CN105293855A - Method of synchronously degrading excess sludge and treating hexavalent chromium wastewater - Google Patents
Method of synchronously degrading excess sludge and treating hexavalent chromium wastewater Download PDFInfo
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- CN105293855A CN105293855A CN201510874359.6A CN201510874359A CN105293855A CN 105293855 A CN105293855 A CN 105293855A CN 201510874359 A CN201510874359 A CN 201510874359A CN 105293855 A CN105293855 A CN 105293855A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
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- Y02E60/30—Hydrogen technology
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Abstract
The invention provides a method of synchronously degrading excess sludge and treating hexavalent chromium wastewater, and relates to a method of recycling the excess sludge and treating the chromium-containing wastewater. The invention aims to solve the problem that the current treatment cost for treating excess pollutants is high by utilizing microbial fuel cells. The method comprises the steps of 1, setting up a double-cell-structure reactor; 2, adding the excess sludge and nutrient solutions into an anode chamber of the reactor, adding potassium ferricyanidecatholyte into a cathode chamber, and performing cultivation, wherein when the voltage output is greater than 0.6 V, starting is successful; 3, adding the excess sludge and the nutrient solutions to be treated into the anode chamber, adding the hexavalent chromium wastewater to be treated into the cathode chamber, and performing treatment, wherein a treatment period of the excess sludge is 40 to 50 days, the degradation rate of the excess sludge can reach 38 percent to 62 percent, a reduction period of the hexavalent chromium wastewater is 2 to 10 days, the degradation rate of hexavalent chromium can reach 66.4 percent to 93.2 percent, and the purpose of synchronously degrading the excess sludge and treating the hexavalent chromium wastewater is realized.
Description
Technical field
The invention belongs to technical field of microbial fuel battery, be specifically related to a kind ofly realize excess sludge resource utilization, chromate waste water reduction and the method for synchronous electrogenesis.
Background technology
Biomass energy as uniquely can the renewable energy source of fixed carbon, its efficiently conversion and clean utilization be day by day subject to global attention, biomass energy is defined as future source of energy developing goal by many countries.The problem such as to grow for high, the hydraulic detention time of energy consumption in global energy shortage and traditional wastewater/specific resistance to filtration process, by introducing microbiological fuel cell technology, while process contaminant remaining, the chemical energy in pollutent is reclaimed with the form of electric energy, realize resource utilization and the recovery energy of pollutent.Chemical energy in organic waste can be directly converted to clean electric energy by microbiological fuel cell under normal temperature and pressure conditions, in biological restoration, sewage and field of sludge treatment, there is potential application prospect, there is the advantages such as high efficiency, low cost, environmental friendliness, operational condition gentleness.
The existing method utilizing microbiological fuel cell process contaminant remaining is using contaminant remaining as anode substrate, adds the Tripotassium iron hexacyanide, potassium permanganate etc. carry out chemistry of micro-organisms reaction in cathodic area.As the article " microbiological fuel cell process excess sludge and synchronous electrogenesis performance " be published on Harbin Engineering University's journal volume the 6th phase June the 31st in 2010 discloses a kind of method adopting microbiological fuel cell technical finesse excess sludge, take the Tripotassium iron hexacyanide as cathode electronics acceptor, the chemical energy in mud is directly transformed into electric energy.But this method will add cathode electronics acceptor in addition, makes processing cost increase.
Summary of the invention
The present invention will solve existingly to utilize the technical problem that the method processing cost of microbiological fuel cell process contaminant remaining is high, and provides a kind of method of synchronous degradation excess sludge and process hexavalent chromium wastewater.
The method of a kind of synchronous degradation excess sludge of the present invention and process hexavalent chromium wastewater, carry out according to the following steps:
One, two pool structure reactor is built: this pair of pool structure reactor is made up of housing, cationic exchange membrane, carbon fiber brush, reference electrode and agitator, cationic exchange membrane is arranged in the housing, housing is divided into anolyte compartment and cathode compartment, the carbon fiber brush be arranged in anolyte compartment is anode, the carbon fiber brush be arranged in cathode compartment is negative electrode, arrange stopple coupon respectively in the bottom of anolyte compartment and cathode compartment, the top of anolyte compartment is provided with effuser; Anode is connected by external circuit with negative electrode; Reference electrode penetrates in anolyte compartment; Agitator is arranged in anolyte compartment;
Two, start: in the anolyte compartment of two pool structure reactor, add excess sludge and nutrient solution, wherein under excess sludge, the volume ratio of nutrient solution is (20 ~ 30): 1, Tripotassium iron hexacyanide catholyte is added in cathode compartment, pass into nitrogen in anolyte compartment and ensure its anaerobic environment, in culturing process, agitator in anolyte compartment stirs 3 ~ 5 minutes every 1h, changes the substrate in an anolyte compartment and cathode compartment every 2 ~ 3 days; After two pool structure reactor voltage output is greater than 0.6V, start successfully;
Three, pending excess sludge and nutrient solution are added in anolyte compartment, anode indoor pass into nitrogen and ensure its anaerobic environment, pending hexavalent chromium wastewater is joined in cathode compartment, agitator 5 in anolyte compartment stirs 3 ~ 5 minutes every 1h, in anolyte compartment, excess sludge aftertreatment in 40 ~ 50 days is complete, the pending excess sludge more renewed; Hexavalent chromium wastewater in cathode compartment is disposed for 2 ~ 10 days, the pending hexavalent chromium wastewater more renewed, and completes the operation of synchronous degradation excess sludge and process hexavalent chromium wastewater
Chromium and chromic salts are indispensable raw materials in industrial production, and be widely used in the industries such as plating, printing and dyeing and process hides, these industries all can produce a large amount of chromate waste water, contaminate environment.Chromium in environment directly or indirectly can enter human body, works the mischief to HUMAN HEALTH, method timely and effectively therefore should be taked to administer chromate waste water, control pollution of chromium.Chromium is a Heavy Metallic Elements, has the multiple valence state of divalence, trivalent and sexavalence, wherein trivalent and sexavalence compound more common.In chromium cpd, chromic bio-toxicity is the most powerful, and trivalent is taken second place, and divalent toxic is minimum, and chromic toxicity is about chromic 100 times, one of environmental carcinogen that sexavalent chrome is still generally acknowledged.Therefore, sexavalent chrome is changed into trivalent chromium, be not only a kind of effective removing toxic substances mode, and be the committed step finally removing chromium from water surrounding.The theoretical oxidation reduction potential that the present invention utilizes sexavalent chrome to change into this process of trivalent chromium reaches the feature of higher 1.33V, using sexavalent chrome as microorganism fuel cell cathode electron acceptor(EA), so both reach the effect of hexavalent chromium removal, also certain energy output can be obtained, cathode potential is improve than typical Tripotassium iron hexacyanide negative electrode, and to a certain extent the operation of whole battery is promoted to some extent, the reaction pattern of the two-way removal of this kind of anode and cathode contamination thing simultaneously also has certain positive effect for the research and development of novel environmental engineering equipment.Its action principle is: anode of microbial fuel cell room mud is in anaerobic environment, therefore mud this be under the effect of anerobe slowly in anaerobic fermentation process, namely organism is slowly degraded.This battery through unloading phase, anolyte compartment tames out mud inside electrochemical activity bacterium (Geobacter gradually, Clostridium etc.), the solubility small organic molecule that this bacterioid utilizes anode slime anaerobic fermentation process to produce carries out metabolism, and derive lasting electronics, anaerobic fermentation process in anolyte compartment can be accelerated, thus the degraded of accelerate sludge, the reaction principle of this to be mud be microbiological fuel cell of anode substrate simultaneously.Compared to other sludge fuel battery, catholyte adopts hexavalent chromium wastewater to improve cathode potential, thus the output speed of accelerating anode indoor electronic, improve efficiency of fuel cell generation and the activity of electrochemical activity bacterium, improve sludge degradation effect and electrogenesis usefulness thus.Therefore this technique not only can realize excess sludge stabilization and hexavalent chromium wastewater reduction, can also improve sludge degradation effect and electrogenesis effect.In anolyte compartment, the treatment cycle of excess sludge is 40 ~ 50 days, and excess sludge degradation rate can reach 38% ~ 62%, and in cathode compartment, the reduction cycle of hexavalent chromium wastewater is 2 ~ 10 days, and hexavalent chrome reduction rate can reach 66.4% ~ 93.2%.Utilize present method to process excess sludge and hexavalent chromium wastewater simultaneously, cost of investment be low, energy consumption is little, pollution-free.The present invention achieves excess sludge resource utilization, chromate waste water reduction and synchronous electrogenesis simultaneously.
Accompanying drawing explanation
Fig. 1 is the structural representation of the two pool structure reactor of the present invention.Wherein 1 is housing, 2 cationic exchange membranes, and 3 is carbon fiber brush, and 4 is reference electrode, and 5 is agitator, and 1-1 is anolyte compartment, and 1-2 is cathode compartment, and 1-3 is stopple coupon, and 1-4 is effuser.
Embodiment
Embodiment: a kind of synchronous degradation excess sludge of present embodiment and the method for process hexavalent chromium wastewater, carry out according to the following steps:
One, two pool structure reactor is built: this pair of pool structure reactor is made up of housing 1, cationic exchange membrane 2, carbon fiber brush 3, reference electrode 4 and agitator 5, cationic exchange membrane 2 arranges within the case 1, housing 1 is divided into anolyte compartment 1-1 and cathode compartment 1-2, the carbon fiber brush 3 be arranged in anolyte compartment 1-1 is anode, the carbon fiber brush 3 be arranged in cathode compartment 1-2 is negative electrode, arrange stopple coupon 1-3 respectively in the bottom of anolyte compartment 1-1 and cathode compartment 1-2, the top of anolyte compartment is provided with effuser 1-4; Anode is connected by external circuit with negative electrode; Reference electrode 4 penetrates in anolyte compartment; Agitator 5 is arranged in anolyte compartment;
Two, start: in the anolyte compartment 1-1 of two pool structure reactor, add excess sludge and nutrient solution, wherein under excess sludge, the volume ratio of nutrient solution is (20 ~ 30): 1, Tripotassium iron hexacyanide catholyte is added in cathode compartment 1-2, pass into nitrogen in anolyte compartment and ensure its anaerobic environment, in culturing process, agitator 5 in anolyte compartment stirs 3 ~ 5 minutes every 1h, changes the substrate in an anolyte compartment and cathode compartment every 2 ~ 3 days; After two pool structure reactor voltage output is greater than 0.6V, start successfully;
Three, pending excess sludge and nutrient solution are added in anolyte compartment 1-1, anode indoor pass into nitrogen and ensure its anaerobic environment, pending hexavalent chromium wastewater is joined in cathode compartment 1-2, agitator 5 in anolyte compartment stirs 3 ~ 5 minutes every 1h, in anolyte compartment, excess sludge aftertreatment in 40 ~ 50 days is complete, the pending excess sludge more renewed; Hexavalent chromium wastewater in cathode compartment is disposed for 2 ~ 10 days, the pending hexavalent chromium wastewater more renewed, and completes the operation of synchronous degradation excess sludge and process hexavalent chromium wastewater.
Embodiment two: present embodiment and embodiment one unlike the composition of step 2 Middle nutrition solution and proportioning as shown in table 1:
The composition of table 1 nutrient solution and proportioning
Other are identical with embodiment one.
Embodiment three: present embodiment and embodiment one or two are by the Tripotassium iron hexacyanide (K unlike Tripotassium iron hexacyanide catholyte in step 2
3[Fe (CN)
6] concentration be 30 ~ 35g/L, potassium primary phosphate (KH
2pO
4) concentration be 25 ~ 30g/L, the Tripotassium iron hexacyanide and potassium primary phosphate are added to the water formulated; Other is identical with embodiment one or two.
Embodiment four: one of present embodiment and embodiment one to three are unlike the negative electrode described in step one and these two electrodes of anode treatment process before use: first rinsed with water by electrode, then respectively 2h is soaked with HCl and the 1mol/LNaOH solution of 1mol/L successively, to remove the impurity of electrode material surface, finally soak 5h with deionized water, for subsequent use; Other is identical with one of embodiment one to three.
Embodiment five: one of present embodiment and embodiment one to four are unlike the treatment process before use of the proton exchange membrane described in step one: cationic exchange membrane first uses the H of 30%
2o
2boil 30min, then respectively soak 2h with HCl and the 1mol/LNaOH solution of 1mol/L successively, to remove film surface contaminant and impurity, finally soak 5h with deionized water, for subsequent use.Other is identical with one of embodiment one to four.
Embodiment six: one of present embodiment and embodiment one to five are 25:1 unlike the volume ratio of excess sludge in step 2 and nutrient solution, and other is identical with one of embodiment one to five.
With following verification experimental verification beneficial effect of the present invention:
Test 1: a kind of synchronous degradation excess sludge of this test and the method for process hexavalent chromium wastewater, carry out according to the following steps:
One, two pool structure reactor is built: this pair of pool structure reactor is made up of housing 1, cationic exchange membrane 2, carbon fiber brush 3, reference electrode 4 and agitator 5, cationic exchange membrane 2 arranges within the case 1, housing 1 is divided into anolyte compartment 1-1 and cathode compartment 1-2, the carbon fiber brush 3 be arranged in anolyte compartment 1-1 is anode, the carbon fiber brush 3 be arranged in cathode compartment 1-2 is negative electrode, arrange stopple coupon 1-3 respectively in the bottom of anolyte compartment 1-1 and cathode compartment 1-2, the top of anolyte compartment is provided with effuser 1-4; Anode is connected by external circuit with negative electrode; Reference electrode 4 penetrates in anolyte compartment; Agitator 5 is arranged in anolyte compartment; Negative electrode and these two electrodes of anode treatment process before use: electrode is first rinsed with water, then respectively soaks 2h by the NaOH solution of HCl and 1mol/L of 1mol/L successively, to remove the impurity of electrode material surface, finally soak 5h with deionized water; Proton exchange membrane treatment process before use: cationic exchange membrane first uses the H of 30%
2o
2boil 30min, then respectively soak 2h with HCl and the 1mol/LNaOH solution of 1mol/L successively, to remove film surface contaminant and impurity, finally soak 5h with deionized water;
Two, start: in two pool structure reactor anolyte compartment 1-1, add the second pond excess sludge that 500mL water ratio is 92%, TCOD is 48435mg/L as anode substrate, add 15mL nutrient solution (moiety is in table 1) again, 350mL Tripotassium iron hexacyanide catholyte is added in cathode compartment 1-2, in culturing process, agitator 5 in anolyte compartment stirs 3 minutes every 1h, changes the substrate in an anolyte compartment and cathode compartment every 2 days; After 5 days, when two pool structure reactor voltage stable output is at 0.6V, start successfully, wherein Tripotassium iron hexacyanide catholyte is by the Tripotassium iron hexacyanide (K
3[Fe (CN)
6]) concentration be 32.9g/L, potassium primary phosphate (KH
2pO
4) concentration be 27.2g/L, the Tripotassium iron hexacyanide and potassium primary phosphate are added to the water formulated; Start successfully, turn out electrochemical activity bacterium (Geobacter, Clostridium etc.);
Three, be 92% by water ratio pending for 500mL, TCOD is that the second pond excess sludge of 48435mg/L adds in anolyte compartment 1-1 as anode substrate, again 15mL nutrient solution (moiety is in table 1) is added in anolyte compartment 1-1, anode indoor pass into nitrogen and ensure its anaerobic environment, the hexavalent chromium wastewater being 9mg/L by hexavalent chromium concentration pending for 350mL joins in cathode compartment 1-2, agitator 5 in anolyte compartment stirs 3 minutes every 1h, to reduce the mass transfer internal resistance of battery and to promote organic fast degradation, every 6 hours sampling and testing results, after 2 days, total chromium clearance is 83.20%, hexavalent chromium removal rate is 93.2%, after this every 2 days, namely each end of term in cathodic reaction week changes negative electrode hexavalent chromium wastewater, after 50 days, the TCOD degradation rate of excess sludge is 38.03%, after this excess sludge was changed every 50 days, realize synchronous degradation excess sludge and process hexavalent chromium wastewater.
Test 2: this test 1 to substitute in order to lower operation unlike step 3 with testing: be 92% by water ratio pending for 500mL, TCOD is that the second pond excess sludge of 48435mg/L adds in anolyte compartment 1-1 as anode substrate, again 15mL nutrient solution (moiety is in table 1) is added in anolyte compartment 1-1, the hexavalent chromium wastewater being 18mg/L by pending 350mL hexavalent chromium concentration joins in cathode compartment 1-2, agitator 5 in anolyte compartment stirs 3 minutes every 1h, to reduce the mass transfer internal resistance of battery and to promote organic fast degradation, every 8 hours sampling and testing results, after 4 days, total chromium clearance is about 83.01%, hexavalent chromium removal rate is 85.03%, the TCOD degradation rate of excess sludge is 40.15%, synchronous degradation excess sludge and process hexavalent chromium wastewater can be realized.
Test 3: this test 1 to substitute in order to lower operation unlike step 3 with testing: be 92% by water ratio pending for 500mL, TCOD is that the second pond excess sludge of 48435mg/L adds in anolyte compartment 1-1 as anode substrate, again 15mL nutrient solution (moiety is in table 1) is added in anolyte compartment 1-1, be that 27mg/L hexavalent chromium wastewater joins in cathode compartment 1-2 by pending hexavalent chromium concentration, agitator 5 in anolyte compartment stirs 3 minutes every 1h, to reduce the mass transfer internal resistance of battery and to promote organic fast degradation, every 8 hours test processes results, after 4 days, total chromium clearance is about 68.95%, hexavalent chromium removal rate is 80.3%, the TCOD degradation rate of excess sludge is 53.86%, synchronous degradation excess sludge and process hexavalent chromium wastewater can be realized.
Test 4: this test 1 to substitute in order to lower operation unlike step 3 with testing: be 92% by water ratio pending for 500mL, TCOD is that the second pond excess sludge of 48435mg/L adds in anolyte compartment 1-1 as anode substrate, again 15mL nutrient solution (moiety is in table 1) is added in anolyte compartment 1-1, be that the hexavalent chromium wastewater of 35mg/L joins in cathode compartment 1-2 by pending hexavalent chromium concentration, agitator 5 in anolyte compartment stirs 3 minutes every 1h, to reduce the mass transfer internal resistance of battery and to promote organic fast degradation, every 8 hours test processes results, after 4 days, total chromium clearance is about 64.93%, hexavalent chromium removal rate is 66.38%, the TCOD degradation rate of excess sludge is 62.18%, synchronous degradation excess sludge and process hexavalent chromium wastewater can be realized.
Claims (5)
1. a method for synchronous degradation excess sludge and process hexavalent chromium wastewater, is characterized in that the method is carried out according to the following steps:
One, build two pool structure reactor: this pair of pool structure reactor is by housing (1), cationic exchange membrane (2), carbon fiber brush (3), reference electrode (4) and agitator (5) composition, cationic exchange membrane (2) is arranged in housing (1), housing (1) is divided into anolyte compartment (1-1) and cathode compartment (1-2), the carbon fiber brush (3) be arranged in anolyte compartment (1-1) is anode, the carbon fiber brush (3) be arranged in cathode compartment (1-2) is negative electrode, in the bottom of anolyte compartment (1-1) and cathode compartment (1-2), stopple coupon (1-3) is set respectively, the top of anolyte compartment is provided with effuser (1-4), anode is connected by external circuit with negative electrode, reference electrode (4) penetrates in anolyte compartment, agitator (5) is arranged in anolyte compartment,
Two, start: in the anolyte compartment (1-1) of two pool structure reactor, add excess sludge and nutrient solution, wherein under excess sludge, the volume ratio of nutrient solution is (20 ~ 30): 1, Tripotassium iron hexacyanide catholyte is added in cathode compartment (1-2), pass into nitrogen in anolyte compartment and ensure its anaerobic environment, in culturing process, agitator (5) in anolyte compartment stirs 3 ~ 5 minutes every 1h, changes the substrate in an anolyte compartment and cathode compartment every 2 ~ 3 days; After two pool structure reactor voltage output is greater than 0.6V, start successfully;
Three, pending excess sludge and nutrient solution are added in anolyte compartment (1-1), anode indoor pass into nitrogen and ensure its anaerobic environment, pending hexavalent chromium wastewater is joined in cathode compartment (1-2), agitator (5) in anolyte compartment stirs 3 ~ 5 minutes every 1h, in anolyte compartment, excess sludge aftertreatment in 40 ~ 50 days is complete, the pending excess sludge more renewed; Hexavalent chromium wastewater in cathode compartment is disposed for 2 ~ 10 days, the pending hexavalent chromium wastewater more renewed, and completes the operation of synchronous degradation excess sludge and process hexavalent chromium wastewater.
2. the method for a kind of synchronous degradation excess sludge according to claim 1 and process hexavalent chromium wastewater, to it is characterized in that in step 2 Tripotassium iron hexacyanide catholyte be by the concentration of the Tripotassium iron hexacyanide be 30 ~ 35g/L, the concentration of potassium primary phosphate is 25 ~ 30g/L, is added to the water formulated by the Tripotassium iron hexacyanide and potassium primary phosphate.
3. the method for a kind of synchronous degradation excess sludge according to claim 1 and 2 and process hexavalent chromium wastewater, it is characterized in that the negative electrode described in step one and these two electrodes of anode treatment process before use: first rinsed with water by electrode, then respectively 2h is soaked with HCl and the 1mol/LNaOH solution of 1mol/L successively, to remove the impurity of electrode material surface, finally soak 5h with deionized water, for subsequent use.
4. the method for a kind of synchronous degradation excess sludge according to claim 1 and 2 and process hexavalent chromium wastewater, is characterized in that the treatment process before use of the proton exchange membrane described in step one: cationic exchange membrane first uses the H of 30%
2o
2boil 30min, then respectively soak 2h with HCl and the 1mol/LNaOH solution of 1mol/L successively, to remove film surface contaminant and impurity, finally soak 5h with deionized water, for subsequent use.
5. the method for a kind of synchronous degradation excess sludge according to claim 1 and 2 and process hexavalent chromium wastewater, is characterized in that the volume ratio of excess sludge and nutrient solution in step 2 is 25:1.
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| CN107311294A (en) * | 2017-08-23 | 2017-11-03 | 哈尔滨工业大学 | A kind of apparatus and method for handling garden sludge and electroplating wastewater simultaneously for plating industrial district |
| CN107352636A (en) * | 2017-08-23 | 2017-11-17 | 哈尔滨工业大学 | It is a kind of to reclaim the apparatus and method for handling garden mud and sewage simultaneously for plating industrial district heavy metal in waste water |
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| CN106587280A (en) * | 2016-11-11 | 2017-04-26 | 西安交通大学 | Photoelectrochemical method and device for cooperatively treating organic waste liquid and heavy metal waste liquid and generating electricity |
| CN106926140A (en) * | 2017-04-24 | 2017-07-07 | 南华大学 | A kind of Magnetorheologicai polishing liquid electrochemistry preserving device and method |
| CN107311294A (en) * | 2017-08-23 | 2017-11-03 | 哈尔滨工业大学 | A kind of apparatus and method for handling garden sludge and electroplating wastewater simultaneously for plating industrial district |
| CN107352636A (en) * | 2017-08-23 | 2017-11-17 | 哈尔滨工业大学 | It is a kind of to reclaim the apparatus and method for handling garden mud and sewage simultaneously for plating industrial district heavy metal in waste water |
| CN107352636B (en) * | 2017-08-23 | 2020-06-02 | 哈尔滨工业大学 | Device and method for recovering heavy metals in electroplating industrial park wastewater and treating park sludge sewage simultaneously |
| CN109085161B (en) * | 2018-08-28 | 2021-05-07 | 上海大学 | Method for rapidly judging anaerobic biodegradation degree of wastewater by using microbial fuel cell |
| CN109179860A (en) * | 2018-08-28 | 2019-01-11 | 哈尔滨工业大学 | A kind of method of Recalcitrant chemicals and degradation excess sludge in synchronous catalysis oxidation secondary effluent |
| CN109085161A (en) * | 2018-08-28 | 2018-12-25 | 上海大学 | The method that anaerobic waste water biological degradability is quickly judged using microbiological fuel cell |
| CN109179860B (en) * | 2018-08-28 | 2022-06-03 | 哈尔滨工业大学 | Method for synchronously catalytic oxidation of nondegradable pollutants in secondary effluent and degradation of excess sludge |
| CN110590091A (en) * | 2019-09-24 | 2019-12-20 | 天津大学 | Microbial fuel cell for synchronously reducing hexavalent chromium in soil through oil sludge treatment |
| CN112919756A (en) * | 2021-03-22 | 2021-06-08 | 大连海事大学 | Method for treating antibiotic resistance genes in medical wastewater or sludge generated by medical wastewater treatment process |
| CN114906996A (en) * | 2022-06-06 | 2022-08-16 | 北京林业大学 | Method for recovering phosphorus in sludge and synchronously generating electricity by using bluestone generated by microbial fuel cell |
| CN115286073A (en) * | 2022-07-28 | 2022-11-04 | 禹州市瑞和智能科技有限公司 | Hydroxyl water catalyst efficient anti-blocking disinfection sink system |
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