CN107337301A - A kind of method of the electric Fenton processing waste water of additional hydrogen peroxide - Google Patents
A kind of method of the electric Fenton processing waste water of additional hydrogen peroxide Download PDFInfo
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- CN107337301A CN107337301A CN201710790707.0A CN201710790707A CN107337301A CN 107337301 A CN107337301 A CN 107337301A CN 201710790707 A CN201710790707 A CN 201710790707A CN 107337301 A CN107337301 A CN 107337301A
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- waste water
- processing
- acid waste
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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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
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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
- C02F1/5281—Installations for water purification using chemical agents
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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
Abstract
The present invention provides a kind of additional H2O2Electric Fenton processing waste water method, comprise the following steps：The pH value for adjusting waste water is acidity, obtains acid waste water；Continuous flowing decontamination processing is carried out to the acid waste water, obtains oxidized waste water；The continuous flowing decontamination processing includes：H is added at the source of the acid waste water2O2；, as anode, using inert electrode as negative electrode, H is added to described containing iron electrode2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；The continuous flowing decontamination processing is carried out under conditions of lasting aeration；The oxidized waste water is subjected to flocculation sediment processing.Test result indicates that when method provided by the invention handles certain reverse osmosis concentrated water of petrochemical enterprises 10min, COD clearances are i.e. up to 57.1%, TOC clearances up to 41.6%；After handling 30min, COD and TOC clearances are respectively 61.8% and 47.2%.
Description
Technical field
The present invention relates to technical field of waste water processing, more particularly to a kind of additional H2O2Electric Fenton processing waste water method.
Background technology
Electro-fenton process is because with process is easy to control, treatment effeciency is high, advantages of environment protection, turning into more welcome in recent years
It is a kind of it is new based on Fenton chemical reaction advanced electrochemical oxidation process.When handling waste water using Fenton process, in the solution
Electric current is passed through, medicament needed for all or part of generation Fenton's reaction, generation OH are reacted by cathode and anode.Wherein Fenton reagent
Required Fe2+It can be added by outside, anode iron aoxidizes, negative electrode iron restoring method obtains；And H2O2It can then be thrown by outside
Add or cathodic reduction produces.According to H2O2Different producing methods, electro-fenton process can be divided into negative electrode generation H in situ2O2Electric Fenton
Method and additional H2O2Electro-fenton process.
Negative electrode is in situ to produce H2O2Electro-fenton process to cathode material combination property require it is higher, do not require nothing more than electrode possess compared with
High liberation of hydrogen overvoltage and two electron redox catalytic activity, and require electrode in waste water have higher stability and
Corrosion resistance, so as to cause electrode cost higher, increase investment.Also, H2O2Generation efficiency in situ is very low, so as to cause OH
Yield is very low, final to influence advanced oxidation effect.To sum up, it is in situ to produce H2O2Electro-fenton process because its efficiency is low, cost is high etc.
Problem, engineer applied is not yet realized at present.
Additional H2O2Electro-fenton process H is directly launched in waste water2O2, H is prepared without cathode reaction2O2, therefore to electrode
Requirement it is relatively low；In addition, additional H2O2Mode be easy to control and adjust H2O2Concentration, it is ensured that there is abundance in reaction system
H2O2, waste water treatment efficiency is high, can avoid H2O2When original position produces asking for waste water treatment efficiency is influenceed because its yield is low
Topic.Therefore, additional H2O2Electro-fenton process there is significant advantage in terms of construction investment and treatment effect.
In addition, produce H for original position2O2Electro-fenton process, produce H because negative electrode is in situ2O2Need dissolved oxygen, therefore one
As need to be aerated.And for the additional H of routine2O2Electro-fenton process, because need not for negative electrode produce H2O2Dissolved oxygen is provided,
And it is generally acknowledged that aeration can be by the Fe in electric Fenton-like system2+It is converted into Fe3+, it is unfavorable for Fenton's reaction, therefore without aeration.
But conventional additional H2O2Electro-fenton process treatment effeciency it is still relatively low, even if during using longer hydraulic retention
Between, its removal efficiency to organic matter is still limited.If any scholar using inert electrode as yin, yang two-stage, additional Fe2+With
H2O2, when handling reverse osmosis concentrated water, even if after reacting 120min under optimum condition, organic removal rate is only 49.7%.
The content of the invention
It is an object of the invention to provide a kind of additional H2O2Electric Fenton processing waste water method.It is provided by the invention outer
Add H2O2Electric Fenton processing waste water method it is high to the treatment effeciency of waste water.
The invention provides a kind of additional H2O2Electric Fenton processing waste water method, comprise the following steps：
(1) pH value for adjusting waste water is acidity, obtains acid waste water；
(2) acid waste water obtained to the step (1) carries out continuous flowing decontamination processing, obtains oxidized waste water；It is described
Continuous flowing decontamination processing includes：H is added at the source of the acid waste water2O2；Using electric as anode, with inertia containing iron electrode
Extremely negative electrode, H is added to described2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；At the continuous flowing decontamination
Reason is carried out under conditions of lasting aeration；
(3) oxidized waste water for obtaining the step (2) carries out flocculation sediment processing.
Preferably, the pH value of acid waste water is 2.5~4.5 in the step (1).
Preferably, the flow velocity of acid waste water is 0.1~1.5m/s in the step (2), the continuous water for flowing decontamination processing
The power residence time is 15~60min.
Preferably, H at the source of acid waste water in the step (2)2O2Dosage be 50~500mg/L.
Preferably, the current density in the step (2) in acid waste water is 5~30mA/cm2。
Preferably, the gas of aeration is air or oxygen in the step (2).
Preferably, the aeration quantity of the aeration is 100~2000mL/ (Lmin).
Preferably, the time of the flocculation sediment processing in the step (3) is 30~120min.
Preferably, also include after flocculation sediment processing in the step (3)：The sludge that the flocculation sediment is handled to obtain
Concentrated and be dehydrated successively.
Preferably, also include before the pH value regulation of the step (1)：Waste water is filtered.
The invention provides a kind of additional H2O2Electric Fenton processing waste water method, comprise the following steps：Adjust waste water
PH value is acidity, obtains acid waste water；Continuous flowing decontamination processing is carried out to the acid waste water, obtains oxidized waste water；It is described
Continuous flowing decontamination processing includes：H is added at the source of the acid waste water2O2；Using electric as anode, with inertia containing iron electrode
Extremely negative electrode, H is added to described2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；At the continuous flowing decontamination
Reason is carried out under conditions of lasting aeration；The oxidized waste water is subjected to flocculation sediment processing.
The pH of present invention regulation waste water is acidity, and acid condition is provided for Fenton's reaction；By in the source of acid waste water
Place adds H2O2, make the upstream H of acid waste water2O2It is horizontal in higher concentration, and because pH value is low, Fe2+It is not easy to be oxidized, sun
The Fe that pole is electrolysed out2+Can rapidly and H2O2Reaction produces OH, and OH can efficiently be removed with carrying out non-selectivity to organic matter；
The immixture played using aeration, the mass transport process of fortification system so that useless Organic substance in water obtains effectively in a short time
Remove；With the flowing of acid waste water, H2O2Constantly consumption, Fe caused by anode electrolysis2+It is gradually excessive.Under acid waste water
Trip, due to H2O2Concentration reduces, and electric Fenton declines, is now aerated the Fe in system2+It is stronger to be oxidized to charge neutrality ability
Fe3+, system pH rise in addition, Fe3+With OH-Form the Fe (OH) that effect is caught with net3Precipitation or colloid, further strengthen
The removal of organic matter simultaneously improves sludge settling efficiency, therefore based on this stage acted on electric flocculation.
Test result indicates that method provided by the invention handles the reverse osmosis concentrated water of certain petroleum chemical enterprise, 10min is only handled
When, COD clearances are i.e. up to 57.1%, TOC clearances up to 41.6%；After handling 30min, COD and TOC clearances are high respectively
Up to 61.8% and 47.2%.
Brief description of the drawings
Fig. 1 is additional H in the present invention2O2Electric Fenton processing waste water method process flow diagram；
Fig. 2 is change curve of the embodiment of the present invention 1 with COD clearances in comparative example 1 with processing time；
Fig. 3 is change curve of the embodiment of the present invention 1 with TOC clearances in comparative example 1 with processing time.
Embodiment
The invention provides a kind of additional H2O2Electric Fenton processing waste water method, comprise the following steps：
(1) pH value for adjusting waste water is acidity, obtains acid waste water；
(2) acid waste water obtained to the step (1) carries out continuous flowing decontamination processing, obtains oxidized waste water；It is described
Continuous flowing decontamination processing includes：H is added at the source of the acid waste water2O2；Using electric as anode, with inertia containing iron electrode
Extremely negative electrode, H is added to described2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；At the continuous flowing decontamination
Reason is carried out under conditions of lasting aeration；
(3) oxidized waste water for obtaining the step (2) carries out flocculation sediment processing.
The pH value of present invention regulation waste water is acidity, obtains acid waste water.The present invention is to the source of the waste water without spy
Different restriction, method provided by the invention are applied to all waste water containing organic matter, the difficult degradation industry preferably containing organic matter
Waste water.
In the present invention, the pH value of the acid waste water is preferably 2.5~4.5, and more preferably 3~4.The present invention is to described
The no special restriction of operation of the regulation of pH value, is entered using pH value regulator well known to those skilled in the art and adjusting method
Row regulation.In the present invention, the pH value regulator is preferably sulfuric acid solution or hydrochloric acid solution.In the present invention, it is described
Acid waste water pH value is acidity, and acid condition is provided for Fenton's reaction.In the preferred scheme of the present invention, the pH value is Fenton
Reaction provides suitable environment.
The present invention does not have special restriction to the device of pH value regulation, waste water can be made to be mixed i.e. with pH value regulator
Can.The present invention preferably makes the waste water flow through the pipeline before electro-Fenton reaction pond, into the pipeline before the electro-Fenton reaction pond
PH value regulator is added, pH value regulation is carried out, obtains acid waste water.In the present invention, the flow velocity of the waste water be preferably 0.1~
1.5m/s, more preferably 0.4~1.0m/s, most preferably 0.6~0.8m/s.
In the present invention, preferably also include before the pH value regulation：Waste water is filtered.In the present invention, the mistake
Filter is preferred to remove the suspension that particle diameter is more than 1mm.Operation no special restriction of the present invention to the filtering, using ability
The technical scheme of waste water filtering known to field technique personnel.In the present invention, the filtering is preferably grid filtration.This hair
The bright specification to the grid does not have special restriction, can filter out the suspension of above-mentioned particle size range.
After the completion of filtering, the product filtered described in preferred pair of the present invention carries out water quality, runoff investigation.The present invention is to the water
The no special restriction of operation of matter, runoff investigation, using the skill of waste water quality well known to those skilled in the art, runoff investigation
Art scheme.In the present invention, the water quality, runoff investigation are carried out preferably in regulating reservoir.
After obtaining acid waste water, the acid waste water is carried out continuous flowing decontamination processing by the present invention, obtains oxidized waste water.
In the present invention, the continuous flowing decontamination processing includes：H is added at the source of the acid waste water2O2；With containing iron electrode
For anode, using inert electrode as negative electrode, add H to described2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination.
In the present invention, the flow velocity of the acid waste water is preferably 0.1~1.5m/s, more preferably 0.4~1.0m/s, most preferably 0.6
~0.8m/s.In the present invention, the hydraulic detention time of the continuous flowing decontamination processing is preferably 15~60min, more preferably
For 20~50min, most preferably 30~40min.
In the present invention, the current density in the acid waste water is preferably 5~30mA/cm2, more preferably 10~
25mA/cm2, most preferably 15~20mA/cm2.The present invention is preferably realized to Fe in reaction system by control electric current density2+It is dense
The control of degree.In the present invention, the Fe2+Theoretical growing amount calculated by Faraday's law：M=56It/zF；In formula, m mono-
Determine the Fe that anode separates out under current strength I (A) and conduction time t (s)2+Quality (g)；Z is the electron number of 1 atom transfer；
56 be the molal weight (g/mol) of Fe atoms；F is Faraday constant (96486C/mol), current density be current strength divided by
Electrode plate suqare.The Fe according to caused by above-mentioned formula can calculate system in certain current density lower certain time2+Amount.
The present invention does not have special restriction to the material containing iron electrode and inert electrode and shape, using this area skill
It is used for the electrode of electro-fenton process known to art personnel.In the present invention, the material containing iron electrode is preferably iron, cast iron
Or stainless steel；It is described to be preferably shaped to tabular, netted or tubular containing iron electrode.In an embodiment of the present invention, the iron content
Electrode is specially iron plate or stainless steel plate.In the present invention, the material of the inert electrode is preferably stainless steel, graphite or activity
Charcoal；The inert electrode is preferably shaped to tabular, netted or tubular.In an embodiment of the present invention, the inert electrode tool
Body is stainless steel plate, graphite felt or ACF felts.
The present invention is to the H2O2Dosing method there is no special restriction, using well known to those skilled in the art additional
H2O2Method.In the present invention, the H2O2It is preferred that with H2O2The form of the aqueous solution adds；The H2O2The matter of the aqueous solution
It is preferably 25~35% to measure concentration.In the present invention, H at the source of the acid waste water2O2Dosage be preferably 50~
500mg/L, more preferably 100~400mg/L, most preferably 200~300mg/L.
In the present invention, the H2O2Content of organics of the dosage preferably in acid waste water determine：According to waste water
In COD contents, according to 2mol H2O21mol O is provided2(or 2mol OH, be 32g equivalent to COD value) oxidation is organic
The theory relation of thing, the H required for 1mol COD is removed in computational theory2O2Amount.Calculating process is with H2O2Utilization rate be 40~
60% is defined.
In the present invention, the continuous flowing decontamination processing is carried out under conditions of lasting aeration.In the present invention, it is described
The gas of aeration is preferably air or oxygen；The aeration quantity of the aeration is preferably 100~2000mL/ (Lmin), more preferably
For 500~1500mL/ (Lmin), most preferably 800~1200mL/ (Lmin).
In the present invention, H is added at the source of the acid waste water2O2, make the upstream H of acid waste water2O2In higher concentration
Level, and because pH value is low, Fe2+It is not easy to be oxidized, the Fe that anode electrolysis goes out2+Can rapidly and H2O2Reaction produces OH, right
Organic matter efficiently removes with carrying out non-selectivity；Mixed by aeration, the mass transport process of fortification system so that have in waste water
Machine thing is effectively removed in a short time；With the continuous flowing of acid waste water, H2O2Constantly consumption, the Fe of anode electrolysis2+
It is gradually excessive.In the downstream of acid waste water, due to H2O2Concentration reduces, and electric Fenton declines, is now aerated in system
Fe2+It is oxidized to the stronger Fe of charge neutrality ability3+, system pH rise in addition, Fe3+With OH-Form the Fe that effect is caught with net
(OH)3Precipitation or colloid, further strengthen the removal of organic matter and improve sludge settling efficiency, therefore this stage is with electric flocculation
Based on effect.
In the present invention, the continuous flowing decontamination processing is preferably carried out in electro-Fenton reaction pond.In the present invention, institute
It is preferably deflector type reaction tank to state electro-Fenton reaction pond；The hop count of the baffling is preferably more than 2 sections, more preferably 3~10 sections.
The present invention does not have special restriction to the structure of the deflector type reaction tank, and use is well known to those skilled in the art
Deflector type reaction tank.In an embodiment of the present invention, it is provided with dividing plate in the deflector type reaction tank；The divider upright
In the bottom of pond of deflector type reaction tank, and it is staggered successively.In the present invention, reaction tank is separated to form multiple by the dividing plate
Baffling section.
In the present invention, one or more groups of electrodes are preferably provided with each baffling section.In the present invention, between every group of electrode
Distance be preferably 3~15mm, more preferably 5~10mm.In the present invention, the acid waste water in each baffling section is preferably
Identical current density.
In an embodiment of the present invention, the bottom in the electro-Fenton reaction pond is provided with aerator.The present invention is to described
Aerator does not have special restriction, using aerator well known to those skilled in the art.
In an embodiment of the present invention, it is provided with the electro-Fenton reaction pond and scrapes slag system.The present invention scrapes slag to described
The structure and species of system do not have special restriction, and slag system is scraped using well known to those skilled in the art.In the present invention
In, caused scum silica frost is struck off by scraping slag system during the continuous flowing decontamination processing.
After obtaining oxidized waste water, the oxidized waste water is carried out flocculation sediment processing by the present invention.In the present invention, the wadding
The time of solidifying precipitation process is preferably 30~120min, more preferably 45~90min.The present invention is to flocculation sediment processing
Device does not have special restriction, using equipment well known to those skilled in the art.In the present invention, at the flocculation sediment
Reason is carried out preferably in sedimentation basin.
In the present invention, preferably also include after the flocculation sediment processing：The sludge that the flocculation sediment is handled to obtain
Concentrated and be dehydrated successively.In the present invention, the product of the flocculation sediment processing includes supernatant and sludge.In the present invention
In, the supernatant directly can be reclaimed or discharged.The sludge is preferably concentrated and is dehydrated successively post processing by the present invention.
As shown in figure 1, in an embodiment of the present invention, the waste water removes the suspension of greater particle size after grid filtration
Thing, then flow into regulating reservoir and carry out water quality, runoff investigation, pH is then adjusted to acidity in the presence of pH regulating systems, then
Flow into electro-Fenton reaction pond；H is added in the front end in electro-Fenton reaction pond2O2, bottom is provided with aerating system, caused by course of reaction
Scum silica frost is struck off by scraping slag system, is precipitated after the completion of reaction into sedimentation basin, and the supernatant for precipitating to obtain flows into clear water reserviors,
Precipitate after obtained sludge enters sludge concentration tank concentration and be dehydrated.
In order to further illustrate the present invention, with reference to embodiment to additional H provided by the invention2O2Electric Fenton processing
The method of waste water is described in detail, but they can not be interpreted as into limiting the scope of the present invention.
Embodiment 1:
Certain reverse osmosis concentrated water of petrochemical enterprises is taken, its CODCrFor 60.20~82.77mg/L, turbidity is 1.12~3.15NTU,
Electrical conductivity is 9020~9150 μ S/cm.
Flow is handled according to Fig. 1, but does not include grid filtration, water quality and quantity regulation and sludge condensation and dehydration
Process.Anode uses iron plate, and negative electrode uses stainless steel plate, passes through 1mol/L H2SO4Solution adjusts to obtain pH=4 spent acidic
Water；
Experimental power supply takes constant current mode, current density 10mA/cm2, acid waste water flows through reaction with 0.5m/s flow velocitys
Device, H is added in acid waste water source2O2So that the H at source in acid waste water2O2Concentration is 150mg/L, while passes through aeration
Air is passed through into system, aeration quantity is 2000mL/ (Lmin), and it is fragrant to carry out electricity to reverse osmosis concentrated water in electro-Fenton reaction pond
Processing and flocculation treatment, the hydraulic detention time in electro-Fenton reaction pond be 30min；
After reaction terminates, waste water settles 30min in sedimentation basin, takes supernatant to cross 0.45um filter membranes measure COD and TOC
(total organic carbon).Under conditions of aeration quantity is 2000mL/ (Lmin), only 10min, COD clearances i.e. reachable 57.1%,
TOC clearances are up to 41.6%；After reacting 30min, COD and TOC clearances are respectively 61.8% and 47.2% under aeration condition.
Comparative example 1:
Using the identical waste water of embodiment 1 and processing method, as different from Example 1：Hybrid mode is stirred using machinery
Mix, no Air Exposure.Anode uses iron plate, and negative electrode uses stainless steel plate, passes through 1mol/L H2SO4Solution adjusts to obtain pH=4
Acid waste water.
Experimental power supply takes constant current mode, current density 10mA/cm2, by adding H2O2So that H in system2O2Concentration
For 150mg/L.System homogeneous reaction is made using mechanical agitation mode, mixing speed 120rpm is right in electro-Fenton reaction pond
Reverse osmosis concentrated water carries out electric Fenton processing, processing time 30min.
After reaction terminates, waste water settles 30min in sedimentation basin, takes supernatant to cross 0.45um filter membranes measure COD and TOC.
After reacting 30min under non-aeration condition, COD clearances are that 51.4%, TOC clearances are 35.2%, and sludge is not apparent from settling, body
System is in yellow green, and turbidity and colourity are larger.
Embodiment 1 contrasts respectively as shown in Figures 2 and 3 with the processing time of comparative example 1 and COD and TOC removal effects.By scheming
Understand, in additional H2O2Electric Fenton-like system in, aeration can significantly improve organic matter removal efficiency, and 10min is more mechanical stirs for reaction
Mix (120rpm) and improve nearly 16% and 13.6%,
Reaction 30min has carried nearly 10.4% and 12% compared with not being aerated.
Also, the embodiment of the present invention 1 with《Fered-Fenton methods handle petrochemical wastewater reverse osmosis concentrated water》、《Refinery(waste) water
Reverse osmosis concentrated water advanced treatment process research》Disclosed in two kinds of electric Fenton technical finesse petrochemical wastewater reverse osmosis concentrated water sides
Method is compared, and has obvious advantage, can at lower voltages (5V), and (30min) it is anti-efficiently to remove petrochemical wastewater in the short time
Hardly degraded organic substance in concentrated water, or even when only handling 10min (COD clearances are 57.1%) are permeated, it goes to organic matter
Except rate is substantially better than effect of the two kinds of electro-fenton processes of document report when handling 30min, even 120min.
Embodiment 1 and influence of the processing mode to sludge settling situation in comparative example 1 are as shown in table 1.Can from table 1
Go out, aeration can be effectively improved sludge settling property.But under mechanical agitation, in the 30min of sludge settling, feed liquid is without bright
Aobvious layering, turbidity and colourity are higher；And compared with mechanical agitation, it is passed through air and is remarkably improved flocculation sludge effect of settling, carries
High supernatant water quality.
The influence of the embodiment 1 of table 1 and comparative example 1 to sludge settling situation
Embodiment 2:
Certain paper mill paper-making deinking waste water two is taken to settle out water, after measured its CODcrFor 451.4~511.6mg/L.
It is handled using device same as Example 1, anode uses iron plate, and negative electrode uses stainless steel plate, leads to
Cross 1mol/L H2SO4Solution adjusts to obtain pH=4 acid waste water.
Experimental power supply takes constant current mode, current density 10mA/cm2, acid waste water flows through reaction with 0.5m/s flow velocitys
Device.H is added in acid waste water source2O2So that so that H at source2O2Concentration is 300mg/L, while by being aerated into system
Oxygen is passed through, aeration quantity is 2000mL/ (Lmin), and it is fragrant to carry out electricity to paper waste secondary clarifier effluent in electro-Fenton reaction pond
Pause and handle, the hydraulic detention time in electro-Fenton reaction pond is 30min；
After reaction terminates, waste water settles 30min in sedimentation basin, takes supernatant to cross 0.45um filter membranes measure COD.Aeration is strong
When changing electro-fenton process processing paper waste secondary clarifier effluent, 10min is only reacted, COD clearances are i.e. up to 48.8%；Reaction
After 30min, COD clearances are maximum up to 66.5%, improved than the electric Fenton technology water outlet COD clearances without aeration reinforcing
5.9%.
Method provided by the invention is can be seen that from above comparative example and embodiment, and aeration reinforcing is applied to additional H2O2
Electric Fenton-like system, pass through additional H first2O2To ensure Fenton's reaction initiating reagent concentration, generation H in situ is overcome2O2Electricity it is fragrant
The problems such as system waste water treatment efficiency that pauses is low, investment is high；In additional H2O2Under conditions of introduce aeration reinforcing means, in initial electricity
Fenton controls the stage, aeration reinforcing system mass transport process, improves reaction efficiency so that the short time can preferably be had
Machine thing removal effect, and in rear journey, it is aerated excessive Fe2+It is converted into Fe3+, fortification system flocculation process, improve pollutant and go
Except effect and sludge settling efficiency, adding for flocculation medicament is avoid or reduced, reduces sludge yield.The technique is by electric Fenton mistake
Journey is coupling in one reaction pool with flocculation process and carried out, and saves project occupation of land area.
The present invention has the advantages that treatment effeciency is high, energy consumption is low, mud amount is few, floor space is small, easily controllable, for difference
The organic wastewater with difficult degradation thereby of concentration has good treatment effect, has a wide range of application, and is easy to Project Realization, has good market
Application prospect.
Described above is only the preferred embodiment of the present invention, not makees any formal limitation to the present invention.Should
Point out, for those skilled in the art, under the premise without departing from the principles of the invention, if can also make
Dry improvements and modifications, these improvements and modifications also should be regarded as protection scope of the present invention.
Claims (10)
- A kind of 1. additional H2O2Electric Fenton processing waste water method, comprise the following steps：(1) pH value for adjusting waste water is acidity, obtains acid waste water；(2) acid waste water obtained to the step (1) carries out continuous flowing decontamination processing, obtains oxidized waste water；It is described continuous Flowing decontamination processing includes：H is added at the source of the acid waste water2O2；Using containing iron electrode as anode, using inert electrode as Negative electrode, H is added to described2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；The continuous flowing decontamination processing exists Carried out under conditions of lasting aeration；(3) oxidized waste water for obtaining the step (2) carries out flocculation sediment processing.
- 2. according to the method for claim 1, it is characterised in that in the step (1) pH value of acid waste water be 2.5~ 4.5。
- 3. according to the method for claim 1, it is characterised in that in the step (2) flow velocity of acid waste water be 0.1~ 1.5m/s, the continuous hydraulic detention time for flowing decontamination processing is 15~60min.
- 4. the method according to claim 1 or 3, it is characterised in that H at the source of acid waste water in step (2)2O2Add Measure as 50~500mg/L.
- 5. the method according to claim 1 or 3, it is characterised in that the current density in the step (2) in acid waste water For 5~30mA/cm2。
- 6. the method according to claim 1 or 3, it is characterised in that the gas of aeration is air or oxygen in the step (2) Gas.
- 7. according to the method for claim 6, it is characterised in that the aeration quantity of the aeration is 100~2000mL/ (L min)。
- 8. according to the method for claim 1, it is characterised in that the time of flocculation sediment in the step (3) processing is 30~120min.
- 9. the method according to claim 1 or 8, it is characterised in that also wrapped after flocculation sediment processing in the step (3) Include：The sludge that the flocculation sediment is handled to obtain is concentrated and is dehydrated successively.
- 10. according to the method for claim 1, it is characterised in that also include before the pH value regulation of the step (1)：To useless Water is filtered.
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