CN111422954A - Advanced wastewater treatment method and system for realizing sludge source reduction - Google Patents
Advanced wastewater treatment method and system for realizing sludge source reduction Download PDFInfo
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Abstract
The invention discloses a wastewater advanced treatment method and a system for realizing sludge source reduction, wherein wastewater firstly enters a first acid-base adjusting tank, a sulfuric acid solution is added to adjust the pH value to 3-5, then the wastewater enters an electro-Fenton reactor to carry out Fenton advanced oxidation, and an aeration device aerates a cathode; and after the electro-Fenton reaction is finished, the effluent enters a second acid-base adjusting tank, the pH value is adjusted to 7-9 by adding a sodium hydroxide solution, and then the effluent enters an electrochemical reaction unit for treatment to finish the advanced treatment of the wastewater. The invention has wide application range and is suitable for the advanced treatment of different sewage.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a wastewater advanced treatment method and a system for realizing sludge source reduction.
Background
With the improvement of water treatment standard, an advanced treatment process is generally required to be added after the traditional biochemical method, and the Fenton method as an efficient and stable advanced treatment method for wastewater gradually occupies a main position in engineering treatment, and the effluent can stably reach the standard. However, the traditional fenton method has more problems: (1) the sludge yield is high, and a large amount of generated iron sludge needs to be further treated; (2) the operation cost is high, the medicament cost is high, and the sludge treatment cost also brings no small economic burden to enterprises; (3) difficulty in operation management, H2O2Potential safety hazards exist in the transportation, storage and addition processes; (4) the efficiency of the latter reaction period becomes low, and Fe proceeds with the progress of the Fenton reaction2+Conversion to Fe3+Ferric iron floc is generated, and the whole oxidation process becomes slow.
The electro-Fenton method is Fe produced by electrochemical method2+And H2O2As a continuous source of the Fenton reagent, the two reagents act immediately after being generated to generate hydroxyl radicals with high activity so as to degrade organic matters, and the essence is that the Fenton reagent is directly generated in the electrolytic process. Compared with the traditional Fenton method, the electro-Fenton method has the unique advantages that: (1) a small amount of chemical agent is not needed or only needed to be added, so that the treatment cost can be greatly reduced; (2) the treatment process is clean and does not cause secondary pollution to water quality; (3) the equipment is relatively simple, and parameters to be controlled in the electrolysis process only comprise current and voltage, so that automatic control is easy to realize; (4) fe in electro-Fenton process2+And H2O2The sludge is continuously generated at a considerable rate, so that long-time continuous and effective degradation is guaranteed, organic matters can be more completely oxidized, the sludge amount is small, and the post-treatment is simple; (5) small occupied area and short processing period. The electrochemical method is a chemical action that pollutants are subjected to direct electrochemical reaction or indirect electrochemical conversion on an electrode under the action of current, has the advantages of wide application range, simple process, convenient operation and the like, and has some problems in practical use, such as pollutant decompositionIncomplete, thus leading to the electrochemical process being less useful in wastewater treatment. The existing electro-Fenton also has the problems of low current efficiency and unstable treatment efficiency in practical application, and can not discharge the wastewater up to the standard only by using the electro-Fenton method for certain high-concentration wastewater difficult to treat.
The existing method does not reduce the generation of sludge from the source; an iron source needs to be added, the system is complex in structure, and the operation and maintenance are complex; the flocculation effect is not good, and the sewage treatment effect is unknown; the electro-Fenton and electrochemical methods have the problems of incomplete treatment, low efficiency and large sludge yield, and certain electro-Fenton methods need additional medicaments, are complex in device and are complex to operate.
Disclosure of Invention
The invention aims to solve the technical problems of insufficient electro-Fenton and electrochemical treatment, low efficiency and high sludge yield.
The invention adopts the following technical scheme:
a wastewater advanced treatment method for realizing sludge source reduction comprises the following steps:
s1, enabling the wastewater to enter a first acid-base adjusting tank, adding a sulfuric acid solution to adjust the pH value to 3-5, then entering an electro-Fenton reactor to carry out Fenton deep oxidation, and aerating the cathode by an aerating device;
s2, after the electro-Fenton reaction in the step S1 is finished, enabling the effluent to enter a second acid-base adjusting tank, adding a sodium hydroxide solution to adjust the pH value to 7-9, and then entering an electrochemical reaction unit to be treated, so that the advanced treatment of the wastewater is finished.
Specifically, in step S1, the electro-Fenton reaction time is 30-70 min, the voltage is 3-7V, the current is 30-300 mA, and the aeration amount is 1.0-2.5 m3/h。
Further, under acidic conditions, iron is anodized to produce Fe2+Cathodic aeration oxygen reduction to produce H2O2The cathode adopts an active carbon fiber plate or an active carbon fiber net, Fe2+And H2O2Reaction to produce Fenton's reagentGeneration of Fe3+Moves to the cathode under the action of an electric field, and obtains electrons to be reduced into Fe2+Regenerated Fe2+Is continued with H2O2The reaction continues to produce Fenton's reagent.
Specifically, in step S2, the time of the electrochemical reaction is 20-60 min, the voltage is 1-6V, and the current is 20-100 mA.
Further, the reaction process mainly based on the electric flocculation is specifically as follows:
iron or aluminum is used as an anode, stainless steel or graphite is used as a cathode, the anode is corroded under the action of direct current to generate Al and Fe ions, and colloidal impurities and suspended impurities in the wastewater are coagulated, precipitated and separated after hydrolysis, polymerization and ferrous oxidation processes.
Further, the reaction process mainly based on the electro-oxidation is specifically as follows:
titanium is used as an anode, stainless steel or graphite is used as a cathode, and oxidation or sterilization and disinfection treatment are carried out on the wastewater;
furthermore, the titanium anode adopts an iridium tantalum titanium electrode, a nano platinum titanium electrode or a lead titanium dioxide anode which mainly uses oxygen evolution to fully oxidize the wastewater; adopts ruthenium iridium titanium anode and ruthenium iridium tin titanium anode which mainly separate chlorine to fully sterilize and disinfect the wastewater.
Further, the reaction process mainly comprising the electric floating is specifically as follows:
graphite is used as an anode and a cathode, and suspended matters, oil drops and/or organic pollutants in sewage or wastewater are separated through the floating action of micro bubbles generated during the working of the electrodes.
According to another technical scheme, the system for advanced wastewater treatment for realizing sludge source reduction is characterized by comprising an electro-Fenton reaction unit and an electrochemical reaction unit which are sequentially connected, wherein the electro-Fenton reaction unit generates Fe by means of electrode reaction2+And H2O2Fe produced by the reaction as a raw material for the Fenton reaction3+The cathodic regeneration is carried out to ensure that the Fenton reaction is continuously carried out, and the electrochemical reaction unit is one or two of electric flocculation, electric oxidation and electric air flotation according to the quality of wastewaterOr more than two of the raw materials are combined, the iron or the aluminum is used as an anode, and the stainless steel or the graphite is used as a cathode for the electric flocculation; the electrooxidation uses titanium as an anode, stainless steel or graphite as a cathode, and the electroflotation uses graphite as the anode and the cathode.
Specifically, the electro-Fenton reaction unit comprises a first acid-base regulating tank, an electro-Fenton reactor, a second acid-base regulating tank and an aeration device which are sequentially connected; production of Fe in an electro-Fenton reactor2+Produce H2O2And the Fenton reaction is integrated in a reaction tank.
Compared with the prior art, the invention has at least the following beneficial effects:
the advanced wastewater treatment method for realizing sludge source reduction can greatly reduce the dosage and save the operating cost; fe2+ can be regenerated circularly without adding iron salt, so that the sludge yield is greatly reduced; the treatment efficiency is high, and besides the oxidation effect of hydroxyl radicals, the treatment also has the electric flocculation effect, the electric oxidation effect and the electric floating effect of an electrochemical reaction unit; the process is short, the equipment structure is simple, and the operation is convenient.
Furthermore, the electro-Fenton combined electrochemical method has higher treatment efficiency, not only has the oxidation effect of directly generating a large amount of hydroxyl radicals in the electrolytic process, but also has the electro-flocculation effect, the electro-oxidation effect and the electro-flotation effect of the electrochemical reaction unit, and can further remove COD (chemical oxygen demand), SS (suspended solid) and total phosphorus by selectively carrying out electrochemical reaction according to the water quality condition, thereby improving the treatment efficiency and leading the effluent to reach the primary standard of the comprehensive sewage discharge standard.
Further, if SS in the wastewater exceeds the standard after the electro-Fenton reaction is finished, an electric flocculation unit can be selected to be started, iron or aluminum is used as an anode, stainless steel or graphite is used as a cathode, the anode is corroded under the action of direct current to generate Al, Fe and other ions, and the ions are developed into various hydroxyl complexes and hydroxides through a series of hydrolysis, polymerization and ferrous oxidation processes, so that residual colloidal impurities and suspended impurities in the wastewater are coagulated, precipitated and separated.
Further, if COD or total phosphorus in the wastewater exceeds the standard after the electro-Fenton reaction is finished, an electro-oxidation unit can be selectively started, and in the reaction process mainly based on electro-oxidation, titanium is used as an anode, stainless steel or graphite is used as a cathode, preferably, the titanium anode can be an iridium tantalum titanium electrode, a nano platinum titanium electrode, a lead titanium dioxide anode or a ruthenium iridium titanium electrode which mainly generate oxygen, so that the wastewater is fully oxidized; or the iridium tantalum titanium electrode mainly used for chlorine separation can be used for fully oxidizing, sterilizing and disinfecting the wastewater.
Furthermore, if SS or petroleum in the wastewater exceeds the standard after the electro-Fenton reaction is finished, the electric floatation unit can be selectively started, the reaction process mainly based on the electric floatation adopts graphite as an anode and a cathode, the electrodes generate micro bubbles during working, and suspended matters, oil drops, organic pollutants and the like in the sewage or the wastewater are separated through the floating action of the micro bubbles.
The utility model provides a realize system for advanced wastewater treatment of mud source minimizing, electro-Fenton combined electrochemical method treatment effeciency is higher, except the oxidation that the direct a large amount of hydroxyl free radicals of production of electrolysis process, the electricity flocculation, the electro-oxidation of electrochemistry unit, the electro-flotation carries out electrochemical reaction according to the selectivity of quality of water condition, can further get rid of COD, SS and total phosphorus, improves treatment effeciency, makes the play water reach the comprehensive emission standard one-level standard of sewage. The invention has wide application range and is suitable for the advanced treatment of different sewage.
Further, the electro-Fenton oxidation unit relies on the generation of Fe by electrode reactions2+And H2O2Fe produced by the reaction as a raw material for the Fenton reaction3+The regeneration is carried out at the cathode, the Fenton reaction can be ensured to be continuously carried out without adding an iron source and Fe3+Can be recycled, can greatly reduce the generation of iron-containing sludge and save the cost of the medicament.
In conclusion, the invention has wide application range and can be suitable for the advanced treatment of different sewage.
The technical solution of the present invention is further described in detail by the accompanying drawings and embodiments.
Drawings
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a schematic diagram of an electro-Fenton reaction unit according to the present invention.
Detailed Description
Referring to fig. 2, the present invention provides a wastewater advanced treatment system for sludge source reduction, which includes an electro-fenton reaction unit and an electrochemical reaction unit.
Selecting and determining a combination mode of an electro-Fenton reaction unit and an electrochemical reaction unit according to the water quality condition of the wastewater and the characteristics of pollutants, wherein the electro-Fenton reaction unit depends on Fe generated by electrode reaction2+And H2O2Fe produced by the reaction as a raw material for the Fenton reaction3+The regeneration is carried out at the cathode, the Fenton reaction can be ensured to be continuously carried out without adding an iron source and Fe3+The recycling can be realized, the generation of iron-containing sludge can be greatly reduced, and the medicament cost is saved; the electrochemical reaction unit is one or the combination of two or more than two of the processes of electric flocculation, electric oxidation and electric air floatation according to the quality of the wastewater.
The device comprises an electro-Fenton reaction unit and an electrochemical reaction unit, wherein the electro-Fenton reaction unit comprises a first acid-base adjusting tank, an electro-Fenton reactor, a second acid-base adjusting tank and an aeration device which are sequentially connected;
production of Fe in an electro-Fenton reactor2+Produce H2O2And the Fenton reaction is integrated in a reaction tank, and Fe is carried out under the acidic condition2+Produced by anodic oxidation, Fe-2e-→Fe2+，H2O2Produced by cathodic aeration reduction of O2+2e-+2H+→H2O2，Fe2+And H2O2Reaction to yield Fenton's reagent, H2O2+Fe2+→OH-+·OH+Fe3+Generation of Fe3+Moves to the cathode under the action of an electric field, and obtains electrons to be reduced into Fe2+，Fe3++e-→Fe2+Regenerated Fe2+Can continue to react with H2O2And (4) continuously generating Fenton reagent by reaction, and keeping the oxidation reaction in the reaction tank continuously going.
In the electrochemical flocculation in the electrochemical reaction unit, iron or aluminum is used as an anode, and stainless steel or graphite is used as a cathode; the electrooxidation uses titanium as an anode, stainless steel or graphite as a cathode, and the electroflotation uses graphite as the anode and the cathode.
Preferably, the titanium anode can be an iridium tantalum titanium electrode, a nano platinum titanium electrode, a lead titanium dioxide anode or a ruthenium iridium titanium electrode.
Referring to fig. 1, according to the advanced wastewater treatment method for sludge source reduction of the present invention, a combination of electro-fenton and electrochemical reaction units is selected and determined according to the wastewater quality and the characteristics of pollutants, and the reaction process of water in the electro-fenton reaction units is as follows:
s1, enabling the wastewater to enter a first acid-base adjusting tank, adding a sulfuric acid solution, adjusting the pH value to 3-5, then entering an electro-Fenton reactor for Fenton deep oxidation, and aerating the cathode by an aerating device;
under acidic conditions, Fe2+Produced by anodic oxidation of iron, H2O2Produced by cathode aeration oxygen reduction, the cathode adopts an active carbon fiber plate or an active carbon fiber net, Fe2+And H2O2Reaction to produce Fenton's reagent, Fe produced3+Moves to the cathode under the action of an electric field, and obtains electrons to be reduced into Fe2+Regenerated Fe2+Can continue to react with H2O2Reacting to continuously generate a Fenton reagent;
the electro-Fenton reaction time is 30-70 min, the voltage is 3-7V, the current is 30-300 mA, and the aeration amount is 1.0-2.5 m3/h。
And S2, after the electro-Fenton reaction is finished, enabling the effluent to enter a second acid-base adjusting tank, adding sodium hydroxide solution to adjust the pH value to 7-9, and then entering an electrochemical reaction unit for treatment.
Wherein, the time of the electrochemical reaction is 20-60 min, the voltage is 1-6V, and the current is 20-100 mA.
The reaction process of the wastewater in the electrochemical reaction unit is as follows:
s201, in a reaction process mainly based on electric flocculation, iron or aluminum is used as an anode, stainless steel or graphite is used as a cathode, the anode is corroded under the action of direct current to generate Al, Fe and other ions, and the Al, Fe and other ions are developed into various hydroxyl complexes and hydroxides through a series of hydrolysis, polymerization and ferrous oxidation processes, so that colloidal impurities and suspended impurities in wastewater are coagulated, precipitated and separated;
s202, a reaction process mainly comprising electro-oxidation, wherein titanium is used as an anode, stainless steel or graphite is used as a cathode,
preferably, the titanium anode can be an iridium tantalum titanium electrode, a nano platinum titanium electrode or a lead titanium dioxide anode which mainly uses oxygen evolution to fully oxidize the wastewater; or the ruthenium iridium titanium anode and the ruthenium iridium tin titanium anode which mainly analyze chlorine can be used for fully sterilizing and disinfecting the wastewater;
s203, in the reaction process mainly based on electro-flotation, graphite is used as an anode and a cathode, micro bubbles are generated when the electrodes work, and suspended matters, oil drops, organic pollutants and the like in the sewage or the wastewater are separated through the floating action of the micro bubbles.
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of the embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations. Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
1. The specific implementation process of the invention is described by taking the biochemical treatment effluent of a sewage treatment plant in a certain industrial park as an example:
the effluent quality of the biochemical treatment of a sewage treatment plant in a certain industrial park is shown in the following table 1:
TABLE 1 quality of wastewater in mg/L (except pH)
| The kind of contaminant | pH | COD | BOD5 | Suspended matter | Total phosphorus |
| Concentration of |
7 | 470 | 16 | 150 | 12 |
Example 1:
this main pollutant of waste water is COD, suspended solid and total phosphorus, this embodiment adopts electro-Fenton combination electric flocculation technology, waste water gets into electro-Fenton reaction unit, go into first acid-base equalizing basin earlier, add sulphuric acid solution, adjust pH value to 3, reentrant electro-Fenton reactor carries out the fenton degree of depth oxidation, aeration equipment is to the cathode aeration, the positive pole adopts iron plate, the active carbon fiber board is adopted to the negative pole, electro-Fenton reaction unit reaction time is 50min, voltage control is 4V, current control is 100mA, aeration flow control is 1.5m3After the electro-Fenton reaction is finished, the effluent enters a second acid-base adjusting tank, the pH value is adjusted to 7 by adding sodium hydroxide solution, then the effluent enters an electro-flocculation reaction unit, an aluminum plate is used as an anode, a stainless steel plate is used as a cathode, the electro-flocculation reaction time is 30min, the voltage is controlled to be 2V, the current is controlled to be 60mA, after the reaction is finished, the COD of the effluent is 37.6 mg/L, the suspended matters are 15 mg/L, the total phosphorus is 0.4 mg/L, and the mud yield is only 82g/m3And the effluent reaches the first-grade standard of comprehensive sewage discharge.
Comparative example 1:
this comparative example adopts ordinary fenton combination chemistry flocculation and precipitation method to handle the biochemical play water of certain industrial park sewage treatment plant, and waste water gets into the fenton reaction unit, adjusts pH value to 3, and reaction time is 50min, and the reentry chemistry flocculation and precipitation unit after the reaction is accomplished, and pH value is 7, and reaction time is 35min, and after the reaction was accomplished, the play water COD was 57.4 mg/L, and the suspended solid was 18.7 mg/L, and total phosphorus is 0.6 mg/L, and the mud production is 145.3g/m3And the effluent reaches the first-grade standard of comprehensive sewage discharge.
Comparative example 2:
this comparative example only adopts the electro-Fenton method to handle a certain industry garden sewage treatment plant biochemical treatment play water, waste water gets into the electro-Fenton reaction unit, go into first acid-base equalizing basin earlier, add sulphuric acid solution, adjust pH value to 3, reentrant electro-Fenton reactor carries out the fenton degree of depth oxidation, aeration equipment is to the cathode aeration, the positive pole adopts iron plate, the active carbon fiber board is adopted to the negative pole, electro-Fenton reaction unit reaction time is 50min, voltage control is 4V, current control is 120mA, aeration amount control is 1.8m3After the electro-Fenton reaction is finished, the effluent enters a second acid-base adjusting tank, the pH value is adjusted to 7 by adding sodium hydroxide liquid, the COD of the effluent is 53.4 mg/L, the suspended matters are 30.0 mg/L, the total phosphorus is 2.6 mg/L, and the sludge yield is only 37g/m3(ii) a Changing electro-Fenton reaction conditions, controlling reaction time at 60min, voltage at 5V, current at 150mA, and aeration amount at 2.0m3After the electro-Fenton reaction is finished, the effluent enters a second acid-base adjusting tank, the pH value is adjusted to 7 by adding sodium hydroxide liquid, the COD of the effluent is 46.2 mg/L, the suspended matters are 28.5 mg/L, the total phosphorus is 2.2 mg/L, and the sludge yield is 37.8g/m3(ii) a Changing electro-Fenton reaction conditions, controlling reaction time at 40min, voltage at 3V, current at 100mA, and aeration amount at 1.5m3After the electro-Fenton reaction is finished, the effluent enters a second acid-base adjusting tank, the pH value is adjusted to 7 by adding sodium hydroxide liquid, and the COD of the effluent is 56.2 mg/L, the suspended matters are 31.4 mg/L, the total phosphorus is 2.7 mg/L, and the sludge yield is 35.3g/m3；
Only adopting the electro-Fenton method, under different reaction conditions, the sludge yield is lower, but the effluent can not reach the first-grade standard of sewage comprehensive discharge. The electro-Fenton method has obvious effect of oxidizing COD and limited removal effect on SS, and the SS is mainly removed through flocculation and precipitation.
Comparative example 3:
this comparative example only adopts the electric flocculation method to handle a certain industrial park sewage treatment plant biochemical treatment effluent, and waste water gets into the electric flocculation reaction unit, and the positive pole adopts aluminum plate, and the negative pole adopts stainless steel plate, and the electric flocculation reaction time is 30min, and voltage control is 2V, and current control is 70mA, and after the reaction was accomplished, the play water COD is 141.0 mg/L, and the suspended solid is 20.8 mg/L, and total phosphorus is 3.2 mg/L, and the mud production is 62g/m3Only the electric flocculation method is adopted, and the effluent cannot reach the first-grade standard of the comprehensive sewage discharge. The electrocoagulation reaction does not generate oxidation, and has limited removal effect on COD.
The results from the above implementation gave: the sludge yield of the technology adopting electro-Fenton combined electro-flocculation is obviously lower than that of the technology adopting common Fenton combined chemical flocculation precipitation method; the embodiment only adopts the electro-Fenton method has the lowest mud yield, but the effluent quality fails to reach the standard; the effluent quality of the embodiment adopting only the electric flocculation method can not reach the standard.
2. Taking the effluent from biochemical treatment of sewage in a certain chemical plant as an example, the specific implementation process of the invention is described as follows:
the effluent quality of biochemical treatment of sewage in a certain chemical plant is shown in the following table 2:
TABLE 2 quality of wastewater in mg/L (except pH)
| The kind of contaminant | pH | COD | BOD5 | Suspended matter | Total phosphorus |
| Concentration of contaminants | 8 | 680 | 18 | 90 | 11 |
Example 2:
this main pollutant of waste water is COD, suspended solid and total phosphorus, COD content is higher, this embodiment adopts electro-Fenton combination electrooxidation + electroflocculation technology, waste water gets into electro-Fenton reaction unit, first acid-base equalizing basin gets into earlier, sulphuric acid solution, adjust pH value to 3, reentrant electro-Fenton reactor carries out the fenton degree of depth oxidation, aeration equipment is to the cathode aeration, the positive pole adopts iron plate, the negative pole adopts the activated carbon fiber board, electro-Fenton reaction unit reaction time is 50min, voltage control is 4V, current control is 120mA, aeration rate control is 1.8m3After electro-Fenton reaction is finished, effluent enters a second acid-base adjusting tank, the pH value is adjusted to 7 by adding sodium hydroxide liquid, then the effluent enters an electro-oxidation reaction unit, an iridium-tantalum-titanium electrode is adopted as an anode, a graphite cathode is adopted as a cathode, the electro-oxidation reaction time is 30min, the voltage is controlled to be 3V, the current is controlled to be 80mA, finally the effluent enters an electro-flocculation reaction unit, an aluminum plate is adopted as the anode, a stainless steel plate is adopted as the cathode, the electro-flocculation reaction time is 30min, the voltage is controlled to be 2V, the current is controlled to be 60mA, after the reaction is finished, the effluent COD (chemical oxygen demand) is 29.1 mg/L, the suspended matters are 18.0 mg/L, the total phosphorus is 0.43 mg/L, and the sludge production3And the effluent reaches the first-grade standard of comprehensive sewage discharge.
Comparative example 4:
this comparative example used ordinary FentonThe effluent of biochemical treatment of sewage of a certain chemical plant is treated by combining a chemical flocculation precipitation method, the wastewater enters a Fenton reaction unit, the pH value is adjusted to 3, the reaction time is 50min, the wastewater enters the chemical flocculation precipitation unit after the reaction is finished, the pH value is adjusted to 7, the reaction time is 35min, the COD of the effluent is 72.8 mg/L, the suspended matters are 26.7 mg/L, the total phosphorus is 0.5 mg/L, and the sludge production is 162.1g/m3And the effluent reaches the first-grade standard of comprehensive sewage discharge.
Comparative example 5:
this comparative example only adopts the electro-Fenton method to handle a certain chemical plant sewage biochemical treatment effluent, waste water gets into the electro-Fenton reaction unit, go into first acid-base equalizing basin earlier, add sulphuric acid solution, adjust pH value to 3, reentrant electro-Fenton reactor carries out the fenton degree of depth oxidation, aeration equipment is to the negative pole aeration, the positive pole adopts iron plate, the negative pole adopts activated carbon fiber plate, the reaction time of electro-Fenton reaction unit is 50min, voltage control is 4V, current control is 120mA, aeration amount control is 1.8m3After electro-Fenton reaction is finished, the effluent enters a second acid-base adjusting tank, the pH value is adjusted to 7 by adding sodium hydroxide liquid, the COD of the effluent is 66.4 mg/L, the suspended matters are 30.5 mg/L, the total phosphorus is 2.1 mg/L, and the sludge yield is only 43g/m3(ii) a Changing the electro-Fenton reaction conditions, controlling the reaction time of the electro-Fenton reaction unit to be 40min, controlling the voltage to be 3V, controlling the current to be 100mA, and controlling the aeration amount to be 1.5m3After the electro-Fenton reaction is finished, the effluent enters a second acid-base adjusting tank, the pH value is adjusted to 7 by adding sodium hydroxide liquid, the COD of the effluent is measured to be 78.5 mg/L, the suspended matters are 36.2 mg/L, the total phosphorus is 2.4 mg/L, and the sludge yield is 40.7g/m3. Changing the electro-Fenton reaction conditions, controlling the reaction time of the electro-Fenton reaction unit to be 60min, controlling the voltage to be 6V, controlling the current to be 150mA, and controlling the aeration amount to be 2.0m3After the electro-Fenton reaction is finished, the effluent enters a second acid-base adjusting tank, the pH value is adjusted to 7 by adding sodium hydroxide liquid, the COD of the effluent is 62.9 mg/L, the suspended matters are 33.1 mg/L, the total phosphorus is 2.0 mg/L, and the sludge yield is 45.5g/m3。
Only adopting the electro-Fenton method, under different reaction conditions, the sludge yield is lower, but the effluent can not reach the first-grade standard of sewage comprehensive discharge.
Comparative example 6:
in the comparative example, only an electrooxidation method is adopted to treat the effluent of biochemical treatment of sewage of a certain chemical plant, the wastewater enters an electrooxidation reaction unit, an iridium-tantalum-titanium electrode is adopted as an anode, a graphite cathode is adopted as a cathode, the time of an electroflocculation reaction is 30min, the voltage is controlled to be 3V, the current is controlled to be 80mA, after the reaction is finished, the COD of the effluent is 163.7 mg/L, the suspended solids are 23.8 mg/L, the total phosphorus is 2.8 mg/L, and the sludge production is 37g/m3Only adopting an electrooxidation method, the effluent can not reach the first-grade standard of sewage comprehensive discharge.
The results from the above implementation gave: the effluent of the embodiment adopting the Fenton combined electrooxidation and electroflocculation process can reach the first-level standard of sewage comprehensive discharge, and the sludge yield is obviously lower than that of the embodiment adopting the common Fenton combined chemical flocculation precipitation process; the embodiment only adopts the electrooxidation method has the lowest sludge production amount, but the effluent quality fails to reach the standard; the effluent quality of the embodiment adopting only the electro-Fenton method can not reach the standard.
In conclusion, the advanced wastewater treatment method for realizing sludge source reduction, disclosed by the invention, has the advantages that the Fenton reaction unit is integrated with the anodic oxidation to produce Fe2+And cathode to produce H2O2、Fe3+The reduction, circulation and regeneration are integrated, an iron source is not required to be added, and the sludge yield can be greatly reduced. And then the electrochemical reaction unit is combined to further treat the unreacted and complete pollutants in the wastewater, the selective starting of electrooxidation with high COD content and the selective electroflocculation or electroflotation with high SS content are realized, the electrochemical reaction unit does not need to add an additional medicament, the whole system realizes self-circulation, the sludge source reduction in the advanced wastewater treatment can be realized, and the effluent can stably reach the standard after the treatment is finished. The reaction sequence of electro-Fenton and electrochemistry, the number of reactors and the combination mode can be flexibly adjusted according to different water quality conditions, the device has compact structure and simple operation and maintenance.
The above-mentioned contents are only for illustrating the technical idea of the present invention, and the protection scope of the present invention is not limited thereby, and any modification made on the basis of the technical idea of the present invention falls within the protection scope of the claims of the present invention.
Claims (10)
1. A wastewater advanced treatment method for realizing sludge source reduction is characterized by comprising the following steps:
s1, enabling the wastewater to enter a first acid-base adjusting tank, adding a sulfuric acid solution to adjust the pH value to 3-5, then entering an electro-Fenton reactor to carry out Fenton deep oxidation, and aerating the cathode by an aerating device;
s2, after the electro-Fenton reaction in the step S1 is finished, enabling the effluent to enter a second acid-base adjusting tank, adding a sodium hydroxide solution to adjust the pH value to 7-9, and then entering an electrochemical reaction unit to be treated, so that the advanced treatment of the wastewater is finished.
2. The advanced wastewater treatment method for realizing sludge source reduction according to claim 1, wherein in step S1, the electro-Fenton reaction time is 30-70 min, the voltage is 3-7V, the current is 30-300 mA, and the aeration rate is 1.0-2.5 m3/h。
3. The method for deeply treating wastewater with reduced sludge source as claimed in claim 2, wherein iron is anodized to generate Fe under acidic condition2+Cathodic aeration oxygen reduction to produce H2O2The cathode adopts an active carbon fiber plate or an active carbon fiber net, Fe2+And H2O2Reaction to produce Fenton's reagent, Fe produced3+Moves to the cathode under the action of an electric field, and obtains electrons to be reduced into Fe2+Regenerated Fe2+Is continued with H2O2The reaction continues to produce Fenton's reagent.
4. The advanced wastewater treatment method for realizing sludge source reduction according to claim 1, wherein in step S2, the time of electrochemical reaction is 20-60 min, the voltage is 1-6V, and the current is 20-100 mA.
5. The advanced wastewater treatment method for realizing sludge source reduction according to claim 4, wherein the reaction process mainly based on electric flocculation is as follows:
iron or aluminum is used as an anode, stainless steel or graphite is used as a cathode, the anode is corroded under the action of direct current to generate Al and Fe ions, and colloidal impurities and suspended impurities in the wastewater are coagulated, precipitated and separated after hydrolysis, polymerization and ferrous oxidation processes.
6. The advanced wastewater treatment method for realizing sludge source reduction according to claim 4, wherein the reaction process mainly based on electro-oxidation comprises the following specific steps:
titanium is used as an anode, stainless steel or graphite is used as a cathode, and oxidation or sterilization and disinfection treatment are carried out on the wastewater.
7. The advanced wastewater treatment method for realizing sludge source reduction according to claim 6, wherein the titanium anode adopts an iridium tantalum titanium electrode, a nano platinum titanium electrode or a lead titanium dioxide anode which mainly adopts oxygen evolution to fully oxidize the wastewater; adopts ruthenium iridium titanium anode and ruthenium iridium tin titanium anode which mainly separate chlorine to fully sterilize and disinfect the wastewater.
8. The advanced wastewater treatment method for realizing sludge source reduction according to claim 4, wherein the reaction process mainly based on electro-flotation comprises:
graphite is used as an anode and a cathode, and suspended matters, oil drops and/or organic pollutants in sewage or wastewater are separated through the floating action of micro bubbles generated during the working of the electrodes.
9. The system for advanced wastewater treatment for sludge source reduction according to claim 1, comprising an electro-Fenton reaction unit and an electrochemical reaction unit which are connected in sequence, wherein the electro-Fenton reaction unit generates Fe by means of electrode reaction2+And H2O2Fe produced by the reaction as a raw material for the Fenton reaction3+The cathodic regeneration is used for ensuring the continuous operation of the Fenton reaction, and the electrochemical reaction unit is electrocoagulation and electrooxidation according to the quality of the wastewaterOne, two or more than two of chemical flotation and electric flotation are combined, electric flocculation takes iron or aluminum as an anode, and stainless steel or graphite as a cathode; the electrooxidation uses titanium as an anode, stainless steel or graphite as a cathode, and the electroflotation uses graphite as the anode and the cathode.
10. The wastewater depth system for realizing sludge source reduction according to claim 9, wherein the electro-Fenton reaction unit comprises a first acid-base adjusting tank, an electro-Fenton reactor, a second acid-base adjusting tank and an aeration device which are connected in sequence; production of Fe in an electro-Fenton reactor2+Produce H2O2And the Fenton reaction is integrated in a reaction tank.
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