CN103319002A - Method for biological treatment of sulfate wastewater employing synchronous electric catalysis of anode and cathode - Google Patents
Method for biological treatment of sulfate wastewater employing synchronous electric catalysis of anode and cathode Download PDFInfo
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- CN103319002A CN103319002A CN2013102634505A CN201310263450A CN103319002A CN 103319002 A CN103319002 A CN 103319002A CN 2013102634505 A CN2013102634505 A CN 2013102634505A CN 201310263450 A CN201310263450 A CN 201310263450A CN 103319002 A CN103319002 A CN 103319002A
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Abstract
The invention provides a method for biological treatment of sulfate wastewater employing synchronous electric catalysis of an anode and a cathode. The method comprises the following concrete steps of: (1) building an electric catalytic bioreactor, which includes a cathode reaction zone, a buffer zone and an anode reaction zone; (2) inoculating mixed bacteria of sulfate reducing bacteria inside the cathode reaction zone, leading to a culture medium, electrifying and acclimatizing, and cultivating for 3-5 days at 28-34 DEG C, so as to achieve cathode hanging membrane of the sulfate reducing bacteria; (3) inoculating sulfur-oxidizing bacteria inside the anode reaction zone, leading to the culture medium to cultivate for 5-7 days at 25-30 DEG C; and (4) starting a reactor, leading the sulfate wastewater to the cathode reaction zone of the reactor, and enabling the sulfate wastewater to flow out of the reactor after flowing inside the anode reaction zone through the buffer zone. By adopting the method, control of an S<2->oxidization process is achieved when the reduction speed of the sulfate reducing bacteria for reducing SO4<-2> is improved. Thus, the yield of S produced by biological metabolism of the wastewater is improved.
Description
Technical field
The invention belongs to technical field of waste water processing, be specifically related to utilize cathode electric field electrocatalysis Growth of Sulfate Reducing Bacteria, utilize the method for sulfate wastewater recycling treatment of the degree of oxidation of anode electric field control sulfide.
Background technology
Along with the development of industrial or agricultural, the fields such as chemical industry, pharmacy, process hides, papermaking, fermentation, food-processing and mining give off the trade effluent that contains in a large number high concentration sulfate in process of production, and ecotope and HUMAN HEALTH have been caused great harm.Technology for Microbial Desulfurization take sulphate reducing bacteria (SRB) as main body is the Pollution abatement technology that development in recent years is got up, through years of researches, biological desulfurizing technology has been obtained very much progress, but still exist some problems not yet to solve, form biological desulfurizing technology and enter the bottleneck of industrialization.These problems mainly comprise:
1, SO
4 2-Rate of reduction is not high
In theory, utilize sulphate reducing bacteria to reduce SO
4 2-Speed can reach 42.5kgSO
4 2-/ m
3D, but in the actual process of sulfate wastewater, SO
4 2-Reduction rate be usually less than 15kg SO
4 2-/ m
3D, this excessively low SO
4 2-The reduction processing speed directly causes the expansion for the treatment of unit, has greatly increased the cost of investment of biological desulfurization process, has had a strong impact on the industrialization promotion process of this technology.
2, S
2-The control of selective oxidation
Through SO
4 2-The S that biological reducing generates
2-, in biological oxidation process, with respect to SO
4 2-Reduction process is easier to realize.Under the effect of sulfur-oxidizing bacteria and oxygen, S
2-At first can be generated S by Quick Oxidation, when dissolved oxygen was excessive in the system, S then can be further oxided into SO
4 2-In order to ensure S
2-Clearance, sufficient aeration rate need to be provided in the system.Yet excessive oxygen can make S
2-After being oxidized to S, continuing oxidation and generate SO
4 2-Control S by the aeration rate in the control reaction process
2-Degree of oxidation, although feasible in theory since waste water in S
2-The fluctuation of concentration, thus make its actual operation easier large.Therefore, seek suitable feasible S
2-The selective oxidation control method is being guaranteed S
2-In the time of clearance, how to control S
2-Degree of oxidation, guarantee S
2-Can become S by selective oxidation, and not continue to be oxidized to SO
4 2-, become S
2-The difficult point of selective oxidation processes research field.
In recent years, the application of electric biological coupling technology in wastewater treatment is more and more extensive.The electronics of negative electrode generation directly transmits or provides electron donor by electrolytic hydrogen production for the microbiological anaerobic breathing on the one hand, suitable electric field can promote the migration of mineral ion on the other hand, by changing the charge property of biofilm surface, improve biomembranous permeability, thereby promote biology growing.
CN201210091967.6 discloses a kind of method of utilizing electric field-enhanced sulphate reducing bacteria to process heavy metal.It is characterized in that sulphate reducing bacteria is grown as unique electron donor with electrode, by the bioelectrochemistry approach, is sulfide with sulfate reduction under the condition that lacks organic carbon, sulfide is applied to the processing of heavy metal wastewater thereby.
Electricity biological coupling technology is expected to become the method that the biological desulfurizing technology bottleneck is broken through.Yet present electric biological coupling technology still has a lot of problems to need to solve, and outstanding problem shows the utilization ratio aspect of electric energy.Present electric biological coupling technology substantially all is for cathode electronics, and often is not used for the electric field anode, thereby so that the utilization rate of electrical in the electrocatalysis process is not high.
Summary of the invention
For the defective of above-mentioned prior art, the object of the present invention is to provide a kind of method of electrocatalysis simple to operate biological treatment sulfate wastewater, the method can realize the continuous biological treatment of sulfate wastewater, is improving sulphate reducing bacteria reduction SO
4 2-In the time of reduction rate, realize S
2-The control of oxidising process, thus the processing efficiency of sulfate wastewater and the rate of recovery of biological S improved.
Above-mentioned purpose of the present invention is achieved through the following technical solutions:
A kind of method of anode and cathode synchronous electric catalysis sulfate wastewater biological treatment, the method comprises following concrete steps:
(1) makes up the electrocatalysis bio-reactor, comprise cathodic reaction zone, buffer zone and anodic reaction district;
(2) the inoculation sulphate reducing bacteria is that master, facultative anaerobe are auxiliary mixed bacterial in cathodic reaction zone, passes into substratum, the energising domestication, and culture temperature is 28～34 ℃, incubation time is 3～5 days, realizes sulphate reducing bacteria negative electrode biofilm and activation;
(3) in the activation of microorganism, inoculate the aerobic flora that sulfur oxidizing bacterium is the master in the anode reaction zone in cathodic reaction zone, pass into substratum, culture temperature is 25～30 ℃, and incubation time is 5～7 days;
(4) start reactor, sulfate wastewater is passed into the reactor cathodic reaction zone, after buffer zone flows into the anodic reaction district, outflow reactor.
In described step (1):
Described cathodic reaction zone is the anaerobic reaction district, and described anodic reaction district is little oxygen reaction zone;
Described structure electrocatalysis bio-reactor also is included in the anodic reaction district reference electrode is installed, and preferably, described reference electrode is mercurous chloride electrode;
Described cathodic reaction zone and anodic reaction district volume ratio are 7～8:1;
Described cathodic reaction zone top seal, described anode reactor open-top;
Described buffer zone bottom is provided with mud discharging mouth, and described anode reactor bottom is provided with sulfur outlet.
In described step (2):
The described step that passes into substratum behind buffer zone, is discharged reactor for substratum is passed into the reactor cathodic reaction zone continuously;
Described energising is tamed step for anode electrode is inserted buffer zone, and begins the energising domestication, and described energising is domesticated for the direct current that passes into 100～300mV, preferred 150mV direct current;
In described step (3):
The described step that passes into substratum is for intermittently to add reactor anodic reaction district with substratum, and every 6h changes a subculture, and each replaced medium volume is 70% of anodic reaction district volume;
In described step (2), described substratum adopts the ultrapure water configuration, and composition is in the substratum: by KH
2PO
40.5g/L, NH
4Cl1g/L, CaCl
20.06g/L, Na
2SO
41.5g/L, FeSO
47H
2O0.007g/L, micro-1ml/L;
In described step (3), described substratum adopts the ultrapure water configuration, and composition is in the substratum: KH
2PO
42g/L, NH
4Cl0.4g/L, K
2HPO
42g/L, Na
2S
2O
35g/L, MgSO
47H
2O0.8g, micro-1ml/L;
Described trace element adopts the ultrapure water configuration, and composition is in the trace element solution: FeCl
24H
2O1.5g/L, MnCl
24H
2O0.1g/L, ZnCl
20.07g/L, H
3BO
30.062g/L, Na
2MoO
42H
2O0.036g/L, NiCl
26H
2O0.024g/L, CuCl
22H
2O0.017g/L, EDTA0.5g/L, 37%HCl8.33ml/L;
In described step (4):
Described sulfate wastewater is 12～15h in the cathodic reaction zone residence time, preferred 15h;
Described cathodic reaction zone temperature is 28～34 ℃, preferred 32 ℃;
Described sulfate wastewater is 1.5～2.5h in the anodic reaction district residence time, preferred 2h;
Described anodic reaction district temperature is 25～30 ℃, preferred 30 ℃;
Described anodic reaction region electrode potential range is 50～150mv, preferred 100mv.
In aforesaid method, described waste water is selected from one or more in pharmacy waste water, mine wastewater, gourmet powder waste water or the electroplating wastewater.
The present invention adopts the steps of processing sulfate wastewater:
(1) makes up anode and cathode synchronous electric catalysis biological reactor, comprise cathodic reaction zone, buffer zone and anodic reaction district, the cathodic reaction zone of reactor is the anaerobic reaction district, the anodic reaction district is little oxygen reaction zone, mercurous chloride electrode is installed as reference electrode in the anodic reaction district, in the reaction zone bottom microporous aeration device is installed;
(2) before reactor start-up, in the reactor cathodic reaction zone, the inoculation sulphate reducing bacteria is that master, facultative anaerobe are auxiliary mixed strains;
(3) the configuration sulfate reduction bacteria culture medium enters the reactor cathodic reaction zone continuously with substratum, directly discharges reactor through buffer zone;
(4) energising domestication cathodic reaction zone microorganism is finished the biofilm of sulphate reducing bacteria on cathode electrode; Energising voltage is the direct current of 100～300mV;
(5) in reactor anodic reaction district, the inoculation sulfur-oxidizing bacteria;
(6) configuration sulfur oxidizing bacterium substratum intermittently adds the anodic reaction district, activation anodic reaction district microorganism;
(7) reactor negative and positive reaction zone activation complete after, sulfate wastewater is passed into reactor electric field cathodic reaction zone continuously, be 12～15h in the residence time of cathodic reaction zone, reaction zone temperature is controlled at 28～34 ℃;
(8) waste water after the cathode electric field enhanced biological is processed enters the anodic reaction district through buffer zone, and the anodic reaction district residence time is 1.5～2.5h, and reaction zone control temperature is 25～30 ℃, and reaction zone anode electrode control of Electric potentials is between 50～150mv;
(9) in the anodic reaction district, S in the anode potential control waste water
2-Oxidising process, the waste water after the anodic reaction district processes, its medium sulphide content is converted into elemental sulfur, elemental sulfur is finished the processing of waste water with the waste water outflow reactor after processing.
The advantage that adopts present method to process sulfate wastewater is:
(1) adopts cathode electric field to strengthen biological sulphate reduction, not only improve sulphate reducing bacteria reduction SO
4 2-Speed can reduce the consumption of electron donor in the waste water simultaneously;
(2) utilize anode potential to realize S
2-The control of oxidising process;
(3) with SO
4 2-Reduction process and S
2-Oxidising process in a reaction system, realize;
(4) adopting the method to process the sulfate wastewater process is continuous operational process.
Description of drawings
Fig. 1 anode and cathode synchronous electric biological coupling sulfur-containing wastewater treatment device schematic diagram
1. reactor water-in; 2. cathodic reaction zone; 3. cathode electrode; 4. anaerobion (take SRB as main); 5. buffer zone; 6. anodic reaction district; 7. anode electrode; 8. reference electrode; 9. anode water proof weir; 10. reactor water outlet; 11. direct supply; 12. aerobic microbiological (take SOB as main)
Embodiment
Referring to accompanying drawing and specific embodiment the present invention is described.It will be appreciated by those skilled in the art that these embodiment only are used for explanation the present invention, the scope that it does not limit the present invention in any way.
Experimental technique among the following embodiment if no special instructions, is ordinary method.Used raw material, reagent etc. if no special instructions, are commercially available purchase product among the following embodiment.
The electrocatalysis bioreactor construction that the present invention is constructed such as accompanying drawing 1, this device comprise successively adjacent and the cathodic reaction zone, buffer zone and the anodic reaction district that are interconnected.The sulfur-containing waste water of processing enter cathodic reaction zone (2) from reactor water-in (1) continuously.Sulfur-containing waste water in cathodic reaction zone under the effect of cathode electric field (3) and the anaerobion take sulphate reducing bacteria as main body (4), the high price SO in the waste water
x 2-Be reduced to S
2-Waste water after cathodic reaction zone is processed enters anodic reaction district (6) through buffer zone (5).Waste water in the anodic reaction district under the effect of anode electric field (7) and the aerobic microbiological take sulfur oxidizing bacterium as main body (12), the S in the waste water
2-Be oxidized into S.In the anodic reaction district, pass through reference electrode (8) monitor anode electropotential.Be provided with water proof weir (9) in the anodic reaction district, to guarantee waste water enough residence time and the direct outflow reactor of short flow phenomenon can not occur in the anodic reaction district.The waste water of processing through the anodic reaction district is discharged reactor through the bottom of water proof weir (9) from reactor water outlet (10), finishes the processing of waste water.
Embodiment 1
The present embodiment is to utilize the electrocatalysis biological reaction apparatus to process the process of 7-ACA pharmacy waste water.
Handled 7-ACA pharmacy waste water characteristic is as follows:
Wastewater pH: 8.02～8.29, SO
4 2-: 1800～3200mg/L, COD:6000～8000mg/L, NH
4-N:700～800mg/L.
Process the step of 7-ACA pharmacy waste water:
(1) waste water is before entering continuously the electrocatalysis bio-reactor, microbe inoculation in reactor cathodic reaction zone and the anodic reaction district respectively, simultaneously and independently the microorganism in the electric field anode and cathode reaction zone is activated.Cathodic reaction zone institute microbe inoculation is take desulfovibrio (Desulfovibriosp.) as main, and anodic reaction district institute microbe inoculation is take grate sulfur thiobacillus (Thiobacillus thioparus) as main;
(2) the cathodic reaction zone substratum adopts the ultrapure water configuration, and composition is in the substratum: by KH
2PO
40.5g/L, NH
4Cl1g/L, CaCl
20.06g/L, Na
2SO
41.5g/L, FeSO
47H
2O0.007g/L, micro-1ml/L;
(3) anodic reaction district substratum adopts the ultrapure water configuration, and composition is in the substratum: KH
2PO
42g/L, NH
4Cl0.4g/L, K
2HPO
42g/L, Na
2S
2O
35g/L, MgSO
47H
2O0.8g, micro-1ml/L;
(4) trace element adopts the ultrapure water configuration, and composition is in the trace element solution: FeCl
24H
2O1.5g/L, MnCl
24H
2O0.1g/L, ZnCl
20.07g/L, H
3BO
30.062g/L, Na
2MoO
42H
2O0.036g/L, NiCl
26H
2O0.024g/L, CuCl
22H
2O0.017g/L, EDTA0.5g/L, 37%HCl8.33ml/L;
(5) in the activation of microorganism process, the direct current that applies 300mv to the reactor anode and cathode domestication of switching on, cathodic reaction zone microorganism culturing acclimation temperature is 32 ℃, incubation time is 3 days; The anode electrode control of Electric potentials is at 50mv, and anodic reaction district microorganism culturing acclimation temperature is 30 ℃, and incubation time is 5 days;
(6) after anode and cathode reaction zone activation of microorganism finishes, the 7-ACA pharmacy waste water is entered the electrocatalysis bio-reactor continuously by peristaltic pump;
(7) sulfate wastewater is passed into continuously reactor electric field cathodic reaction zone, waste water is 15h in the residence time of cathodic reaction zone, and reaction zone temperature is controlled at 32 ℃;
(8) waste water of processing through the reactor cathodic reaction zone enters the anodic reaction district through buffer zone, and the anodic reaction district residence time is 2.5h, and reaction zone control temperature is 30 ℃;
(9) waste water after the anodic reaction district processes, sulfides from wastewater is converted into elemental sulfur, and elemental sulfur is finished the processing of waste water with the processed waste water outflow reactor.
(10) the salt wastewater treatment tended towards stability after reactor moved 7 days, at cathodic reaction zone, and SO in the waste water
4 2Treatment rate reach 19.5kg/m
3D, the rate of recovery of anodic reaction district S reaches 86.3%, flows out the SO of water from the anodic reaction district
4 2Concentration is lower than 80mg/L.
The present embodiment is the process of utilizing electrocatalysis biological reaction apparatus same for treating acidic mine wastewater.
To process the acidic mine waste water characteristic as follows:
Wastewater pH: 3.00～3.46, SO
4 2-: 6000～8000mg/L, COD＜100mg/L, NH
4-N:35～50mg/L.
The step of same for treating acidic mine wastewater:
(1) waste water is before entering continuously the electrocatalysis bio-reactor, microbe inoculation in reactor cathodic reaction zone and the anodic reaction district respectively, simultaneously and independently the microorganism in the electric field anode and cathode reaction zone is activated.Cathodic reaction zone institute microbe inoculation is take desulfovibrio (Desulfovibriosp.) as main, and anodic reaction district institute microbe inoculation is take grate sulfur thiobacillus (Thiobacillus thioparus) as main;
(2) the cathodic reaction zone substratum adopts the ultrapure water configuration, and composition is in the substratum: by KH
2PO
40.5g/L, NH
4Cl1g/L, CaCl
20.06g/L, Na
2SO
41.5g/L, FeSO
47H
2O0.007g/L, micro-1ml/L;
(3) anodic reaction district substratum adopts the ultrapure water configuration, and composition is in the substratum: KH
2PO
42g/L, NH
4Cl0.4g/L, K
2HPO
42g/L, Na
2S
2O
35g/L, MgSO
47H
2O0.8g, micro-1ml/L;
(4) trace element adopts the ultrapure water configuration, and composition is in the trace element solution: FeCl
24H
2O1.5g/L, MnCl
24H
2O0.1g/L, ZnCl
20.07g/L, H
3BO
30.062g/L, Na
2MoO
42H
2O0.036g/L, NiCl
26H
2O0.024g/L, CuCl
22H
2O0.017g/L, EDTA0.5g/L, 37%HCl8.33ml/L;
(5) in the activation of microorganism process, the direct current that applies 300mv to the reactor anode and cathode domestication of switching on, cathodic reaction zone microorganism culturing acclimation temperature is 28 ℃, incubation time is 5 days; The anode electrode control of Electric potentials is at 100mv, and the microorganism culturing temperature is 25 ℃, and incubation time is 7 days;
(6) after anode and cathode reaction zone activation of microorganism finishes, waste water is entered the electrocatalysis bio-reactor continuously by peristaltic pump;
(7) sulfate wastewater is passed into continuously reactor electric field cathodic reaction zone, waste water is 12h in the residence time of cathodic reaction zone, and reaction zone temperature is controlled at 28 ℃;
(8) waste water of processing through the reactor cathodic reaction zone enters the anodic reaction district through buffer zone, and the anodic reaction district residence time is 1.5h, and reaction zone control temperature is 25 ℃;
(9) because the pH of mine wastewater is lower, and the SO in the waste water
4 2-Concentration is higher, therefore, in the actual treatment waste water process, with the return of waste water after the anodic reaction district processes, and mixes with Jinsui River, improves the pH of waste water, thus the SO of reduction actual treatment sulfate wastewater
4 2-Concentration, wherein return of waste water is than being 2:1.Because mine wastewater is inorganic wastewater, need to serve as the electron donor of sulphate reducing bacteria metabolism to additional suitable organism in the waste water, additional electron donor is industrial alcohol, adds 0.4 milliliter industrial alcohol in every liter of waste water.
(10) sulfides from wastewater after above-mentioned processing is converted into elemental sulfur, and elemental sulfur is finished the processing of waste water with the processed waste water outflow reactor.
(11) answer device operation after 20 days sulfate wastewater treatment tend towards stability, at cathodic reaction zone, SO in the waste water
4 2Treatment rate reach 17.9kg/m
3D, the rate of recovery of anodic reaction district S reaches 84.4%, flows out the SO of water from the anodic reaction district
4 2Concentration is lower than 80mg/L.
The present embodiment is to utilize the electrocatalysis biological reaction apparatus to process the process of gourmet powder waste water.
To process the gourmet powder waste water characteristic as follows:
Wastewater pH: 6.5～6.8, SO
4 2-: 12000～15000mg/L, COD:10000mg/L.
Process the step of gourmet powder waste water:
(1) waste water is before entering continuously the electrocatalysis bio-reactor, microbe inoculation in reactor cathodic reaction zone and the anodic reaction district respectively, simultaneously and independently the microorganism in the electric field anode and cathode reaction zone is activated.Cathodic reaction zone institute microbe inoculation is take desulfovibrio (Desulfovibriosp.) as main, and anodic reaction district institute microbe inoculation is take grate sulfur thiobacillus (Thiobacillus thioparus) as main;
(2) the cathodic reaction zone substratum adopts the ultrapure water configuration, and composition is in the substratum: by KH
2PO
40.5g/L, NH
4Cl1g/L, CaCl
20.06g/L, Na
2SO
41.5g/L, FeSO
47H
2O0.007g/L, micro-1ml/L;
(3) anodic reaction district substratum adopts the ultrapure water configuration, and composition is in the substratum: KH
2PO
42g/L, NH
4Cl0.4g/L, K
2HPO
42g/L, Na
2S
2O
35g/L, MgSO
47H
2O0.8g, micro-1ml/L;
(4) trace element adopts the ultrapure water configuration, and composition is in the trace element solution: FeCl
24H
2O1.5g/L, MnCl
24H
2O0.1g/L, ZnCl
20.07g/L, H
3BO
30.062g/L, Na
2MoO
42H
2O0.036g/L, NiCl
26H
2O0.024g/L, CuCl
22H
2O0.017g/L, EDTA0.5g/L, 37%HCl8.33ml/L;
(5) in the activation of microorganism process, the direct current that applies 300mv to the reactor anode and cathode domestication of switching on, cathodic reaction zone microorganism culturing acclimation temperature is 34 ℃, incubation time is 3 days; The anode electrode control of Electric potentials is at 150mv, and the microorganism culturing temperature is 30 ℃, and incubation time is 5 days;
(6) after anode and cathode reaction zone activation of microorganism finishes, waste water is entered the electrocatalysis bio-reactor continuously by peristaltic pump;
(7) sulfate wastewater is passed into continuously reactor electric field cathodic reaction zone, waste water is 12h in the residence time of cathodic reaction zone, and reaction zone temperature is controlled at 34 ℃;
(8) waste water of processing through the reactor cathodic reaction zone enters the anodic reaction district through buffer zone, and the anodic reaction district residence time is 2h, and reaction zone control temperature is 30 ℃;
(9) because the SO in the gourmet powder waste water
4 2-Concentration is higher, therefore, in the actual treatment waste water process, with the return of waste water after the anodic reaction district processes, and mixes the SO of reduction actual treatment sulfate wastewater with Jinsui River
4 2-Concentration, wherein return of waste water is than being 4:1.
(10) sulfides from wastewater after above-mentioned processing is converted into elemental sulfur, and elemental sulfur is finished the processing of waste water with the processed waste water outflow reactor.
(11) answer device operation after 15 days sulfate wastewater treatment tend towards stability, at cathodic reaction zone, SO in the waste water
4 2Treatment rate reach 20.6kg/m
3D, the rate of recovery of anodic reaction district S reaches 87.4%, flows out the SO of water from the anodic reaction district
4 2Concentration is lower than 100mg/L.
In a word, above specific description of embodiments of the present invention does not limit the present invention, and those skilled in the art can make according to the present invention various changes or distortion, only otherwise break away from spirit of the present invention, all should belong to the scope of claims of the present invention.
Claims (9)
1. the method for anode and cathode synchronous electric catalysis sulfate wastewater biological treatment, the method comprises following concrete steps:
(1) makes up the electrocatalysis bio-reactor, comprise cathodic reaction zone, buffer zone and anodic reaction district;
(2) the inoculation sulphate reducing bacteria is that master, facultative anaerobe are auxiliary mixed strains in cathodic reaction zone, passes into substratum, the energising domestication, energising voltage is 100～300mV direct current, culture temperature is 28～34 ℃, and incubation time is 3～5 days, realizes sulphate reducing bacteria negative electrode biofilm;
(3) inoculate sulfur-oxidizing bacteria in the anodic reaction district, intermittently add substratum, culture temperature is 25～30 ℃, and incubation time is 5～7 days;
(4) start reactor, sulfate wastewater is passed into the reactor cathodic reaction zone continuously, after buffer zone flowed into the anodic reaction district, outflow reactor was realized the continuous biological treatment of sulfate wastewater again.
2. method according to claim 1 is characterized in that, in the described step (1):
Described cathodic reaction zone is the anaerobic reaction district, and described anodic reaction district is little oxygen reaction zone;
Described structure electrocatalysis bio-reactor also is included in the anodic reaction district reference electrode is installed, and preferably, described reference electrode is mercurous chloride electrode;
Microporous aeration device is installed in the bottom by described anodic reaction district;
Described cathodic reaction zone and anodic reaction district volume ratio are 7～8:1;
Described cathodic reaction zone top seal, described anode reactor open-top;
Described buffer zone bottom is provided with mud discharging mouth, and described anode reactor bottom is provided with sulfur outlet.
3. method according to claim 1 is characterized in that, in the described step (2), the described step that passes into substratum behind buffer zone, is discharged reactor for substratum is passed into the reactor cathodic reaction zone continuously;
Described energising is tamed step for anode electrode is inserted buffer zone, and begins the energising domestication, and described energising is domesticated for the direct current that passes into 100～300mV, preferred 150mV direct current.
4. method according to claim 1, it is characterized in that, in the described step (3), the described step of substratum that passes into is for intermittently to add reactor anodic reaction district with substratum, every 6h changes a subculture, and each replaced medium volume is 70% of anodic reaction district volume.
5. according to claim 1 or 3 described methods, it is characterized in that, in the described step (2), described substratum adopts the ultrapure water configuration, and composition is in the substratum: KH
2PO
40.5g/L, NH
4Cl1g/L, CaCl
20.06g/L, Na
2SO
41.5g/L, FeSO
47H
2O0.007g/L, micro-1ml/L.
6. according to claim 1 or 4 described methods, it is characterized in that, in the described step (3), described substratum adopts the ultrapure water configuration, and composition is in the substratum: KH
2PO
42g/L, NH
4Cl0.4g/L, K
2HPO
42g/L, Na
2S
2O
35g/L, MgSO
47H
2O0.8g, micro-1ml/L.
7. according to claim 5 or 6 described methods, it is characterized in that, described trace element adopts the ultrapure water configuration, and composition is in the trace element solution: FeCl
24H
2O1.5g/L, MnCl
24H
2O0.1g/L, ZnCl
20.07g/L, H
3BO
30.062g/L, Na
2MoO
42H
2O0.036g/L, NiCl
26H
2O0.024g/L, CuCl
22H
2O0.017g/L, EDTA0.5g/L, 37%HCl8.33ml/L.
8. method according to claim 1 is characterized in that, in the described step (4):
Described sulfate wastewater is 12～15h in the cathodic reaction zone residence time, preferred 15h;
Described cathodic reaction zone temperature is 28～34 ℃, preferred 32 ℃;
Described sulfate wastewater is 1.5～2.5h in the anodic reaction district residence time, preferred 2h;
Described anodic reaction district temperature is 25～30 ℃, preferred 30 ℃;
Described anodic reaction region electrode potential range is 50～150mv, preferred 100mv.
9. each described method is characterized in that according to claim 1～8, and described waste water is selected from one or more in pharmacy waste water, mine wastewater, gourmet powder waste water or the electroplating wastewater.
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| CN201310263450.5A CN103319002B (en) | 2013-06-27 | 2013-06-27 | Method for biological treatment of sulfate wastewater employing synchronous electric catalysis of anode and cathode |
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