CN103319002B - 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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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 anode electric field to control the method for the sulfate wastewater recycling treatment of the degree of oxidation of 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 a large amount of trade effluent containing high concentration sulfate in process of production, cause great harm to ecotope and HUMAN HEALTH.The pollutant abatement technology that development in recent years is got up based on the Technology for Microbial Desulfurization of sulphate reducing bacteria (SRB), through years of researches, biological desulfurizing technology has achieved very much progress, but still there are some problems and not yet solve, form the bottleneck that biological desulfurizing technology enters 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 too low SO
4 2-reduction treatment speed directly causes the expansion for the treatment of unit, considerably increases 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, relative to SO
4 2-reduction process is easier to realize.Under the effect of sulfur-oxidizing bacteria and oxygen, S
2-first can be generated S by Quick Oxidation, when in system, dissolved oxygen is excessive, S then can be further oxided into SO
4 2-.In order to ensure S
2-clearance, need to provide sufficient aeration rate in system.But excessive oxygen can make S
2-after being oxidized to S, continuing oxidation and generate SO
4 2-.By controlling the aeration rate control S in reaction process
2-degree of oxidation, although feasible in theory, due to S in waste water
2-the fluctuation of concentration, thus make its actual operation easier large.Therefore, suitable feasible S is found
2-selective oxidation control method, is guaranteeing S
2-while clearance, how control S
2-degree of oxidation, guarantee S
2-s can be become 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 in the treatment of waste water of electric biological coupling technology is more and more extensive.The electronics that on the one hand negative electrode produces directly is transmitted or to be breathed for microbiological anaerobic by electrolytic hydrogen production provides electron donor, 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, thus promote biology growing.
CN201210091967.6 discloses a kind of method utilizing electric field-enhanced sulphate reducing bacteria process heavy metal.It is characterized in that sulphate reducing bacteria grows using electrode as sole electron donor, and by bioelectrochemistry approach, be sulfide by sulfate reduction, sulfide is applied to the process of heavy metal wastewater thereby under the condition lacking organic carbon.
Electricity biological coupling technology is expected to the method becoming the breakthrough of biological desulfurizing technology bottleneck.But current electric biological coupling technology still has a lot of problem to need to solve, outstanding problem shows the utilization ratio aspect of electric energy.Current electric biological coupling technology is substantially all for cathode electronics, and is not often used for electric field anode, thus makes the utilization rate of electrical in electrocatalysis process not high.
Summary of the invention
For the defect of above-mentioned prior art, the object of the present invention is to provide the method for a kind of electrocatalysis simple to operate biological treatment sulfate wastewater, the method can realize the continuous biological treatment of sulfate wastewater, at raising sulphate reducing bacteria reduction SO
4 2-while reduction rate, realize S
2-the control of oxidising process, thus improve the processing efficiency of sulfate wastewater and the rate of recovery of biological S.
Above-mentioned purpose of the present invention is achieved through the following technical solutions:
A method for anode and cathode synchronous electric catalysis sulfate wastewater biological treatment, the method comprises following concrete steps:
(1) build electrocatalysis bio-reactor, comprise cathodic reaction zone, buffer zone and anodic reaction district.Described cathodic reaction zone is anaerobic reaction district, and described anodic reaction district is micro-oxygen reaction zone, and install reference electrode in anodic reaction district, anodic reaction installs microporous aeration device bottom district; Described cathodic reaction zone and anodic reaction district volume ratio are 7 ~ 8:1; Described cathodic reaction zone top seal, top, described anodic reaction district is opened wide; Be provided with mud discharging mouth bottom described buffer zone, bottom described anode reactor, be provided with sulfur outlet;
(2) in cathodic reaction zone, inoculate sulphate reducing bacteria be main, facultative anaerobe is auxiliary mixed bacterial, and pass into substratum, energising domestication, culture temperature is 28 ~ 34 DEG C, and incubation time is 3 ~ 5 days, realizes sulphate reducing bacteria negative electrode biofilm and activation;
(3) in cathodic reaction zone while activation of microorganism, inoculating sulfur oxidizing bacterium in anode reaction zone is main aerobic flora, and pass into substratum, culture temperature is 25 ~ 30 DEG C, and incubation time is 5 ~ 7 days; Culturing process Anodic reaction zone electropotential span of control is 50 ~ 150mv;
(4) start reactor, sulfate wastewater is passed into reactor cathodic reaction zone, flow into through buffer zone behind anodic reaction district, outflow reactor.Described in the continuous treating processes of waste water, sulfate wastewater is 12 ~ 15h in the cathodic reaction zone residence time; Described cathodic reaction zone temperature is 28 ~ 34 DEG C; Described sulfate wastewater is 1.5 ~ 2.5h in the anodic reaction district residence time; Described anodic reaction district temperature is 25 ~ 30 DEG C; Described anodic reaction region electrode control of Electric potentials scope is 50 ~ 150mv.
In described step (2):
The described step passing into substratum, for substratum is passed into reactor cathodic reaction zone continuously, behind buffer zone, discharges reactor;
Described energising domestication step for anode electrode is inserted buffer zone, and starts energising domestication, and described energising is domesticated for the direct current passing into 100 ~ 300mV, preferred 150mV direct current;
In described step (3):
The described step passing into substratum is that substratum interval is added reactor anodic reaction district, 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 ultrapure water configuration, and in substratum, composition is: by KH
2pO
40.5g/L, NH
4cl 1g/L, CaCl
20.06g/L, Na
2sO
41.5g/L, FeSO
47H
2o0.007g/L, micro-1ml/L, described trace element adopts ultrapure water configuration, and in trace element solution, composition is: FeCl
24H
2o1.5g/L, MnCl
24H
2o 0.1g/L, ZnCl
20.07g/L, H
3bO
30.062g/L, Na
2moO
42H
2o 0.036g/L, NiCl
26H
2o 0.024g/L, CuCl
22H
2o 0.017g/L, EDTA 0.5g/L, 37%HCl 8.33ml/L;
In described step (3), described substratum adopts ultrapure water configuration, and in substratum, composition is: KH
2pO
42g/L, NH
4cl 0.4g/L, K
2hPO
42g/L, Na
2s
2o
35g/L, MgSO
47H
2o 0.8g, micro-1ml/L, described trace element adopts ultrapure water configuration, and in trace element solution, composition is: FeCl
24H
2o1.5g/L, MnCl
24H
2o 0.1g/L, ZnCl
20.07g/L, H
3bO
30.062g/L, Na
2moO
42H
2o 0.036g/L, NiCl
26H
2o 0.024g/L, CuCl
22H
2o 0.017g/L, EDTA 0.5g/L, 37%HCl 8.33ml/L.
The present invention adopts steps of processing sulfate wastewater:
(1) anode and cathode synchronous electric catalysis biological reactor is built, comprise cathodic reaction zone, buffer zone and anodic reaction district, the cathodic reaction zone of reactor is anaerobic reaction district, anodic reaction district is micro-oxygen reaction zone, mercurous chloride electrode is installed as reference electrode in anodic reaction district, bottom reaction zone, microporous aeration device is installed;
(2) before reactor start-up, in reactor cathodic reaction zone, inoculation sulphate reducing bacteria is master, facultative anaerobe is auxiliary mixed strains;
(3) configure sulfate reduction bacteria culture medium, substratum is entered reactor cathodic reaction zone continuously, directly discharges reactor through buffer zone;
(4) energising domestication cathodic reaction zone microorganism, completes sulphate reducing bacteria biofilm on the cathode electrode; Power-on voltage is the direct current of 100 ~ 300mV;
(5) in reactor anodic reaction district, inoculation sulfur-oxidizing bacteria;
(6) configure sulfur oxidizing bacterium substratum interval and add anodic reaction district, active anode reaction zone microorganism;
(7), after the activation of reactor negative and positive reaction zone, sulfate wastewater being passed into continuously reactor electric field cathodic reaction zone, is 12 ~ 15h in the residence time of cathodic reaction zone, and reaction zone temperature controls at 28 ~ 34 DEG C;
(8) waste water after cathode electric field enhance biological treatment, enters anodic reaction district through buffer zone, the anodic reaction district residence time is 1.5 ~ 2.5h, and reaction zone control temperature is 25 ~ 30 DEG C, and reaction zone anode electrode control of Electric potentials is between 50 ~ 150mv;
(9) in anodic reaction district, anode potential controls S in waste water
2-oxidising process, through anodic reaction district process after waste water, wherein sulphidic conversion is elemental sulfur, elemental sulfur with process after waste water outflow reactor, complete the process of waste water.
The advantage of present method process sulfate wastewater is adopted to be:
(1) adopt cathode electric field strengthening biological sulphate reduction, not only improve sulphate reducing bacteria reduction SO
4 2-speed, can reduce the consumption of electron donor in waste water simultaneously;
(2) anode potential is utilized to realize S
2-the control of oxidising process;
(3) by SO
4 2-reduction process and S
2-oxidising process realize in a reaction system;
(4) the method process sulfate wastewater process is adopted to be continuous operational process.
Accompanying drawing explanation
Fig. 1 device schematic diagram of the present invention.
In figure: 1-reactor water-in; 2-cathodic reaction zone; 3-cathode electrode; 4-anaerobion (based on SRB); 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 (based on SOB)
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 embodiments are only for illustration of the present invention, its scope do not limited the present invention in any way.
Experimental technique in following embodiment, if no special instructions, is ordinary method.Raw material used in following embodiment, reagent etc., if no special instructions, be commercially available purchase product.
Electrocatalysis bioreactor construction constructed by the present invention is as accompanying drawing 1, and this device comprises adjacent successively and the cathodic reaction zone be interconnected, buffer zone and anodic reaction district.Handled sulfur-containing waste water enters 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 based on sulphate reducing bacteria (4), the high price SO in waste water
x 2-be reduced to S
2-.Waste water after the process of cathodic reaction zone enters anodic reaction district (6) through buffer zone (5).Waste water in anodic reaction district anode electric field (7) and the aerobic microbiological based on sulfur oxidizing bacterium (12) effect under, the S in waste water
2-be oxidized into S.By reference electrode (8) monitor anode electropotential in anodic reaction district.Be provided with water proof weir (9) in anodic reaction district, there will not be the direct outflow reactor of short flow phenomenon to guarantee the residence time that waste water is enough in anodic reaction district.Waste water through the process of anodic reaction district discharges reactor through the bottom of water proof weir (9) from reactor water outlet (10), completes the process of waste water.
Embodiment 1
The present embodiment is the process utilizing electrocatalysis biological reaction apparatus process 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.
The step of process 7-ACA pharmacy waste water:
(1) waste water is before entering electrocatalysis bio-reactor continuously, respectively to microbe inoculation in reactor cathodic reaction zone and anodic reaction district, also activates the microorganism in electric field anode and cathode reaction zone independently simultaneously.Cathodic reaction zone institute microbe inoculation is based on desulfovibrio (Desulfovibriosp.), and institute of anodic reaction district microbe inoculation is based on grate sulfur thiobacillus (Thiobacillus thioparus);
(2) cathodic reaction zone substratum adopts ultrapure water configuration, and in substratum, composition is: by KH
2pO
40.5g/L, NH
4cl 1g/L, CaCl
20.06g/L, Na
2sO
41.5g/L, FeSO
47H
2o0.007g/L, micro-1ml/L;
(3) anodic reaction district substratum adopts ultrapure water configuration, and in substratum, composition is: KH
2pO
42g/L, NH
4cl 0.4g/L, K
2hPO
42g/L, Na
2s
2o
35g/L, MgSO
47H
2o 0.8g, micro-1ml/L;
(4) trace element adopts ultrapure water configuration, and in trace element solution, composition is: FeCl
24H
2o1.5g/L, MnCl
24H
2o 0.1g/L, ZnCl
20.07g/L, H
3bO
30.062g/L, Na
2moO
42H
2o 0.036g/L, NiCl
26H
2o 0.024g/L, CuCl
22H
2o 0.017g/L, EDTA 0.5g/L, 37%HCl 8.33ml/L;
(5) in activation of microorganism process, the direct current applying 300mv to reactor anode and cathode carries out energising domestication, and cathodic reaction zone microorganism culturing acclimation temperature is 32 DEG C, and incubation time is 3 days; Anode electrode control of Electric potentials is at 50mv, and anodic reaction district microorganism culturing acclimation temperature is 30 DEG C, and incubation time is 5 days;
(6) after anode and cathode reaction zone activation of microorganism terminates, 7-ACA pharmacy waste water is entered 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 controls at 32 DEG C;
(8) through the waste water of reactor cathodic reaction zone process, enter anodic reaction district through buffer zone, the anodic reaction district residence time is 2.5h, and reaction zone control temperature is 30 DEG C;
(9) waste water after the process of anodic reaction district, sulfides from wastewater is converted into elemental sulfur, and elemental sulfur, with processed waste water outflow reactor, completes the process of waste water.
(10) after reactor runs 7 days, salt wastewater treatment tends towards stability, in cathodic reaction zone, and SO in 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 anodic reaction district
4 2concentration is lower than 80mg/L.
Embodiment 2
The present embodiment is the process utilizing electrocatalysis biological reaction apparatus same for treating acidic mine wastewater.
Handled acidic mine waste water characteristic is 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 electrocatalysis bio-reactor continuously, respectively to microbe inoculation in reactor cathodic reaction zone and anodic reaction district, also activates the microorganism in electric field anode and cathode reaction zone independently simultaneously.Cathodic reaction zone institute microbe inoculation is based on desulfovibrio (Desulfovibriosp.), and institute of anodic reaction district microbe inoculation is based on grate sulfur thiobacillus (Thiobacillus thioparus);
(2) cathodic reaction zone substratum adopts ultrapure water configuration, and in substratum, composition is: by KH
2pO
40.5g/L, NH
4cl 1g/L, CaCl
20.06g/L, Na
2sO
41.5g/L, FeSO
47H
2o0.007g/L, micro-1ml/L;
(3) anodic reaction district substratum adopts ultrapure water configuration, and in substratum, composition is: KH
2pO
42g/L, NH
4cl 0.4g/L, K
2hPO
42g/L, Na
2s
2o
35g/L, MgSO
47H
2o 0.8g, micro-1ml/L;
(4) trace element adopts ultrapure water configuration, and in trace element solution, composition is: FeCl
24H
2o1.5g/L, MnCl
24H
2o 0.1g/L, ZnCl
20.07g/L, H
3bO
30.062g/L, Na
2moO
42H
2o 0.036g/L, NiCl
26H
2o 0.024g/L, CuCl
22H
2o 0.017g/L, EDTA 0.5g/L, 37%HCl 8.33ml/L;
(5) in activation of microorganism process, the direct current applying 300mv to reactor anode and cathode carries out energising domestication, and cathodic reaction zone microorganism culturing acclimation temperature is 28 DEG C, and incubation time is 5 days; Anode electrode control of Electric potentials is at 100mv, and microorganism culturing temperature is 25 DEG C, and incubation time is 7 days;
(6) after anode and cathode reaction zone activation of microorganism terminates, waste water is entered 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 controls at 28 DEG C;
(8) through the waste water of reactor cathodic reaction zone process, enter anodic reaction district through buffer zone, the anodic reaction district residence time is 1.5h, and reaction zone control temperature is 25 DEG C;
(9) pH due to mine wastewater is lower, and the SO in waste water
4 2-concentration is higher, therefore, in actual treatment waste water process, by the return of waste water after the process of anodic reaction district, and mixes with Jinsui River, improves the pH of waste water, thus reduce the SO of actual treatment sulfate wastewater
4 2-concentration, wherein return of waste water is than being 2:1.Because mine wastewater is inorganic wastewater, need supplementary suitable organism in waste water to serve as the electron donor of sulphate reducing bacteria metabolism, supplementary electron donor is industrial alcohol, adds the industrial alcohol of 0.4 milliliter in often liter of waste water.
(10) sulfides from wastewater after above-mentioned process is converted into elemental sulfur, and elemental sulfur, with processed waste water outflow reactor, completes the process of waste water.
(11) after answering device to run 20 days, sulfate wastewater treatment tends towards stability, in cathodic reaction zone, and SO in 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 anodic reaction district
4 2concentration is lower than 80mg/L.
Embodiment 3
The present embodiment is the process utilizing electrocatalysis biological reaction apparatus process gourmet powder waste water.
Handled gourmet powder waste water characteristic is as follows:
Wastewater pH: 6.5 ~ 6.8, SO
4 2-: 12000 ~ 15000mg/L, COD:10000mg/L.
The step of process gourmet powder waste water:
(1) waste water is before entering electrocatalysis bio-reactor continuously, respectively to microbe inoculation in reactor cathodic reaction zone and anodic reaction district, also activates the microorganism in electric field anode and cathode reaction zone independently simultaneously.Cathodic reaction zone institute microbe inoculation is based on desulfovibrio (Desulfovibriosp.), and institute of anodic reaction district microbe inoculation is based on grate sulfur thiobacillus (Thiobacillus thioparus);
(2) cathodic reaction zone substratum adopts ultrapure water configuration, and in substratum, composition is: by KH
2pO
40.5g/L, NH
4cl 1g/L, CaCl
20.06g/L, Na
2sO
41.5g/L, FeSO
47H
2o0.007g/L, micro-1ml/L;
(3) anodic reaction district substratum adopts ultrapure water configuration, and in substratum, composition is: KH
2pO
42g/L, NH
4cl 0.4g/L, K
2hPO
42g/L, Na
2s
2o
35g/L, MgSO
47H
2o 0.8g, micro-1ml/L;
(4) trace element adopts ultrapure water configuration, and in trace element solution, composition is: FeCl
24H
2o1.5g/L, MnCl
24H
2o 0.1g/L, ZnCl
20.07g/L, H
3bO
30.062g/L, Na
2moO
42H
2o 0.036g/L, NiCl
26H
2o 0.024g/L, CuCl
22H
2o 0.017g/L, EDTA 0.5g/L, 37%HCl 8.33ml/L;
(5) in activation of microorganism process, the direct current applying 300mv to reactor anode and cathode carries out energising domestication, and cathodic reaction zone microorganism culturing acclimation temperature is 30 DEG C, and incubation time is 5 days; Anode electrode control of Electric potentials is at 150mv, and microorganism culturing temperature is 30 DEG C, and incubation time is 5 days;
(6) after anode and cathode reaction zone activation of microorganism terminates, waste water is entered 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 controls at 30 DEG C;
(8) through the waste water of reactor cathodic reaction zone process, enter anodic reaction district through buffer zone, the anodic reaction district residence time is 2h, and reaction zone control temperature is 30 DEG C;
(9) due to the SO in gourmet powder waste water
4 2-concentration is higher, therefore, in actual treatment waste water process, by the return of waste water after the process of anodic reaction district, and mixes with Jinsui River, reduces the SO of actual treatment sulfate wastewater
4 2-concentration, wherein return of waste water is than being 4:1.
(10) sulfides from wastewater after above-mentioned process is converted into elemental sulfur, and elemental sulfur, with processed waste water outflow reactor, completes the process of waste water.
(11) after answering device to run 15 days, sulfate wastewater treatment tends towards stability, in cathodic reaction zone, and SO in 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 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 various change or distortion according to the present invention, only otherwise depart from spirit of the present invention, all should belong to the scope of claims of the present invention.
Claims (5)
1. a method for anode and cathode synchronous electric catalysis sulfate wastewater biological treatment, the method comprises following concrete steps:
(1) build electrocatalysis bio-reactor, comprise cathodic reaction zone, buffer zone and anodic reaction district; Described cathodic reaction zone is anaerobic reaction district, and described anodic reaction district is micro-oxygen reaction zone, and install reference electrode in anodic reaction district, anodic reaction installs microporous aeration device bottom district; Described cathodic reaction zone and anodic reaction district volume ratio are 7 ~ 8:1; Described cathodic reaction zone portion closes, and described anode reactor top is opened wide; Be provided with mud discharging mouth bottom described buffer zone, bottom described anode reactor, be provided with sulfur outlet;
(2) in cathodic reaction zone, inoculate sulphate reducing bacteria be main, facultative anaerobe is auxiliary mixed strains, passes into substratum, energising domestication, power-on voltage is 100 ~ 300mV direct current, culture temperature is 28 ~ 34 DEG C, and incubation time is 3 ~ 5 days, realizes sulphate reducing bacteria negative electrode biofilm;
(3) in anodic reaction district, inoculate sulfur-oxidizing bacteria, interval adds substratum, and culture temperature is 25 ~ 30 DEG C, and incubation time is 5 ~ 7 days; Culturing process Anodic reaction zone electropotential span of control is 50 ~ 150mv;
(4) start reactor, sulfate wastewater is passed into reactor cathodic reaction zone continuously, then flow into behind anodic reaction district through buffer zone, outflow reactor, realizes the continuous biological treatment of sulfate wastewater; Described in the continuous treating processes of waste water, sulfate wastewater is 12 ~ 15h in the cathodic reaction zone residence time; Described cathodic reaction zone temperature is 28 ~ 34 DEG C; Stating sulfate wastewater in the anodic reaction district residence time is 1.5 ~ 2.5h; Described anodic reaction district temperature is 25 ~ 30 DEG C; Described anodic reaction region electrode control of Electric potentials scope is 50 ~ 150mv.
2. method according to claim 1, is characterized in that, in described step (2), described in pass into the step of substratum for substratum is passed into reactor cathodic reaction zone continuously, behind buffer zone, discharge reactor;
Described energising domestication step for anode electrode is inserted buffer zone, and starts energising domestication, and described energising is domesticated for the direct current passing into 100 ~ 300mV, preferred 150mV direct current.
3. method according to claim 1, it is characterized in that, in described step (3), described in pass into substratum step for substratum interval is added reactor anodic reaction district, every 6h changes a subculture, and each replaced medium volume is 70% of anodic reaction district volume.
4. the method according to claim 1 or 3, is characterized in that, in described step (2), described substratum adopts ultrapure water configuration, and in substratum, composition is: KH
2pO
40.5g/L, NH
4cl 1g/L, CaCl
20.06g/L, Na
2sO
41.5g/L, FeSO
47H
2o0.007g/L, micro-1ml/L, described trace element adopts ultrapure water configuration, and in trace element solution, composition is: FeCl
24H
2o1.5g/L, MnCl
24H
2o 0.1g/L, ZnCl
20.07g/L, H
3bO
30.062g/L, Na
2moO
42H
2o 0.036g/L, NiCl
26H
2o 0.024g/L, CuCl
22H
2o0.017g/L, EDTA 0.5g/L, 37%HCl 8.33ml/L.
5. the method according to claim 1 or 3, is characterized in that, in described step (3), described substratum adopts ultrapure water configuration, and in substratum, composition is: KH
2pO
42g/L, NH
4cl0.4g/L, K
2hPO
42g/L, Na
2s
2o
35g/L, MgSO
47H
2o 0.8g, micro-1ml/L, described trace element adopts ultrapure water configuration, and in trace element solution, composition is: FeCl
24H
2o1.5g/L, MnCl
24H
2o 0.1g/L, ZnCl
20.07g/L, H
3bO
30.062g/L, Na
2moO
42H
2o 0.036g/L, NiCl
26H
2o 0.024g/L, CuCl
22H
2o 0.017g/L, EDTA 0.5g/L, 37%HCl 8.33ml/L.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| 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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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| 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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| Publication Number | Publication Date |
|---|---|
| CN103319002A CN103319002A (en) | 2013-09-25 |
| CN103319002B true CN103319002B (en) | 2015-04-15 |
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