CN105948407B - IFBR-UASB-ICEAS handles industrial wastewater technique - Google Patents

IFBR-UASB-ICEAS handles industrial wastewater technique Download PDF

Info

Publication number
CN105948407B
CN105948407B CN201610485470.0A CN201610485470A CN105948407B CN 105948407 B CN105948407 B CN 105948407B CN 201610485470 A CN201610485470 A CN 201610485470A CN 105948407 B CN105948407 B CN 105948407B
Authority
CN
China
Prior art keywords
water
fenton
fluidized bed
industrial wastewater
reactor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201610485470.0A
Other languages
Chinese (zh)
Other versions
CN105948407A (en
Inventor
金建祥
周佳玮
任生鼎
张文杰
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Anhui Anfeng Environmental Technology Co., Ltd
Original Assignee
Yangcheng Institute of Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Yangcheng Institute of Technology filed Critical Yangcheng Institute of Technology
Priority to CN201610485470.0A priority Critical patent/CN105948407B/en
Publication of CN105948407A publication Critical patent/CN105948407A/en
Application granted granted Critical
Publication of CN105948407B publication Critical patent/CN105948407B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • 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
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/02—Specific form of oxidant
    • C02F2305/026—Fenton's reagent
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • 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
    • 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 IFBR-UASB-ICEAS to handle industrial wastewater technique, which includes conditioning tank, modified Fenton fluidized bed, degassing neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket and ICEAS 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

IFBR-UASB-ICEAS handles industrial wastewater technique
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 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 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: IFBR-UASB-ICEAS Industrial wastewater technique is handled, which is that modified Fenton fluidized bed (IFBR), up-flow anaerobic sludge blanket is used in combination (UASB) industrial wastewater is handled with ICEAS reactor；Group technology includes conditioning tank, modified Fenton fluidized bed, takes off Gas neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket and ICEAS reactor, are sequentially connected through water pipe.
The technique of the processing 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 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 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 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, is then discharged, biogas is discharged by gas chamber；Pass through anaerobe Effect removes useless water part COD and persistent organic pollutants, further decreases the SS of waste water；Controlling hydraulic detention time is 12~36 h；Sludge Bed area granule sludge is from anaerobic sludge domestication；
(6) up-flow anaerobic sludge blanket water outlet enters ICEAS reactor, and reactor is designed as two parts along pond length direction, Front is that biological selecting area is also referred to as pre-reaction zone, and rear portion is main reaction region；The aeration of main reaction region, draining, leaves unused and waited at precipitating The operation of journey loop cycle；Micro- aerator is arranged in pre-reaction zone, and the water decanter of liftable draining is installed at main reaction region rear portion；Simultaneously Realize continuum micromeehanics, interruption draining；
(7) discharged wastewater met the national standard after ICEAS reactor for treatment.
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 B of iron carbon reaction zone setting can be used column-shaped active carbon, column-shaped active carbon, and round end diameter 3 ~ 4mm, 8 ~ 12 mm of height, first loads zeroth order Nanoscale Iron using liquid phase reduction on the activated carbon, refills filling iron carbon reaction zone, Refill filling iron carbon reaction zone.
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 design volumetric loading of up-flow anaerobic sludge blanket is 10 ~ 12 kgCOD/(m3D).
Further, the processes cycle period such as the aeration of ICEAS reactor main reaction region, precipitating, draining, idle is 4 small When, aeration, precipitating, draining, idle time distribution are respectively 120 minutes, 60 minutes, 40 minutes, 20 minutes；Reactor operation Sludge loading is 0.15 ~ 0.35 kgCOD/(kgMLSSd).
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 and load, forms the iron of light electrolysis Carbon battery.The potential difference generated using the micro-electrolysis material being filled in waste water itself carries out electrolysis processing, catalysis drop to waste water Solve the organic substance in waste water.After the zeroth order Nanoscale Iron of load consumes, active carbon is taken out, again with liquid phase reduction It is raw, it is recycled.
2, upflow anaerobic sludge blanket reactor (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.Majority of organic pollutants in sewage is degraded to by anaerobic fermentation here Methane and carbon dioxide.This anaerobic processes is proper absolute anaerobic processes, and biological effect process does not have oxygen ginseng With the anaerobic bacteria dominance of culture.Anaerobic bacteria forms granule sludge and rises mainly to COD in waste water and organic pollutant difficult to degrade Removal effect, and removal efficiency is high.Upflow anaerobic sludge blanket reactor (UASB) main body is reaction tower, can be divided into water cloth Water system, reaction zone (anaerobic granular sludge bed layer), three-phase separation area, outlet system and return-flow system.UASB is relied primarily on Grain sludge handles waste water, currently belongs to more advanced anaerobic process.Waste water enters reactor by the water distributor of bottom, by being rich in The sludge area of anaerobic bacteria, under the action of anaerobic bacteria, COD and persistent organic pollutants are largely removed, while being generated big Biogas is measured, is discharged respectively at the top of reactor by the effect of three phase separator, gas and water outlet, sludge then settles back sludge Area.It passes through maintains higher upflow velocity (6 ~ 12 m/ h) in operation, and granule sludge is made to be in suspended state, while Higher reactor can be used or use effluent recycling to obtain high stirring intensity, to ensure that into water and mud granule Come into full contact with, promote the fast degradation of organic matter.UASB reactor is equipped with special effluent recycling system.UASB reactor one As be it is cylindric tower-shaped, feature is that have very big ratio of height to diameter, general up to 3 ~ 5, the height of process units reactor up to 15 ~ 20 m.For stable anaerobic reactor using anaerobic grain sludge, the sinking speed of sludge is greater than the upper raising speed of sewage Degree.
UASB 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 UASB: 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. UASB 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, ICEAS reactor working principle
What ICEAS reactor developed on the basis of sequencing batch active sludge (SBR).Reactor is designed along pond length direction For two parts, front is that biological selecting area is also referred to as pre-reaction zone, and rear portion is main reaction region；Main reaction region rear portion is mounted with liftable Strain water installations automatically；The Period Process circular flow such as the aeration of main reaction region, precipitating, draining, idle；Simultaneously realize continuously into Water, interruption draining；Eliminate the secondary settling tank and sludge recirculation system of conventional activated sludge method；Simultaneously can continuum micromeehanics, interruption row Water.In pre-reaction zone, microorganism can by dissolved organic matter most of in the rapid absorption effluent of fast transfer mechanism of enzyme, Undergo the matrix Rapid Accumulation process an of high load capacity.Then a substrate degradation mistake compared with underload is undergone in main reaction region Journey.ICEAS technique integrates reaction, precipitating, draining, function, and the degradation of pollutant is a plug-flow process in time, and Microorganism is then in aerobic, anoxic, among anaerobism cyclically-varying, acts on to reach pollutant removal, while also having Preferable denitrogenation, phosphorus removal functional.Especially for industrial wastewater, the volume for expanding biological selecting area makes COD and difficult drop in waste water The organic pollutant of solution carries out sufficient biological hydrolysis reaction wherein.ICEAS reactor major advantage: process flow is simple, Occupied area is small, invests lower；Biochemical reaction motive force is big；Sedimentation effect is good；Flexible operation, strong shock resistance；It is not easy to send out Primary sludge expansion；It is applied widely, it is suitble to built by separate periods；Surplus sludge volume is small, and property is stablized.
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 compared with existing technique the invention has the advantages that.
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 (improving Fenton fluidized bed IFBR), then carries out Biochemical treatment (the UASB reactor+ICEAS reactor for treatment of absolute anaerobism), is finally discharged after precipitation, and technique composition is reasonable, Biochemical treatment and materializing strategy are orderly organically combined, three main body processing units IFBR, UASB and ICEAS are mutually supported.
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.
Detailed description of the invention
Fig. 1 is that IFBR-UASB-ICEAS provided by the invention handles industrial wastewater process schematic representation.
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), up-flow anaerobic sludge blanket is used in combination (UASB) wastewater from chemical industry is handled with ICEAS reactor；Including conditioning tank, modified Fenton fluidized bed, degassing neutralization pond, Coagulative precipitation tank, up-flow anaerobic sludge blanket, ICEAS reactor, are sequentially connected through water pipe.
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；The filler A of Fenton oxidation area setting uses quartz sand, and the partial size of quartz sand is in 0.5 ~ 1.5 mm；Iron carbon reaction zone is set The filler B set, using Alveolate activated carbon, honeycomb mouth is consistent with water flow flow direction；Alveolate activated carbon, wall thickness are 0.5mm, volume density are 380 ~ 450 kg/m3；First zeroth order Nanoscale Iron is loaded using liquid phase reduction on the activated carbon, refills filling Iron carbon reaction zone refills filling iron carbon reaction zone；
(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, is then discharged, biogas is discharged by gas chamber；Pass through anaerobe Effect removes useless water part COD and persistent organic pollutants, further decreases the SS of waste water；Controlling hydraulic detention time is 12~36 h；Sludge Bed area granule sludge is from anaerobic sludge domestication；
(6) up-flow anaerobic sludge blanket water outlet enters ICEAS reactor, and reactor is designed as two parts along pond length direction, Front is that biological selecting area is also referred to as pre-reaction zone, and rear portion is main reaction region；The aeration of main reaction region, draining, leaves unused and waited at precipitating The operation of journey loop cycle；Micro- aerator is arranged in pre-reaction zone, and the water decanter of liftable draining is installed at main reaction region rear portion；Simultaneously Realize continuum micromeehanics, interruption draining；
(7) discharged wastewater met the national standard after ICEAS reactor for treatment.
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 up-flow anaerobic sludge blanket is 4, and 9 m/h of upflow velocity is maintained to keep particle dirty in operation Mud is in suspended state；Design volumetric loading is 11kgCOD/(m3D).
ICEAS reactor, the processes cycle period such as the aeration of main reaction region, precipitating, draining, idle is 4 hours, is exposed Gas, precipitating, draining, idle time distribution are respectively 120 minutes, 60 minutes, 40 minutes, 20 minutes；Reactor runs sludge Load is 0.3 kgCOD/(kgMLSSd).
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 (7)

  1. The technique of 1.IFBR-UASB-ICEAS processing industrial wastewater, it is characterised in that: the technique is that modified Fenton is used in combination Fluidized bed, up-flow anaerobic sludge blanket and ICEAS reactor handle industrial wastewater；The technique include conditioning tank, Modified Fenton fluidized bed, degassing neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket and ICEAS reactor, through water pipe according to Secondary connection；
    The technique of the processing 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；The filler A of Fenton oxidation area setting 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 bee Nest shaped activated carbon, honeycomb mouth are consistent with water flow flow direction；The Alveolate activated carbon, wall thickness 0.5mm, volume density are 380~450 kg/m3；First zeroth order Nanoscale Iron is loaded using liquid phase reduction on the activated carbon, refills filling iron carbon reaction zone；
    (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, are then discharged, and biogas is discharged by gas chamber；Pass through the effect of anaerobe Useless water part COD and persistent organic pollutants are removed, the SS of waste water is further decreased；Control hydraulic detention time be 12~ 36 h；Sludge Bed area granule sludge is from anaerobic sludge domestication；
    (6) up-flow anaerobic sludge blanket water outlet enters ICEAS reactor, and reactor is designed as two parts, front along pond length direction It is also referred to as pre-reaction zone for biological selecting area, rear portion is main reaction region；Aeration, precipitating, draining, the idle Period Process of main reaction region Circular flow；Micro- aerator is arranged in pre-reaction zone, and the water decanter of liftable draining is installed at main reaction region rear portion；The company of realization simultaneously Continuous water inlet, interruption draining；
    (7) discharged wastewater met the national standard after ICEAS reactor for treatment.
  2. 2. the technique of processing industrial wastewater according to claim 1, it is characterised in that: the lower part of the conditioning tank is equipped with Microporous aeration device adjusts the water quality and quantity of waste water；Industrial wastewater water quality indicator after adjusting: COD is 5000 ~ 6000 mg/ L, SS is 150~300mg/L, and chlorobenzene class is 60 ~ 80 mg/L.
  3. 3. the technique of processing industrial wastewater according to claim 1, it is characterised in that: the iron carbon of modified Fenton fluidized bed The filler B of reaction zone setting uses column-shaped active carbon, the column-shaped active carbon, round end 3 ~ 4mm of diameter, 8 ~ 12 mm of height.
  4. 4. the technique of processing industrial wastewater according to claim 1, it is characterised in that: the water outlet of modified Fenton fluidized bed Area connects circulator, and two water inlet pipes be divided to be respectively fed to water inlet at the two of Fenton oxidation area lower part and iron carbon reaction zone lower part Mouthful, backflow water yield is respectively Q1And Q2, Q1With Q2The ratio between with m3It is 8:1-10:1 that/d, which counts ratio,.
  5. 5. the technique of processing industrial wastewater according to claim 1, it is characterised in that: modified Fenton fluidized bed is at which During reason, H2O2Ratio is 2 ~ 4:1, H in terms of mg/L with COD2O2With Fe2+Molar ratio be 3 ~ 5:1, waste water is in Fenton oxygen Change the mean residence time control in area at 0.5 ~ 1.5 hour, waste water is controlled in the mean residence time of iron carbon reaction zone 15 ~ 45 Minute, the pH value of waste water in Fenton fluidized bed is adjusted by medicine system and online pH meter, maintains it between 3.0 ~ 4.0.
  6. 6. the technique of processing industrial wastewater according to claim 1, it is characterised in that: the design of up-flow anaerobic sludge blanket Volumetric loading is 10 ~ 12 kgCOD/(m3D).
  7. 7. the technique of processing industrial wastewater according to claim 1, it is characterised in that: the main reaction region of ICEAS reactor Aeration, precipitating, draining, idle process cycle period be 4 hours, aeration, precipitating, draining, idle time is respectively 120 minutes, 60 minutes, 40 minutes, 20 minutes；It is 0.15 ~ 0.35 kgCOD/(kgMLSSd that reactor, which runs sludge loading).
CN201610485470.0A 2016-06-29 2016-06-29 IFBR-UASB-ICEAS handles industrial wastewater technique Active CN105948407B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610485470.0A CN105948407B (en) 2016-06-29 2016-06-29 IFBR-UASB-ICEAS handles industrial wastewater technique

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610485470.0A CN105948407B (en) 2016-06-29 2016-06-29 IFBR-UASB-ICEAS handles industrial wastewater technique

Publications (2)

Publication Number Publication Date
CN105948407A CN105948407A (en) 2016-09-21
CN105948407B true CN105948407B (en) 2019-05-07

Family

ID=56904113

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610485470.0A Active CN105948407B (en) 2016-06-29 2016-06-29 IFBR-UASB-ICEAS handles industrial wastewater technique

Country Status (1)

Country Link
CN (1) CN105948407B (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114044610A (en) * 2021-11-22 2022-02-15 盐城工学院 Method for treating industrial wastewater by combined process

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103613247A (en) * 2013-12-02 2014-03-05 安徽省绿巨人环境技术有限公司 Treatment process for bearing production 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

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
CN103613247A (en) * 2013-12-02 2014-03-05 安徽省绿巨人环境技术有限公司 Treatment process for bearing production wastewater

Also Published As

Publication number Publication date
CN105948407A (en) 2016-09-21

Similar Documents

Publication Publication Date Title
CN105884154A (en) Novel combined process for treating chemical wastewater
US8894855B2 (en) Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods
CN103693738B (en) Composite semi-nitration-anaerobic ammonia oxidation autotrophic denitrification device and operating method thereof
CN201024125Y (en) Nitrosation-anaerobic ammonium oxidation coupled synergistic biological denitrification device
CN101525207A (en) Integrated pre-denitrification and denitrogenation biological filter sewerage treatment process
CN105948412B (en) The group technology of FBR-UASB-A/OBR processing industrial wastewater
CN103880248A (en) Coking wastewater treatment system and treatment method
CN105948408A (en) Method for treating chemical wastewater through IFBR-EGSB-CASS (Improved Fluidized Bed Reactor-Expanded Granular Sludge Bed-Cyclic Activated Sludge System) process
CN103539262B (en) Improved A<2>O sewage treatment method
CN105948410A (en) IFBR-EGSB-SBR (Improved Fluidized Bed Reactor-Expanded Granular Sludge Bed-Sequencing Batch Reactor) combined process for treating chemical wastewater
CN101376553A (en) Method for processing low temperature sewerage using low-intensity ultrasonic strengthened membrane bioreactor
CN105884152B (en) IFBR-UASB-A/OBR handles wastewater from chemical industry group technology
CN109970196A (en) A kind of integrated form integrated waste water treating tank of application biology multiplication and fluidized-bed process
CN201962120U (en) Efficient two-phase integrated anaerobic reactor
CN206512058U (en) A kind of efficient villages and small towns waste water treating and reutilizing device
CN103112948A (en) Method for rapidly culturing autotrophic nitrogen removal granule sludge under conditions of low substrate concentration and high ascending velocity
CN105948411B (en) A kind of technique for treating industrial wastewater
CN105884153A (en) Novel chemical wastewater treatment process
CN105948407B (en) IFBR-UASB-ICEAS handles industrial wastewater technique
CN105884151B (en) The method of group technology processing industrial wastewater
CN105948409A (en) Novel method for treating industrial wastewater through combined processes
CN207845440U (en) Production waste water mixes purification system with sanitary wastewater
CN213680293U (en) Integrated biological fluidized bed sewage treatment device
CN208454610U (en) A kind of intensified denitrification and dephosphorization circulating biological membranous system for sanitary sewage disposal
CN202671366U (en) Cross-flow anaerobic sludge bed reactor

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant
TR01 Transfer of patent right

Effective date of registration: 20200218

Address after: 510530 room 1923, building 3, Ruifeng center, Kaichuang Avenue, Huangpu District, Guangzhou City, Guangdong Province

Patentee after: Guangzhou bud rice Intellectual Property Service Co., Ltd.

Address before: 224051 Yancheng City hope road, Jiangsu, No. 1

Patentee before: YANCHENG INSTITUTE OF TECHNOLOGY

TR01 Transfer of patent right
TR01 Transfer of patent right

Effective date of registration: 20200602

Address after: Room 2602, B-1, Dongyi Financial Plaza, 169 Funan Road, Luyang District, Hefei City, Anhui Province 230000

Patentee after: Anhui Anfeng Environmental Technology Co., Ltd

Address before: 510530 room 1923, building 3, Ruifeng center, Kaichuang Avenue, Huangpu District, Guangzhou City, Guangdong Province

Patentee before: Guangzhou bud rice Intellectual Property Service Co.,Ltd.

TR01 Transfer of patent right