CN105884151B - The method of group technology processing industrial wastewater - Google Patents
The method of group technology processing industrial wastewater Download PDFInfo
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- CN105884151B CN105884151B CN201610485435.9A CN201610485435A CN105884151B CN 105884151 B CN105884151 B CN 105884151B CN 201610485435 A CN201610485435 A CN 201610485435A CN 105884151 B CN105884151 B CN 105884151B
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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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
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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
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
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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
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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
- C02F3/30—Aerobic and anaerobic processes
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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
Abstract
The present invention provides the methods of a new combined process processing industrial wastewater, including conditioning tank, modified Fenton fluidized bed, degassing neutralization pond, coagulative precipitation tank, anaerobic expanded granular bed and aerobic/anaerobic baffled reactor；Each unit is sequentially connected through water pipe, is handled industrial wastewater.Present invention process optimization, clear route are succinct；Whole COD removal rate >=95%, removal rate >=95% of organic properties pollutant, operational management is convenient, process stabilizing, and investment operating cost is low.
Description
Technical field
The present invention relates to a kind of wastewater treatment methods, and in particular to the process of Industrial Wastewater Treatment belongs at waste water
Manage technical field.
Background technique
Industrial wastewater, have water quantity and quality variation greatly, biodegradability is poor, be difficult to the feature degraded and pollutant complexity it is more
The features such as sample, generally takes preprocess method appropriate according to the water quality of actual waste water, such as flocculation, light electrolysis, absorption, photocatalysis
Etc. techniques, the biodegradability destroyed hardly degraded organic substance in waste water, improve waste water then biological method is combined, such as ABR, SBR, A/O
Technique etc., handles industrial wastewater.The research of processing industrial wastewater technique is also tended to using a variety of both at home and abroad at present
The group technology of method.
From the point of view of existing Patent data, Chinese patent " process for treating waste water by aerobic-anaerobic microbic repeated coupling
(CN200310121766.7) " although effect is fine, the cost of device can be improved to a certain extent, and Aerobic-anaerobic is anti-
Complex coupling is unfavorable for the absolute anaerobic environment of microorganism, and biological treatment efficiency is not high.Patent " a kind of baffled reactor and its place
Manage the method (CN200610012070) of sewage " and patent " Integrative processing plant for high concentration organic wasted water
(CN200310100513.1) " it is related to the multiple coupling of anaerobic processes and aerobic process, increases the complexity and fortune of equipment
The difficulty of row management, and there is no advanced oxidation processes.
Currently, there are processing cost height, persistent organic pollutants removal efficiency for the treatment process of existing industrial wastewater
The problems such as not high, process operation is unstable, and treatment effect is undesirable, cannot meet environmental requirements.
Summary of the invention
Goal of the invention: It is an object of the present invention to solve the deficiency of the existing technology and provide a kind of conjunctions of process optimization
Reason, persistent organic pollutants treatment effeciency are high, treatment effect is stable and the process of the Industrial Wastewater Treatment of economical rationality.
Technical solution: in order to achieve the object of the present invention, the technical solution adopted by the present invention are as follows: a new combined process processing
The method of industrial wastewater is that modified Fenton fluidized bed (IFBR), anaerobic expanded granular bed (EGSB) and anaerobism/good is used in combination
Oxygen baffled reactor (A/OBR) handles industrial wastewater；Group technology include conditioning tank, modified Fenton fluidized bed,
Deaerate neutralization pond, coagulative precipitation tank, anaerobic expanded granular bed and aerobic/anaerobic baffled reactor, is sequentially connected through water pipe.
The process includes following operating procedure:
(1) industrial wastewater after pretreatment, into conditioning tank；
(2) waste water by intake pump is conveyed into modified Fenton fluidized bed after adjusting, by medicine system to modified sweet smell
H is separately added into fluidized bed2SO4Solution, FeSO4Solution and H2O2Solution, by reflux pump by part effluent recycling into improvement
In type Fenton fluidized bed, make that fluidisation state is presented in Fenton fluidized bed；The reaction tower of modified Fenton fluidized bed is cylinder-shaped, and three pieces
Sieve plate is from bottom to top divided into oxidizing tower into water water distribution area, Fenton oxidation area, iron carbon reaction zone and exhalant region；Fenton oxidation area adds
There is filler A, iron carbon reaction zone is added with filler B；Circulator is connected to water inlet at the two of exhalant region and oxidizing tower；Pass through Fenton
The Fenton's reaction of zoneofoxidation and the micro-electrolysis reaction of iron carbon reaction zone remove useless water part COD and most difficult to degrade have
Machine pollutant；
(3) water outlet of modified Fenton fluidized bed enters degassing neutralization pond, sloughs a small amount of gas by stirring, it is molten that NaOH is added
Liquid adjusts the pH value of waste water；
(4) water outlet of degassing neutralization pond enters coagulative precipitation tank, coagulant is added by coagulant medicine system, and control and stir
It mixes speed and forms big wadding body；Sediment fraction is entered back into, the big wadding body of formation realizes that precipitation and separation, precipitating are dirty in settling zone
Mud is handled through sludge treating system；
(5) coagulative precipitation tank water outlet injects anaerobic expanded granular bed through pump, and anaerobic expanded granular bed reactor (EGSB) is main
Body is oxidizing tower, is divided into water water distribution system, reaction zone (anaerobic granular sludge bed layer), three-phase separation area, outlet system, reflux
System and sludge area；EGSB relies primarily on granule sludge to handle waste water, and waste water enters reactor by the water distributor of bottom, passes through
Sludge area rich in anaerobic bacteria, under the action of anaerobic bacteria, COD and persistent organic pollutants are largely removed, and are produced simultaneously
Raw a large amount of biogas are discharged at the top of reactor by the effect of three phase separator, gas and water outlet respectively, and sludge then settles back
Sludge area；
(6) anaerobic expanded granular bed water outlet enters aerobic/anaerobic baffled reactor, utilizes first at anaerobism section (ABR)
Anaerobe carries out anaerobic bio-treated, and anaerobism section is using box-cage type ABR reactor；Subsequent waste water is deflected into aerobic
Section (OBR) carries out Aerobic biological process using aerobic microbiological, and aerobic section uses baffling pattern, is arranged in specific conversion zone
Aerator, so that dissolved oxygen therein is greater than 2.0 mg/L；
(7) treated that waste water is discharged after sedimentation in secondary sedimentation tank for aerobic/anaerobic baffled reactor.
Further, the lower part of conditioning tank is equipped with microporous aeration device, adjusts the water quality and quantity of waste water；Work after adjusting
Industry waste water quality index: COD is that 5000 ~ 6000 mg/L, SS are 150 ~ 300mg/L, and chlorobenzene class is 60 ~ 80 mg/L.
Further, the filler A of modified Fenton fluidized bed uses quartz sand, the partial size of quartz sand in 0.5 ~ 1.5 mm,
The filler B of iron carbon reaction zone setting, using active carbon fiber felt；Zero is first loaded on active carbon fiber felt using liquid phase reduction
Valence Nanoscale Iron refills filling iron carbon reaction zone；Active carbon fiber felt, in netted intersection be placed in upper sieve plate and intermediate sieve plate it
Between.
Further, the exhalant region of modified Fenton fluidized bed connects circulator, and two water inlet pipes is divided to be respectively fed to sweet smell
Water inlet at the two of zoneofoxidation lower part and iron carbon reaction zone lower part, backflow water yield is respectively Q1And Q2, Q1With Q2The ratio between with m3/d
Meter ratio is 8:1-10:1.
Further, during modified Fenton fluidized bed processing, H2O2Ratio is 2 ~ 4:1, H in terms of mg/L with COD2O2
With Fe2+Molar ratio be 3 ~ 5:1, waste water Fenton oxidation area mean residence time control at 0.5 ~ 1.5 hour, waste water exists
The mean residence time of iron carbon reaction zone was controlled at 15 ~ 45 minutes, adjusted Fenton fluidized bed by medicine system and online pH meter
The pH value of middle waste water, maintains it between 3.0 ~ 4.0.
Further, the oxidizing tower ratio of height to diameter of anaerobic expanded granular bed is 3 ~ 5, maintains upflow velocity 6 ~ 12 in operation
M/h makes granule sludge be in suspended state；Design volumetric loading is 8 ~ 15 kgCOD/(m3D).
Further, aerobic/anaerobic baffled reactor, anaerobism section (ABR) using box-cage type ABR reactor,
Be made of 3 ~ 6 compartments, each compartment include upward flow cell compartment and it is lower to stream cell compartment, upward flow cell compartment and it is lower to stream cell compartment appearance
Product is equipped with boxes and baskets in upward flow cell compartment, filler is loaded in boxes and baskets, transmission device is equipped at the top of compartment, pass than being 3 ~ 5:1
Dynamic device is connected by cable wire with boxes and baskets；Change upper and lower position of the boxes and baskets in upward flow cell compartment by transmission device.
Further, box-cage type ABR reactor, boxes and baskets are made of stainless steel grizzly bar, are rectangular shape；The length of boxes and baskets
Degree and width are respectively less than the length and width of upward flow cell compartment, highly 35 ~ 50% for upward flow cell compartment effective height, boxes and baskets with
The wall surface of upward flow cell compartment is apart less than 5mm；Size of mesh opening between stainless steel grizzly bar is less than the minimum dimension of filler；Filler is
Floating stuffing, density is in 0.90 ~ 0.96 g/cm3, filler 10 ~ 25mm of diameter, material is polypropylene or polyethylene.
Further, box-cage type ABR reactor, starting method are that seed sludge is seeded to above-mentioned box-cage type ABR is anti-
It answers in device, is pumped into and has been heated to 35 DEG C for the treatment of sewage, make 10 ~ 15 g/L of concentration of sludge, then boxes and baskets are filled into filler,
Adjust reactor in hydraulic detention time be 6 ~ for 24 hours；Boxes and baskets are placed in the lower part of upward flow cell compartment by initial start stage, on to
After the amount increase for flowing cell compartment lower part suspension anaerobic sludge and biomembrane, into mid-term；Start mid-term, boxes and baskets are placed in upward flow lattice
The middle part of room, after the amount increase of suspension anaerobic sludge and biomembrane in the middle part of upward flow cell compartment, into the later period；Start the later period, it will
Boxes and baskets are placed in the top of upward flow cell compartment, until start completion；Initial start stage, starting mid-term and start the later period time distribution with
Its meter, ratio 3:4:5,3:5:4,5:4:4 or 5:4:3.
Basic principle is summarized as follows.
1, modified Fenton fluidized bed (IFBR) working principle
(1) waste water enters the Fenton oxidation area of modified Fenton fluidized bed, while passing through medicine system to Fenton fluidized bed
In be separately added into H2SO4Solution, FeSO4Solution and H2O2Solution by water part flows back into Fenton fluidized bed by reflux pump
It is interior, make that fluidisation state is presented in Fenton fluidized bed, the part COD of waste water is removed by Fenton's reaction and most difficult to degrade is had
Machine pollutant (is difficult to biodegradable organic pollutant, also known as characteristic contamination or characteristic organic pollutants)；Adjust reflux
The height of flow, control filler expansion is no more than intermediate sieve plate.
The principle of Fenton fluidized bed process: using carrier as crystallization nuclear species, waste water to be processed and addition medicament are by sweet smell
The fluidized-bed bottom that pauses enters into and up flowing.It is circumscribed with effluent recycling pipeline, to adjust influent stream water degree of supersaturation and reach load
Body upstream speed makes carrier surface form stable state crystalline solid, after crystal particle diameter is up to 2.5 mm ~ 3 mm, is recycled outside discharge slot
It recycles.Fenton fluidized bed process enables ferric iron major part caused by Fenton method to crystallize or sink using the mode of fluidized bed
It forms sediment, is coated on the carrier surface of liquid bed, is one and combines same phase chemical oxidation (Fenton method), out-phase chemical oxidation
(H2O2/ FeOOH), fluidized bed crystallization etc. functions new technology.This technology has made traditional Fenton oxidation method significantly
The iron oxygen that improvement can so reduce using tradition Fenton method and generate a large amount of chemical sludge, while be formed in carrier surface
Compound has the effect of heterocatalysis, and the mode of fluidized bed also promotes chemical oxidation reaction and mass-transfer efficiency, removes COD
Rate is promoted.Flowing water out after it is reacted can generate iron containing sludge after pH value adjusts.Iron containing sludge is reduced than traditional Fenton oxidation
70%, also reduce H2O2The waste of medication, while being adjusted using hydrogen peroxide dosage, COD removal amount is adjusted, is achieved effective control
The reduction of the COD of waste water is the guarantee of wastewater treatment qualified discharge.The one kind of Fenton process as advanced oxidation simultaneously, the present invention
Mainly the most of waste water is removed using Fenton process is difficult to biodegradable organic pollutant, efficiently makes difficult to degrade organic
Pollutant chain rupture, resolves into small organic molecule at open loop, improves the biodegradability of waste water, is easy in subsequent biological treatment list
Member is further processed.
(2) waste water enters the iron carbon reaction zone of modified Fenton fluidized bed through intermediate sieve plate, in iron-carbon micro-electrolysis condition
Under, persistent organic pollutants in catalysis oxidation waste water.Micro electrolysis tech is a kind of reason of current processing high concentrated organic wastewater
Think technique.It is in cold situation, and the potential difference generated using the micro-electrolysis material being filled in waste water itself is to useless
Water carries out electrolysis processing, to achieve the purpose that degradable organic pollutant.Intermediate sieve plate play support iron carbon reaction zone filler and
The effect of rectification.Modified Fenton fluidized bed is mainly the zeroth order Nanoscale Iron for utilizing activated carbon fiber and load, forms light electrolysis
Iron carbon battery.Electrolysis processing is carried out to waste water using the potential difference that the micro-electrolysis material being filled in waste water itself generates, is urged
Change the organic substance in degrading waste water.Active carbon fiber felt takes fibrofelt after the zeroth order Nanoscale Iron of load consumes
Out, it is regenerated with liquid phase reduction, it is recycled.
2, anaerobic expanded granular bed reactor (EGSB) working principle
Anaerobic expanded granular bed reactor (EGSB) anaerobic reaction process as other Anaerobic treatment techniques, including
Hydrolysis, acidification produce acetic acid and methane phase etc..Majority of organic pollutants in sewage passes through anaerobic fermentation here and is degraded to first
Alkane and carbon dioxide.This anaerobic processes is proper absolute anaerobic processes, and biological effect process does not have oxygen participation,
The anaerobic bacteria of culture is dominant.Anaerobic bacteria forms granule sludge and mainly goes to COD in waste water and organic pollutant difficult to degrade
Except effect, and removal efficiency is high.Anaerobic expanded granular bed reactor (EGSB) main body is reaction tower, can be divided into water cloth water system
System, reaction zone (anaerobic granular sludge bed layer), three-phase separation area, outlet system and return-flow system.EGSB relies primarily on particle dirt
Mud handles waste water, currently belongs to more advanced anaerobic process.Waste water enters reactor by the water distributor of bottom, by being rich in anaerobism
The sludge area of bacterium, under the action of anaerobic bacteria, COD and persistent organic pollutants are largely removed, while generating a large amount of natural ponds
Gas is discharged at the top of reactor by the effect of three phase separator, gas and water outlet respectively, and sludge then settles go back to sludge area.
It makes granule sludge be in suspended state, while can also by maintaining higher upflow velocity (6 ~ 12 m/ h) in operation
To use higher reactor or use effluent recycling to obtain high stirring intensity, to ensure that into water and mud granule
It comes into full contact with, promotes the fast degradation of organic matter.EGSB reactor is equipped with special effluent recycling system.EGSB reactor is general
To be cylindric tower-shaped, feature is that have very big ratio of height to diameter, and general up to 3 ~ 5, the height of process units reactor is up to 15 ~ 20
m.For stable anaerobic reactor using anaerobic grain sludge, the sinking speed of sludge is greater than the rate of climb of sewage.
EGSB load-bearing capacity is very big, the high concentrated organic wastewater generated suitable for industrial production, such as wastewater from chemical industry
Processing.Compared with other anaerobic biological reactors, the characteristics of EGSB: 1. high liquid surface upflow velocity and COD removal are negative
Lotus；2. anaerobic sludge grain diameter is larger, starting is fast, and volumetric loading is high；In addition reflux effect is so that reactor anti-shock loading
Ability is strong；3. reactor designs for pyramidal structure, ratio of height to diameter with higher, occupied area is small；4. it is high to can be used for SS content
With to the virose wastewater treatment of microorganism；5. EGSB reactor has very big adaptability to all kinds of waste water, it is mainly used for highly concentrated
Treatment of Organic Wastewater is spent, low energy consumption, and sludge output is few.Shortcoming is the nitrogen and phosphorus that cannot be removed in waste water.
3, aerobic/anaerobic baffled reactor (A/OBR) working principle
Aerobic/anaerobic baffled reactor is by anaerobism section (ABR, box-cage type ABR reactor) and aerobic section (OBR, aerobic folding
Streaming reaction zone) composition.
Boxes and baskets are set in the upward flow cell compartment of box-cage type ABR reactor, filler is loaded in boxes and baskets, is set beside cell compartment
Transmission device is set, boxes and baskets are moved up or down, is formed with the moving bed of packing layer, waste water to be processed enters reaction by water inlet
Device successively passes through compartment, is discharged after processing by water outlet.On the basis of traditional ABR reactor, in conjunction with moving bed biological
Membrane technology, and in order to make the position of moving bed and run controllably, increase the transmission device on boxes and baskets and compartment top.It is reacting
Filler is added in the upward flow cell compartment of device, purpose seeks to hang biomembrane on filler, forms anaerobism suspended sludge and biomembrane
Synergy, generally sludge concentration in increase reactor, enable reactor to bear higher COD processing load, improve biology
Treatment effeciency.The setting and control of boxes and baskets, so that filler sufficiently connects with seed sludge in ABR during entire Primary culture
Touching thus plays the role of the start-up course for accelerating ABR, realizes the effect for shortening the starting time.Grizzly bar at the top of boxes and baskets
Grid plays the role of retaining filler, and filler is not allowed to be lost to next compartment；Boxes and baskets packing layer is occupy to stream cell compartment top simultaneously
When, also there is crown_interception to suspension anaerobic sludge, reduce number of dropouts, maintain high suspended sludge concentration, improves at biology
Manage efficiency.Aerobic deflector type reaction zone is provided with the biofilm filler of suspension, using biotechnology, screens, tames and construct
Can degrade out common are the dominant microflora of machine characteristic contamination in industrial wastewater, especially industrial wastewater, and by dominant microflora
It is fixed on aerobic zone.The high biomass of aerobic deflector type reaction zone is kept, thus improves biological treatment efficiency.
Denitrogenation dephosphorizing may be implemented with anaerobism, replacing for aerobic process in OBR in ABR.Aerobic process in OBR can be substantially
COD and ammonia nitrogen, total phosphorus, waste water are able to achieve qualified discharge after precipitation in removal waste water.
Process of the invention is suitable for the industrial wastewater that wastewater from chemical industry etc. contains organic properties pollutant difficult to degrade
Processing, the total removal rate of COD and organic pollutant difficult to degrade is greater than 95% in waste water, and effluent quality is able to satisfy in environmental protection
It is required that.
The utility model has the advantages that beneficial effects of the present invention are as described below compared with existing technique.
1, the present invention provides a kind of group technologies of different designs.
2, process optimization, clear route are succinct；Bio-chemical effluent is through materializing strategy (modified Fenton fluidized bed), then is given birth to
Change handles (the EGSB reactor of absolute anaerobism+box-cage type ABR reactor+OBR Aerobic biological process), finally goes out after precipitation
Water, technique composition rationally, biochemical treatment and materializing strategy are orderly organically combined, three main body processing units IFBR, EGSB
It is mutually supported with A/OBR.
3, technique provided by the invention can effectively be handled commonly industrial wastewater, can obtain processing effect well
Fruit meets the requirement in environmental protection.Technique provided by the invention, whole COD removal rate >=95%, organic properties pollutants removal rate
>=95%, operational management is convenient, process stabilizing, and investment operating cost is low.Overcome processing cost height, persistent organic pollutants
The deficiencies of inefficient, process operation is unstable, and treatment effect is undesirable, cannot meet environmental requirements.
4, technique provided by the invention, wherein the catalysis reaction of the same phase and out-phase of Fenton fluidized bed, the iron content of generation are dirty
Mud reduces 70% than traditional Fenton oxidation, also reduces H2O2The waste of medication, while being adjusted using hydrogen peroxide dosage, adjustment
COD removal amount achieves effective control the reduction of the COD of waste water, ensures effluent quality.Modified Fenton fluidized bed by Fenton oxygen
Change and organically combined with micro-electrolysis reaction, especially efficiently makes persistent organic pollutants chain rupture, open loop, resolves into small molecule
Organic matter.It is identical in water inlet indices and added pharmaceutical quantities compared with the common Fenton fluidized bed of co-content and treating capacity
In the case of, 10% can be improved to the removal rate of the organic pollutant of difficult for biological degradation, further increase the biodegradability of waste water.
5, technique provided by the invention, the wherein use of box-cage type ABR reactor accelerate the starting time of anaerobism, mention
The high removal efficiency to organic matter.
Detailed description of the invention
Fig. 1 is the method schematic diagram that a new combined process provided by the invention handles industrial wastewater.
Specific embodiment
In the following with reference to the drawings and specific embodiments, the present invention is furture elucidated, it should be understood that embodiment is merely to illustrate this hair
Bright rather than limit the scope of the invention, after the present invention has been read, those skilled in the art are to of the invention various etc.
The modification of valence form falls within the application range as defined in the appended claims.
Embodiment 1:
The comprehensive wastewater that certain chemical company generates is handled, influent concentration COD≤6000mg/L before processing,
PH 6.5 ~ 8.5, SS≤300mg/L, NH3- N≤100mg/L, TP≤2.5mg/L, characteristic contamination concentration chlorobenzene class≤
80mg/L.Water outlet requires to reach " the main pollution discharge standard of Chemical Industry in Jiangsu Province " (DB32/939-2006) second level mark
It is quasi-.Effluent index requires COD≤120mg/L, pH 6.5 ~ 8.5, SS≤150mg/L, NH3-N≤25mg/L, TP≤1.0mg/
L, characteristic contamination concentration chlorobenzene class≤1.0 mg/L.
Using the group technology in attached drawing 1, modified Fenton fluidized bed (IFBR), anaerobic expanded granular bed is used in combination
(EGSB) wastewater from chemical industry is handled with aerobic/anaerobic baffled reactor (A/OBR)；Including conditioning tank, modified Fenton
Fluidized bed, degassing neutralization pond, coagulative precipitation tank, anaerobic expanded granular bed, aerobic/anaerobic baffled reactor, successively through water pipe
Connection.
The technique includes following operating procedure:
(1) wastewater from chemical industry after pretreatment, into conditioning tank；
(2) waste water by intake pump is conveyed into modified Fenton fluidized bed after adjusting, by medicine system to modified sweet smell
H is separately added into fluidized bed2SO4Solution, FeSO4Solution and H2O2Solution, by reflux pump by part effluent recycling into improvement
In type Fenton fluidized bed, make that fluidisation state is presented in Fenton fluidized bed；The oxidizing tower of modified Fenton fluidized bed is cylinder-shaped, and three pieces
Sieve plate is from bottom to top divided into oxidizing tower into water water distribution area, Fenton oxidation area, iron carbon reaction zone and exhalant region；Fenton oxidation area adds
There is filler A, iron carbon reaction zone is added with filler B；Circulator is connected to water inlet at exhalant region and oxidizing tower two；Pass through Fenton oxygen
Change the Fenton's reaction in area and the micro-electrolysis reaction of iron carbon reaction zone, removes useless water part COD and most difficult to degrade organic
Pollutant；
(3) water outlet of modified Fenton fluidized bed enters degassing neutralization pond, sloughs a small amount of gas by stirring, it is molten that NaOH is added
Liquid adjusts the pH value of waste water；
(4) water outlet of degassing neutralization pond enters coagulative precipitation tank, coagulant is added by coagulant medicine system, and control and stir
It mixes speed and forms big wadding body；Sediment fraction is entered back into, the big wadding body of formation realizes that precipitation and separation, precipitating are dirty in settling zone
Mud is handled through sludge treating system；
(5) coagulative precipitation tank water outlet injects anaerobic expanded granular bed through pump, and anaerobic expanded granular bed reactor body is anti-
Tower is answered, is divided into water water distribution system, reaction zone, three-phase separation area, outlet system and return-flow system；EGSB relies primarily on particle dirt
Mud handles waste water, and waste water enters reactor by the water distributor of bottom, by being rich in the sludge area of anaerobic bacteria, in the work of anaerobic bacteria
Under, COD and persistent organic pollutants are largely removed, while generating a large amount of biogas, pass through three at the top of reactor
The effect of phase separator, gas and water outlet are discharged respectively, and sludge then settles go back to sludge area；
(6) anaerobic expanded granular bed water outlet enters aerobic/anaerobic baffled reactor, micro- using anaerobism in anaerobism section first
Biology carries out anaerobic bio-treated, and anaerobism section is using box-cage type ABR reactor；Subsequent waste water is deflected into aerobic section
(OBR), Aerobic biological process is carried out using aerobic microbiological, aerobic section uses baffling pattern, is arranged in specific conversion zone and exposes
Device of air, so that dissolved oxygen therein is greater than 2.0 mg/L；
(7) treated that waste water is discharged after sedimentation in secondary sedimentation tank for aerobic/anaerobic baffled reactor.
Waste water is conveyed into Fenton fluidized bed inhalant region by intake pump, passes through bottom sieve plate water distribution；Waste water enters Fenton stream
Hua Chuan Fenton oxidation area, while H is separately added into Fenton fluidized bed by medicine system2SO4Solution, FeSO4Solution and H2O2
Solution is flowed back into the water section in effluent trough in Fenton fluidized bed by reflux pump, makes that fluidisation is presented in Fenton fluidized bed
State removes useless water part COD and most of chlorobenzene class organic pollutant by Fenton's reaction；Return flow is adjusted, control is filled out
The height of material expansion is no more than intermediate sieve plate；Waste water enters iron carbon reaction zone through intermediate sieve plate, in iron-carbon micro-electrolysis condition
Under, persistent organic pollutants in catalysis oxidation waste water；Waste water through iron-carbon micro-electrolysis catalysis oxidation is by upper sieve plate, through going out
Mill weir enters in effluent trough, enters next processing unit by outlet pipe；Connect circulator in the effluent trough of top, be divided to two into
Water pipe is respectively fed to water inlet at the two of Fenton oxidation area lower part and iron carbon reaction zone lower part, and reflux flow of inlet water is respectively Q1With
Q2, Q1With Q2With m3It is 8:1 that/d, which counts ratio,.During Fenton fluidized bed processing, H2O2Concentration ratio (mg/L) with COD is 2.5:1,
H2O2With Fe2+Molar ratio be 4:1, waste water Fenton oxidation area mean residence time control at 1 hour, waste water is in iron carbon
The mean residence time of reaction zone was controlled at 30 minutes, adjusted waste water in Fenton fluidized bed by medicine system and online pH meter
PH value maintains pH value between 3.0 ~ 4.0.
The oxidizing tower ratio of height to diameter of anaerobic expanded granular bed is 4, maintains upflow velocity 9m/h to make at granule sludge in operation
In suspended state；Design volumetric loading is 12kgCOD/(m3D).
Box-cage type moving bed modified ABR reactor, is made of 4 compartments, each compartment be divided into again upward flow cell compartment and
It is lower to stream cell compartment, upward flow cell compartment and lower the ratio between volume to stream cell compartment are 3:1, wherein boxes and baskets are set in upward flow cell compartment,
Filler is loaded in boxes and baskets, transmission device is equipped at the top of upward flow cell compartment, and transmission device is connected by cable wire with boxes and baskets, controllably
Boxes and baskets processed move up or down, and are formed with the moving bed of packing layer.Upward flow cell compartment bottom is equipped with reflux recoil tube, successively passes through
4 compartments are crossed, are discharged after processing.Boxes and baskets are made of stainless steel grizzly bar, are in rectangular shape, and the length and width of boxes and baskets is smaller
In the length and width of upward flow cell compartment, highly for the effective height of upward flow cell compartment 35%.Filler, filler are filled up in boxes and baskets
Using Kaldnes floating stuffing, density is 0.95 g/cm3, filler diameter is 10mm, and material is polyethylene.
The starting method of box-cage type ABR reactor is seeded to seed sludge in above-mentioned box-cage type ABR reactor, is pumped into
It has been heated to 35 DEG C for the treatment of sewage, has made 15 g/L of concentration of sludge, then boxes and baskets are filled into filler, initial start stage, by case
Cage is placed in upward flow cell compartment lower part, after the amount increase of upward flow cell compartment lower part suspension anaerobic sludge and biomembrane, into mid-term；
Start mid-term, boxes and baskets are placed in the middle part of upward flow cell compartment, increases to the amount of suspension anaerobic sludge and biomembrane in the middle part of upward flow cell compartment
After adding, into the later period；Start the later period, boxes and baskets are placed in upward flow cell compartment top, until start completion；In initial start stage, starting
The time in phase and starting later period distributes the ratio 5:4:4 in terms of day.Controlling the hydraulic detention time in reactor is 12 ~ 18h；
Influent COD is gradually upgraded to 1000mg/L, and the hydraulic detention time controlled in reactor is 18h, gradually reduces hydraulic detention time
To 12h.Main indicator each unit treatment effect see the table below.
After combined process, effluent index COD≤80mg/L, pH 6.5 ~ 8.5, SS≤50mg/L, NH3-N≤
20mg/L, TP≤1.0mg/L, characteristic contamination concentration chlorobenzene class≤0.8mg/L.
1 main indicator each unit treatment effect list of table
Claims (8)
1. the method for group technology processing industrial wastewater, it is characterised in that: the group technology is that modified Fenton stream is used in combination
Change bed, anaerobic expanded granular bed and aerobic/anaerobic baffled reactor to handle industrial wastewater；The group technology packet
Include conditioning tank, modified Fenton fluidized bed, degassing neutralization pond, coagulative precipitation tank, anaerobic expanded granular bed and aerobic/anaerobic baffling
Plate reactor, is sequentially connected through water pipe；
The method for handling industrial wastewater includes following operating procedure:
(1) industrial wastewater after pretreatment, into conditioning tank；
(2) waste water by intake pump is conveyed into modified Fenton fluidized bed after adjusting, by medicine system to modified Fenton stream
Change in bed and is separately added into H2SO4Solution, FeSO4Solution and H2O2Solution, it is by reflux pump that part effluent recycling is fragrant into modified
Pause in fluidized bed, makes that fluidisation state is presented in Fenton fluidized bed；
The oxidizing tower of the modified Fenton fluidized bed is cylindrical shape, and three pieces of sieve plates are from bottom to top divided into oxidizing tower into water cloth
Pool, Fenton oxidation area, iron carbon reaction zone and exhalant region；Fenton oxidation area is added with filler A, and iron carbon reaction zone is added with filler B；It follows
Loop device is connected to water inlet at the two of exhalant region and oxidizing tower；Pass through the Fenton's reaction in Fenton oxidation area and iron carbon reaction zone
Micro-electrolysis reaction removes useless water part COD and most persistent organic pollutants；
(3) water outlet of modified Fenton fluidized bed enters degassing neutralization pond, sloughs a small amount of gas by stirring, NaOH solution is added,
Adjust the pH value of waste water；
(4) water outlet of degassing neutralization pond enters coagulative precipitation tank, and coagulant is added by coagulant medicine system, and controls stirring speed
Degree forms big wadding body；Sediment fraction is entered back into, the big wadding body of formation realizes precipitation and separation, precipitating sludge warp in settling zone
Sludge treating system processing；
(5) coagulative precipitation tank water outlet injects anaerobic expanded granular bed through pump, and anaerobic expanded granular bed reactor body is reaction tower,
It is divided into water water distribution system, reaction zone, three-phase separation area, outlet system and return-flow system；EGSB relies primarily on granule sludge
Waste water is handled, waste water enters reactor by the water distributor of bottom, by being rich in the sludge area of anaerobic bacteria, in the effect of anaerobic bacteria
Under, COD and persistent organic pollutants are largely removed, while generating a large amount of biogas, pass through three-phase at the top of reactor
The effect of separator, gas and water outlet are discharged respectively, and sludge then settles go back to sludge area；
(6) anaerobic expanded granular bed water outlet enters aerobic/anaerobic baffled reactor, utilizes anaerobe in anaerobism section first
Anaerobic bio-treated is carried out, anaerobism section is using box-cage type ABR reactor, the box-cage type ABR reactor, by 3 ~ 6
Compartment composition, each compartment include upward flow cell compartment and it is lower to stream cell compartment, upward flow cell compartment and it is lower to stream cell compartment volumetric ratio be 3
~ 5:1 is equipped with boxes and baskets in upward flow cell compartment, filler is loaded in boxes and baskets, and transmission device, transmission device are equipped at the top of compartment
It is connected by cable wire with boxes and baskets；Change upper and lower position of the boxes and baskets in upward flow cell compartment by transmission device；Subsequent waste water baffling
Into aerobic section, Aerobic biological process is carried out using aerobic microbiological, aerobic section uses baffling pattern, sets in specific conversion zone
Aerator is set, so that dissolved oxygen therein is greater than 2.0 mg/L；
(7) treated that waste water is discharged after sedimentation in secondary sedimentation tank for aerobic/anaerobic baffled reactor.
2. the method for group technology processing industrial wastewater according to claim 1, it is characterised in that: the conditioning tank
Lower part is equipped with microporous aeration device, adjusts the water quality and quantity of waste water；Industrial wastewater water quality indicator after adjusting: COD be 5000 ~
6000 mg/L, SS are 150 ~ 300mg/L, and chlorobenzene class is 60 ~ 80 mg/L.
3. the method for group technology processing industrial wastewater according to claim 1, it is characterised in that: the modified is fragrant
Pause in fluidized bed, filler A uses quartz sand, and in 0.5 ~ 1.5 mm, the iron carbon reaction zone is set the partial size of the quartz sand
The filler B set, using active carbon fiber felt；Zeroth order Nanoscale Iron is first loaded on active carbon fiber felt using liquid phase reduction, then
It is packed into iron carbon reaction zone；The active carbon fiber felt is placed between upper sieve plate and intermediate sieve plate in netted intersection.
4. the method for group technology processing industrial wastewater according to claim 1, it is characterised in that: the modified is fragrant
Pause in fluidized bed, exhalant region connects circulator, and two water inlet pipes is divided to be respectively fed to Fenton oxidation area lower part and iron carbon reaction zone
Water inlet at the two of lower part, backflow water yield are respectively Q1And Q2, Q1With Q2The ratio between with m3It is 8:1-10:1 that/d, which counts ratio,.
5. the method for group technology processing industrial wastewater according to claim 1, it is characterised in that: the modified is fragrant
Pause fluidized bed, during managing at which, H2O2Ratio is 2 ~ 4:1, H in terms of mg/L with COD2O2With Fe2+Molar ratio be 3 ~ 5:
1, waste water Fenton oxidation area mean residence time control at 0.5 ~ 1.5 hour, average stop of the waste water in iron carbon reaction zone
Time controlled at 15 ~ 45 minutes, and the pH value of waste water in Fenton fluidized bed is adjusted by medicine system and online pH meter, makes its maintenance
Between 3.0 ~ 4.0.
6. the method for group technology processing industrial wastewater according to claim 1, it is characterised in that: described is anaerobic expanded
In grain bed, the reaction tower ratio of height to diameter of anaerobic expanded granular bed is 3 ~ 5, and 6 ~ 12 m/ h of upflow velocity is maintained to make in operation
Grain sludge is in suspended state；Design volumetric loading is 8 ~ 15 kgCOD/(m3D).
7. the method for group technology processing industrial wastewater according to claim 1, it is characterised in that: the anaerobism/good
In oxygen baffled reactor, anaerobism section is using box-cage type ABR reactor, the box-cage type ABR reactor, boxes and baskets by
Stainless steel grizzly bar is made, and is rectangular shape；The length and width of boxes and baskets is respectively less than the length and width of upward flow cell compartment, height
It is the 35 ~ 50% of upward flow cell compartment effective height, the wall surface of boxes and baskets and upward flow cell compartment is apart less than 5mm；Between stainless steel grizzly bar
Size of mesh opening be less than filler minimum dimension；The filler is floating stuffing, and density is in 0.90 ~ 0.96 g/cm3, filler is straight
10 ~ 25mm of diameter, material are polypropylene or polyethylene.
8. the method for group technology processing industrial wastewater according to claim 1, it is characterised in that: the anaerobism/good
In oxygen baffled reactor, anaerobism section is using box-cage type ABR reactor, the starting side of the box-cage type ABR reactor
Method is seeded to seed sludge in above-mentioned box-cage type ABR reactor, is pumped into and has been heated to 35 DEG C for the treatment of sewage, makes sludge
Concentration be 10 ~ 15 g/L, then boxes and baskets are filled into filler, adjust the hydraulic detention time in reactor be 6 ~ for 24 hours；Starting is just
Boxes and baskets are placed in the lower part of upward flow cell compartment by the phase, after the amount increase of upward flow cell compartment lower part suspension anaerobic sludge and biomembrane,
Into mid-term；Start mid-term, boxes and baskets are placed in the middle part of upward flow cell compartment, to suspension anaerobic sludge and life in the middle part of upward flow cell compartment
After the amount increase of object film, into the later period；Start the later period, boxes and baskets are placed in the top of upward flow cell compartment, until start completion；Starting
The time at initial stage, starting mid-term and starting later period distributes ratio 3:4:5,3:5:4,5:4:4 or 5:4:3 in terms of day.
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| CN101781066A (en) * | 2010-03-23 | 2010-07-21 | 哈尔滨工业大学 | Caffeine production wastewater treatment method |
| CN103663802A (en) * | 2012-08-29 | 2014-03-26 | 安徽南风环境工程技术有限公司 | Microelectrolysis-fenton oxidizing reaction device |
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