CN108529834A - A kind of method and its device of Fenton-SMAD-BBR processing high concentrated organic wastewater - Google Patents

A kind of method and its device of Fenton-SMAD-BBR processing high concentrated organic wastewater Download PDF

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CN108529834A
CN108529834A CN201810683096.4A CN201810683096A CN108529834A CN 108529834 A CN108529834 A CN 108529834A CN 201810683096 A CN201810683096 A CN 201810683096A CN 108529834 A CN108529834 A CN 108529834A
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water
zone
smad
sludge
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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Qingdao University of Technology
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Priority to CN201810683096.4A priority Critical patent/CN108529834A/en
Publication of CN108529834A publication Critical patent/CN108529834A/en
Priority to CN201910558015.2A priority patent/CN110104912B/en
Priority to CN201920967198.9U priority patent/CN210457831U/en
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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 invention discloses methods and its device that a kind of Fenton-SMAD-BBR handle high concentrated organic wastewater, device specifically includes integral type Fenton oxidation tower, self mixing type anaerobic reactor, water conservancy diversion bioreactor, regulating reservoir, sludge concentration tank and centrifugal dehydrator, integral type Fenton oxidation tower supernatant outlet is connected to self mixing type anaerobic reactor water inlet pipe, self mixing type anaerobic reactor water outlet is connected to water conservancy diversion bioreactor water inlet, self mixing type anaerobic reactor and the outlet of water conservancy diversion bioreactor base sludge are connected to sludge concentration tank one end, the sludge concentration tank other end connects centrifugal dehydrator.Waste water carries out initial breakdown by integral type Fenton oxidation tower, improve the biodegradability of waste water, then using SMAD the and BBR group technologies improved to existing biochemical processing process, COD, BOD and ammonia nitrogen in waste water are reduced, the two is mutually coordinated, synergistic effect is realized and is handled safe and harmlessization of organic wastewater, simple for process compact, capital construction area is saved, management and transport are facilitated.

Description

A kind of method of Fenton-SMAD-BBR processing high concentrated organic wastewater and its Device
Technical field
The invention belongs to technical field of waste water processing, and in particular to it is a kind of it is effective degradation high concentrated organic wastewater device and Method, the biodegradability of waste water is improved by Fenton oxidation, and waste water further passes through improved biochemical reaction device (SMAD- BBR), the efficiency of wastewater treatment is improved, whole device floor space is small, is easy to control, and is readily transported.
Background technology
It is rapidly developed with the chemical industry in China, chemical industry produces a large amount of organic contamination during production Object, these pollutants enter water body, quality of water environment are caused to deteriorate by all means, and threaten human life's safety.Change Work waste water has the characteristics that change of water quality is big, biodegradability is poor, is difficult to degrade, using general biochemical treatment, it is difficult to drop completely The useless Organic substance in water of solution, treatment effect are undesirable.Under normal conditions, it can be taken according to the water quality situation of actual waste water appropriate pre- Processing method, such as flocculation, light electrolysis, Fenton oxidation technique destroy organic matter difficult to degrade in waste water, while improving waste water Biodegradability, then it is combined biological treatment, such as SBR, A/O, A2The techniques such as/O, handle waste water.Fenton oxidation method is Hydrogen peroxide and ferrous sulfate are mixed in a certain ratio, under the conditions of pH appropriate, hydroxyl radical free radical (OH) is generated, utilizes The oxidation operation of bio-refractory in waste water is decomposed into the strong oxidizing property non-selectivity of hydroxyl radical free radical H2O and CO2.It is existing Some Fenton oxidation devices generally use the device disclosed in patent CN105621740B, including Fenton's reaction device and coagulation Integral pool is precipitated, waste water passes through Fenton oxidation device under the action of Fenton reagent, into coagulating sedimentation integral pool.Although it has There is good treatment effect, but occupation area of equipment is big, construction cost is high.In addition, the process of Fenton oxidation processing organic wastewater In, a large amount of chemical agent is not only consumed, and generate a large amount of reluctant iron cement, for this purpose, past in actual application Toward by Fenton oxidation and other biochemical treatment processes, for example, patent CN201310446135.6 disclose a kind of Fenton oxidation and The method of the life assemblage process poly- waste water of height with high salt passes sequentially through Fenton oxidation, dephosphorization of flocculating, hydrolysis acidification, anaerobism Reaction, secondary chemical oxidation, level-one Aerobic Process for Treatment and two level Aerobic Process for Treatment handle waste water, and technique is cumbersome, complex management, Only water retention system just needs Pyatyi, and occupation area of equipment is big, is not easy to move, and patent CN2012102755721 discloses one kind It is anti-to pass sequentially through coagulation air-float, iron-carbon micro-electrolysis and ultraviolet Fenton oxidation for the processing method of high concentration hard-degraded organic waste water It answers device to pre-process waste water, reduces organic matter difficult to degrade in waste water, improve biodegradability, then pass through again through waste water normal The A of rule2/ O biochemical process, this method front end pretreating process is complicated, consumes a large amount of chemical agent, ultraviolet Fenton oxidation reaction Flocculation sediment is also needed to after device processing, while entire technique has the deficiencies of taking up a large area, being difficult to control.Therefore, anxious at present Need a kind of floor space small, the high concentrated organic wastewater processing unit for being moved easily and managing.
Invention content
It is an object of the invention to overcome disadvantage existing in the prior art, seek to design at a kind of high concentrated organic wastewater Reason method and its device, which solve existing treatment process/devices, and existing complex process, occupation area of equipment are big, heavy, The problem of not easily shifted and control management.
To achieve the goals above, Fenton-SMAD-BBR high concentrated organic wastewater processing units of the present invention, Specifically include integral type Fenton oxidation tower, self mixing type anaerobic reactor (SMAD), water conservancy diversion bioreactor (BBR), regulating reservoir, dirt Mud thickener and centrifugal dehydrator, integral type Fenton oxidation tower supernatant outlet are connected to self mixing type anaerobic reactor water inlet pipe, Self mixing type anaerobic reactor water outlet is connected to water conservancy diversion bioreactor water inlet, and self mixing type anaerobic reactor and water conservancy diversion biology are anti- The outlet of device base sludge is answered to be connected to sludge concentration tank one end, the sludge concentration tank other end connects centrifugal dehydrator.
Integral type Fenton oxidation tower (Fenton) of the present invention, including tank body, mechanical stirring device, time relay Device, elevator pump, sulfuric acid drug slot, sodium hydroxide drug slot, ferrous sulfate drug slot, hydrogen peroxide drug slot, the first water outlet, the first sludge row Put mouth, water inlet, sulfuric acid dispensing mouth, sodium hydroxide dispensing mouth, ferrous sulfate dispensing mouth and hydrogen peroxide dispensing mouth, tank body on to Under be followed successively by the reaction zone of circular cylinder body composition and settling zone that infundibulate cylinder is constituted, mechanical stirring device is fixedly mounted on tank On body head cover, the stirring rod of mechanical stirring device stretches into tank body cavity, and the first water outlet, infundibulate cylinder are arranged in the middle part of tank body The first mud discharging mouth is arranged in body bottom, and sulfuric acid drug slot, sodium hydroxide drug slot, ferrous sulfate is fixedly installed respectively on the outside of tank body Water inlet, sulfuric acid dispensing mouth, sodium hydroxide dispensing mouth, ferrous sulfate dispensing is arranged on tank body top in drug slot and hydrogen peroxide drug slot Mouth and hydrogen peroxide dispensing mouth, sulfuric acid drug slot pass sequentially through sulfuric acid dosing pump, and on sulfuric acid dosing pump external pipe The time relay is connected to sulfuric acid dispensing mouth, and ferrous sulfate drug slot passes sequentially through ferrous sulfate dosing pump, and is mounted on sulfuric acid The time relay on ferrous dosing pump external pipe is connected to ferrous sulfate dispensing mouth, and hydrogen peroxide drug slot passes sequentially through hydrogen peroxide Dosing pump, and the time relay on hydrogen peroxide dosing pump external pipe are connected to hydrogen peroxide dispensing mouth, hydroxide Sodium drug slot passes sequentially through sodium hydroxide dosing pump, and the time relay on sodium hydroxide dosing pump external pipe with Sodium hydroxide dispensing mouth connection, water inlet are connected to promoting 106 by pipeline, and waste water is pumped into tank body.
Further, the angle α of the external pipeline of the first water outlet and horizontal plane is 15 °.
To be conducive to infall process, the angle β of circular cylinder body and infundibulate cylinder junction is 135 °.
Further, self mixing type anaerobic reactor, including reactor body, the periodical great waves formula lifting device from driving And thermostat, thermostatically-controlled equipment are mounted on inside reactor body for controlling reactor body water temperature inside, water inlet pipe One end is fixed on reactor body top, and the other end is extend into inside reactor body, reactor body bottom fixed setting branch Support, riser are fixed on supporting rack top, and gas collection ring is fixed on riser, and gas is formed in gas collection ring lower part Collecting region is fixedly mounted the baffle around riser in plenum zone, opens up aperture on the riser on the inside of baffle, second goes out The mouth of a river and gas outlet are arranged at reactor body top, and the second mud discharging mouth, the second sludge row is arranged in reactor bottom It puts mouth to be connected to sludge concentration tank, riser, gas collection ring, aperture and baffle, which are constituted, periodically to be promoted from the great waves formula of driving Device；Water conservancy diversion bioreactor, including the anoxic zone, aerobic zone and the static decanting zone that are separated by partition and are sequentially communicated, Reflux is set between anoxic zone and aerobic zone, sludge refluxing apparatus is set between anoxic zone and static decanting zone, is being lacked Mixed stirring device is fixedly installed in oxygen area, and aerator, the external air blower of aerator, static state sedimentation are installed in aerobic zone bottom Supernatant outlet and third mud discharging mouth is respectively set in area side.
Further, self mixing type anaerobic reactor further includes circulating pump, circulating pump by pipeline by gas collection ring with go out Gas port is connected to.
Fenton-SMAD-BBR High-concentration organic wastewater treatment methods of the present invention, specifically include following steps：
(1) waste water is transported to regulating reservoir, waste water COD content≤60000mg/L is adjusted by dilution；
(2) waste water obtained by step (1) is pumped into integral type Fenton oxidation tower, is then added into integral type Fenton oxidation tower Sulfuric acid adjusts wastewater pH between 3-4, hydrogen peroxide dosing pump and sodium hydroxide ferrous iron dosing pump is controlled respectively, according to molar ratio FeSO4：H2O2It is 1:3, hydrogen peroxide solution and ferrous hydroxide ferrous solution are pumped into integral type Fenton oxidation tower, in machinery It under the action of agitating device, reacts 1 hour, stops stirring, it is useless that sodium hydroxide solution adjustment is added in control sodium hydroxide dosing pump After water pH=7.5-8.5, residence time 8h, integral type Fenton oxidation tower bottom sludge is excluded from the first mud discharging mouth, on Clear liquid enters next step；
(3) supernatant enters self mixing type anaerobic reactor (SMAD), and adjustment self mixing type anaerobic reactor temperature is in 25-30 DEG C, anaerobic bacteria in reactor consumes the organic matter in waste water, after processing water outlet by the tops SMAD water outlet be discharged into Enter next step, SMAD generates biogas while reducing useless Organic substance in water, and gas collection ring captures the bubble to be formed, in gas Merge in body collecting region and rise subsequently into riser, and along riser, in the process, very strong suction is generated in riser The solid of reactor bottom and liquid are sucked from the trepanning of supporting rack, and rise to reactor top along riser by power；
(4) SMAD water outlets first pass around anoxic zone into water conservancy diversion bioreactor (BBR), will under the action of microorganism Dissolved organic matter is hydrolyzed to organic acid, and larger molecular organics is made to be decomposed into small organic molecule, insoluble organic matter conversion It removes the BOD in waste water subsequently into aerobic zone at dissolved organic matter and is nitrified, by NH4+It is oxidized to NO3-, part Waste water returns to anoxic zone using reflux, denitrification is carried out under the action of microorganism, by NO3-It is reduced to molecular state Nitrogen, finally, aerobic zone waste water enter static decanting zone, and supernatant is discharged by water outlet, and static decanting zone partial sludge passes through Sludge refluxing apparatus returns to anoxic zone, and the third mud discharging mouth that excess sludge is arranged by static decanting zone bottom is transported to dirt Mud thickener, whole process realize the removal of organic matter and ammonia nitrogen；
(5) sludge is further conveyed to centrifugal dehydrator dehydration, completes Treatment of Sludge by concentration in sludge concentration tank.
Compared with prior art, the present invention haing the following advantages：(1) pass through integral type Fenton oxidation tower, the difficulty in waste water Degradation of organic substances is effectively degraded, while improving the biodegradability of waste water, reduces the usage amount of Fenton reagent, from basic On reduce the generation of Fenton sludge, reduce operating cost；(2) integral type Fenton oxidation tower will aoxidize epoxy reaction area and precipitation Area is merged, and device is without being arranged sedimentation basin, while SMAD and BBR improves existing biochemical processing process, overcomes Prior art takes up a large area, complex process, high energy consumption, it is difficult to the shortcomings that maintaining compared with high sludge concentration；(3)Fenton— The group technology of SMAD-BBR designs, on the basis of integral type Fenton oxidation tower improves wastewater biodegradability, SMAD-BBR Biochemical treatment is carried out to waste water, reduces COD, BOD and ammonia nitrogen, the higher biochemical treatment performances of SMAD-BBR further reduced Integral type Fenton oxidation tower processing pressure, the two is mutually coordinated, and synergistic effect realizes the safe and harmlessization place to organic wastewater Reason, it is simple for process compact, capital construction area is saved, management and transport are facilitated, enhances the capacity of resisting impact load of device.
Description of the drawings
Fig. 1 is Fenton-SMAD-BBR High-concentration organic wastewater treatment method technique streams that the embodiment of the present invention 1 is related to Cheng Tu.
Fig. 2 is the integral type Fenton oxidation tower structure schematic diagram involved in the embodiment of the present invention 1.
Fig. 3 is the integral type Fenton oxidation tower sectional view involved in the embodiment of the present invention 1.
Fig. 4 is the integral type Fenton oxidation tower vertical view involved in the embodiment of the present invention 1.
Fig. 5 is the self mixing type anaerobic reactor principle schematic diagram involved in the embodiment of the present invention 1.
Fig. 6 is the water conservancy diversion bioreactor construction principle schematic involved in the embodiment of the present invention 1.
Specific implementation mode
The present invention is described further below by specific implementation mode.
Embodiment 1：
As shown in Figure 1, Fenton-SMAD-BBR high concentrated organic wastewater processing units that the present embodiment is related to, specifically Including integral type Fenton oxidation tower 1, self mixing type anaerobic reactor (SMAD) 2, water conservancy diversion bioreactor (BBR) 3, regulating reservoir 4, dirt Mud thickener 5 and centrifugal dehydrator 6,1 supernatant outlet of integral type Fenton oxidation tower connect with 2 water inlet pipe of self mixing type anaerobic reactor Logical, 2 water outlet of self mixing type anaerobic reactor is connected to 3 water inlet of water conservancy diversion bioreactor, self mixing type anaerobic reactor 2 and water conservancy diversion The outlet of bioreactor base sludge is connected to 5 one end of sludge concentration tank, and 5 other end of sludge concentration tank connects centrifugal dehydrator 6。
As in Figure 2-4, the integral type Fenton oxidation tower (Fenton) 1 that the present embodiment is related to, including tank body, mechanical agitation Device 103, the time relay 105, elevator pump 106, sulfuric acid drug slot 107, sodium hydroxide drug slot 108, ferrous sulfate drug slot 109, Hydrogen peroxide drug slot 110, the first water outlet 111, the first mud discharging mouth 112, water inlet 113, sulfuric acid dispensing mouth 115, hydroxide Sodium dispensing mouth 115, ferrous sulfate dispensing mouth 116 and hydrogen peroxide dispensing mouth 117, tank body are followed successively by circular cylinder body 101 from the top down The settling zone that the reaction zone and infundibulate cylinder 102 of composition are constituted, mechanical stirring device 103 are fixedly mounted on tank body head cover, The stirring rod 104 of mechanical stirring device 103 stretches into tank body cavity, and the first water outlet 111, infundibulate cylinder are arranged in the middle part of tank body The first mud discharging mouth 112 is arranged in 102 bottom of body, and sulfuric acid drug slot 107, sodium hydroxide drug slot is fixedly installed respectively on the outside of tank body 108, water inlet 113, sulfuric acid dispensing mouth 115, hydrogen-oxygen is arranged on tank body top in ferrous sulfate drug slot 109 and hydrogen peroxide drug slot 110 Change sodium dispensing mouth 115, ferrous sulfate dispensing mouth 116 and hydrogen peroxide dispensing mouth 117, sulfuric acid drug slot 107 and passes sequentially through sulfuric acid dosing It pumps, and the time relay 105 on sulfuric acid dosing pump external pipe is connected to sulfuric acid dispensing mouth 115, ferrous sulfate Drug slot 109 passes sequentially through ferrous sulfate dosing pump, and the time relay on ferrous sulfate dosing pump external pipe 105 are connected to ferrous sulfate dispensing mouth 116, and hydrogen peroxide drug slot 110 passes sequentially through hydrogen peroxide dosing pump, and is mounted on hydrogen peroxide The time relay 105 on dosing pump external pipe is connected to hydrogen peroxide dispensing mouth 117, and sodium hydroxide drug slot 108 passes sequentially through Sodium hydroxide dosing pump, and the time relay 105 on sodium hydroxide dosing pump external pipe and sodium hydroxide throwing Medicine mouth 115 is connected to, and water inlet 113 is connected to elevator pump 106 by pipeline, and waste water is pumped into tank body.
Further, the angle α of the first water outlet 111 external pipeline and horizontal plane is 15 °.
To be conducive to infall process, the angle β of circular cylinder body 101 and 102 junction of infundibulate cylinder is 135 °.
As shown in figure 5, self mixing type anaerobic reactor 2, includes the great waves formula promotion dress of reactor body, periodically driving certainly It sets and thermostat, thermostatically-controlled equipment is mounted on inside reactor body for controlling reactor body water temperature inside, intakes 201 one end of pipe is fixed on reactor body top, and the other end is extend into inside reactor body, and reactor body bottom is fixed and set Supporting rack 202 is set, riser 203 is fixed on 202 top of supporting rack, and gas collection ring 204 is fixed on riser 203, in gas Body collects 204 lower part of ring and forms plenum zone 205, and the baffle around riser 203 is fixedly mounted in plenum zone 205 206, aperture 207 is opened up on the riser 203 of the inside of baffle 206, and the second water outlet 208 and gas outlet 209 are arranged at reaction The second mud discharging mouth 210 is arranged in reactor bottom in device body upper part, and the second mud discharging mouth 210 connects with sludge concentration tank 5 It is logical, wherein riser 203, gas collection ring 204, aperture 207 and baffle 206, which are constituted, periodically to be promoted from the great waves formula of driving Device；As shown in fig. 6, water conservancy diversion bioreactor 3, including the anoxic zone 301, the aerobic zone that are separated by partition and are sequentially communicated 302 and static decanting zone 303, reflux 307 is set between anoxic zone 301 and aerobic zone 302, in anoxic zone 301 and quiet Sludge refluxing apparatus 304 is set between state decanting zone 303, mixed stirring device 305 is fixedly installed in anoxic zone 301, mixing is stirred It can be the great waves formula lifting device that mechanical stirring device can also be periodical driving certainly to mix device 305, at 303 bottom of aerobic zone Aerator 306 is installed in portion, and 306 external air blower of aerator, supernatant outlet is respectively set in 303 side of static decanting zone 308 and third mud discharging mouth 309.
Self mixing type anaerobic reactor 2 further includes circulating pump, and circulating pump is by pipeline by gas collection ring 204 and gas outlet 209 connections.
Fenton-SMAD-BBR High-concentration organic wastewater treatment methods that the present embodiment is related to, specifically include following step Suddenly：
(1) waste water is transported to regulating reservoir 4, waste water COD content≤60000mg/L is adjusted by dilution；
(2) waste water obtained by step (1) is pumped into integral type Fenton oxidation tower 1, then added into integral type Fenton oxidation tower 1 Enter sulfuric acid and adjust wastewater pH between 3-4, hydrogen peroxide dosing pump and sodium hydroxide ferrous iron dosing pump is controlled respectively, according to molar ratio FeSO4：H2O2It is 1:3, hydrogen peroxide solution and ferrous hydroxide ferrous solution are pumped into 1 in integral type Fenton oxidation tower, in machinery It under the action of agitating device, reacts 1 hour, stops stirring, it is useless that sodium hydroxide solution adjustment is added in control sodium hydroxide dosing pump After water pH=7.5-8.5, residence time 8h, by 1 base sludge of integral type Fenton oxidation tower from 112 row of the first mud discharging mouth It removes, supernatant enters next step；
(3) supernatant enters self mixing type anaerobic reactor (SMAD) 2, and adjustment self mixing type anaerobic reactor temperature is in 25-30 DEG C, anaerobic bacteria in reactor consumes the organic matter in waste water, after processing water outlet by the tops SMAD water outlet be discharged into Entering next step, SMAD generates biogas while reducing useless Organic substance in water, and gas collection ring 204 captures the bubble formed, Merge subsequently into riser 203 in plenum zone 205, and rises along riser 203, in the process, riser It is interior to generate very strong suction, the solid of reactor bottom and liquid are sucked from the trepanning of supporting rack 202, and along riser 203 rise to reactor top, great waves formula lifting device can periodical improving material, be effectively mixed with material, smash dirt Mud improves biochemical efficiency；
(4) SMAD water outlets first pass around anoxic zone 301 into water conservancy diversion bioreactor (BBR) 3, in the effect of microorganism Under, dissolved organic matter is hydrolyzed to organic acid, larger molecular organics is made to be decomposed into small organic molecule, insoluble organic matter It is converted to dissolved organic matter, subsequently into aerobic zone 302, the BOD in waste water is removed and is nitrified, by NH3-N(NH4+) oxygen Turn to NO3-, effluent part is using the return of reflux 307 anoxic zone 301, progress denitrification work under the action of microorganism With NO3- is reduced to molecular nitrogen (N2), finally, 301 waste water of aerobic zone enters static decanting zone 303, and supernatant is by going out The mouth of a river 308 is discharged, and 303 partial sludge of static decanting zone returns to anoxic zone 301 by sludge refluxing apparatus 304, and excess sludge is logical The third mud discharging mouth 309 for crossing the setting of 303 bottom of static decanting zone is transported to sludge concentration tank 5, and whole process has realized The removal of machine object and ammonia nitrogen；
(5) sludge is further conveyed to the dehydration of centrifugal dehydrator 6, completes at sludge by concentration in sludge concentration tank 5 Reason.
Embodiment 2：
Certain chemical enterprise is handled using 1 described device of embodiment and generates his liquid crystal washes.High concentration washes Water quality：CODCr≤ 150000mg/L, BOD5≤ 80000mg/L, ammonia nitrogen≤60mg/L, SS≤500mg/L, and it is main dirty in waste water Contaminate the lauryl glucosyl and ester DEHP that substance is bio-refractory；Low concentration washes water quality：CODCr≤500mg/ L, BOD5≤ 200mg/L, ammonia nitrogen≤30mg/L.Effluent quality is required to meet《Sewage is discharged into town sewer water standard》(GB/ T31962-2015) B grades of standards, i.e. COD in table 1Cr≤ 500mg/L, BOD5≤ 350mg/L, ammonia nitrogen≤45mg/L, SS≤ 400mg/L。
Concrete processing procedure includes following operating procedure：
(1) enter regulating reservoir, waste water quality after mixing after collecting high concentration washes and low concentration washes： CODCrFor 60000mg/L, BOD5For 25000mg/L, ammonia nitrogen 45mg/L, SS 500mg/L；
(2) rear waste water is transported in integral type Fenton oxidation tower after the adjustment, passes through sulfuric acid dosing pump and H is added2SO4Solution, will Wastewater pH is adjusted to 3, the administration timing of drug of ferrous sulfate dosing pump and hydrogen peroxide dosing pump is controlled, by 1:FeSO is added in 3 molar ratios4It is molten Liquid and H2O2Solution, the reaction time 1h under the stirring of mechanical stirring device stop stirring, NaOH solution are added, by wastewater pH tune Section is precipitated to 8, and supernatant is transported to self mixing type anaerobic reactor by water outlet after residence time 8h, and precipitating sludge is logical It crosses mud discharging mouth and is transported to sludge concentration device.After Fenton oxidation, the biodegradability of waste water can effectively improve.Through Effluent quality after integral type Fenton oxidation tower：CODCrFor 35000mg/L, BOD5It is for 15000mg/L, ammonia nitrogen 45mg/L, SS 350mg/L；
(3) step (2) supernatant enters SMAD processing, effluent quality after SMAD reactions：CODCrFor 4000mg/L, BOD5For 2700mg/L, ammonia nitrogen 45mg/L, SS 350mg/L；
(4) SMAD water outlets enter baffle type biological reactor (BBR), after processing, effluent quality：CODCrFor 480mg/L, BOD5For 200mg/L, ammonia nitrogen 35mg/L, SS 350mg/L；
(5) sludge that step (3) and step (4) generate, which is transported in sludge concentration tank, is concentrated, and is then transported to again Centrifugal dehydrator is dehydrated, and completes Treatment of Sludge.
Final outflow water reaches《Sewage is discharged into town sewer water standard》(GB/T31962-2015) B grades of standards in table 1, Processed waste water is discharged into plant area's wastewater reuse approach station to handle.After wherein sludge concentration tank collects sludge condensation, pass through Centrifugal dehydrator is dehydrated, mud cake outward transport.

Claims (7)

1. a kind of device of Fenton-SMAD-BBR processing high concentrated organic wastewater, which is characterized in that specifically include integral type Fenton oxidation tower, self mixing type anaerobic reactor, water conservancy diversion bioreactor, regulating reservoir, sludge concentration tank and centrifugal dehydrator, one Formula Fenton oxidation tower supernatant outlet is connected to self mixing type anaerobic reactor water inlet pipe, self mixing type anaerobic reactor water outlet with lead Bioreactor water inlet is connected to, and self mixing type anaerobic reactor and the outlet of water conservancy diversion bioreactor base sludge are dense with sludge Contracting pond one end is connected to, and the sludge concentration tank other end connects centrifugal dehydrator.
2. the device of Fenton-SMAD-BBR processing high concentrated organic wastewater according to claim 1, feature exist In, integral type Fenton oxidation tower, including tank body, mechanical stirring device, the time relay, elevator pump, sulfuric acid drug slot, sodium hydroxide Drug slot, ferrous sulfate drug slot, hydrogen peroxide drug slot, the first water outlet, the first mud discharging mouth, water inlet, sulfuric acid dispensing mouth, hydrogen-oxygen Change sodium dispensing mouth, ferrous sulfate dispensing mouth and hydrogen peroxide dispensing mouth, tank body and is followed successively by the reaction of circular cylinder body composition from the top down The settling zone that area and infundibulate cylinder are constituted, mechanical stirring device are fixedly mounted on tank body head cover, and mechanical stirring device stirs It mixes stick to stretch into tank body cavity, the first water outlet is set in the middle part of tank body, the first mud discharging mouth is arranged in infundibulate cylinder body bottom, Sulfuric acid drug slot, sodium hydroxide drug slot, ferrous sulfate drug slot and hydrogen peroxide drug slot is fixedly installed respectively on the outside of tank body, on tank body Water inlet, sulfuric acid dispensing mouth, sodium hydroxide dispensing mouth, ferrous sulfate dispensing mouth and hydrogen peroxide dispensing mouth, sulfuric acid drug slot is arranged in portion Pass sequentially through sulfuric acid dosing pump, and the time relay on sulfuric acid dosing pump external pipe and sulfuric acid dispensing mouth company Logical, ferrous sulfate drug slot passes sequentially through ferrous sulfate dosing pump, and on ferrous sulfate dosing pump external pipe when Between relay and ferrous sulfate dispensing mouth be connected to, hydrogen peroxide drug slot passes sequentially through hydrogen peroxide dosing pump, and mounted on hydrogen peroxide The time relay on dosing pump external pipe is connected to hydrogen peroxide dispensing mouth, and sodium hydroxide drug slot passes sequentially through sodium hydroxide and adds Teat pipette, and the time relay on sodium hydroxide dosing pump external pipe be connected tos with sodium hydroxide dispensing mouth, water inlet Mouth is connected to promoting 106 by pipeline, and waste water is pumped into tank body.
3. the device of Fenton-SMAD-BBR processing high concentrated organic wastewater according to claim 2, feature exist In the angle α of the external pipeline of the first water outlet and horizontal plane is 15 °.
4. the device of Fenton-SMAD-BBR processing high concentrated organic wastewater according to claim 2, feature exist In to be conducive to infall process, the angle β of circular cylinder body and infundibulate cylinder junction is 135 °.
5. the device of high concentrated organic wastewater is handled according to claim 2-4 any one of them Fenton-SMAD-BBR, It is characterized in that, self mixing type anaerobic reactor, including reactor body, periodical great waves formula lifting device and constant temperature dress from driving It sets, thermostatically-controlled equipment is mounted on for controlling reactor body water temperature inside inside reactor body, and water inlet pipe one end is fixed On reactor body top, the other end is extend into inside reactor body, and supporting rack is fixedly installed in reactor body bottom, is promoted Pipe is fixed on supporting rack top, and gas collection ring is fixed on riser, and plenum zone is formed in gas collection ring lower part, The baffle around riser is fixedly mounted in plenum zone, opens up aperture on the riser on the inside of baffle, the second water outlet and goes out Gas port is arranged at reactor body top, and the second mud discharging mouth, the second mud discharging mouth and dirt is arranged in reactor bottom Mud thickener is connected to, and riser, gas collection ring, aperture and baffle constitute the great waves formula lifting device periodically from driving；It leads Bioreactor, including the anoxic zone, aerobic zone and the static decanting zone that are separated by partition and are sequentially communicated, in anoxic zone and Reflux is set between aerobic zone, sludge refluxing apparatus is set between anoxic zone and static decanting zone, is fixed in anoxic zone Mixed stirring device is set, aerator, the external air blower of aerator, static decanting zone side point are installed in aerobic zone bottom It She Zhi not supernatant outlet and third mud discharging mouth.
6. the device of high concentrated organic wastewater is handled according to claim 5 any one of them Fenton-SMAD-BBR, it is special Sign is that self mixing type anaerobic reactor further includes circulating pump, and gas collection ring is connected to by circulating pump by pipeline with gas outlet.
7. a kind of method of Fenton-SMAD-BBR processing high concentrated organic wastewater described in claim 1, feature exist In specifically including following steps：
(1) waste water is transported to regulating reservoir, waste water COD content≤60000mg/L is adjusted by dilution；
(2) waste water obtained by step (1) is pumped into integral type Fenton oxidation tower, sulfuric acid then is added into integral type Fenton oxidation tower Wastewater pH is adjusted between 3-4, hydrogen peroxide dosing pump and sodium hydroxide ferrous iron dosing pump are controlled respectively, according to molar ratio FeSO4： H2O2It is 1:3, hydrogen peroxide solution and ferrous hydroxide ferrous solution are pumped into integral type Fenton oxidation tower, filled in mechanical agitation It under the action of setting, reacts 1 hour, stops stirring, control sodium hydroxide dosing pump addition sodium hydroxide solution adjustment wastewater pH= After 7.5-8.5, residence time 8h, integral type Fenton oxidation tower bottom sludge is excluded from the first mud discharging mouth, supernatant into Enter next step；
(3) supernatant enters self mixing type anaerobic reactor, and adjustment self mixing type anaerobic reactor temperature is in 25-30 DEG C, reactor Anaerobic bacteria the organic matter in waste water is consumed, after processing water outlet next step is discharged by the tops SMAD water outlet, SMAD generates biogas while reducing useless Organic substance in water, and gas collection ring captures the bubble to be formed, in plenum zone Merging rises subsequently into riser, and along riser, in the process, very strong suction is generated in riser, will be reacted The solid and liquid of device bottom are sucked from the trepanning of supporting rack, and rise to reactor top along riser；
(4) SMAD water outlets first pass around anoxic zone into water conservancy diversion bioreactor, will be soluble organic under the action of microorganism Object is hydrolyzed to organic acid, so that larger molecular organics is decomposed into small organic molecule, insoluble organic matter, which is converted to solubility, to be had Machine object removes the BOD in waste water and is nitrified, by NH subsequently into aerobic zone4+It is oxidized to NO3-, effluent part using Reflux returns to anoxic zone, denitrification is carried out under the action of microorganism, by NO3-It is reduced to molecular nitrogen, it is finally, good Oxygen area waste water enters static decanting zone, and supernatant is discharged by water outlet, and static decanting zone partial sludge is filled by sludge reflux It sets and returns to anoxic zone, the third mud discharging mouth that excess sludge is arranged by static decanting zone bottom is transported to sludge concentration tank, Whole process realizes the removal of organic matter and ammonia nitrogen；
(5) sludge is further conveyed to centrifugal dehydrator dehydration, completes Treatment of Sludge by concentration in sludge concentration tank.
CN201810683096.4A 2018-06-28 2018-06-28 A kind of method and its device of Fenton-SMAD-BBR processing high concentrated organic wastewater Pending CN108529834A (en)

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