CN105884152B - IFBR-UASB-A/OBR handles wastewater from chemical industry group technology - Google Patents
IFBR-UASB-A/OBR handles wastewater from chemical industry group technology Download PDFInfo
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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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46176—Galvanic cells
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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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
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- 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
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
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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
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
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Abstract
The present invention provides IFBR-UASB-A/OBR to handle wastewater from chemical industry group technology, including conditioning tank, modified Fenton fluidized bed, degassing neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket and aerobic/anaerobic baffled reactor；Each unit is sequentially connected through water pipe, is handled wastewater from chemical industry.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 chemical wastewater treatment belongs at waste water
Manage technical field.
Background technique
Wastewater from chemical industry have water quantity and quality change 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 wastewater from chemical industry.The research of processing wastewater from chemical industry 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.
Currently, there are processing cost height, persistent organic pollutants removal efficiency for the treatment process of existing wastewater from chemical industry
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 chemical 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: it is useless that IFBR-UASB-A/OBR handles chemical industry
Water group technology, the group technology are combination modified Fenton fluidized bed (IFBR), up-flow anaerobic sludge blanket (UASB) and detest
Oxygen/aerobic baffled reactor (A/OBR) handles wastewater from chemical industry；Group technology includes balancing tank, modified Fenton
Fluidized bed, degassing neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket, aerobic/anaerobic baffled reactor, through water pipe according to
Secondary connection.
The technique includes following operating procedure:
(1) wastewater from chemical industry after pretreatment, into balancing 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；
It is cylindrical shape that modified Fenton fluidized bed, which aoxidizes tower body, and three pieces of sieve plates are 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 is added with filler A, and iron carbon reaction zone is added with filler B；Circulation
Device is connected to tower body water inlet at water outlet and two；Pass through the Fenton's reaction in Fenton oxidation area and the light electrolysis of iron carbon reaction zone
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, 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 up-flow anaerobic sludge blanket through pump, after waste water is entered by reactor lower part, upwards
It by Sludge Bed area, suspended sludge area, three phase separator, then drains, is removed in the middle part of waste water by the effect of anaerobe
Divide COD and persistent organic pollutants, further decreases the SS of waste water；Residence time is 12~36 h；
(6) up-flow anaerobic sludge blanket water outlet enters aerobic/anaerobic baffled reactor, utilizes anaerobism in anaerobism section first
Microorganism 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.
Further, the lower part of balancing tank is equipped with microporous aeration device, adjusts the water quality and quantity of waste water；Change after adjusting
Work 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, and partial size is in 0.5 ~ 1.5 mm, the reaction of iron carbon
The filler B of area's setting, using active carbon fiber felt；Zeroth order nanometer is first loaded on active carbon fiber felt using liquid phase reduction
Iron refills filling iron carbon reaction zone；Active carbon fiber felt is placed between upper sieve plate and intermediate sieve plate in netted intersection.
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
The lower part for zoneofoxidation of pausing and the lower part of iron carbon reaction zone, backflow water yield is respectively Q1And Q2, Q1With Q2The ratio between with m3/ d counts ratio
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 design volumetric loading of up-flow anaerobic sludge blanket is 10 ~ 12 kgBOD/(kg MLSSd).
Further, the anaerobism section of aerobic/anaerobic baffled reactor is using box-cage type ABR reactor, box-cage type
ABR reactor is 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
The volumetric ratio for flowing cell compartment is 3~5:1, and boxes and baskets are equipped in upward flow cell compartment, filler is loaded in boxes and baskets, is equipped at the top of compartment
Transmission device, transmission device are connected by cable wire with boxes and baskets.
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
Be respectively less than the length and width of upward flow cell compartment, highly 35~50% for upward flow cell compartment effective height with width, boxes and baskets with it is upper
Apart it is less than 5mm to the wall surface of stream cell compartment；Size of mesh opening between stainless steel grizzly bar is less than the minimum dimension of filler；Filler is outstanding
Floating filler, density is in 0.90~0.96 g/cm3, filler 10~25mm of diameter, material is polypropylene or polyethylene.
Further, the starting method of box-cage type ABR reactor is that seed sludge is seeded to above-mentioned box-cage type ABR reaction
In device, it 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 upward flow cell compartment lower part, to upward flow by initial start stage
After the amount increase of cell compartment lower part suspension anaerobic sludge and biomembrane, into mid-term；Start mid-term, boxes and baskets are placed in upward flow cell compartment
Middle part, 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, by boxes and baskets
It is placed in upward flow cell compartment top, until start completion；The time of initial start stage, starting mid-term and starting later period distributes in terms of day,
Ratio is 3:4:5,3:5:4,5:4:4 or 5:4:3.
Basic principle is summarized as follows.
1, IFBR(modified Fenton fluidized bed) 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, UASB working principle
Upflow anaerobic sludge blanket reactor (UASB) anaerobic reaction process is as other Anaerobic treatment techniques, packet
Hydrolysis is included, is acidified, acetic acid and methane phase etc. are produced.It is converted a substrate by the conversion process that different microorganisms participates in substrate
The inorganic matters such as final product-natural pond gas and water.UASB is by sludge reaction area, gas-liquid-solid three-phase separator (including settling zone) and gas chamber
Three parts composition.Sewage passes through from bottom to top, and reactor bottom has a high concentration, the Sludge Bed of high activity, big in sewage
Some organic pollutants pass through anaerobic fermentation here and are degraded to methane and carbon dioxide.This anaerobic processes is on stricti jurise
Absolute anaerobic processes, biological effect process do not have an oxygen participation, and the anaerobic bacteria of culture is dominant.Anaerobic bacteria forms granule sludge
Main removal is played to COD in waste water and organic pollutant difficult to degrade, and removal efficiency is high.Because of stirring for water flow and bubble
It is dynamic, there is a sludge suspension layer on Sludge Bed.Reactor top has equipped with three phase separator, to separating digesting gas, digestion
Liquid and mud granule.Export at the top of digestion gas autoreactor；Mud granule slides the Sludge Bed for being settled down to reactor bottom automatically；
Digestive juice is discharged from settling section.
UASB load-bearing capacity is very big, is suitable for high concentrated organic wastewater, such as the processing of wastewater from chemical industry.Operational excellence
UASB has very high organic pollutant removal rate, does not need to stir, and load impact, temperature and the pH adapted to by a relatively large margin becomes
Change.The essential characteristic of UASB reactor is not have to absorption carrier, can form the good granule sludge of settling property, keeps reaction
The speck of high concentration in device, thus higher COD load can be born, COD removal rate is up to 90% or more.It is raw with other anaerobism
The characteristics of object reactor is compared, UASB: (1) simple structure is ingenious, and anaerobic grain sludge can be turned out in reactor, realizes dirt
The separation of mud sludge age (SRT) and hydraulic detention time (HRT), thus biomass is more in Sludge Bed, convert into concentration calculation up to 20 ~
30g/L；(2) volumetric loading rate is high, and under the conditions of mesophilic digestion, general up to the left and right 10kgCOD/(m3d), waste water is reacting
Hydraulic detention time in device is shorter, therefore required pool capacity is substantially reduced.(3) UASB reactor has very big fit to all kinds of waste water
Ying Xing, low energy consumption, and sludge output is few.Shortcoming is the nitrogen and phosphorus that cannot be removed in waste water.
3, A/OBR working principle
(OBR, aerobic deflector type are anti-with aerobic section by anaerobism section box-cage type ABR reactor for aerobic/anaerobic baffled reactor
Answer area) 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 comes into full contact with seed sludge in ABR during entire Primary culture,
The start-up course for thus playing the role of accelerating ABR, realizes the effect for shortening the starting time.Grizzly bar grid at the top of boxes and baskets
Play the role of retaining filler, filler is not allowed to be lost to next compartment；Simultaneously boxes and baskets packing layer occupy to stream cell compartment top when
It waits, also has crown_interception to suspension anaerobic sludge, reduce number of dropouts, maintain high suspended sludge concentration, improve biological treatment effect
Rate.Aerobic deflector type reaction zone is provided with the biofilm filler of suspension, using biotechnology, screens, tames and construct energy
It common are the dominant microflora of machine characteristic contamination in degradation wastewater from chemical industry, and dominant microflora be fixed on aerobic zone.It keeps
The high biomass of oxygen deflector type reaction zone, thus improve biological treatment efficiency.
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 follows 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 through materializing strategy (modified Fenton fluidized bed IFBR), then into
Row biochemical treatment (the UASB reactor of absolute anaerobism+box-cage type ABR reactor+OBR Aerobic biological process), finally after precipitation
Rationally, biochemical treatment and materializing strategy are orderly organically combined for water outlet, technique composition, three main body processing unit IFBR,
UASB and A/OBR are mutually supported.
3, technique provided by the invention can effectively be handled general wastewater from chemical industry, 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.
Detailed description of the invention
Fig. 1 is that IFBR-UASB-A/OBR provided by the invention handles wastewater from chemical industry group technology schematic diagram.
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:
Certain Production in Chemical Plant process synthesis waste water, belongs to high concentrated organic wastewater, and the influent concentration COD before processing≤
6000mg/L, pH 6.5~8.5, SS≤300mg/L, NH3- N≤100mg/L, TP≤5mg/L, characteristic contamination concentration chlorine
Benzene class≤80mg/L.Water outlet requires to reach " the main pollution discharge standard of Chemical Industry in Jiangsu Province " (DB32/939-2006)
Secondary standard.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 modified Fenton fluidized bed (IFBR) provided by the invention, up-flow anaerobic sludge blanket (UASB) and anaerobism/
The group technology of aerobic baffled reactor (A/OBR) handles wastewater from chemical industry；Including balancing tank, modified Fenton stream
Change bed, degassing neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket, aerobic/anaerobic baffled reactor, successively through water pipe
Connection.
The technique includes following operating procedure:
(1) wastewater from chemical industry after pretreatment, into balancing 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；
It is cylindrical shape that modified Fenton fluidized bed, which aoxidizes tower body, and three pieces of sieve plates are 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 is added with filler A, and iron carbon reaction zone is added with filler B；Circulation
Device is connected to tower body water inlet at water outlet and two；Pass through the Fenton's reaction in Fenton oxidation area and the light electrolysis of iron carbon reaction zone
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, 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 up-flow anaerobic sludge blanket through pump, after waste water is entered by reactor lower part, upwards
It by Sludge Bed area, suspended sludge area, three phase separator, then drains, is removed in the middle part of waste water by the effect of anaerobe
Divide COD and persistent organic pollutants, further decreases the SS of waste water；Residence time is 24 h；
(6) up-flow anaerobic sludge blanket water outlet enters aerobic/anaerobic baffled reactor, utilizes anaerobism in anaerobism section first
Microorganism 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 the lower part in Fenton oxidation area and the lower part of iron carbon reaction zone, and reflux flow of inlet water is respectively Q1And Q2, Q1With Q2
With 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
For 4:1, mean residence time of the waste water in Fenton oxidation area was controlled at 1 hour, and waste water is in the average stop of iron carbon reaction zone
Between control at 30 minutes, the pH value of waste water in Fenton fluidized bed is adjusted by medicine system and online pH meter, maintains pH value
Between 3.0~4.0.
Up-flow anaerobic sludge blanket, design volumetric loading are 11 kgBOD/(kg MLSSd).
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 4 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.
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.Main indicator each unit treatment effect is seen below
Table.
1 main indicator each unit treatment effect list of table
Claims (8)
1.IFBR-UASB-A/OBR handles wastewater from chemical industry group technology, it is characterised in that: the group technology is that combination modified is fragrant
Fluidized bed, up-flow anaerobic sludge blanket and aerobic/anaerobic baffled reactor handle wastewater from chemical industry；The combination
Technique includes balancing tank, modified Fenton fluidized bed, degassing neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket, detests
Oxygen/aerobic baffled reactor, is sequentially connected through water pipe；
The group technology includes following operating procedure:
(1) wastewater from chemical industry after pretreatment, into balancing 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 modified Fenton fluidized bed oxidation tower body 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 tower body water inlet at water outlet and two；Pass through the Fenton's reaction in Fenton oxidation area and micro- electricity of iron carbon reaction zone
Solution 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 up-flow anaerobic sludge blanket through pump, after waste water is entered by reactor lower part, passes upward through
Sludge Bed area, suspended sludge area, three phase separator, then drain, and remove useless water part COD by the effect of anaerobe
And persistent organic pollutants, further decrease the SS of waste water；Residence time is 12~36 h；
(6) up-flow anaerobic sludge blanket water outlet enters aerobic/anaerobic baffled reactor, utilizes the micro- life of anaerobism in anaerobism section first
Object carries out anaerobic bio-treated, and anaerobism section is using box-cage type ABR reactor, the box-cage type ABR reactor, by 3~6
A compartment composition, each compartment include upward flow cell compartment and lower to stream cell compartment, upward flow cell compartment and the lower volumetric ratio to stream cell compartment
For 3~5:1, it is equipped with boxes and baskets in upward flow cell compartment, filler is loaded in boxes and baskets, transmission device, transmission are equipped at the top of compartment
Device is connected by cable wire with boxes and baskets；Subsequent waste water is deflected into aerobic section, carries out Aerobic biological process using aerobic microbiological,
Aerobic section uses baffling pattern, aerator is arranged in specific conversion zone, 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. group technology according to claim 1, it is characterised in that: the lower part of the balancing tank is equipped with micro-pore aeration
Device adjusts the water quality and quantity of waste water；Wastewater from chemical industry water quality indicator after adjusting: COD is 5000 ~ 6000 mg/L, SS 150
~300mg/L, chlorobenzene class are 60 ~ 80 mg/L.
3. group technology according to claim 1, it is characterised in that: the filler A of modified Fenton fluidized bed is using quartz
Sand, the partial size of the quartz sand is in 0.5 ~ 1.5 mm, the filler B of the iron carbon reaction zone setting, using activated carbon fibre
Felt；Zeroth order Nanoscale Iron is first loaded on active carbon fiber felt using liquid phase reduction, refills filling iron carbon reaction zone；The work
Property Carbon fibe felt, be placed between upper sieve plate and intermediate sieve plate in netted intersection.
4. group technology according to claim 1, it is characterised in that: the exhalant region of modified Fenton fluidized bed connects circulation
Device is divided to two water inlet pipes to be respectively fed to the lower part in Fenton oxidation area and the lower part of iron carbon reaction zone, and backflow water yield is respectively Q1
And Q2, Q1With Q2The ratio between with m3It is 8:1-10:1 that/d, which counts ratio,.
5. group technology according to claim 1, it is characterised in that: during modified Fenton fluidized bed processing, H2O2With
COD ratio in terms of mg/L is 2 ~ 4:1, H2O2With Fe2+Molar ratio be 3 ~ 5:1, average stop of the waste water in Fenton oxidation area
At 0.5 ~ 1.5 hour, waste water was controlled in the mean residence time of iron carbon reaction zone at 15 ~ 45 minutes for time control, passed through dosing
System and online pH meter adjust the pH value of waste water in Fenton fluidized bed, maintain it between 3.0 ~ 4.0.
6. group technology according to claim 1, it is characterised in that: the design volumetric loading of up-flow anaerobic sludge blanket is
10 ~ 12 kgBOD/(kg MLSSd).
7. group technology according to claim 1, it is characterised in that: the anaerobism section of aerobic/anaerobic baffled reactor is adopted
It is box-cage type ABR reactor, the box-cage type ABR reactor, boxes and baskets are made of stainless steel grizzly bar, are cuboid
Shape；The length and width of boxes and baskets is respectively less than the length and width of upward flow cell compartment, highly 35 for upward flow cell compartment effective height
~50%, boxes and baskets and the wall surface of upward flow cell compartment are apart less than 5mm；Size of mesh opening between stainless steel grizzly bar is less than filler most
Small size；The filler is floating stuffing, and density is in 0.90~0.96 g/cm3, filler 10~25mm of diameter, material is poly- third
Alkene or polyethylene.
8. group technology according to claim 1, it is characterised in that: the anaerobism section of aerobic/anaerobic baffled reactor is adopted
It is box-cage type ABR reactor, the starting method of the box-cage type ABR reactor is that seed sludge is seeded to above-mentioned case
It in cage ABR reactor, 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 by case
Cage mounted expires filler, adjust the hydraulic detention time in reactor be 6~for 24 hours；Boxes and baskets are placed under upward flow cell compartment by initial start stage
Portion, 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 set
In the middle part of upward flow cell compartment, after the amount increase of suspension anaerobic sludge and biomembrane in the middle part of upward flow cell compartment, into the later period；Starting
Boxes and baskets are placed in upward flow cell compartment top by the later period, until start completion；Initial start stage, starting mid-term and the time for starting the later period
Distribution is in terms of day, ratio 3:4:5,3:5:4,5:4:4 or 5:4:3.
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| CN102642911A (en) * | 2012-05-02 | 2012-08-22 | 山东绿泉环保工程有限公司 | Advanced oxidation treatment device and advanced oxidation treatment process of refractory organic wastewater |
| 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 |
| CN104649512A (en) * | 2014-12-23 | 2015-05-27 | 安徽省天虹绿洲环保科技有限公司 | High-concentration medicinal adjuvant wastewater treatment process |
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| CN102642911A (en) * | 2012-05-02 | 2012-08-22 | 山东绿泉环保工程有限公司 | Advanced oxidation treatment device and advanced oxidation treatment process of refractory organic wastewater |
| 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 |
| CN104649512A (en) * | 2014-12-23 | 2015-05-27 | 安徽省天虹绿洲环保科技有限公司 | High-concentration medicinal adjuvant wastewater treatment process |
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