CN107082485A - The method that azo dyes composite pollution waste water is removed using bio-electrochemical reactor system - Google Patents
The method that azo dyes composite pollution waste water is removed using bio-electrochemical reactor system Download PDFInfo
- Publication number
- CN107082485A CN107082485A CN201710474021.0A CN201710474021A CN107082485A CN 107082485 A CN107082485 A CN 107082485A CN 201710474021 A CN201710474021 A CN 201710474021A CN 107082485 A CN107082485 A CN 107082485A
- Authority
- CN
- China
- Prior art keywords
- pond
- azo dyes
- concentration
- anaerobic
- bio
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/005—Combined electrochemical biological processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
- C02F2101/163—Nitrates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/308—Dyes; Colorants; Fluorescent agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/06—Nutrients for stimulating the growth of microorganisms
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Water Supply & Treatment (AREA)
- Hydrology & Water Resources (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Engineering & Computer Science (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Molecular Biology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Electrochemistry (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The method that azo dyes composite pollution waste water is removed using bio-electrochemical reactor system, the present invention relates to the processing method of azo dyes composite pollution waste water.Will the present invention is to solve the technical problem that existing anaerobic biological process azo dyes wastewater treatment speed is slow, efficiency is low and physico-chemical process cost is high.This method：First, bio-electrochemical reactor system is built；2nd, the culturing sludge of bio-electrochemical reactor system and domestication；3rd, the operation of bio-electrochemical reactor system.The reactor water outlet COD of the present invention, the clearance of inorganic nitrogen and azo dyes respectively reach 89%, 75%, 92%, the composite pollution waste water containing azo dyes can be effectively removed, available in sewage treatment project.
Description
Technical field
The present invention relates to the processing method of azo dyes composite pollution waste water.
Technical background
Dyeing waste water, the especially waste water containing azo dyes, with discharge capacity is big, content of organics is high, bio-toxicity
Greatly, the characteristics of colourity is high, it handles the emphasis and difficult point of always water treatment field.Reducing the colourity containing azo dye wastewater is
The key link of waste water from dyestuff is handled, the color development and auxochromes of dyestuff can be targetedly destroyed using biological and chemical method
Group, make it is dye decolored, meanwhile, the bio-toxicity of dye decolored product is greatly reduced, and realizes the mesh of decoloring dye waste water detoxification
's.Wherein, anaerobic biological process is main technique technology of the processing containing azo dye wastewater, and anaerobe utilizes organic in water
During substrate is as carbon source, electronics is provided to azo group (- N=N-), makes its azo bond Fragmentative reduction.Anaerobic organism work
Skill have cost it is low, it is environment-friendly the characteristics of, but there is also reaction speed is slow, the drawbacks of efficiency is low, floor space is big.And utilize
Although what physico-chemical process can be rapidly and efficiently makes decoloring dye waste water, the cost of great number also makes physical-chemical process be difficult to greatly
Sizable application.
The content of the invention
Existing anaerobic biological process azo dyes wastewater treatment speed is slow, efficiency is low the invention aims to solving and
The high technical problem of physico-chemical process cost, and provide and remove azo using electro photoluminescence anaerobic-aerobic continuous stream reaction unit
The method of dyestuff composite pollution waste water.
The utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit of the present invention removes the side of azo dyes composite pollution waste water
Method is carried out according to the following steps：
First, bio-electrochemical reactor system is built：Bio-electrochemical reactor system by reactor shell, dividing plate,
Second pond, the first reflux pump, the second reflux pump and adjustable DC power supply composition；
Dividing plate divides housing 135 into anaerobic pond, Aerobic Pond；The lower partition has water hole；
Agitator and a pair of electrodes are provided with anaerobic pond；Electrode is connected with adjustable DC power supply；The side of anaerobic pond
Side wall lower ends set water inlet to set sludge reflux mouthful with nitrification liquid refluxing opening, upper end；
Aerator is set in Aerobic Pond；In Aerobic Pond side, side wall lower ends set nitrification liquid to export, and upper end is set out
The mouth of a river；
Second pond upper end sets water inlet and gap, and discharge pipeline is connected with lower end；
First reflux pump is arranged on the pipeline between the outlet of Aerobic Pond nitrification liquid and anaerobic pond nitrification liquid refluxing opening；
Second reflux pump is arranged on the pipeline between the discharge pipeline of second pond and anaerobic pond sludge reflux mouthful；
2nd, the culturing sludge of bio-electrochemical reactor system and domestication：
A, it is that 1.0g/L, the concentration of alizarin yellow R are 0.04g/L, NH by the concentration of glucose4Cl concentration be 0.04g/L,
KNO3Concentration be that 0.07g/L, the concentration of vitamin liquid are that the ratio that 0.5ml/L, the concentration of mineral element liquid are 0.1ml/L is matched somebody with somebody
System domestication water distribution, then by domestication water distribution and activated sludge volume ratio be 1：Domestication water distribution and activated sludge are added to reaction by 10
In device housing, by anaerobic pond plus cover plate for sealing, turn on agitator is aerated 24~26h into Aerobic Pond by aerator；
B, will domestication water distribution be passed through through water inlet in anaerobic pond, then by water hole enter Aerobic Pond in, Aerobic Pond bottom
The liquid in portion is exported through nitrification liquid, the first reflux pump is back in anaerobic pond；The water flowed out from Aerobic Pond delivery port enters two and sunk
Pond, after precipitation, clear water are flowed out from gap, and partial sludge is back in anaerobic pond through the second reflux pump, and excess sludge is from row
Mud pipe is discharged；Run time is 7~10 days；During running, nitrification liquid backflow volume ratio is gradually reduced from 400%~500%
To 300%, sludge reflux volume ratio is gradually reduced to 50% from 100%~120%, hydraulic detention time from 20~24h progressively
It is reduced to 9h；
C, holding mixed liquid recycle ratio are that 300%, return sludge ratio is that 50%, hydraulic detention time is 9h constant, will be tamed and dociled
The concentration for changing alizarin yellow R in water distribution is gradually increased by 0.005~0.01g/L of daily increase speed, until the concentration of alizarin yellow R
Reach 0.1g/L；
D, the mixed liquid recycle ratio of holding bio-electrochemical reactor system are that 300%, return sludge ratio is 50%, waterpower
Residence time is that 9h, the concentration of alizarin yellow R are 0.1g/L constant, the COD and alizarin yellow R concentration of METHOD FOR CONTINUOUS DETERMINATION water outlet, works as water outlet
COD and alizarin yellow R concentration reach stabilization, complete reactor start-up；
3rd, the operation of bio-electrochemical reactor system：
Domestication water distribution in the bio-electrochemical reactor system for completing startup is substituted for into pending azo dyes to mix
Pollutant effluents is closed, electrode is connected into adjustable DC power supply, using adjustable DC power supply by voltage from V1=0.1V starts, by daily
0.1V amplification is incrementally increased to V2=0.5~1.5V；Then the mixed liquid recycle ratio is controlled to be while it is V2 to keep voltage
300%th, return sludge ratio is that 50%, hydraulic detention time is 9h, runs bio-electrochemical reactor system, completes azo dyes
The processing of composite pollution waste water.
The reaction unit and method of wastewater treatment of the present invention is powered up by the way that the anaerobism section in traditional anaerobic-aerobic disposal is outer
Pressure, which is stimulated, promotes micro-reduction, COD in the waste water of composite pollution containing azo dyes, inorganic nitrogen and azo dyes is synchronously removed.
On the basis of biological reducing method, by inputting the extra electric field of very little, extra reducing power is provided for microorganism, micro- life is stimulated
The extracellular electron transmission efficiency of thing, to reach that enhancement microbiological reduces azo dyes, realizes quick reduction and the ore deposit of azo dyes
The purpose of change.The present invention is coupled using traditional anaerobic-aerobic disposal with bioelectrochemical system to be promoted to mix dirty containing azo dyes
The treatment effect of waste water is contaminated, it is necessary to two processes：(1) microculture is tamed；(2) extra electric field is stimulated.Extra electric field is pierced
The degradation efficiency for swashing lower anaerobic-aerobic disposal carries out quantitative and qualitative analysis, realizes and synchronously removes COD, inorganic nitrogen and azo dyes.
The method applied in the present invention respectively reaches 90%, 88%, 87% to the clearance of water outlet COD, inorganic nitrogen and azo dyes,
Relative to traditional physics, chemistry, bioremediation, with efficiency high, energy consumption is low, be produced on a large scale the characteristics of.For solution
Certainly the waste water handling problem of composite pollution containing azo dyes is provided a method that in sewage disposal.
Brief description of the drawings
Fig. 1 is the schematic diagram of the bio-electrochemical reactor system of the present invention, wherein 1 is reactor shell, 2 be dividing plate, 3
It is the first reflux pump for second pond, 4,5 be the second reflux pump, and 6 be adjustable DC power supply；1-1 is that anaerobic pond, 1-1-1 are stirring
Device, 1-1-2 is electrode；1-1-3 is water inlet, and 1-1-4 is nitrification liquid refluxing opening, and 1-1-5 is sludge reflux mouthful；1-2 is aerobic
Pond, 1-2-1 are aerator, and 1-2-2 exports for nitrification liquid, and 1-2-3 is delivery port；2-1 is water hole；3-1 is water inlet, 3-
2 be gap, and 3-3 is discharge pipeline；
Fig. 2 is the clearance situation of change of sewage index in testing 1 in additional 1.5V voltages；
When Fig. 3 is access failure power supply in contrast test 1, the clearance situation of change of sewage index.
Fig. 4 is COD, inorganic nitrogen, the comparison diagram of azo dyes removal effect after being handled through experiment 1 and contrast test 1；
Embodiment
Embodiment one：The utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit of present embodiment removes azo
The method of dyestuff composite pollution waste water is carried out according to the following steps：
First, bio-electrochemical reactor system is built：Bio-electrochemical reactor system is by reactor shell 1, dividing plate
2nd, second pond 3, the first reflux pump 4, the second reflux pump 5 and adjustable DC power supply 6 are constituted；Housing 1 is divided into anaerobic pond 1- by dividing plate 2
1st, Aerobic Pond 1-2；Water hole 2-1 is arranged at the bottom of dividing plate 2；Agitator 1-1-1 and a pair of electrodes 1-1- are provided with anaerobic pond 1-1
2；Electrode 1-1-2 is connected with adjustable DC power supply 6；Anaerobic pond 1-1 side side wall lower ends set water inlet 1-1-3 and nitrification liquid
Refluxing opening 1-1-4, upper end set sludge reflux mouthful 1-1-5；Aerator 1-2-1 is set in Aerobic Pond 1-2；In Aerobic Pond 1-
2 side side wall lower ends set nitrification liquid to export 1-2-2, and upper end sets delivery port 1-2-3；The upper end of second pond 3 sets water inlet 3-1
With gap 3-2, discharge pipeline 3-3 is connected with lower end；First reflux pump 4 is arranged on Aerobic Pond 1-2 nitrification liquids outlet 1-2-2 and detested
On pipeline between the 1-1 nitrification liquid refluxing openings 1-1-4 of oxygen pond；Second reflux pump 5 is arranged on the discharge pipeline 3-3 of second pond 3 and detested
On pipeline between oxygen pond 1-1 sludge refluxes mouthful 1-1-5；
2nd, the culturing sludge of bio-electrochemical reactor system and domestication：
A, it is that 1.0g/L, the concentration of alizarin yellow R are 0.04g/L, NH by the concentration of glucose4Cl concentration be 0.04g/L,
KNO3Concentration be that 0.07g/L, the concentration of vitamin liquid are that the ratio that 0.5ml/L, the concentration of mineral element liquid are 0.1ml/L is matched somebody with somebody
System domestication water distribution, then by domestication water distribution and activated sludge volume ratio be 1：(9~10) will tame water distribution and be added with activated sludge
Into reactor shell 1, anaerobic pond 1-1 is added into cover plate for sealing, turn on agitator 1-1-1, by aerator 1-2-1 to aerobic
24~26h of aeration in the 1-2 of pond；
B, domestication water distribution is passed through in anaerobic pond 1-1 through water inlet 1-1-3, then enters Aerobic Pond by water hole 2-1
In 1-2, the liquid of Aerobic Pond 1-2 bottoms exports 1-2-2, the first reflux pump 4 through nitrification liquid and is back in anaerobic pond 1-1；From good
The water of oxygen pond 1-2 delivery ports 1-2-3 outflows enters second pond 3, after precipitation, and clear water flows out from gap 3-2, partial sludge warp
Second reflux pump 5 is back in anaerobic pond 1, and excess sludge is discharged from discharge pipeline 3-3；Run time is 7~10 days；In the runtime
Between, nitrification liquid backflow volume ratio is gradually reduced to 300% from 400%~500%, and sludge reflux volume ratio is from 100%~120%
Gradually reduce to 50%, hydraulic detention time is gradually reduced to 9h from 20~24h；
C, holding mixed liquid recycle ratio are that 300%, return sludge ratio is that 50%, hydraulic detention time is 9h constant, will be tamed and dociled
The concentration for changing alizarin yellow R in water distribution is gradually increased by 0.005~0.01g/L of daily increase speed, until the concentration of alizarin yellow R
Reach 0.1g/L；
D, the mixed liquid recycle ratio of holding bio-electrochemical reactor system are that 300%, return sludge ratio is 50%, waterpower
Residence time is that 9h, the concentration of alizarin yellow R are 0.1g/L constant, the COD and alizarin yellow R concentration of METHOD FOR CONTINUOUS DETERMINATION water outlet, works as water outlet
COD and alizarin yellow R concentration reach stabilization, complete reactor start-up；
3rd, the operation of bio-electrochemical reactor system：
Domestication water distribution in the bio-electrochemical reactor system for completing startup is substituted for into pending azo dyes to mix
Pollutant effluents is closed, electrode 1-1-2 is connected into dc source 6, using adjustable DC power supply by voltage from V1=0.1V starts, by every
Its 0.1V amplification is incrementally increased to V2=0.5~1.5V；Then it is V keeping voltage2While control the mixed liquid recycle ratio to be
300%th, return sludge ratio is that 50%, hydraulic detention time is 9h, runs bio-electrochemical reactor system, completes azo dyes
The processing of composite pollution waste water.
Embodiment two：Present embodiment and wherein vitamin in step 2 a unlike embodiment one
Liquid is by biotin 2.0mg, folic acid 2.0mg, puridoxine hydrochloride 10.0mg, thiamine 5.0mg, riboflavin 5.0mg, nicotinic acid
5.0mg, D-VB5 calcium 5.0mg, vitamin B12 0.1mg, p-aminobenzoic acid 5.0mg, lipoic acid 5.0mg and 1L distilled water are mixed
The solution closed；It is other identical with embodiment one.
Embodiment three：Present embodiment and mineral member in step 2 a unlike embodiment one or two
Plain liquid is by NTA 1.5g, MgSO4·7H2O 3.0g、MnSO4·H2O 0.5g、NaCl 1.0g、FeSO4·
7H2O0.1g、CoCl2·6H2O 0.1g、CaCl2 0.1g、ZnSO4·7H2O 0.1g、CuSO4·5H2O 0.01g、AlK
(SO4)2·12H2O 0.01g、H3BO3 0.01g、Na2MoO4·2H2The solution that O 0.01g and 1L distilled water is mixed；It is other
It is identical with embodiment one or two.
Embodiment four：Nitre in step 2 b unlike one of present embodiment and embodiment one to three
Change liquid backflow volume than reduction speed be daily reduction by 10%~29%；Other phases one of with embodiment one to three
Together.
Embodiment five：It is dirty in step 2 b unlike one of present embodiment and embodiment one to four
Mud backflow volume than reduction speed be by daily reduction by 5%~10%；It is other identical with one of embodiment one to four.
Embodiment six：Step 2 b reclaimed waters unlike one of present embodiment and embodiment one to five
The reduction speed of power residence time is daily reduction 1.1h~2.2h；It is other identical with one of embodiment one to five.
Embodiment seven：COD in step 2 d unlike one of present embodiment and embodiment one to six
Concentration reach that the stable rate of change for referring to COD clearance within continuous three days is less than 2%；Other and embodiment one
It is identical to one of six.
Embodiment eight：It is alizarin in step 2 d unlike one of present embodiment and embodiment one to seven
Plain Huang R concentration reaches that the stable rate of change for referring to the clearance of alizarin yellow R within continuous three days is less than 2%；It is other with it is specific
One of embodiment one to seven is identical.
With following verification experimental verification beneficial effects of the present invention：
Experiment 1：It is dirty that the utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit of present embodiment removes azo dyes mixing
The method of dye waste water is carried out according to the following steps：
First, bio-electrochemical reactor system is built：Bio-electrochemical reactor system is by reactor shell 1, dividing plate
2nd, second pond 3, the first reflux pump 4, the second reflux pump 5 and adjustable DC power supply 6 are constituted；Wherein reactor shell 1 is cuboid
Structure, dischargeable capacity 24L, is made by pmma material；Housing 1 is divided into anaerobic pond 1-1, Aerobic Pond 1-2 by dividing plate 2；
Water hole 2-1 is arranged at the bottom of dividing plate 2；Agitator 1-1-1 and a pair of electrodes 1-1-2 are provided with anaerobic pond 1-1；Electrode 1-1-2
It is connected by titanium silk with dc source 6；Titanium electrode silk and carbon brush are made, wherein a diameter of Φ 10cm of bristle part, and length is
12cm；Adjustable DC power supply 1-30v voltages are adjustable；Anaerobic pond 1-1 side side wall lower ends set water inlet 1-1-3 and nitrification liquid
Refluxing opening 1-1-4, upper end set sludge reflux mouthful 1-1-5；Aeration head 1-2-1, aeration head 1-2-1 are set in Aerobic Pond 1-2
It is connected with aeration pump；In Aerobic Pond 1-2 sides, side wall lower ends set nitrification liquid to export 1-2-2, and upper end sets delivery port 1-2-3；
The upper end of second pond 3 sets water inlet 3-1 and gap 3-2, and discharge pipeline 3-3 is connected with lower end；First reflux pump 4 is arranged on aerobic
On pipeline between pond 1-2 nitrification liquids outlet 1-2-2 and anaerobic pond 1-1 nitrification liquid refluxing openings 1-1-4；Second reflux pump 5 is set
On pipeline between discharge pipeline 3-3 and anaerobic pond 1-1 sludge reflux mouthful 1-1-5 of second pond 3；
2nd, the culturing sludge of bio-electrochemical reactor system and domestication：
A, it is that 1.0g/L, the concentration of alizarin yellow R are 0.04g/L, NH by the concentration of glucose4Cl concentration be 0.04g/L,
KNO3Concentration be that 0.07g/L, the concentration of vitamin liquid are that the ratio that 0.5ml/L, the concentration of mineral element liquid are 0.1ml/L is matched somebody with somebody
System domestication water distribution, then by domestication water distribution and activated sludge volume ratio be 1：Domestication water distribution and activated sludge are added to reaction by 10
In device housing 1, anaerobic pond 1-1 is added into cover plate for sealing, turn on agitator 1-1-1, by aerator 1-2-1 to Aerobic Pond 1-2
Interior aeration 24h；Wherein vitamin liquid is by biotin 2.0mg, folic acid 2.0mg, puridoxine hydrochloride 10.0mg, thiamine
5.0mg, riboflavin 5.0mg, nicotinic acid 5.0mg, D-VB5 calcium 5.0mg, vitamin B12 0.1mg, p-aminobenzoic acid 5.0mg,
The solution that lipoic acid 5.0mg and 1L distilled water is mixed；Mineral element liquid is by NTA 1.5g, MgSO4·7H2O
3.0g、MnSO4·H2O 0.5g、NaCl 1.0g、FeSO4·7H2O0.1g、CoCl2·6H2O 0.1g、CaCl2 0.1g、
ZnSO4·7H2O 0.1g、CuSO4·5H2O 0.01g、AlK(SO4)2·12H2O 0.01g、H3BO3 0.01g、Na2MoO4·
2H2The mixed solution of O 0.01g and 1L distilled water.
B, domestication water distribution is passed through in anaerobic pond 1-1 through water inlet 1-1-3, then enters Aerobic Pond by water hole 2-1
In 1-2, the liquid of Aerobic Pond 1-2 bottoms exports 1-2-2, the first reflux pump 4 through nitrification liquid and is back in anaerobic pond 1-1；From good
The water of oxygen pond 1-2 delivery ports 1-2-3 outflows enters second pond 3, after precipitation, and clear water flows out from gap 3-2, partial sludge warp
Second reflux pump 5 is back in anaerobic pond 1, and excess sludge is discharged from discharge pipeline 3-3；Run time is 7 days；During running,
Nitrification liquid backflow volume from 500% by the speed of daily reduction by 28.6% than being down to 300%, and sludge reflux volume ratio is from 100%
50% is down to by the speed of daily reduction by 7.1%, hydraulic detention time is down to 9h from 20h by daily reduction 1.6h speed；
C, holding mixed liquid recycle ratio are that 300%, return sludge ratio is that 50%, hydraulic detention time is 9h constant, will be tamed and dociled
The concentration of alizarin yellow R is gradually increased to the concentration of alizarin yellow R by daily increase 0.01g/L speed in change water distribution reaches 0.1g/
L；
D, the mixed liquid recycle ratio of holding bio-electrochemical reactor system are that 300%, return sludge ratio is 50%, waterpower
Residence time is that 9h, the concentration of alizarin yellow R are 0.1g/L constant, the COD and alizarin yellow R concentration of METHOD FOR CONTINUOUS DETERMINATION water outlet, works as water outlet
COD and alizarin yellow R concentration reach continuous three days change be less than 1%, it is believed that electrochemical reactor system reach stabilization,
Complete reactor start-up；
3rd, the operation of bio-electrochemical reactor system：
Domestication water distribution in the bio-electrochemical reactor system for completing startup is substituted for into pending azo dyes to mix
Pollutant effluents is closed, electrode 1-1-2 is connected into dc source 6, using the adjustable DC power supply on loop by voltage from V1=0.1V
Start, incrementally increased by daily 0.1V amplification to V2=0.5,1.0 or 1.5V；Then it is V keeping voltage2While control
Mixed liquid recycle ratio is that 300%, return sludge ratio is that 50%, hydraulic detention time is 9, operation bio-electrochemical reactor system
System, completes the processing of azo dyes composite pollution waste water.The COD of wherein pending azo dyes composite pollution waste water concentration
For 1050-1100mg/L, the concentration of nitrate nitrogen is 24.6-25.3mg/L, and the concentration of ammoniacal nitrogen is 25.5-26.5mg/L, alizarin
Yellow R concentration is 39.9-40.7mg/L.
V in the step of testing 1 three2The COD of azo dyes composite pollution waste water after being handled under the conditions of=1.5V, nitre state
The clearance of nitrogen, ammoniacal nitrogen and azo dyes as shown in Fig. 2 from figure 2 it can be seen that the fluctuation of early stage reactor for treatment effect compared with
Greatly, start detection the 7th day or so treatment effect reach stable state, now reactor to COD, nitrate nitrogen, ammoniacal nitrogen and
The clearance of azo dyes respectively reaches 89%, 71%, 80% and 90%.
Contrast test 1：Contrast test and the operation of step 3 unlike experiment 1 are as follows：
3rd, the operation of bio-electrochemical reactor system：
Domestication water distribution in the bio-electrochemical reactor system for completing startup is substituted for into pending azo dyes to mix
Pollutant effluents is closed, is that 300%, return sludge ratio is that 50%, hydraulic detention time is 9 keeping mixed liquid recycle ratio, operation life
Thing electrochemical reactor system, completes the processing of azo dyes composite pollution waste water.Wherein pending azo dyes mixing is dirty
The concentration for contaminating the COD of waste water is 1050-1100mg/L, and the concentration of nitrate nitrogen is 24.6-25.3mg/L, and the concentration of ammoniacal nitrogen is
25.5-26.5mg/L, the concentration of alizarin yellow R is 39.9-40.7mg/L.
COD, nitrate nitrogen, ammoniacal nitrogen and the azo dyes of azo dyes composite pollution waste water after experiment 1 is handled by contrast
Clearance as shown in figure 3, from figure 3, it can be seen that early stage treatment effect fluctuate larger, the 9th day or so place of continuous monitoring
Reason effect reaches stable state, and now reactor is respectively reached to the clearance of COD, nitrate nitrogen, ammoniacal nitrogen and azo dyes
85%th, 65%, 55% and 41%.
Applied voltage V in the step of testing 1 three2For being reacted when being not powered on pressure for 0.5V, 1.0V, 1.5V and contrast test 1
Device reaches that the clearance of stable state is integrated as shown in figure 4, from fig. 4, it can be seen that examination to COD, nitrate nitrogen, ammoniacal nitrogen and AYR
Test 1 water outlet indices has lifting, wherein the lifting effect of AYR clearances the most than contrast test 1 when being not powered on pressure
Substantially.By inputting the extra electric field of very little, extra reducing power is provided for microorganism, the extracellular electron transmission effect of microorganism is stimulated
Rate, to reach that enhancement microbiological reduces azo dyes, makes quick reduction and the mineralising of azo dyes.
Claims (8)
1. the method for azo dyes composite pollution waste water, its feature are removed using electro photoluminescence anaerobic-aerobic continuous stream reaction unit
It is that this method is carried out according to the following steps：
First, bio-electrochemical reactor system is built：Bio-electrochemical reactor system is by reactor shell (1), dividing plate
(2), second pond (3), the first reflux pump (4), the second reflux pump (5) and adjustable DC power supply (6) composition；Dividing plate (2) is by housing
(1) it is divided into anaerobic pond (1-1), Aerobic Pond (1-2)；Water hole (2-1) is arranged at dividing plate (2) bottom；It is provided with anaerobic pond (1-1)
Agitator (1-1-1) and a pair of electrodes (1-1-2)；Electrode (1-1-2) is connected with adjustable DC power supply (6)；Anaerobic pond (1-1)
Side side wall lower ends set water inlet (1-1-3) to set sludge reflux mouthful (1-1-5) with nitrification liquid refluxing opening (1-1-4), upper end；
Aerator 1-2-1 is set in Aerobic Pond (1-2)；In Aerobic Pond (1-2) side, side wall lower ends set nitrification liquid to export (1-2-
2), upper end sets delivery port (1-2-3)；Second pond (3) upper end sets water inlet (3-1) and gap (3-2), is connected with lower end
Discharge pipeline (3-3)；First reflux pump (4) is arranged on Aerobic Pond (1-2) nitrification liquid outlet (1-2-2) and anaerobic pond (1-1) nitrification
On pipeline between liquid refluxing opening (1-1-4)；Second reflux pump (5) is arranged on the discharge pipeline (3-3) and anaerobic pond of second pond (3)
On pipeline between (1-1) sludge reflux mouthful (1-1-5)；
2nd, the culturing sludge of bio-electrochemical reactor system and domestication：
A, it is that 1.0g/L, the concentration of alizarin yellow R are 0.04g/L, NH by the concentration of glucose4Cl concentration is 0.04g/L, KNO3
Concentration be that 0.07g/L, the concentration of vitamin liquid are that the proportions that 0.5ml/L, the concentration of mineral element liquid are 0.1ml/L are tamed and dociled
Change water distribution, then by domestication water distribution and activated sludge volume ratio be 1：(9~10) are added to water distribution is tamed instead with activated sludge
Answer in device housing (1), by anaerobic pond (1-1) plus cover plate for sealing, turn on agitator (1-1-1) is become better by aerator 1-2-1
24~26h of aeration in oxygen pond (1-2)；
B, will domestication water distribution be passed through through water inlet (1-1-3) in anaerobic pond (1-1), then by water hole (2-1) enter it is aerobic
In pond (1-2), the liquid of Aerobic Pond (1-2) bottom exports (1-2-2), the first reflux pump (4) through nitrification liquid and is back to anaerobic pond
In (1-1)；The water flowed out from Aerobic Pond (1-2) delivery port (1-2-3) enters second pond (3), and after precipitation, clear water is from gap
(3-2) is flowed out, and partial sludge is back in anaerobic pond 1 through the second reflux pump (5), and excess sludge is discharged from discharge pipeline (3-3)；Fortune
The row time is 7~10 days；During running, nitrification liquid backflow volume ratio is gradually reduced to 300%, sludge from 400%~500%
Backflow volume ratio is gradually reduced to 50% from 100%~120%, and hydraulic detention time is gradually reduced to 9h from 20~24h；
C, holding mixed liquid recycle ratio are that 300%, return sludge ratio is that 50%, hydraulic detention time is 9h constant, and domestication is matched somebody with somebody
The concentration of alizarin yellow R is gradually increased by 0.005~0.01g/L of daily increase speed in water, until the concentration of alizarin yellow R reaches
0.1g/L；
D, the mixed liquid recycle ratio of holding bio-electrochemical reactor system are that 300%, return sludge ratio is 50%, hydraulic retention
Time is that 9h, the concentration of alizarin yellow R are 0.1g/L constant, the COD and alizarin yellow R concentration of METHOD FOR CONTINUOUS DETERMINATION water outlet, as the COD of water outlet
Stabilization is reached with the concentration of alizarin yellow R, reactor start-up is completed；
3rd, the operation of bio-electrochemical reactor system：
Domestication water distribution in the bio-electrochemical reactor system for completing startup is substituted for pending azo dyes and mixes dirty
Waste water is contaminated, electrode (1-1-2) is connected into dc source (6), using adjustable DC power supply by voltage from V1=0.1V starts, by every
Its 0.1V amplification is incrementally increased to V2=0.5~1.5V；Then it is V keeping voltage2While control the mixed liquid recycle ratio to be
300%th, return sludge ratio is that 50%, hydraulic detention time is 9h, runs bio-electrochemical reactor system, completes azo dyes
The processing of composite pollution waste water.
It is dirty that 2. utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit according to claim 1 removes azo dyes mixing
Contaminate the method for waste water, it is characterised in that wherein vitamin liquid is by biotin 2.0mg, folic acid 2.0mg, hydrochloric acid in step 2 a
Pyridoxol 10.0mg, thiamine 5.0mg, riboflavin 5.0mg, nicotinic acid 5.0mg, D-VB5 calcium 5.0mg, vitamin B12 0.1mg,
The solution that p-aminobenzoic acid 5.0mg, lipoic acid 5.0mg and 1L distilled water are mixed.
3. utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit according to claim 1 or 2 removes azo dyes mixing
The method of pollutant effluents, it is characterised in that step 2 a Mineral Elements liquid is by NTA 1.5g, MgSO4·7H2O
3.0g、MnSO4·H2O 0.5g、NaCl 1.0g、FeSO4·7H2O 0.1g、CoCl2·6H2O 0.1g、CaCl2 0.1g、
ZnSO4·7H2O 0.1g、CuSO4·5H2O 0.01g、AlK(SO4)2·12H2O 0.01g、H3BO3 0.01g、Na2MoO4·
2H2The solution that O 0.01g and 1L distilled water is mixed.
4. utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit according to claim 1 or 2 removes azo dyes mixing
The method of pollutant effluents, it is characterised in that in step 2 b nitrification liquid backflow volume than reduction speed be daily reduction by 10%~
29%.
5. utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit according to claim 1 or 2 removes azo dyes mixing
The method of pollutant effluents, it is characterised in that in step 2 b the reduction speed of sludge reflux volume ratio be by daily reduction by 5%~
10%.
6. utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit according to claim 1 or 2 removes azo dyes mixing
The method of pollutant effluents, it is characterised in that the reduction speed of hydraulic detention time is daily reduction 1.1h~2.2h in step 2 b.
7. utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit according to claim 1 or 2 removes azo dyes mixing
The method of pollutant effluents, it is characterised in that COD concentration reaches the stable removal for referring to COD within continuous three days in step 2 d
The rate of change of rate is less than 2%.
8. utilization electro photoluminescence anaerobic-aerobic continuous stream reaction unit according to claim 1 or 2 removes azo dyes mixing
The method of pollutant effluents, it is characterised in that the concentration of alizarin yellow R reaches that stabilization refers to alizarin yellow within continuous three days in step 2 d
The rate of change of R clearance is less than 2%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710474021.0A CN107082485B (en) | 2017-06-21 | 2017-06-21 | Method for removing azo dye mixed polluted wastewater by using bioelectrochemical reactor system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710474021.0A CN107082485B (en) | 2017-06-21 | 2017-06-21 | Method for removing azo dye mixed polluted wastewater by using bioelectrochemical reactor system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107082485A true CN107082485A (en) | 2017-08-22 |
| CN107082485B CN107082485B (en) | 2020-05-12 |
Family
ID=59607080
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710474021.0A Active CN107082485B (en) | 2017-06-21 | 2017-06-21 | Method for removing azo dye mixed polluted wastewater by using bioelectrochemical reactor system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107082485B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112010420A (en) * | 2020-08-11 | 2020-12-01 | 盐城工学院 | Electrochemical biological accelerated treatment reaction device for azo dye wastewater |
| CN112142267A (en) * | 2020-10-09 | 2020-12-29 | 哈尔滨工业大学 | Anaerobic bioelectrochemistry-aerobic moving bed biofilm integrated wastewater treatment device and wastewater treatment method thereof |
| CN113003703A (en) * | 2021-03-16 | 2021-06-22 | 南京理工大学 | Device and method for treating nitrogen-containing heterocyclic compound wastewater |
| CN113651414A (en) * | 2021-08-12 | 2021-11-16 | 同济大学 | Electrically-promoted bioreactor for organic wastewater treatment in semiconductor industry and use method thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102491516A (en) * | 2011-11-25 | 2012-06-13 | 天津工业大学 | Method for treating wastewater difficult to be biodegraded by electric microorganism and membrane filtration coupled technology |
| CN104817175A (en) * | 2015-04-29 | 2015-08-05 | 深圳北航新兴产业技术研究院 | Method for reinforcing sewage denitrification and dephosphorization efficiency and simultaneously generating electricity |
| US20150299014A1 (en) * | 2014-04-20 | 2015-10-22 | Paul Q. McLaine | Non-Chemical Water Treatment Apparatus and System |
| CN205740503U (en) * | 2016-04-12 | 2016-11-30 | 沈阳建筑大学建筑设计研究院 | An O processes the product electric installation of sewage |
| CN106565015A (en) * | 2015-10-13 | 2017-04-19 | 内蒙古天环境技术有限公司 | Integrated biofilm reaction system |
-
2017
- 2017-06-21 CN CN201710474021.0A patent/CN107082485B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102491516A (en) * | 2011-11-25 | 2012-06-13 | 天津工业大学 | Method for treating wastewater difficult to be biodegraded by electric microorganism and membrane filtration coupled technology |
| US20150299014A1 (en) * | 2014-04-20 | 2015-10-22 | Paul Q. McLaine | Non-Chemical Water Treatment Apparatus and System |
| CN104817175A (en) * | 2015-04-29 | 2015-08-05 | 深圳北航新兴产业技术研究院 | Method for reinforcing sewage denitrification and dephosphorization efficiency and simultaneously generating electricity |
| CN106565015A (en) * | 2015-10-13 | 2017-04-19 | 内蒙古天环境技术有限公司 | Integrated biofilm reaction system |
| CN205740503U (en) * | 2016-04-12 | 2016-11-30 | 沈阳建筑大学建筑设计研究院 | An O processes the product electric installation of sewage |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112010420A (en) * | 2020-08-11 | 2020-12-01 | 盐城工学院 | Electrochemical biological accelerated treatment reaction device for azo dye wastewater |
| CN112142267A (en) * | 2020-10-09 | 2020-12-29 | 哈尔滨工业大学 | Anaerobic bioelectrochemistry-aerobic moving bed biofilm integrated wastewater treatment device and wastewater treatment method thereof |
| CN113003703A (en) * | 2021-03-16 | 2021-06-22 | 南京理工大学 | Device and method for treating nitrogen-containing heterocyclic compound wastewater |
| CN113651414A (en) * | 2021-08-12 | 2021-11-16 | 同济大学 | Electrically-promoted bioreactor for organic wastewater treatment in semiconductor industry and use method thereof |
| CN113651414B (en) * | 2021-08-12 | 2022-09-16 | 同济大学 | Electrically-promoted bioreactor for organic wastewater treatment in semiconductor industry and use method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107082485B (en) | 2020-05-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107082485A (en) | The method that azo dyes composite pollution waste water is removed using bio-electrochemical reactor system | |
| CN104761097B (en) | It is a kind of suitable for high concentration, the processing method of organic wastewater with difficult degradation thereby total nitrogen | |
| CN100526233C (en) | Anerobic ammoxidation and denitrification synergistic denitrification method for garbage leachate | |
| Brito et al. | Feasibility of a pulsed sequencing batch reactor with anaerobic aggregated biomass for the treatment of low strength wastewaters | |
| CN104944689B (en) | Device for treating high ammonia-nitrogen wastewater and method thereof | |
| CN101734792B (en) | System and method for treating waste water and sewage containing sulfate radicals | |
| CN106115915A (en) | Low C/N is than the apparatus and method of city domestic sewage short-cut denitrification/short distance nitration Anammox biomembrane process | |
| CN106565017A (en) | Bicirculating nitrogen and phosphorus removal wastewater treatment system and method | |
| CN101428946A (en) | Integrated treatment process and equipment for domestic wastewater | |
| US11827550B2 (en) | Simultaneous nitrification/denitrification (SNDN) in sequencing batch reactor applications | |
| CN104211252B (en) | Percolate short-cut nitrification and denitrification denitrification process | |
| CN107162339A (en) | Return flow technique | |
| CN207016557U (en) | A kind of high concentration methacrylic acid wastewater processing system up to standard | |
| CN101386445A (en) | Water pump-driving baffling internal circulation bioreactor and use method thereof | |
| CN105967435A (en) | Double-circulation nitrogen and phosphorus removal wastewater treatment system and process | |
| CN107381967A (en) | The processing unit and method of high ammonia nitrogen coking chemical waste water | |
| CN104649518B (en) | Device and method for treating ammonium nitrate wastewater by biological method | |
| CN104163494A (en) | Autotrophic nitrogen removal device for landfill leachate, and running method | |
| CN101386446B (en) | Air-lift baffling internal circulation bioreactor and use method thereof | |
| CN107129037B (en) | Method for quickly starting anaerobic ammonia oxidation coupling denitrification synergistic denitrification reactor | |
| CN105254115B (en) | A kind of processing method of high salt organic pigment production waste water | |
| CN107129119A (en) | A kind of biochemical treatment apparatus and technique for realizing high CO_2 density | |
| CN207361952U (en) | A kind of iron carbon catalyst oxidation reactor | |
| CN205710299U (en) | A kind of flow-type film mud coupling pond type denitrogenation dephosphorizing wastewater treatment equipment | |
| CN201971700U (en) | Buried sewage treatment equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |