting zone is formed at the lower part of the gas collecting ring, a baffle surrounding the riser is fixedly arranged in the gas collecting zone, the riser at the inner side of the baffle is provided with an orifice, the second water outlet and the gas outlet are both arranged at the upper part of the reactor body, a second sludge discharge port is arranged at the bottom of the reactor and is communicated with a sludge concentration tank, and a lifting pipe, a gas collecting ring, an orifice and a baffle form a periodic self-driven surge type lifting device; flow guide bioreactor, including the anoxic zone, aerobic zone and the static settlement zone that separate and communicate in proper order through the baffle, set up reflux unit between anoxic zone and aerobic zone, set up sludge reflux unit between anoxic zone and static settlement zone, at the fixed mixed agitating unit that sets up in anoxic zone, at aerobic zone bottom installation aeration equipment, the external air-blower of aeration equipment, static settlement zone one side sets up supernatant export and third sludge discharge mouth respectively.
Further, the self-mixing anaerobic reactor also comprises a circulating pump, and the circulating pump is communicated with the gas collecting ring and the gas outlet through a pipeline.
The utility model relates to a Fenton-SMAD-BBR high concentration organic wastewater treatment method specifically includes following steps:
(1) conveying the wastewater to a regulating reservoir, and adjusting the COD content of the wastewater to be less than or equal to 60000mg/L by dilution;
(2) pumping the wastewater obtained in the step (1) into an integrated Fenton oxidation tower, and adding the wastewater into the integrated Fenton oxidation towerAdding sulfuric acid to adjust the pH value of the wastewater to 3-4, respectively controlling a hydrogen peroxide dosing pump and a ferrous sodium hydroxide dosing pump according to the molar ratio FeSO4：H2O2Pumping a hydrogen peroxide solution and a ferrous iron hydroxide solution into an integrated Fenton oxidation tower, reacting for 1 hour under the action of a mechanical stirring device, stopping stirring, controlling a sodium hydroxide dosing pump to add the sodium hydroxide solution to adjust the pH value of wastewater to be 7.5-8.5, after the retention time is 8 hours, discharging sludge at the bottom of the integrated Fenton oxidation tower from a first sludge discharge port, and allowing supernatant to enter the next step;
(3) the supernatant enters a self-mixing anaerobic reactor (SMAD), the temperature of the self-mixing anaerobic reactor is adjusted to 25-30 ℃, anaerobic bacteria in the reactor consume organic matters in the wastewater, the treated effluent is discharged through a water outlet at the upper part of the SMAD and enters the next step, the SMAD reduces the organic matters in the wastewater and simultaneously generates methane, a gas collecting ring captures formed bubbles, the bubbles are combined in a gas collecting region and then enter a riser and ascend along the riser, and in the process, strong suction is generated in the riser to suck solids and liquid at the bottom of the reactor from an open hole of a support frame and ascend to the upper part of the reactor along the riser;
(4) SMAD effluent enters a flow guide bioreactor (BBR) and firstly passes through an anoxic zone, under the action of microorganisms, soluble organic matters are hydrolyzed into organic acid, macromolecular organic matters are decomposed into micromolecular organic matters, insoluble organic matters are converted into soluble organic matters, then the organic acid enters an aerobic zone, BOD in wastewater is removed, nitrification is carried out, and NH is carried out4+Oxidation to NO3-Part of the wastewater returns to the anoxic zone through the reflux device and is subjected to denitrification under the action of microorganisms to remove NO3-Reducing the wastewater into molecular nitrogen, finally, discharging supernatant liquid from the static settling zone through a water outlet, returning partial sludge in the static settling zone to the anoxic zone through a sludge reflux device, and conveying residual sludge to a sludge concentration tank through a third sludge discharge port arranged at the bottom of the static settling zone, so that organic matters and ammonia nitrogen are removed in the whole process;
(5) and (4) concentrating the sludge in the sludge concentration tank, and further conveying the sludge to a centrifugal dehydrator for dehydration to finish sludge treatment.
Compared with the prior art, the utility model, have following advantage: (1) through the integrated Fenton oxidation tower, the organic matters which are difficult to degrade in the wastewater are effectively degraded, the biodegradability of the wastewater is improved, the usage amount of a Fenton reagent is reduced, the generation of Fenton sludge is reduced fundamentally, and the operation cost is reduced; (2) the integrated Fenton oxidation tower integrates the oxidation-oxidation reaction zone and the sedimentation zone, a sedimentation tank is not required to be arranged in the device, and meanwhile, the SMAD and the BBR improve the existing biochemical treatment process, so that the defects of large occupied area, complex process, high energy consumption and difficulty in maintaining higher sludge concentration in the existing process are overcome; (3) Fenton-SMAD-BBR's combination process design, on the basis that the fragrant oxidation tower of integral type improves waste water biochemical nature, SMAD-BBR carries out biochemical treatment to waste water, reduce COD, BOD and ammonia nitrogen, the higher biochemical treatment performance of SMAD-BBR, the fragrant oxidation tower treatment pressure of integral type has further been reduced, both coordinate each other, the synergism, the realization is to the safe innocent treatment of organic waste water, simple process is compact, the capital construction area has been saved, convenient management and transportation, the anti impact load capacity of device has been strengthened.
Drawings
FIG. 1 is a process flow diagram of a Fenton-SMAD-BBR high-concentration organic wastewater treatment method related to embodiment 1 of the present invention.
Fig. 2 is a schematic diagram of the structure of the integrated fenton oxidation tower according to embodiment 1 of the present invention.
Fig. 3 is a sectional view of the integrated fenton oxidation tower according to embodiment 1 of the present invention.
Fig. 4 is a plan view of the integrated fenton oxidation tower according to embodiment 1 of the present invention.
Fig. 5 is a schematic structural diagram of a self-mixing anaerobic reactor according to embodiment 1 of the present invention.
FIG. 6 is a schematic view of the structure of a flow-through bioreactor according to example 1 of the present invention.
Detailed Description
The invention is further described below by means of specific embodiments.
Example 1:
as shown in fig. 1, the high concentration organic wastewater treatment apparatus of Fenton-SMAD-BBR according to the present embodiment specifically includes an integrated Fenton oxidation tower 1, a self-mixing anaerobic reactor (SMAD)2, a guided flow bioreactor (BBR)3, a regulation tank 4, a sludge concentration tank 5 and a centrifugal dehydrator 6, wherein a supernatant outlet of the integrated Fenton oxidation tower 1 is communicated with a water inlet pipe of the self-mixing anaerobic reactor 2, a water outlet of the self-mixing anaerobic reactor 2 is communicated with a water inlet of the guided flow bioreactor 3, sludge outlets at bottoms of the self-mixing anaerobic reactor 2 and the guided flow bioreactor are both communicated with one end of the sludge concentration tank 5, and the other end of the sludge concentration tank 5 is connected with the centrifugal dehydrator 6.
As shown in fig. 2 to 4, the integrated Fenton oxidation tower (Fenton)1 according to this embodiment includes a tank, a mechanical stirring device 103, a lift pump 106, a sulfuric acid tank 107, a sodium hydroxide tank 108, a ferrous sulfate tank 109, a hydrogen peroxide tank 110, a first water outlet 111, a first sludge discharge port 112, a water inlet 113, a sulfuric acid dosing port 115, a sodium hydroxide dosing port 115, a ferrous sulfate dosing port 116, and a hydrogen peroxide dosing port 105, where the tank is sequentially a reaction zone formed by a circular cylinder 101 and a settling zone formed by a funnel-shaped cylinder 102 from top to bottom, the mechanical stirring device 103 is fixedly installed on a top cover of the tank, a stirring rod 104 of the mechanical stirring device 103 extends into a cavity of the tank, the first water outlet 111 is disposed in the middle of the tank, the first sludge discharge port 112 is disposed at the bottom of the funnel-shaped cylinder 102, the sulfuric acid tank 107, the sodium hydroxide tank 108, the hydrogen peroxide tank 108, and the hydrogen, The waste water treatment device comprises a ferrous sulfate medicine tank 109 and a hydrogen peroxide medicine tank 110, wherein a water inlet 113, a sulfuric acid medicine feeding port 115, a sodium hydroxide medicine feeding port 115, a ferrous sulfate medicine feeding port 116 and a hydrogen peroxide medicine feeding port 105 are arranged at the upper part of the tank body, the sulfuric acid medicine tank 107 is communicated with the sulfuric acid medicine feeding port 115 through a sulfuric acid medicine feeding pump in a pipeline mode, the ferrous sulfate medicine tank 109 is communicated with the ferrous sulfate medicine feeding port 116 through a ferrous sulfate medicine feeding pump in a pipeline mode, the hydrogen peroxide medicine tank 110 is communicated with the hydrogen peroxide medicine feeding port 105 through a hydrogen peroxide medicine feeding pump in a pipeline mode, the sodium hydroxide medicine tank 108 is communicated with the sodium hydroxide medicine feeding port 115 through a sodium hydroxide medicine feeding pump in a pipeline mode, and the water inlet 113 is.
Further, the angle α between the pipe circumscribed by the first water outlet 111 and the horizontal plane is 15 °.
To facilitate the settling process, the angle β at the junction of the circular cylinder 101 and the funnel-shaped cylinder 102 is 135 °.
As shown in FIG. 5, the self-mixing anaerobic reactor 2 comprises a reactor body, a periodically self-driven surge type lifting device and a thermostatic device, wherein the thermostatic control device is installed inside the reactor body and used for controlling the water temperature inside the reactor body, one end of a water inlet pipe 201 is fixed on the upper part of the reactor body, the other end of the water inlet pipe extends into the reactor body, a support frame 202 is fixedly arranged at the bottom of the reactor body, a lifting pipe 203 is fixed on the upper part of the support frame 202, a gas collecting ring 204 is fixed on the lifting pipe 203, a gas collecting zone 205 is formed at the lower part of the gas collecting ring 204, a baffle plate 206 surrounding the lifting pipe 203 is fixedly installed in the gas collecting zone 205, an orifice 207 is formed on the lifting pipe 203 at the inner side of the baffle plate 206, a second water outlet 208 and a gas outlet 209 are both arranged on the upper part of the reactor body, a second sludge discharge, wherein riser 203, gas collection ring 204, orifice 207, and baffle 206 comprise a periodically self-driven billowed lift; as shown in fig. 6, the flow-guiding bioreactor 3 comprises an anoxic zone 301, an aerobic zone 302 and a static settling zone 303 which are separated by a partition plate and sequentially communicated, wherein a reflux device 307 is arranged between the anoxic zone 301 and the aerobic zone 302, a sludge reflux device 304 is arranged between the anoxic zone 301 and the static settling zone 303, a mixing and stirring device 305 is fixedly arranged in the anoxic zone 301, the mixing and stirring device 305 can be a mechanical stirring device or a periodic self-driven wave type lifting device, an aeration device 306 is arranged at the bottom of the aerobic zone 303, the aeration device 306 is externally connected with an air blower, and a supernatant outlet 308 and a third sludge discharge port 309 are respectively arranged on one side of the static settling zone 303.
The self-mixing anaerobic reactor 2 further comprises a circulating pump which communicates the gas collecting ring 204 with the gas outlet 209 through a pipeline.
The Fenton-SMAD-BBR high-concentration organic wastewater treatment method related by the embodiment specifically comprises the following steps:
(1) conveying the wastewater to a regulating tank 4, and adjusting the COD content of the wastewater to be less than or equal to 60000mg/L by dilution;
(2) pumping the wastewater obtained in the step (1) into an integrated Fenton oxidation tower 1, adding sulfuric acid into the integrated Fenton oxidation tower 1 to adjust the pH value of the wastewater to be 3-4, respectively controlling a hydrogen peroxide dosing pump and a ferrous sodium hydroxide dosing pump, and feeding FeSO according to a molar ratio4：H2O2Pumping a hydrogen peroxide solution and a ferrous iron hydroxide solution into an integrated Fenton oxidation tower 1, reacting for 1 hour under the action of a mechanical stirring device, stopping stirring, controlling a sodium hydroxide dosing pump to add the sodium hydroxide solution to adjust the pH value of wastewater to be 7.5-8.5, keeping the time for 8 hours, discharging sludge at the bottom of the integrated Fenton oxidation tower 1 from a first sludge discharge port 112, and allowing supernatant to enter the next step;
(3) the supernatant enters a self-mixing anaerobic reactor (SMAD)2, the temperature of the self-mixing anaerobic reactor is adjusted to be 25-30 ℃, anaerobic bacteria in the reactor consume organic matters in the wastewater, the treated effluent is discharged through a water outlet at the upper part of the SMAD and enters the next step, the SMAD reduces the organic matters in the wastewater and simultaneously generates methane, a gas collecting ring 204 captures formed bubbles, the bubbles are combined in a gas collecting region 205 and then enter a lifting pipe 203 and rise along the lifting pipe 203, in the process, strong suction is generated in the lifting pipe to suck solids and liquid at the bottom of the reactor from an opening of a supporting frame 202 and rise to the upper part of the reactor along the lifting pipe 203, and a wave type lifting device can periodically lift materials, effectively mix the materials, break the sludge and improve the biochemical efficiency;
(4) SMAD effluent enters a diversion bioreactor (BBR)3, firstly passes through an anoxic zone 301, under the action of microorganisms, soluble organic matters are hydrolyzed into organic acids, macromolecular organic matters are decomposed into micromolecular organic matters, insoluble organic matters are converted into soluble organic matters, then the organic acids enter an aerobic zone 302, BOD in wastewater is removed, nitrification is carried out, and NH is carried out3-N(NH4+) Oxidation to NO3-Part of the wastewater returns to the anoxic zone 301 through the reflux device 307 and is subjected to denitrification under the action of microorganisms, so thatNO 3-reduction to molecular Nitrogen (N)2) Finally, the wastewater in the aerobic zone 301 enters the static settling zone 303, the supernatant is discharged through a water outlet 308, part of the sludge in the static settling zone 303 returns to the anoxic zone 301 through a sludge reflux device 304, and the residual sludge is conveyed to the sludge concentration tank 5 through a third sludge discharge port 309 arranged at the bottom of the static settling zone 303, so that the removal of organic matters and ammonia nitrogen is realized in the whole process;
(5) and (3) concentrating the sludge in the sludge concentration tank 5, and further conveying the sludge to a centrifugal dehydrator 6 for dehydration to finish sludge treatment.
Example 2:
the apparatus described in example 1 was used to treat liquid crystal washing wastewater from a chemical plant. High-concentration washing wastewater quality: CODCr≤150000mg/L，BOD580000mg/L or less, ammonia nitrogen 60mg/L or less, SS 500mg/L or less, and main pollutants in the wastewater are dodecyl glucoside and DEHP which are difficult to degrade biochemically; low-concentration washing wastewater quality: CODCr≤500mg/L，BOD5Less than or equal to 200mg/L, and ammonia nitrogen less than or equal to 30 mg/L. The effluent quality requirement meets the B-level standard in Table 1 of Water quality Standard for Sewage discharge into urban sewer (GB/T31962-2015), namely CODCr≤500mg/L，BOD5Less than or equal to 350mg/L, ammonia nitrogen less than or equal to 45mg/L and SS less than or equal to 400 mg/L.
The specific treatment process comprises the following operation steps:
(1) collecting high-concentration washing wastewater and low-concentration washing wastewater, and then feeding the collected high-concentration washing wastewater and low-concentration washing wastewater into a regulating tank, wherein the quality of the mixed wastewater is as follows: CODCr60000mg/L, BOD525000mg/L of ammonia nitrogen, 45mg/L of ammonia nitrogen and 500mg/L of SS;
(2) the regulated wastewater is conveyed into an integrated Fenton oxidation tower and added with H through a sulfuric acid dosing pump2SO4Adjusting the pH value of the wastewater to 3, controlling the dosing time of a ferrous sulfate dosing pump and a hydrogen peroxide dosing pump, and adding FeSO according to the molar ratio of 1:34Solution and H2O2Reacting the solution for 1h under the stirring of a mechanical stirring device, stopping stirring, adding NaOH solution, adjusting the pH value of the wastewater to 8, precipitating, conveying supernate to a self-mixing anaerobic reactor through a water outlet after the supernate stays for 8h, and allowing the precipitated sludge to pass throughThe sludge discharge port is conveyed to a sludge concentration device. After Fenton oxidation, the biodegradability of the wastewater can be effectively improved. The effluent quality after passing through the integrated Fenton oxidation tower is as follows: CODCrAt 35000mg/L, BOD515000mg/L, 45mg/L ammonia nitrogen and 350mg/L SS;
(3) and (3) treating the supernatant obtained in the step (2) by using SMAD, wherein the effluent quality after SMAD reaction is as follows: CODCr4000mg/L, BOD52700mg/L, 45mg/L ammonia nitrogen and 350mg/L SS;
(4) SMAD goes out water and enters into water conservancy diversion formula bioreactor (BBR), handles the back, goes out water quality: CODCr480mg/L, BOD5200mg/L, 35mg/L ammonia nitrogen and 350mg/L SS;
(5) and (4) conveying the sludge generated in the step (3) and the step (4) into a sludge concentration tank for concentration, and then conveying the sludge into a centrifugal dehydrator for dehydration to finish sludge treatment.
And finally, the final effluent reaches the B-level standard in Table 1 of Water quality Standard for wastewater discharge to urban sewer (GB/T31962-2015), and the treated wastewater is discharged into a factory sewage centralized treatment station for treatment. Wherein, the sludge is collected by the sludge concentration tank, concentrated and dewatered by the centrifugal dehydrator, and the mud cake is transported outside.

Claims (6)

1. The utility model provides a device that high concentration organic waste water was handled to Fenton-SMAD-BBR, its characterized in that specifically includes the fragrant oxidation tower of integral type, from mixing formula anaerobic reactor, water conservancy diversion bioreactor, equalizing basin, sludge thickening tank and centrifugal dehydrator, the fragrant oxidation tower supernatant outlet of integral type and from mixing formula anaerobic reactor inlet tube intercommunication, from mixing formula anaerobic reactor delivery port and water conservancy diversion bioreactor water inlet intercommunication, from mixing formula anaerobic reactor and water conservancy diversion bioreactor bottom sludge outlet all with sludge thickening tank one end intercommunication, centrifugal dehydrator is connected to the sludge thickening tank other end.
2. The Fenton-SMAD-BBR device for treating high concentration organic wastewater according to claim 1, wherein the integrated Fenton oxidation tower comprises a tank, a mechanical stirring device, a lift pump, a sulfuric acid tank, a sodium hydroxide tank, a ferrous sulfate tank, a hydrogen peroxide tank, a first water outlet, a first sludge discharge port, a water inlet, a sulfuric acid dosing port, a sodium hydroxide dosing port, a ferrous sulfate dosing port and a hydrogen peroxide dosing port, the tank is sequentially a reaction zone formed by a circular cylinder and a settling zone formed by a funnel-shaped cylinder from top to bottom, the mechanical stirring device is fixedly installed on a top cover of the tank, a stirring rod of the mechanical stirring device extends into a cavity of the tank, the first water outlet is arranged in the middle of the tank, the first sludge discharge port is arranged at the bottom of the funnel-shaped cylinder, the sulfuric acid tank, the sodium hydroxide tank, the ferrous sulfate tank and the hydrogen peroxide tank are respectively and fixedly arranged outside the tank, the upper part of the tank body is provided with a water inlet, a sulfuric acid dosing port, a sodium hydroxide dosing port, a ferrous sulfate dosing port and a hydrogen peroxide dosing port, a sulfuric acid dosing tank is communicated with a sulfuric acid dosing port pipeline through a sulfuric acid dosing pump, a ferrous sulfate dosing tank is communicated with a ferrous sulfate dosing port pipeline through a ferrous sulfate dosing pump, a hydrogen peroxide dosing tank is communicated with a hydrogen peroxide dosing port pipeline through a hydrogen peroxide dosing pump, a sodium hydroxide dosing tank is communicated with a sodium hydroxide dosing port pipeline through a sodium hydroxide dosing pump, a water inlet is communicated with a lifting pump through a pipeline, and wastewater is pumped into the tank body.
3. The Fenton-SMAD-BBR device for treating high concentration organic wastewater according to claim 2, wherein the angle α between the external pipe of the first water outlet and the horizontal plane is 15 °.
4. The Fenton-SMAD-BBR apparatus of claim 2, wherein the angle β between the connection of the circular cylinder and the funnel cylinder is 135 ° to facilitate the settling process.
5. The Fenton-SMAD-BBR device for treating high concentration organic wastewater according to any one of claims 2 to 4, wherein the self-mixing anaerobic reactor comprises a reactor body, a periodically self-driven surge type lifting device and a thermostatic device, the thermostatic device is installed inside the reactor body for controlling the water temperature inside the reactor body, one end of the water inlet pipe is fixed on the upper part of the reactor body, the other end of the water inlet pipe extends into the reactor body, a support frame is fixedly arranged at the bottom of the reactor body, a lifting pipe is fixed on the upper part of the support frame, a gas collecting ring is fixed on the lifting pipe, a gas collecting zone is formed at the lower part of the gas collecting ring, a baffle plate surrounding the lifting pipe is fixedly installed in the gas collecting zone, an orifice is formed on the lifting pipe at the inner side of the baffle plate, a second water outlet and a gas outlet are both arranged at the upper part of the reactor body, the second sludge discharge port is communicated with a sludge concentration tank, and the lifting pipe, the gas collecting ring, the orifice and the baffle form a periodic self-driven billow type lifting device; flow guide bioreactor, including the anoxic zone, aerobic zone and the static settlement zone that separate and communicate in proper order through the baffle, set up reflux unit between anoxic zone and aerobic zone, set up sludge reflux unit between anoxic zone and static settlement zone, at the fixed mixed agitating unit that sets up in anoxic zone, at aerobic zone bottom installation aeration equipment, the external air-blower of aeration equipment, static settlement zone one side sets up supernatant export and third sludge discharge mouth respectively.
6. The apparatus for Fenton-SMAD-BBR treatment of high concentration organic wastewater according to claim 5, wherein the self-mixing anaerobic reactor further comprises a circulating pump, and the circulating pump connects the gas collecting ring with the gas outlet through a pipeline.
CN201920967198.9U 2018-06-28 2019-06-26 Device for treating high-concentration organic wastewater by Fenton-SMAD-BBR Withdrawn - After Issue CN210457831U (en)

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CN110104912A (en) * 2018-06-28 2019-08-09 青岛理工大学 Method and device for treating high-concentration organic wastewater by Fenton-SMAD-BBR
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CN110104912A (en) * 2018-06-28 2019-08-09 青岛理工大学 Method and device for treating high-concentration organic wastewater by Fenton-SMAD-BBR
CN110104912B (en) * 2018-06-28 2023-06-23 青岛理工大学 Method and device for treating high-concentration organic wastewater by Fenton-SMAD-BBR
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