CN107337301B - 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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- CN107337301B CN107337301B CN201710790707.0A CN201710790707A CN107337301B CN 107337301 B CN107337301 B CN 107337301B CN 201710790707 A CN201710790707 A CN 201710790707A CN 107337301 B CN107337301 B CN 107337301B
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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
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Abstract
The present invention provides a kind of additional H2O2Electric Fenton processing waste water method, comprising the following steps: adjust the pH value of waste water as acidity, obtain 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: to add H at the source of the acid waste water2O2；, as anode, using inert electrode as cathode, to add H to described containing iron electrode2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；The continuous flowing decontamination processing carries out under conditions of lasting aeration；The oxidized waste water is subjected to flocculation sedimentation processing.The experimental results showed that COD removal rate is i.e. up to 57.1%, TOC removal rate up to 41.6% when method provided by the invention handles certain reverse osmosis concentrated water of petrochemical enterprises 10min；After handling 30min, COD and TOC removal rate is respectively 61.8% and 47.2%.
Description
Technical field
The present invention relates to technical field of waste water processing, in particular to a kind of additional H2O2Electric Fenton processing waste water method.
Background technique
Electro-fenton process because have process is easy to control, treatment effeciency is high, advantages of environment protection, become more welcome in recent years
One kind it is novel based on Fenton chemical reaction advanced electrochemical oxidation process.When handling waste water using Fenton process, in the solution
It is passed through electric current, medicament needed for reacting all or part of generation Fenton's reaction by cathode and anode generates OH.Wherein Fenton reagent
Required Fe2+It can be added by outside, the oxidation of anode iron, the acquisition of cathode iron restoring method；And H2O2It can then be thrown by outside
Add or cathodic reduction generates.According to H2O2Electro-fenton process can be divided into cathode and generate H in situ by different producing methods2O2Electric Fenton
Method and additional H2O2Electro-fenton process.
Cathode generates H in situ2O2Electro-fenton process is more demanding to cathode material comprehensive performance, do not require nothing more than electrode have compared with
High liberation of hydrogen overvoltage and two electron redox catalytic activity, and require electrode in waste water stability with higher and
Corrosion resistance increases investment so as to cause electrode higher cost.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, in situ to generate H2O2Electro-fenton process because of its low efficiency, at high cost etc.
Problem not yet realizes engineer application 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 lower；In addition, additional H2O2Mode convenient for control and adjust H2O2Concentration, it is ensured that there is abundance in reaction system
H2O2, waste water treatment efficiency is high, can be avoided H2O2Generation Shi Yinqi yield in situ is low and influences asking for waste water treatment efficiency
Topic.Therefore, additional H2O2Electro-fenton process in terms of construction investment and treatment effect have significant advantage.
In addition, generating H in situ2O2Electro-fenton process, due to cathode in situ generate H2O2Need dissolved oxygen, therefore one
As be aerated.And for conventional additional H2O2Electro-fenton process, because without for cathode generate 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 lower, even if when using longer hydraulic retention
Between, it is still limited to the removal efficiency of organic matter.If any scholar using inert electrode as yin, yang two-stage, additional Fe2+With
H2O2, when handling reverse osmosis concentrated water, even if organic removal rate is only 49.7% after reacting 120min under optimum condition.
Summary of the invention
The purpose of the present invention is 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 present invention provides a kind of additional H2O2Electric Fenton processing waste water method, comprising the following steps:
(1) pH value for adjusting waste water is acidity, obtains acid waste water；
(2) continuous flowing decontamination processing is carried out to the acid waste water that the step (1) obtains, obtains oxidized waste water；It is described
Continuous flowing decontamination processing includes: to add H at the source of the acid waste water2O2；Using electric as anode, with inertia containing iron electrode
Extremely cathode adds H to described2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；At the continuous flowing decontamination
Reason carries out under conditions of lasting aeration；
(3) oxidized waste water for obtaining the step (2) carries out flocculation sedimentation 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 being aerated in the step (2) is air or oxygen.
Preferably, the aeration quantity of the aeration is 100~2000mL/ (Lmin).
Preferably, the time of the flocculation sedimentation processing in the step (3) is 30~120min.
Preferably, in the step (3) after flocculation sedimentation processing further include: the sludge for handling the flocculation sedimentation
It is successively concentrated and is dehydrated.
Preferably, before the pH value of the step (1) is adjusted further include: be filtered to waste water.
The present invention provides a kind of additional H2O2Electric Fenton processing waste water method, comprising 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: to add H at the source of the acid waste water2O2；Using electric as anode, with inertia containing iron electrode
Extremely cathode adds H to described2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；At the continuous flowing decontamination
Reason carries out under conditions of lasting aeration；The oxidized waste water is subjected to flocculation sedimentation processing.
The pH that the present invention adjusts waste water is acidity, provides acid condition for Fenton's reaction；By in the source of acid waste water
Place adds H2O2, make the upstream H of acid waste water2O2In higher concentration level, and since pH value is low, Fe2+It is not easy to be oxidized, sun
The Fe that pole is electrolysed out2+It can rapidly and H2O2Reaction generates OH, and OH can with the carrying out non-selectivity efficiently removal 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
Removal；With the flowing of acid waste water, H2O2Constantly consumption, the Fe that anode electrolysis generates2+It is gradually excessive.Under acid waste water
Trip, due to H2O2Concentration reduces, and electric Fenton declines are aerated at this time by the Fe in system2+It is stronger to be oxidized to charge neutrality ability
Fe3+, system pH increases in addition, Fe3+With OH-Form the Fe (OH) that there is net to catch effect3Precipitating or colloid are further strengthened
The removal of organic matter simultaneously improves sludge settling efficiency, therefore based on this stage acts on electric flocculation.
The experimental results showed that method provided by the invention handles the reverse osmosis concentrated water of certain petroleum chemical enterprise, 10min is only handled
When, COD removal rate is i.e. up to 57.1%, TOC removal rate up to 41.6%；After handling 30min, COD and TOC removal rate is high respectively
Up to 61.8% and 47.2%.
Detailed description of the invention
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 removal rate in comparative example 1 with the processing time；
Fig. 3 is change curve of the embodiment of the present invention 1 with TOC removal rate in comparative example 1 with the processing time.
Specific embodiment
The present invention provides a kind of additional H2O2Electric Fenton processing waste water method, comprising the following steps:
(1) pH value for adjusting waste water is acidity, obtains acid waste water；
(2) continuous flowing decontamination processing is carried out to the acid waste water that the step (1) obtains, obtains oxidized waste water；It is described
Continuous flowing decontamination processing includes: to add H at the source of the acid waste water2O2；Using electric as anode, with inertia containing iron electrode
Extremely cathode adds H to described2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；At the continuous flowing decontamination
Reason carries out under conditions of lasting aeration；
(3) oxidized waste water for obtaining the step (2) carries out flocculation sedimentation processing.
The pH value that the present invention adjusts 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 suitable for all waste water containing organic matter, the preferably industry difficult to degrade 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 not special restriction of operation of the adjusting of pH value, using pH adjusting agent well known to those skilled in the art and adjusting method into
Row is adjusted.In the present invention, the pH adjusting agent is preferably sulfuric acid solution or hydrochloric acid solution.In the present invention, described
Acid waste water pH value is acidity, provides acid condition for Fenton's reaction.In a preferred embodiment of the invention, the pH value is Fenton
Reaction provides suitable environment.
The device that the present invention adjusts the pH value does not have special restriction, waste water can be made to mix i.e. with pH adjusting agent
It can.The present invention preferably makes the waste water flow through the pipeline before electro-Fenton reaction pond, in the pipeline before Xiang Suoshu electro-Fenton reaction pond
PH adjusting agent is added, pH value adjusting 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, before the pH value is adjusted it is also preferable to include: waste water is filtered.In the present invention, the mistake
The suspended matter that the preferred removal partial size of filter is 1mm or more.The not special restriction of operation of the present invention to the filtering, using ability
The technical solution 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 suspended matter of above-mentioned particle size range.
After the completion of filtering, the present invention preferably carries out water quality, runoff investigation to the product of the filtering.The present invention is to the water
The not 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 carry out preferably in conditioning tank.
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: to add H at the source of the acid waste water2O2；To contain iron electrode
For anode, using inert electrode as cathode, 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, and 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 preferably passes through control current density and realizes to Fe in reaction system2+It is dense
The control of degree.In the present invention, the Fe2+Theoretical production quantity calculated by Faraday's law: m=56It/zF；In formula, m mono-
The Fe that anode is precipitated under constant current intensity 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 atom；F be Faraday constant (96486C/mol), current density be current strength divided by
Electrode plate suqare.The Fe that certain time inner body system generates under certain current density can be calculated according to above-mentioned formula2+Amount.
The present invention does not have special restriction to the material containing iron electrode and inert electrode and shape, using this field skill
The electrode of electro-fenton process is used for 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 plate, 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 plate, netted or tubular.In an embodiment of the present invention, the inert electrode tool
Body is stainless steel plate, graphite felt or ACF felt.
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 aqueous solution adds；The H2O2The matter of aqueous solution
Measuring concentration is preferably 25~35%.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 H2O2Dosage preferably according in acid waste water content of organics determine: according to waste water
In COD content, according to the H of 2mol2O2The O of 1mol is provided2(or OH of 2mol, being equivalent to COD value is 32g) oxidation is organic
The theory relation of object removes H required for the COD of 1mol in computational theory2O2Amount.Calculating process is with H2O2Utilization rate be 40~
Subject to 60%.
In the present invention, the continuous flowing decontamination processing carries out under conditions of lasting aeration.In the present invention, 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 since pH value is low, Fe2+It is not easy to be oxidized, the Fe that anode electrolysis goes out2+It can rapidly and H2O2Reaction generates OH, right
Organic matter with carrying out non-selectivity efficiently removal；It is mixed by aeration, the mass transport process of fortification system, so that having in waste water
Machine object 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, being aerated at this time will be in system
Fe2+It is oxidized to the stronger Fe of charge neutrality ability3+, system pH increases in addition, Fe3+With OH-Form the Fe that there is net to catch effect
(OH)3Precipitating 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 preferably carries out in electro-Fenton reaction pond.In the present invention, institute
Stating electro-Fenton reaction pond is preferably deflector type reaction tank；The number of segment of the baffling is preferably 2 sections or more, and 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, partition is provided in the deflector type reaction tank；The divider upright
It is staggered in the bottom of pond of deflector type reaction tank, and successively.In the present invention, reaction tank is separated to form multiple by the partition
Baffling section.
In the present invention, one or more groups of electrodes are preferably provided in 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 on the electro-Fenton reaction pond and scrapes slag system.The present invention scrapes slag to described
The structure and type of system do not have special restriction, scrape slag system using well known to those skilled in the art.In the present invention
In, the dross generated during the continuous flowing decontamination processing is struck off by scraping slag system.
After obtaining oxidized waste water, the oxidized waste water is carried out flocculation sedimentation 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 handles the flocculation sedimentation
Device does not have special restriction, using equipment well known to those skilled in the art.In the present invention, at the flocculation sedimentation
Reason carries out preferably in sedimentation basin.
In the present invention, it is also preferable to include the sludge for handling the flocculation sedimentation after flocculation sedimentation processing
It is successively concentrated and is dehydrated.In the present invention, the product of the flocculation sedimentation processing includes supernatant and sludge.In the present invention
In, the supernatant directly can be recycled or be discharged.The sludge is preferably successively concentrated and is dehydrated 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
Then object flows into conditioning tank and carries out water quality, runoff investigation, pH is then adjusted to acidity under the action of pH regulating system, then
Flow into electro-Fenton reaction pond；H is added in the front end in electro-Fenton reaction pond2O2, bottom is generated equipped with aerating system, reaction process
Dross is struck off by scraping slag system, is entered sedimentation basin after the reaction was completed and is precipitated, and the supernatant precipitated flows into clear water reserviors,
It precipitates after obtained sludge enters sludge concentration tank concentration and is dehydrated.
In order to further illustrate the present invention, below with reference to embodiment to additional H provided by the invention2O2Electric Fenton processing
The method of waste water is described in detail, but they cannot be interpreted as limiting the scope of the present invention.
Embodiment 1:
Take certain reverse osmosis concentrated water of petrochemical enterprises, CODCrFor 60.20~82.77mg/L, turbidity is 1.12~3.15NTU,
Conductivity is 9020~9150 μ S/cm.
Process is handled according to Fig. 1, but does not include grid filtration, water quality and quantity adjusting and sludge condensation and dehydration
Process.Anode uses iron plate, and cathode uses stainless steel plate, passes through the H of 1mol/L2SO4Solution adjusts to obtain the spent acidic of pH=4
Water；
Experimental power supply takes constant current mode, current density 10mA/cm2, acid waste water flows through reaction with 0.5m/s flow velocity
Device adds H in acid waste water source2O2, so that the H at source in acid waste water2O2Concentration is 150mg/L, while passing 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, hydraulic detention time in electro-Fenton reaction pond is 30min；
After reaction, waste water settles 30min in sedimentation basin, and supernatant is taken to cross 0.45um filter membrane measurement COD and TOC
(total organic carbon).Under conditions of aeration quantity is 2000mL/ (Lmin), only 10min, COD removal rate are reachable 57.1%,
TOC removal rate is up to 41.6%；After reacting 30min, COD and TOC removal rate is respectively 61.8% and 47.2% under aeration condition.
Comparative example 1:
Using the identical waste water of embodiment 1 and processing method, unlike the first embodiment: hybrid mode is stirred using machinery
It mixes, no Air Exposure.Anode uses iron plate, and cathode uses stainless steel plate, passes through the H of 1mol/L2SO4Solution 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 stirring mode, mixing speed 120rpm is right in electro-Fenton reaction pond
Reverse osmosis concentrated water carries out electric Fenton processing, and the processing time is 30min.
After reaction, waste water settles 30min in sedimentation basin, and supernatant is taken to cross 0.45um filter membrane measurement COD and TOC.
After reacting 30min under non-aeration condition, COD removal rate is that 51.4%, TOC removal rate is 35.2%, and sludge is not apparent from sedimentation, body
System is in yellow green, and turbidity and coloration are larger.
Embodiment 1 handles the time with comparative example 1 and the comparison of COD and TOC removal effect is as shown in Figures 2 and 3 respectively.By scheming
It is found that adding H outside2O2Electric Fenton-like system in, aeration can significantly improve organic matter removal efficiency, and 10min is more mechanical stirs for reaction
It mixes (120rpm) and improves nearly 16% and 13.6%,
Reaction 30min has mentioned nearly 10.4% and 12% compared with not being aerated.
Also, the embodiment of the present invention 1 and " Fered-Fenton method handles 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 treatment petrochemical wastewater reverse osmosis concentrated water sides
Method is compared, and has apparent 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 is permeated, or even when only handling 10min (COD removal rate is 57.1%), organic matter is gone
Except rate is substantially better than effect of the two kinds of electro-fenton processes reported in the literature 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.It can from table 1
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 coloration are higher；And compared with mechanical stirring, it is passed through air and is remarkably improved flocculation sludge effect of settling, mention
High supernatant water quality.
The influence of 1 embodiment 1 of table 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 cathode uses stainless steel plate, leads to
Cross the H of 1mol/L2SO4Solution adjusts to obtain the acid waste water of pH=4.
Experimental power supply takes constant current mode, current density 10mA/cm2, acid waste water flows through reaction with 0.5m/s flow velocity
Device.H is added in acid waste water source2O2, so that making H at source2O2Concentration is 300mg/L, while through aeration into system
It is passed through oxygen, 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, waste water settles 30min in sedimentation basin, and supernatant is taken to cross 0.45um filter membrane measurement COD.Aeration is strong
When changing electro-fenton process processing paper waste secondary clarifier effluent, 10min is only reacted, COD removal rate is i.e. up to 48.8%；Reaction
After 30min, COD removal rate maximum is improved up to 66.5% than the electric Fenton technology water outlet COD removal rate without aeration reinforcing
5.9%.
It can be seen that method provided by the invention from the above comparative example and embodiment and aeration reinforcing be applied to additional H2O2
Electric Fenton-like system, first pass through additional H2O2Guarantee Fenton's reaction initiating reagent concentration, overcomes and in situ generate H2O2Electricity it is fragrant
The problems such as system waste water treatment efficiency that pauses is low, investment is high；Adding H outside2O2Under conditions of introduce aeration reinforcing means, in initial electricity
Fenton controls the stage, and aeration reinforcing system mass transport process improves reaction efficiency, so that the short time, which can be obtained, preferably to be had
Machine object removal effect, and in rear journey, it is aerated excessive Fe2+It is converted into Fe3+, fortification system flocculation process improves pollutant and goes
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 coupled in one reaction pool with flocculation process and carries out, and saves project occupation of land area.
The present invention has many advantages, such as that treatment effeciency is high, low energy consumption, mud amount is few, occupied area 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.
The above is only a preferred embodiment of the present invention, it is not intended to limit the present invention in any form.It should
It points out, for those skilled in the art, without departing from the principle of the present invention, if can also make
Dry improvements and modifications, these modifications and embellishments should also be considered as the scope of protection of the present invention.
Claims (9)
1. a kind of additional H2O2Electric Fenton processing waste water method, comprising the following steps:
(1) pH value for adjusting waste water is acidity, obtains acid waste water；
(2) continuous flowing decontamination processing is carried out to the acid waste water that the step (1) obtains, obtains oxidized waste water；It is described continuous
Flowing decontamination processing includes: to add H at the source of the acid waste water2O2；To be as anode, with inert electrode containing iron electrode
Cathode adds H to described2O2Acid waste water lead to direct current carry out electro-Fenton reaction decontamination；The continuous flowing decontamination processing exists
It is carried out under conditions of lasting aeration；The gas of the aeration is air or oxygen；
(3) oxidized waste water for obtaining the step (2) carries out flocculation sedimentation processing.
2. the method according to claim 1, wherein in the step (1) acid waste water pH value be 2.5~
4.5。
3. the method according to claim 1, wherein in the step (2) acid waste water flow velocity be 0.1~
1.5m/s, the continuous hydraulic detention time for flowing decontamination processing are 15~60min.
4. method according to claim 1 or 3, it is characterised in that H at the source of acid waste water in step (2)2O2Add
Amount is 50~500mg/L.
5. method according to claim 1 or 3, which is characterized in that the current density in the step (2) in acid waste water
For 5~30mA/cm2。
6. the method according to claim 1, wherein the aeration quantity of the aeration is 100~2000mL/ (L
min)。
7. the method according to claim 1, wherein the time that the flocculation sedimentation in the step (3) is handled is
30~120min.
8. method according to claim 1 or claim 7, which is characterized in that also wrapped after flocculation sedimentation processing in the step (3)
It includes: the sludge that the flocculation sedimentation is handled successively is concentrated and is dehydrated.
9. the method according to claim 1, wherein before the pH value of the step (1) is adjusted further include: to waste water
It is filtered.
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| CN108793537A (en) * | 2018-07-02 | 2018-11-13 | 武夷学院 | A kind of processing method of laboratory waste water |
| CN109231596A (en) * | 2018-10-16 | 2019-01-18 | 珠海市水通环保设备有限公司 | A kind of hotel's Treated sewage reusing processing system |
| CN109879379A (en) * | 2019-04-23 | 2019-06-14 | 上海荣和环保科技有限公司 | A kind of three-stage electricity Fenton reduces the system and method for waste water COD |
| CN110668620A (en) * | 2019-11-07 | 2020-01-10 | 沈阳工业大学 | Jet fluidized bed type electro-Fenton treatment system |
| CN112408434B (en) * | 2020-09-15 | 2023-03-21 | 泉州南京大学环保产业研究院 | Iron removal method for natural alkali mother liquor |
| CN113461235A (en) * | 2021-07-27 | 2021-10-01 | 青岛理工大学 | Electrolysis-electro-Fenton flocculation composite system without adding acid, alkali and iron salt and with less mud production |
| CN113979574A (en) * | 2021-09-30 | 2022-01-28 | 深圳市中金岭南有色金属股份有限公司凡口铅锌矿 | Waste water treatment method |
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