CN105884154A - Novel combined process for treating chemical wastewater - Google Patents
Novel combined process for treating chemical wastewater Download PDFInfo
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- CN105884154A CN105884154A CN201610485528.1A CN201610485528A CN105884154A CN 105884154 A CN105884154 A CN 105884154A CN 201610485528 A CN201610485528 A CN 201610485528A CN 105884154 A CN105884154 A CN 105884154A
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- 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
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- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/722—Oxidation by peroxides
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- C02F2305/026—Fenton's reagent
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Abstract
The invention provides a novel combined process for treating chemical wastewater. The process adopts a regulating tank, an improved Fenton fluidized bed, a degassing neutralizing tank, a coagulative precipitation tank, an up-flow anaerobic sludge bed and an SBR (sequencing batch reactor), wherein the units are connected by a water pipe in sequence to treat the chemical wastewater. The novel combined process has the beneficial effects that the process is optimized and is clear and concise in route; the overall COD (chemical oxygen demand) removal rate is not less than 95%; the removal rate of characteristic organic pollutants is not less than 95%; and the process is convenient to operate and manage, is stable and is low in investment and operating costs.
Description
Technical field
The present invention relates to a kind of method of wastewater treatment, be specifically related to the process of chemical wastewater treatment, belong to technical field of waste water processing.
Background technology
The features such as wastewater from chemical industry has that water quantity and quality changes greatly, biodegradability is poor, be difficult to the feature degraded and pollutant complexity is various, the water quality being typically based on actual waste water takes suitable preprocess method, such as techniques such as flocculation, light electrolysis, absorption, photocatalysis, destroy hardly degraded organic substance in waste water, improve the biodegradability of waste water, it is combined biological method again, such as ABR, SBR, A/O technique etc., wastewater from chemical industry is processed.Research to processing wastewater from chemical industry technique the most both at home and abroad also tends to use the group technology of multiple 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) " is although effect is fine, but the cost of device can be improved to a certain extent, and Aerobic-anaerobic couples the absolute anaerobic environment being unfavorable for microorganism repeatedly, biological treatment efficiency is the highest.Patent " a kind of baffled reactor and the method (CN200610012070) of process sewage thereof " and patent " Integrative processing plant for high concentration organic wasted water (CN200310100513.1) " relate to many secondary coupling of anaerobic processes and aerobic process, add the complexity of equipment and the difficulty of operational management, and there is no advanced oxidation processes.
At present, it is high to there is processing cost in the process technique of existing wastewater from chemical industry, and persistent organic pollutants removal efficiency is the highest, and process operation is unstable, and treatment effect is undesirable, it is impossible to meet the problems such as environmental requirement.
Summary of the invention
Goal of the invention: the invention aims to solve the deficiencies in the prior art, it is provided that a kind of process optimization is rationally, persistent organic pollutants treatment effeciency is high, treatment effect is stable and the process of the chemical wastewater treatment of economical rationality.
Technical scheme: in order to realize the purpose of the present invention, the technical solution used in the present invention is: a kind of a new combined process processing wastewater from chemical industry, and this group technology is modified model Fenton fluid bed (IFBR), up-flow anaerobic sludge blanket (UASB) and sbr reactor device (A/OBR) to be used in combination process wastewater from chemical industry；Group technology includes regulating reservoir, modified model Fenton fluid bed, degassing neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket and sbr reactor device, is sequentially connected with through water pipe.
This technique includes following operating procedure:
(1) wastewater from chemical industry is after pretreatment, enters regulating reservoir；
(2) it is adjusted rear waste water and is conveyed into modified model Fenton fluid bed by intake pump, in modified model Fenton fluid bed, be separately added into H by medicine system2SO4Solution, FeSO4Solution and H2O2Solution, is entered part effluent recycling in modified model Fenton fluid bed by reflux pump, presents fluidisation state in making Fenton fluid bed；The oxidizing tower of modified model Fenton fluid bed is cylindrical shape, and three pieces of sieve plates are divided into oxidizing tower from bottom to top into water water distribution area, Fenton oxidation district, ferrum carbon reaction zone and exhalant region；Fenton oxidation district is added with filler A, and ferrum carbon reaction zone is added with filler B；Circulating device is connected to water inlet at the two of exhalant region and oxidizing tower；By Fenton's reaction and the micro-electrolysis reaction of ferrum carbon reaction zone in Fenton oxidation district, remove part COD and most persistent organic pollutants in waste water；
(3) water outlet of modified model Fenton fluid bed enters degassing neutralization pond, sloughs a small amount of gas by stirring, adds NaOH solution, the pH value of regulation waste water；
(4) degassing neutralization pond water outlet enters coagulative precipitation tank, adds coagulant by coagulant medicine system, and controls mixing speed and form big flco；Entering back into sediment fraction, the big flco of formation realizes precipitate and separate in settling zone, and precipitating sludge processes through sludge treating system；
(5) coagulative precipitation tank water outlet enters up-flow anaerobic sludge blanket through infusion, after waste water is entered by reactor lower part, passes upward through Sludge Bed district, suspended sludge area, three phase separator, then water outlet, and biogas is discharged by air chamber；Remove part COD and persistent organic pollutants in waste water by the effect of anaerobe, reduce the SS of waste water further；Controlling hydraulic detention time is 12～36 h；Sludge Bed district granule sludge is tamed by anaerobic sludge；
(6) up-flow anaerobic sludge blanket water outlet enters sbr reactor device, the aeration of reaction zone, precipitation, draining, the Period Process circular flow such as idle；Rear portion, reaction zone is mounted with liftable automatic slash water device；
(7) discharged wastewater met the national standard after sbr reactor device processes.
Further, the bottom of regulating reservoir is provided with microporous aeration device, the water quality and quantity of regulation waste water；Wastewater from chemical industry water quality index after being adjusted: COD be 5000 ~ 6000 mg/L, SS be 150～300mg/L, chlorobenzene class is 60 ~ 80 mg/L.
Further, the filler A of modified model Fenton fluid bed uses quartz sand, and the particle diameter of quartz sand is 0.5 ~ 1.5
Mm, the filler B that ferrum carbon reaction zone is arranged, use active carbon fiber felt；First use liquid phase reduction to load zeroth order Nanoscale Iron on active carbon fiber felt, refill and insert ferrum carbon reaction zone；Active carbon fiber felt, is placed in netted intersection between upper strata sieve plate and middle sieve plate.
Further, the exhalant region of modified model Fenton fluid bed connects circulating device, and points of two water inlet pipes are respectively fed to water inlet at the two of bottom, Fenton oxidation district and bottom, ferrum carbon reaction zone, and the backflow water yield is respectively Q1And Q2, Q1With Q2Ratio with m3/ d meter ratio is 8:1-10:1.
Further, during modified model Fenton fluidized bed processing, H2O2It is 2 ~ 4:1, H with COD ratio in terms of mg/L2O2With Fe2+Mol ratio be 3 ~ 5:1, the waste water mean residence time in Fenton oxidation district controls at 0.5 ~ 1.5 hour, the waste water mean residence time in ferrum carbon reaction zone controls at 15 ~ 45 minutes, the pH value of waste water in Fenton fluid bed is regulated so that it is maintain between 3.0 ~ 4.0 by medicine system and online pH meter.
Further, up-flow anaerobic sludge blanket, its design volumetric loading is 10 ~ 12 kgCOD/(m3D).
Further, sbr reactor device, the aeration of its reaction zone, precipitation, draining, the process cycle period such as idle are 4 hours, and aeration, precipitation, draining, the distribution of idle time are respectively 120 minutes, 60 minutes, 40 minutes, 20 minutes；It is 0.2 ~ 0.4 kgCOD/(kgMLSS d that reactor runs sludge loading).
Ultimate principle is summarized as follows.
1, modified model Fenton fluid bed (IFBR) operation principle
(1) waste water enters the Fenton oxidation district of modified model Fenton fluid bed, is separately added into H by medicine system in Fenton fluid bed simultaneously2SO4Solution, FeSO4Solution and H2O2Solution, by reflux pump, water part is flowed back in Fenton fluid bed, fluidisation state is presented in making Fenton fluid bed, part COD and the organic pollution (being i.e. difficult to biodegradable organic pollution, also known as characteristic contamination or characteristic organic pollutants) of most difficult degradation of waste water is removed by Fenton's reaction；Regulation return flow, controls the height of filler expansion less than middle sieve plate.
The principle of Fenton fluidized bed process: utilizing carrier is to be entered into and up flowing by Fenton fluidized-bed bottom as crystallization nuclear species, pending waste water and interpolation medicament.Be circumscribed with effluent recycling pipeline, in order to adjust influent stream water degree of supersaturation and reach Flow Velocity on carrier make carrier surface formed stable state crystalline solid, when crystal particle diameter reaches 2.5
After the mm of mm ~ 3, outside drain tank, carry out recycling.Fenton fluidized bed process utilizes the pattern of fluid bed to make ferric iron major part produced by Fenton method be crystallized or precipitate, and is coated on the carrier surface of liquid bed, is one and combines homophase chemical oxidation (Fenton method), out-phase chemical oxidation (H2O2/ FeOOH), the new technique of the function such as fluid bed crystallization.Traditional Fenton oxidation method has been made significantly to improve by this technology, so can reduce employing traditional F enton method and produce substantial amounts of chemical sludge, the iron oxides simultaneously formed at carrier surface has the effect of heterocatalysis, and the pattern of fluid bed also promotes chemical oxidation reaction and mass-transfer efficiency, COD clearance is made to promote.Its reacted go out flowing water through pH value adjust after can produce iron containing sludge.Iron containing sludge reduces 70% than traditional Fenton oxidation, also reduces H2O2The waste of medication, may utilize hydrogen peroxide chemical feeding quantity simultaneously and adjusts, adjust COD removal amount, it is achieved effectively control the reduction of the COD of waste water, is the guarantee of waste water process qualified discharge.Fenton process is as the one of advanced oxidation simultaneously, the present invention mainly utilizes Fenton process to be difficult to biodegradable organic pollution except the most of waste water, make persistent organic pollutants chain rupture, open loop efficiently, resolve into small organic molecule, improve the biodegradability of waste water, it is easy to be further processed at follow-up biological processing unit.
(2) waste water enters the ferrum carbon reaction zone of modified model Fenton fluid bed through middle sieve plate, under the conditions of iron-carbon micro-electrolysis, and persistent organic pollutants in catalysis oxidized waste water.Micro electrolysis tech is a kind of ideal technology processing high concentrated organic wastewater at present.It is in the case of cold, and the potential difference utilizing the micro-electrolysis material self being filled in waste water to produce carries out electrolysis process to waste water, to reach the purpose of degradable organic pollutant.Middle sieve plate plays support ferrum carbon reaction zone filler and the effect of rectification.Modified model Fenton fluid bed, mainly by the zeroth order Nanoscale Iron of activated carbon fiber Yu load, forms the ferrum carbon battery of light electrolysis.The potential difference utilizing the micro-electrolysis material self being filled in waste water to produce carries out electrolysis process, the organic substance in catalytic degradation waste water to waste water.Active carbon fiber felt, after the zeroth order Nanoscale Iron of load consumes, takes out fiber felt, regenerates with liquid phase reduction, recycled.
2, upflow anaerobic sludge blanket reactor (UASB) operation principle
Upflow anaerobic sludge blanket reactor (UASB) anaerobic reaction process, as other Anaerobic treatment techniques, including hydrolysis, acidifying, produces acetic acid and methane phase etc..Participate in the conversion process of substrate by different microorganisms and convert a substrate into the inorganic matters such as end product natural pond gas and water.UASB is made up of Sludge Bed district, suspended sludge area, gas-liquid-solid three-phase separator (including settling zone) and a few part of air chamber.Sewage passes through from bottom to top, and reactor bottom has a high concentration, highly active Sludge Bed, and the majority of organic pollutants in sewage is degraded to methane and carbon dioxide through anaerobic fermentation here.These anaerobic processes are proper absolute anaerobic processes, and biological agent process does not has oxygen to participate in, and the anaerobe of cultivation is preponderated.Anaerobe forms granule sludge and the organic pollution of COD in waste water and difficult degradation plays main removal effect, and removal efficiency is high.Because of current and the agitation of bubble, on Sludge Bed, there is a sludge suspension layer.Reactor top is provided with three phase separator, in order to separating digesting gas, Digestive system and mud granule.Digestion gas autoreactor top is derived；The automatic landing of mud granule is settled down to the Sludge Bed of reactor bottom；Digestive system is from settling section water outlet.
UASB load-bearing capacity is the biggest, it is adaptable to high concentrated organic wastewater, the process of such as wastewater from chemical industry.The UASB of operational excellence has the highest organic pollutant removal rate, it is not necessary to stirring, adapts to load impact by a relatively large margin, temperature and pH change.The basic feature of UASB reactor is without absorption carrier, just can form the granule sludge that settling property is good, the speck of high concentration in holding reactor, thus can bear higher COD load, and COD clearance is up to more than 90%.Compared with other anaerobic biological reactors, the feature of UASB: (1) simple structure is ingenious, can turn out anaerobic grain sludge in reactor, it is achieved that mud mud age (SRT) separates with hydraulic detention time (HRT), thus Biomass is many in Sludge Bed, equivalent concentration calculates up to 20 ~ 30g/L；(2) volumetric loading rate is high, under the conditions of mesophilic digestion, typically up to 10kgCOD/(m d) left and right, waste water hydraulic detention time in reactor is shorter, and therefore required pond appearance is substantially reduced.(3) UASB reactor has the biggest adaptability to all kinds of waste water, and energy consumption is low, and sludge output is few.Weak point is to remove the nitrogen in waste water and phosphorus.
3, sbr reactor device operation principle
SBR is the abbreviation of sequencing batch active sludge, is a kind of activated sludge sewage disposal technology run by intermittent aerating mode.It is mainly characterized by operationally in order and intermittently operated, the core of SBR technology is sbr reactor pond, and this pond collects homogenizing, the most heavy, biodegradation, two functions such as heavy in a pond, without sludge recirculation system.It is particularly suited for intermittent discharge and the bigger occasion of changes in flow rate.SBR technique integrates reaction, precipitation, draining, function, the degraded of pollutant is a plug-flow process in time, microorganism is then among aerobic, anoxia, anaerobism cyclically-varying, thus reaches, to pollutant removal effect, the most also have preferable denitrogenation, phosphorus removal functional.Sbr reactor device major advantage: technological process is simple, and floor space is little, invests relatively low；Biochemical reaction motive force is big；Sedimentation effect is good；Flexible operation, strong shock resistance；It is not susceptible to sludge bulking；Applied widely, it is suitable for built by separate periods；Surplus sludge volume is little, stable in properties.
The process of the present invention is suitable for the process of the industrial wastewater of the organic properties pollutant containing difficult degradation such as wastewater from chemical industry, and in waste water, the total removal rate of the organic pollution of COD and difficult degradation is more than 95%, and effluent quality can meet the requirement in environmental protection.
Beneficial effect: the invention have the advantages that compared with existing technique.
1, the invention provides the group technology of a kind of different design.
2, process optimization, clear route is succinct；Bio-chemical effluent is through materializing strategy (modified model Fenton fluid bed IFBR), carry out biochemical treatment (the UASB reactor of absolute anaerobism+sbr reactor device processes) again, last water outlet after precipitation, technique composition is rationally, biochemical treatment and materializing strategy the most organically being combined, three main bodys processing unit IFBR, UASB and SBR mutually support.
3, general wastewater from chemical industry can effectively be processed by the technique that the present invention provides, and can obtain good treatment effect, meet the requirement in environmental protection.The technique that the present invention provides, overall COD clearance >=95%, organic properties pollutants removal rate >=95%, operational management is convenient, process stabilizing, and investment operating cost is low.Overcoming processing cost high, persistent organic pollutants are inefficient, and process operation is unstable, and treatment effect is undesirable, it is impossible to meet the deficiencies such as environmental requirement.
4, the technique that the present invention provides, the wherein homophase of Fenton fluid bed and the catalytic reaction of out-phase, the iron containing sludge of generation, than traditional Fenton oxidation minimizing 70%, also reduces H2O2The waste of medication, may utilize hydrogen peroxide chemical feeding quantity simultaneously and adjusts, adjust COD removal amount, it is achieved effectively control the reduction of the COD of waste water, ensure effluent quality.Being organically combined with micro-electrolysis reaction by Fenton oxidation of modified model Fenton fluid bed, makes persistent organic pollutants chain rupture, open loop the most efficiently, resolves into small organic molecule.Compared with the common Fenton fluid bed of co-content and treating capacity, in the case of water inlet indices is identical with added pharmaceutical quantities, the clearance of the organic pollution of difficult for biological degradation can be improved 10%, improve the biodegradability of waste water further.
Accompanying drawing explanation
A kind of a new combined process schematic diagram processing wastewater from chemical industry that Fig. 1 provides for the present invention.
Detailed description of the invention
Below in conjunction with the accompanying drawings and specific embodiment, it is further elucidated with the present invention, it should be understood that embodiment is merely to illustrate the present invention rather than limits the scope of the present invention, after having read the present invention, those skilled in the art all fall within the application claims limited range to the amendment of the various equivalent form of values of the present invention.
Embodiment 1:
The comprehensive wastewater that certain chemical enterprise produces needs to process, influent concentration COD before treatment≤6000mg/L, 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) 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.
Use the group technology in accompanying drawing 1, modified model Fenton fluid bed (IFBR), up-flow anaerobic sludge blanket (UASB) and sbr reactor device are used in combination wastewater from chemical industry is processed；Including regulating reservoir, modified model Fenton fluid bed, degassing neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket, sbr reactor device, it is sequentially connected with through water pipe.
This technique includes following operating procedure:
(1) wastewater from chemical industry is after pretreatment, enters regulating reservoir；
(2) it is adjusted rear waste water and is conveyed into modified model Fenton fluid bed by intake pump, in modified model Fenton fluid bed, be separately added into H by medicine system2SO4Solution, FeSO4Solution and H2O2Solution, is entered part effluent recycling in modified model Fenton fluid bed by reflux pump, presents fluidisation state in making Fenton fluid bed；The oxidizing tower of modified model Fenton fluid bed is cylindrical shape, and three pieces of sieve plates are divided into oxidizing tower from bottom to top into water water distribution area, Fenton oxidation district, ferrum carbon reaction zone and exhalant region；Fenton oxidation district is added with filler A, and ferrum carbon reaction zone is added with filler B；Circulating device is connected to water inlet at exhalant region and oxidizing tower two；By Fenton's reaction and the micro-electrolysis reaction of ferrum carbon reaction zone in Fenton oxidation district, remove part COD and most persistent organic pollutants in waste water；
(3) water outlet of modified model Fenton fluid bed enters degassing neutralization pond, sloughs a small amount of gas by stirring, adds NaOH solution, the pH value of regulation waste water；
(4) degassing neutralization pond water outlet enters coagulative precipitation tank, adds coagulant by coagulant medicine system, and controls mixing speed and form big flco；Entering back into sediment fraction, the big flco of formation realizes precipitate and separate in settling zone, and precipitating sludge processes through sludge treating system；
(5) coagulative precipitation tank water outlet enters up-flow anaerobic sludge blanket through infusion, after waste water is entered by reactor lower part, pass upward through Sludge Bed district, suspended sludge area, three phase separator, then water outlet, remove part COD and persistent organic pollutants in waste water by the effect of anaerobe, reduce the SS of waste water further；Controlling hydraulic detention time is 24 h；Sludge Bed district granule sludge is tamed by anaerobic sludge；
(6) up-flow anaerobic sludge blanket water outlet enters sbr reactor device, and reactor is designed as two parts along pond length direction, and front portion is also referred to as pre-reaction zone for biological selecting area, and rear portion is main reaction region；Rear portion, main reaction region is mounted with liftable automatic slash water device；The aeration of main reaction region, precipitation, draining, the Period Process circular flow such as idle；Realize continuum micromeehanics simultaneously, be interrupted draining；
(7) discharged wastewater met the national standard after sbr reactor device processes.
Waste water is conveyed into Fenton fluid bed inhalant region through intake pump, by bottom sieve plate water distribution；Waste water enters Fenton fluid bed Fenton oxidation district, is separately added into H by medicine system in Fenton fluid bed simultaneously2SO4Solution, FeSO4Solution and H2O2Solution, is flowed back into the water section in effluent trough in Fenton fluid bed by reflux pump, presents fluidisation state in making Fenton fluid bed, removes part COD and major part chlorobenzene class organic pollution in waste water by Fenton's reaction；Regulation return flow, controls the height of filler expansion less than middle sieve plate；Waste water enters ferrum carbon reaction zone through middle sieve plate, under the conditions of iron-carbon micro-electrolysis, and persistent organic pollutants in catalysis oxidized waste water；The waste water aoxidized through iron-carbon micro-electrolysis catalysis passes through upper strata sieve plate, in effluent weir enters effluent trough, enters next processing unit by outlet pipe；Connecting circulating device in the effluent trough of top, points of two water inlet pipes are respectively fed to water inlet at the two of bottom, Fenton oxidation district and bottom, ferrum carbon reaction zone, flow back into discharge and are respectively Q1And Q2, Q1With Q2With m3/ d meter ratio is 8:1.During Fenton fluidized bed processing, H2O2It is 2.5:1, H with concentration ratio (mg/L) of COD2O2With Fe2+Mol ratio be 4:1, the waste water mean residence time in Fenton oxidation district controls at 1 hour, the waste water mean residence time in ferrum carbon reaction zone controls at 30 minutes, regulates the pH value of waste water in Fenton fluid bed by medicine system and online pH meter, makes pH value maintain between 3.0～4.0.
The design volumetric loading of up-flow anaerobic sludge blanket is 11 kgCOD/(m3D).
Sbr reactor device, the aeration of its reaction zone, precipitation, draining, the process cycle period such as idle are 4 hours, and aeration, precipitation, draining, the distribution of idle time are respectively 120 minutes, 60 minutes, 40 minutes, 20 minutes；It is 0.3 kgCOD/(kgMLSS d that reactor runs sludge loading).
After combined PROCESS FOR TREATMENT, 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.Leading indicator each unit treatment effect see table.
Table 1 leading indicator each unit treatment effect catalog
Claims (7)
1. the group technology processing wastewater from chemical industry, it is characterised in that: this group technology is modified model Fenton fluid bed, up-flow anaerobic sludge blanket and sbr reactor device to be used in combination process wastewater from chemical industry；Described group technology includes regulating reservoir, modified model Fenton fluid bed, degassing neutralization pond, coagulative precipitation tank, up-flow anaerobic sludge blanket and sbr reactor device, is sequentially connected with through water pipe；
This technique includes following operating procedure:
(1) wastewater from chemical industry is after pretreatment, enters regulating reservoir；
(2) it is adjusted rear waste water and is conveyed into modified model Fenton fluid bed by intake pump, in modified model Fenton fluid bed, be separately added into H by medicine system2SO4Solution, FeSO4Solution and H2O2Solution, is entered part effluent recycling in modified model Fenton fluid bed by reflux pump, presents fluidisation state in making Fenton fluid bed；
The oxidizing tower of described modified model Fenton fluid bed is cylindrical shape, and three pieces of sieve plates are divided into oxidizing tower from bottom to top into water water distribution area, Fenton oxidation district, ferrum carbon reaction zone and exhalant region；Fenton oxidation district is added with filler A, and ferrum carbon reaction zone is added with filler B；Circulating device is connected to water inlet at the two of exhalant region and oxidizing tower；By Fenton's reaction and the micro-electrolysis reaction of ferrum carbon reaction zone in Fenton oxidation district, remove part COD and most persistent organic pollutants in waste water；
(3) water outlet of modified model Fenton fluid bed enters degassing neutralization pond, sloughs a small amount of gas by stirring, adds NaOH solution, the pH value of regulation waste water；
(4) degassing neutralization pond water outlet enters coagulative precipitation tank, adds coagulant by coagulant medicine system, and controls mixing speed and form big flco；Entering back into sediment fraction, the big flco of formation realizes precipitate and separate in settling zone, and precipitating sludge processes through sludge treating system；
(5) coagulative precipitation tank water outlet enters up-flow anaerobic sludge blanket through infusion, after waste water is entered by reactor lower part, passes upward through Sludge Bed district, suspended sludge area, three phase separator, then water outlet, and biogas is discharged by air chamber；Remove part COD and persistent organic pollutants in waste water by the effect of anaerobe, reduce the SS of waste water further；Controlling hydraulic detention time is 12～36 h；Sludge Bed district granule sludge is tamed by anaerobic sludge；
(6) up-flow anaerobic sludge blanket water outlet enters sbr reactor device, the aeration of reaction zone, precipitation, draining, the Period Process circular flow such as idle；Rear portion, reaction zone is mounted with liftable automatic slash water device；
(7) discharged wastewater met the national standard after sbr reactor device processes.
Group technology the most according to claim 1, it is characterised in that: the bottom of described regulating reservoir is provided with microporous aeration device, the water quality and quantity of regulation waste water；Wastewater from chemical industry water quality index after being adjusted: COD is 5000 ~ 6000
Mg/L, SS are 150～300mg/L, and chlorobenzene class is 60 ~ 80 mg/L.
Group technology the most according to claim 1, it is characterised in that: modified model Fenton fluid bed filler A uses quartz sand, and the particle diameter of described quartz sand, at 0.5 ~ 1.5 mm, the filler B that described ferrum carbon reaction zone is arranged, uses active carbon fiber felt；First use liquid phase reduction to load zeroth order Nanoscale Iron on active carbon fiber felt, refill and insert ferrum carbon reaction zone；Described active carbon fiber felt, is placed in netted intersection between upper strata sieve plate and middle sieve plate.
Group technology the most according to claim 1, it is characterised in that: modified model Fenton fluid bed exhalant region connects circulating device, and points of two water inlet pipes are respectively fed to water inlet at the two of bottom, Fenton oxidation district and bottom, ferrum carbon reaction zone, and the backflow water yield is respectively Q1And Q2, Q1With Q2Ratio with m3/ d meter ratio is 8:1-10:1.
Group technology the most according to claim 1, it is characterised in that: during modified model Fenton fluid bed is managed at which, H2O2It is 2 ~ 4:1, H with COD ratio in terms of mg/L2O2With Fe2+Mol ratio be 3 ~ 5:1, the waste water mean residence time in Fenton oxidation district controls at 0.5 ~ 1.5 hour, the waste water mean residence time in ferrum carbon reaction zone controls at 15 ~ 45 minutes, the pH value of waste water in Fenton fluid bed is regulated so that it is maintain between 3.0 ~ 4.0 by medicine system and online pH meter.
Group technology the most according to claim 1, it is characterised in that: the design volumetric loading of up-flow anaerobic sludge blanket is 10 ~ 12
KgCOD/(m3D).
Group technology the most according to claim 1, it is characterized in that: the aeration of the reaction zone of sbr reactor device, precipitation, draining, the process cycle period such as idle are 4 hours, and aeration, precipitation, draining, the distribution of idle time are respectively 120 minutes, 60 minutes, 40 minutes, 20 minutes；It is 0.2 ~ 0.4 kgCOD/(kgMLSS d that reactor runs sludge loading).
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| CN106517657A (en) * | 2016-11-16 | 2017-03-22 | 宜兴市天立环保有限公司 | Treating method for high-concentration wastewater from chemical production |
| CN106830563A (en) * | 2017-03-24 | 2017-06-13 | 盐城工学院 | Based on photoelectricity Fenton biological reinforced Waste Water Treatment and its method of wastewater treatment |
| CN108862926A (en) * | 2018-07-24 | 2018-11-23 | 长岭炼化岳阳工程设计有限公司 | The method for pre-processing HPPO legal system propylene oxide industry saline sewage |
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| CN111039511A (en) * | 2019-12-30 | 2020-04-21 | 何亚婷 | Modularized integrated process method for treating chemical recovered wastewater |
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| CN106517657A (en) * | 2016-11-16 | 2017-03-22 | 宜兴市天立环保有限公司 | Treating method for high-concentration wastewater from chemical production |
| CN106830563A (en) * | 2017-03-24 | 2017-06-13 | 盐城工学院 | Based on photoelectricity Fenton biological reinforced Waste Water Treatment and its method of wastewater treatment |
| CN109422413A (en) * | 2017-08-16 | 2019-03-05 | 天津科技大学 | A kind of water paint wastewater treatment equipment |
| CN108862926A (en) * | 2018-07-24 | 2018-11-23 | 长岭炼化岳阳工程设计有限公司 | The method for pre-processing HPPO legal system propylene oxide industry saline sewage |
| WO2020258359A1 (en) * | 2019-06-24 | 2020-12-30 | 广西博世科环保科技股份有限公司 | Improved upflow multi-phase wastewater oxidation treatment process and system |
| CN111039511A (en) * | 2019-12-30 | 2020-04-21 | 何亚婷 | Modularized integrated process method for treating chemical recovered wastewater |
| CN111039511B (en) * | 2019-12-30 | 2022-07-22 | 深圳市睿维盛环保科技有限公司 | Modularized integrated process method for treating chemical recovered wastewater |
| CN111925062A (en) * | 2020-08-14 | 2020-11-13 | 天津城建大学 | Combined treatment process for pharmaceutical intermediate production wastewater |
| CN112645549A (en) * | 2021-02-03 | 2021-04-13 | 湖南惟创环境科技有限公司 | Treatment system and operation process for middle and small-scale areca nut production wastewater |
| CN114249494A (en) * | 2021-12-15 | 2022-03-29 | 盐城工学院 | Combined process for treating chemical wastewater by IFBR-HAF-SBR |
| CN114315023A (en) * | 2021-12-25 | 2022-04-12 | 盐城工学院 | Combined chemical wastewater treatment device and treatment method |
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Application publication date: 20160824 |