CN216687821U - Synchronous desulfurization denitrification nitrogen removal coupling electrochemistry dephosphorization system - Google Patents
Synchronous desulfurization denitrification nitrogen removal coupling electrochemistry dephosphorization system Download PDFInfo
- Publication number
- CN216687821U CN216687821U CN202122993217.5U CN202122993217U CN216687821U CN 216687821 U CN216687821 U CN 216687821U CN 202122993217 U CN202122993217 U CN 202122993217U CN 216687821 U CN216687821 U CN 216687821U
- Authority
- CN
- China
- Prior art keywords
- activated carbon
- biological filler
- valve
- desulfurization denitrification
- pump
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Water Treatment By Sorption (AREA)
Abstract
The utility model discloses a synchronous desulfurization denitrification coupling electrochemical phosphorus removal system, and relates to the technical field of water environment treatment and sewage treatment. The water inlet system is connected with the ceramic membrane activated carbon absorber, the activated carbon dosing system is communicated with the ceramic membrane activated carbon absorber, the activated carbon recycling system is connected with the ceramic membrane activated carbon absorber, the water outlet of the ceramic membrane activated carbon absorber is connected with the water inlet of the aerobic biological filler system, the water outlet of the aerobic biological filler system is communicated with the water inlet of the anoxic biological filler system, the water outlet of the anoxic biological filler system is communicated with the synchronous desulfurization and denitrification system, the synchronous desulfurization and denitrification system is communicated with the electrochemical phosphorus removal system, and the electrochemical phosphorus removal system is communicated with the precipitation system. The utility model can remove nitrogen, phosphorus and other nutrient elements in the water body, has obvious denitrification and dephosphorization effects, effectively treats water pollution, reduces water eutrophication and black and odorous risks, has important significance on water ecological safety in China and has wide application prospect.
Description
Technical Field
The utility model relates to the technical field of water environment treatment and sewage treatment, in particular to a synchronous desulfurization denitrification coupling electrochemical phosphorus removal system.
Background
The economy of China is rapidly developed, the living standard of people is improved, the discharge amount of domestic sewage is greatly increased, the treatment energy of a sewage treatment plant is insufficient, part of sewage treatment does not reach the standard, the treated sewage is discharged into landscape water bodies or natural water bodies, a large amount of nutrient elements such as nitrogen, phosphorus and the like can cause water body eutrophication and even black and odorous, and therefore, in order to prevent water body eutrophication and guarantee water ecological safety, the nitrogen removal and the phosphorus removal of the polluted water body in the water environment treatment process are imperative.
The conventional biological denitrification needs to have sufficient organic carbon sources, but the treated domestic sewage, polluted natural water or landscape water has relatively high nitrogen and phosphorus contents, the content of available organic matters of microorganisms is low, and the C/N of the water is low, so the denitrification effect of the sewage with low C/N is poor, and a large amount of organic carbon sources need to be added in the process of low C/N denitrification, thereby increasing the sewage treatment cost. Meanwhile, organic matters are consumed in the biological phosphorus removal process, so that the low C/N sewage needs to be subjected to both nitrogen removal and phosphorus removal, the effect is difficult to guarantee, and the biological phosphorus removal is influenced by factors such as temperature and pH and has larger fluctuation.
In order to make up for the defects of the conventional biological nitrogen and phosphorus removal technology, it is particularly necessary to develop a synchronous desulfurization denitrification nitrogen removal coupled electrochemical phosphorus removal system.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects in the prior art, the utility model aims to provide a synchronous desulfurization denitrification coupling electrochemical phosphorus removal system which is reasonable in structural design, effectively removes nitrogen, phosphorus and other nutrient elements in a water body, controls water pollution, reduces water eutrophication and black and odorous risks, has important significance on water ecological safety in China and is easy to popularize and use.
In order to achieve the purpose, the utility model is realized by the following technical scheme: a synchronous desulfurization denitrification coupling electrochemical phosphorus removal system comprises a ceramic membrane activated carbon adsorption system, a biological filler system, a synchronous desulfurization denitrification coupling electrochemical phosphorus removal system and a temperature control system, wherein the ceramic membrane activated carbon adsorption system consists of a water inlet system, a ceramic membrane activated carbon adsorber, an activated carbon dosing system and an activated carbon recycling system; the water inlet system is connected with the ceramic membrane activated carbon absorber, the activated carbon dosing system is communicated with the ceramic membrane activated carbon absorber, the activated carbon recycling system is connected with the ceramic membrane activated carbon absorber, the water outlet of the ceramic membrane activated carbon absorber is connected with the water inlet of the aerobic biological filler system, the water outlet of the aerobic biological filler system is communicated with the water inlet of the anoxic biological filler system, the water outlet of the anoxic biological filler system is communicated with the synchronous desulfurization denitrification system, the synchronous desulfurization denitrification system is communicated with the electrochemical phosphorus removal system, and the electrochemical phosphorus removal system is communicated with the precipitation system; the aerobic biological filler system, the anoxic biological filler system and the synchronous desulfurization denitrification system are respectively provided with an aerobic temperature controller, an anoxic temperature controller and a desulfurization denitrification temperature controller, and the aerobic temperature controller, the anoxic temperature controller and the desulfurization denitrification temperature controller are all connected to a temperature control center.
Preferably, the water inlet system comprises a grating, a water inlet pipeline, a pressurizing lift pump, a first valve and a connecting pipeline, the ceramic membrane activated carbon adsorber comprises a tank body and a ceramic membrane, the activated carbon dosing system comprises an activated carbon dosing barrel, a first stirrer, a first dosing pump and a second valve, and the activated carbon recycling system comprises a third valve, a recycling pump, an activated carbon collecting tank and a first sludge pump; the grid is installed in water intake system's water inlet department, and the water inlet connects to the import of pressurization elevator pump through the inlet channel, and the export of pressurization elevator pump connects to the cell body through the connecting tube, installs first valve on the connecting tube, the cell body in be provided with ceramic membrane, the export of active carbon dosing bucket connects to the cell body through first dosing pump, installs the second valve on the pipeline that first dosing pump and cell body are connected, installs first agitator in the active carbon dosing bucket, the cell body connect to the active carbon collecting pit through third valve, recycle pump, install first sludge pump in the active carbon collecting pit, first sludge pump connects to the active carbon dosing bucket.
Preferably, the aperture of the ceramic membrane in the ceramic membrane activated carbon adsorber is 1 μm, and the size of the added activated carbon particles is 800-1000 meshes, so that the ceramic membrane can effectively intercept the activated carbon particles after the activated carbon particles adsorb pollutants in a water body, and the purpose of removing the pollutants is achieved.
Preferably, the aerobic biological filler system consists of a nano aeration device, a fourth valve, an aerobic reaction tank, an aerobic biological filler and an aeration head, wherein the aerobic reaction tank is connected with a water outlet of a tank body in the ceramic membrane activated carbon absorber through the fourth valve; the anoxic biological filler system consists of an anoxic reaction tank, anoxic biological fillers and a fifth valve, wherein the anoxic reaction tank is connected to a water outlet of the aerobic reaction tank through the fifth valve, the anoxic biological fillers are arranged in the anoxic reaction tank, and an anoxic temperature controller is also arranged in the anoxic reaction tank.
Preferably, the aerobic biological filler and the anoxic biological filler adopt carbon fiber biological fillers, and have the characteristics of strong adsorption effect, strong microbial affinity and high film forming speed.
Preferably, the synchronous desulfurization and denitrification system comprises a synchronous desulfurization and denitrification reactor, a multi-tooth stirrer, an exhaust hole, a first water pump, a sixth valve, FeS ore filler and spherical biological filler, wherein the synchronous desulfurization and denitrification reactor adopts a water inlet mode of feeding water from top to bottom, the synchronous desulfurization and denitrification reactor is filled with the FeS ore filler and the spherical biological filler, the filler in the synchronous desulfurization and denitrification reactor is divided into two parts, the upper layer is provided with FeS ore filler, the lower layer is provided with spherical biological filler, the two layers of fillers are separated by stainless steel metal grids, the side wall of the synchronous desulfurization and denitrification reactor is provided with a FeS ore inlet and a FeS ore outlet at the corresponding position of the FeS ore filler on the upper layer, and the side wall of the synchronous desulfurization and denitrification reactor is provided with a spherical biological filler inlet and a spherical biological filler outlet at the corresponding position of the spherical biological filler on the lower layer. A multi-tooth stirrer for fully stirring the FeS ore filler and the spherical biological filler is arranged on the synchronous desulfurization denitrification reactor, an exhaust hole for discharging nitrogen generated by denitrification is formed in the top end of the synchronous desulfurization denitrification reactor, and a water inlet of the synchronous desulfurization denitrification reactor is connected to a water outlet of an anoxic reaction tank in an anoxic biological filler system through a first water pump and a sixth valve; and a desulfurization denitrification temperature controller is also arranged in the synchronous desulfurization denitrification reactor.
Preferably, the electrochemical phosphorus removal system comprises an electrochemical phosphorus removal reactor, a Fe anode plate, an AL cathode plate, a second stirrer, a current stabilizer, a third stirrer, a PAM dosing barrel, a second dosing pump, a seventh valve and an eighth valve, wherein the electrochemical phosphorus removal reactor is connected to a water outlet of the synchronous desulfurization denitrification reactor in the synchronous desulfurization denitrification system through the eighth valve, the second stirrer is installed on the electrochemical phosphorus removal reactor, the Fe anode plate and the AL cathode plate which are uniformly arranged at intervals are arranged in the electrochemical phosphorus removal reactor, the interval between the Fe anode plate and the AL cathode plate is cm, the electrochemical phosphorus removal reactor is connected with the current stabilizer, the electrochemical phosphorus removal reactor is connected to the PAM dosing barrel through the second dosing pump and the seventh valve, and the third stirrer is installed on the PAM dosing barrel.
Preferably, the sedimentation system consists of a ninth valve, a second water pump, a sedimentation tank, a tenth valve, an eleventh valve and a second sludge pump, a water outlet of the electrochemical phosphorus removal reactor in the electrochemical phosphorus removal system is connected to the sedimentation tank through the ninth valve and the second water pump, the sedimentation tank is connected with the tenth valve for treating water discharge, and the bottom of the sedimentation tank is connected with the eleventh valve through the second sludge pump.
The utility model has the beneficial effects that: the system can remove nutrient elements such as nitrogen, phosphorus and the like in the water body, has obvious denitrification and dephosphorization effects, reduces COD concentration and heavy metal content in the water body, effectively treats water pollution, reduces water eutrophication and black and odorous risks, has relatively simple equipment maintenance, effectively reduces operation cost, has important significance on water ecological safety in China and has wide application prospect.
Drawings
The utility model is described in detail below with reference to the drawings and the detailed description;
FIG. 1 is a schematic connection diagram of a ceramic membrane-activated carbon adsorption system, a biological filler system, a synchronous desulfurization and denitrification system and a temperature control system according to the present invention;
FIG. 2 is a schematic view of the connection between the electrochemical phosphorus removal system and the precipitation system according to the present invention;
FIG. 3 is a schematic structural diagram of a synchronous desulfurization and denitrification reactor in the synchronous desulfurization and denitrification system according to the present invention;
FIG. 4 is a process flow diagram of the synchronous desulfurization denitrification coupled electrochemical phosphorus removal method of the present invention.
Detailed Description
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the utility model easy to understand, the utility model is further described with the specific embodiments.
Referring to fig. 1 to 4, the following technical solutions are adopted in the present embodiment: a synchronous desulfurization denitrification coupling electrochemical dephosphorization system, which comprises a ceramic membrane-active carbon adsorption system, a biological filler system, a synchronous desulfurization denitrification coupling electrochemical dephosphorization system and a temperature control system 10, the ceramic membrane-active carbon adsorption system consists of a water inlet system 1, a ceramic membrane-active carbon adsorber 2, an active carbon dosing system 3 and an active carbon recycling system 4, the biological filler system consists of an aerobic biological filler system 5 and an anoxic biological filler system 6, the synchronous desulfurization denitrification coupling electrochemical phosphorus removal system consists of a synchronous desulfurization denitrification system 7, an electrochemical phosphorus removal system 8 and a precipitation system 9, the temperature control system 10 consists of a temperature control center 10-1, an aerobic temperature controller 10-2, an anoxic temperature controller 10-3 and a desulfurization and denitrification temperature controller 10-4.
The water inlet system 1 is connected with the ceramic membrane-activated carbon adsorber 2, the activated carbon dosing system 3 is communicated with the ceramic membrane-activated carbon adsorber 2, the activated carbon dosing system 3 is used for adding activated carbon particles into the ceramic membrane-activated carbon adsorber 2, the activated carbon recycling system 4 is connected with the ceramic membrane-activated carbon adsorber 2, and the activated carbon recycling system 4 is used for collecting pollutants, adsorbing saturated activated carbon, and recycling the adsorbed activated carbon after regeneration; the water outlet of the ceramic membrane-activated carbon adsorber 2 is connected with the water inlet of an aerobic biological filler system 5, the water outlet of the aerobic biological filler system 5 is communicated with the water inlet of an anoxic biological filler system 6, the water outlet of the anoxic biological filler system 6 is communicated with a synchronous desulfurization denitrification system 7, the synchronous desulfurization denitrification system 7 is communicated with an electrochemical phosphorus removal system 8, the electrochemical phosphorus removal system 8 is communicated with a precipitation system 9, after the polluted water body is treated, the polluted water body is discharged according to the requirement, and the sludge is transported outside after being dehydrated; the aerobic biological filler system 5, the anoxic biological filler system 6 and the synchronous desulfurization denitrification system 7 are respectively provided with an aerobic temperature controller 10-2, an anoxic temperature controller 10-3 and a desulfurization denitrification temperature controller 10-4, the aerobic temperature controller 10-2, the anoxic temperature controller 10-3 and the desulfurization denitrification temperature controller 10-4 are all connected to a temperature control center 10-1, and the microorganisms in the system are ensured to be in the optimum reaction temperature state by controlling the temperature.
Specifically, the composition architecture and connection relationship of each system are as follows:
(1) the water inlet system 1 comprises a grating 1-1, a water inlet pipeline 1-2, a pressurizing lift pump 1-3, a first valve 1-4 and a connecting pipeline 1-5, the ceramic membrane-activated carbon adsorber 2 comprises a tank body 2-1 and a ceramic membrane 2-2, the activated carbon dosing system 3 consists of an activated carbon dosing barrel 3-1, a first stirrer 3-2, a first dosing pump 3-3 and a second valve 3-4, and the activated carbon recycling system 4 consists of a third valve 4-1, a recycling pump 4-2, an activated carbon collecting tank 4-3 and a first pump sludge 4-4; the grid 1-1 is arranged at the water inlet of the water inlet system 1, the suspended matters in the water body are removed through the grid 1-1, and the pressurizing lift pump 1-3 is arranged between the water inlet and outlet pipelines and is communicated with the ceramic membrane-activated carbon system: a water inlet is connected to an inlet of a pressurizing lift pump 1-3 through a water inlet pipeline 1-2, an outlet of the pressurizing lift pump 1-3 is connected to a pool body 2-1 through a connecting pipeline 1-5, a first valve 1-4 is installed on the connecting pipeline 1-5, a ceramic membrane 2-2 is arranged in the pool body 2-1, an outlet of an active carbon dosing barrel 3-1 is connected to the pool body 2-1 through a first dosing pump 3-3, a second valve 3-4 is installed on a pipeline connecting the first dosing pump 3-3 with the pool body 2-1, a first stirrer 3-2 is installed in the active carbon dosing barrel 3-1, the pool body 2-1 is connected to an active carbon collecting pool 4-3 through a third valve 4-1 and a recovery pump 4-2, a first sludge pump 4-4 is installed in the active carbon collecting pool 4-3, the first sludge pump 4-4 is connected to the activated carbon dosing barrel 3-1.
It is worth noting that the aperture of the ceramic membrane 2-2 in the ceramic membrane-activated carbon adsorber 2 is 1 μm, the size of the added activated carbon particles is 800-1000 meshes, and after the activated carbon particles are ensured to adsorb pollutants in a water body, the ceramic membrane 2-2 can effectively intercept the activated carbon particles, so as to achieve the purpose of removing the pollutants.
(2) The aerobic biological filler system 5 consists of a nano aeration device 5-1, a fourth valve 5-2, an aerobic reaction tank 5-3, an aerobic biological filler 5-4 and an aeration head 5-5, wherein the aerobic reaction tank 5-3 is connected with a water outlet of a tank body 2-1 in the ceramic membrane-activated carbon absorber 2 through the fourth valve 5-2, the aeration head 5-5 and the aerobic biological filler 5-4 are arranged in the aerobic reaction tank 5-3, the aeration head 5-5 is connected with the nano aeration device 5-1, the nano aeration device 5-1 is also connected to the tank body 2-1, and an aerobic temperature controller 10-2 is also arranged in the aerobic reaction tank 5-3; the anoxic biological filler system 6 consists of an anoxic reaction tank 6-1, an anoxic biological filler 6-2 and a fifth valve 6-3, wherein the anoxic reaction tank 6-1 is connected to a water outlet of the aerobic reaction tank 5-3 through the fifth valve 6-3, the anoxic biological filler 6-2 is arranged in the anoxic reaction tank 6-1, and an anoxic temperature controller 10-3 is also arranged in the anoxic reaction tank 6-1.
It is worth noting that the aerobic biological filler 5-4 and the anoxic biological filler 6-2 adopt carbon fiber biological fillers, and have the characteristics of strong adsorption effect, strong microbial affinity and high film forming speed.
In addition, the nano bubbles generated by the nano aeration equipment 5-1 can effectively improve the dissolved oxygen in the water body, strengthen the aerobic nitrification effect and provide nitrate nitrogen required by denitrification for the synchronous desulfurization and denitrification system 7.
(3) The synchronous desulfurization and denitrification system 7 comprises a synchronous desulfurization and denitrification reactor 7-1, a multi-tooth stirrer 7-2, an exhaust hole 7-3, a first water pump 7-4, a sixth valve 7-5, FeS ore fillers 7-6 and spherical biological fillers 7-7, wherein the synchronous desulfurization and denitrification reactor 7-1 adopts a water inlet mode of top inlet and bottom outlet, the FeS ore fillers 7-6 and the spherical biological fillers 7-7 are filled in the synchronous desulfurization and denitrification reactor 7-1, the multi-tooth stirrer 7-2 is arranged on the synchronous desulfurization and denitrification reactor 7-1, the FeS ore fillers 7-6 and the spherical biological fillers 7-7 are fully stirred by the multi-tooth stirrer 7-2, so that the homogeneity of the FeS ore fillers is higher, and the contact area between desulfurization and denitrification bacteria and the spherical biological fillers is increased, enhancing the desulfurization effect; the top end of the synchronous desulfurization denitrification reactor 7-1 is provided with an exhaust hole 7-3 for discharging nitrogen generated by denitrification, and the water inlet of the synchronous desulfurization denitrification reactor 7-1 is connected to the water outlet of the anoxic reaction tank 6-1 in the anoxic biological filler system 6 through a first water pump 7-4 and a sixth valve 7-5; and a desulfurization denitrification temperature controller 10-4 is also arranged in the synchronous desulfurization denitrification reactor 7-1.
The filler in the synchronous desulfurization and denitrification reactor 7-1 is divided into two parts, wherein the upper layer is provided with FeS ore filler 7-6, the upper layer is prepared by taking iron sulfide ore as a substrate, the lower layer is provided with spherical biological filler 7-7, and the lower layer is prepared by inoculating screened desulfurization and denitrification bacteria to the spherical biological filler for synchronous desulfurization and denitrification; the two layers of fillers are separated by stainless steel metal grids 7-8. The polluted water body enters from the upper end through a first water pump 7-4, firstly a certain amount of FeS is dissolved through a FeS ore filler 7-6, and then the polluted water body passes through a spherical biological filler 7-7, wherein a passing sieve grows on the surface of the spherical biological filler 7-7Selecting domesticated desulfurization and denitrification bacillus as a microbial membrane of dominant species, wherein the desulfurization and denitrification bacillus utilizes FeS as an electron donor to convert nitrate nitrogen into nitrogen to complete a denitrification process, and then the nitrogen is discharged from a top exhaust hole 7-3, and meanwhile, phosphate in a polluted water body and Fe generated in the denitrification process are discharged in the process2+Formation of Fe3(PO4)2Precipitating and removing part of total phosphorus.
In addition, a FeS ore inlet 7-9 and a FeS ore outlet 7-10 are formed in the side wall of the synchronous desulfurization and denitrification reactor 7-1 at the corresponding position of the upper FeS ore filler 7-6, and the feeding and discharging of the FeS ore filler 7-6 are respectively carried out through the FeS ore inlet 7-9 and the FeS ore outlet 7-10; the side wall of the synchronous desulfurization denitrification reactor 7-1 is provided with a spherical biological filler inlet 7-11 and a spherical biological filler outlet 7-12 at the corresponding position of the spherical biological filler 7-7 at the lower layer, and the inlet and the outlet of the spherical biological filler 7-7 are respectively carried out through the spherical biological filler inlet 7-11 and the spherical biological filler outlet 7-12.
(4) The electrochemical phosphorus removal system 8 comprises an electrochemical phosphorus removal reactor 8-1, a Fe anode plate 8-2, an AL cathode plate 8-3, a second stirrer 8-4, a current stabilizer 8-5, a third stirrer 8-6, a PAM dosing barrel 8-7, a second dosing pump 8-8, a seventh valve 8-9 and an eighth valve 8-10, wherein the electrochemical phosphorus removal reactor 8-1 is connected to a water outlet of the synchronous desulfurization denitrification reactor 7-1 in the synchronous desulfurization denitrification system 7 through the eighth valve 8-10, the electrochemical phosphorus removal reactor 8-1 is provided with the second stirrer 8-4, the electrochemical phosphorus removal reactor 8-1 is connected with the current stabilizer 8-5, the electrochemical phosphorus removal reactor 8-1 is connected to the PAM dosing barrel 8-7 through the second dosing pump 8-8 and the seventh valve 8-9, a third stirrer 8-6 is arranged on the PAM medicine adding barrel 8-7.
The electrochemical phosphorus removal reactor 8-1 is internally provided with a Fe anode plate 8-2 and an AL cathode plate 8-3 which are uniformly arranged at intervals, the interval between the Fe anode plate 8-2 and the AL cathode plate 8-3 is 2cm, wherein Fe is generated on the Fe anode plate 8-22+OH is generated on the AL cathode plate 8-3-Phosphate with Fe2+Formation of Fe3（PO4）2Precipitating to remove phosphate, thereby removing total phosphorus and Fe2+And OH-Formation of Fe (OH)2Flocculation is enhanced by adding PAMAnd further, the total phosphorus in the water body is removed, and the phosphorus removal process is completed.
(5) The sedimentation system 9 consists of a ninth valve 9-1, a second water pump 9-2, a sedimentation tank 9-3, a tenth valve 9-4, an eleventh valve 9-5 and a second sludge pump 9-6, a water outlet of the electrochemical phosphorus removal reactor 8-1 in the electrochemical phosphorus removal system 8 is connected to the sedimentation tank 9-3 through the ninth valve 9-1 and the second water pump 9-2, the sedimentation tank 9-3 is connected with the tenth valve 9-4 for treating water discharge, and the bottom of the sedimentation tank 9-3 is connected with the eleventh valve 9-5 through the second sludge pump 9-6. After the denitrification and dephosphorization process of the polluted water body is finished, the polluted water body is pumped into a sedimentation tank 9-3 by a second water pump 9-2, clear water is discharged into the storage water body after sedimentation, sludge in the sedimentation tank 9-3 is pumped into a dewatering device by a second sludge pump 9-6, and the precipitated sludge is transported outside after dewatering treatment.
The specific embodiment also provides a synchronous desulfurization denitrification coupling electrochemical phosphorus removal method, which comprises the following steps:
firstly, the polluted water body enters a ceramic membrane-activated carbon adsorption system, the activated carbon particles in the ceramic membrane can effectively adsorb pollutants such as refractory organic matters, soluble organic matters, heavy metals and the like in the water body, and the aperture of the ceramic membrane is smaller than the particle size of the activated carbon particles, so that the activated carbon particles can effectively intercept and adsorb the pollutants, the water body can permeate, and the concentration of the pollutants such as COD (chemical oxygen demand) of the water body is reduced.
Secondly, the polluted water enters a biological filler system after being treated by a ceramic membrane-activated carbon adsorption system. After entering a biological filler system, the polluted water body firstly passes through an aerobic reaction tank to convert ammonia nitrogen in the polluted water body into nitrate nitrogen and simultaneously remove part of residual organic matters; then the polluted water body enters an anoxic reaction tank, in the anoxic reaction tank, the microorganisms utilize the residual organic matters to carry out heterotrophic denitrification to remove part of nitrate nitrogen and simultaneously further remove the organic matters in the water body, and after the polluted water body passes through the anoxic reaction tank, the dissolved oxygen brought in by the aerobic reaction tank can be consumed to a lower level, so that the synchronous desulfurization denitrification can be better carried out.
Thirdly, the polluted water body enters into the synchronous desulfurization denitrification coupling electrochemistry after passing through the biological filler systemA phosphorus removal system. The polluted water body firstly passes through a synchronous desulfurization denitrification system, and the screened synchronous desulfurization denitrification bacteria in the system convert iron sulfide into Fe by taking the iron sulfide as an electron donor2+And sulfate ion, nitrate nitrogen is used as electron acceptor to convert nitrate nitrogen into nitrogen gas to complete denitrification process, and Fe2+Can be mixed with PO4 3-Formation of Fe3(PO4)2And (3) precipitating, thereby removing part of phosphate, reducing the total phosphorus concentration of the polluted water body, synchronously desulfurizing, denitrifying and denitrifying to get rid of the dependence of denitrifying microorganisms on organic matters in the conventional denitrifying and denitrifying process, and having remarkable denitrifying effect and certain dephosphorizing effect. After the denitrification process of the polluted water body is finished by the synchronous desulfurization and denitrification system, the polluted water body enters an electrochemical dephosphorization system. The positive electrode and the negative electrode of the electrochemical phosphorus removal system are respectively an iron electrode and an aluminum electrode, the positive electrode of the system is subjected to oxidation reaction, and Fe is generated from Fe2+The system cathode is subjected to reduction reaction and is formed by H2Formation of OH from O-And H2. PO in polluted water body4 3-And Fe2+Formation of Fe3(PO4)2Precipitation with Fe2+And OH-Formation of Fe (OH)2Flocculating to remove soluble organic phosphorus and phosphate in the water body, adding PAM to enhance flocculation effect, and finally finishing removal of phosphorus element in the polluted water body.
It is worth noting that the activated carbon particles in the ceramic membrane-activated carbon adsorption system in the step I are subjected to adsorption saturation, enter the activated carbon recycling system for regeneration, and then enter the ceramic membrane-activated carbon adsorption system again for recycling.
In addition, the polluted water body is precipitated, the finally treated water body is discharged according to the requirement, and the sludge is transported outside after being dehydrated.
The specific implementation mode is mainly applied to denitrification and dephosphorization of eutrophic water bodies, black and odorous water bodies and sewage with low carbon-nitrogen ratio, can remove nutrient elements such as nitrogen and phosphorus in the water bodies, effectively treat water pollution, reduce water eutrophication and black and odorous risks, and has important significance on water ecological safety in China, and the technical advantages are as follows:
(1) effectively reduce COD concentration and heavy metal content in the water: the system adopts a ceramic membrane-activated carbon technology as a denitrification and dephosphorization pretreatment process, and after the polluted water body enters a ceramic membrane-activated carbon reactor, activated carbon particles in the reactor can effectively adsorb refractory organic matters, soluble organic matters and heavy metals in the water body, so that the COD concentration and the heavy metal content in the water body are reduced.
(2) The denitrification and dephosphorization effects are obvious: firstly, polluted water enters an aerobic biological filling tank and is treated by a nano aeration biomembrane method, so that the conversion efficiency of ammonia nitrogen to nitrate nitrogen can be effectively improved, and a foundation is laid for subsequent denitrification;
secondly, after the polluted water body enters an anoxic biological filling tank, partial nitrate nitrogen can be converted into nitrogen through heterotrophic denitrification, partial organic matters are removed, and the content of the water body can be reduced;
after the polluted water body enters the synchronous desulfurization denitrification system, the screened desulfurization bacilli use nitrate nitrogen as an electron acceptor, use ferric sulfide as electron power supply, convert the nitrate nitrogen into nitrogen, the denitrification efficiency is not limited by the content of organic matters in the water body, and the TN content in the water body can be effectively reduced;
fourthly, adopting electrochemistry to remove phosphorus and generating Fe at the anode2+OH is formed in the negative electrode-PO in polluted water body4 3-And Fe2+Formation of Fe3(PO4)2Precipitation with Fe2+And OH-Formation of Fe (OH)2And the flocculation is removed by removing soluble organic phosphorus and phosphate in the water body, and the flocculation effect is enhanced by adding PAM (polyacrylamide), so that the biological and chemical phosphorus removal effect is more stable and the phosphorus removal effect is better compared with the traditional biological and chemical phosphorus removal effect.
(3) The operation cost is reduced: the low C/N ratio sewage is treated by synchronous desulfurization and denitrification, and the denitrification process can be completed without adding an additional organic carbon source, so that the operation cost of water treatment per ton is effectively reduced, and the operation cost is saved; compared with the traditional chemical phosphorus removal, the electrochemical phosphorus removal can effectively reduce the addition of a flocculating agent and reduce the operation cost.
(4) The equipment maintenance is relatively simple: the ceramic membrane-activated carbon system, the biological filler system, the synchronous desulfurization and denitrification system and the electrochemical phosphorus removal system in the system adopt modular design, are simple to install and easy to operate, and are convenient for equipment maintenance.
The foregoing shows and describes the general principles and features of the present invention, together with the advantages thereof. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the utility model as claimed. The scope of the utility model is defined by the appended claims and equivalents thereof.
Claims (10)
1. The synchronous desulfurization denitrification coupling electrochemical phosphorus removal system is characterized by comprising a ceramic membrane-activated carbon adsorption system, a biological filler system, a synchronous desulfurization denitrification coupling electrochemical phosphorus removal system and a temperature control system (10), wherein the ceramic membrane-activated carbon adsorption system consists of a water inlet system (1), a ceramic membrane-activated carbon adsorber (2), an activated carbon dosing system (3) and an activated carbon recycling system (4), the biological filler system consists of an aerobic biological filler system (5) and an anoxic biological filler system (6), the synchronous desulfurization denitrification coupling electrochemical phosphorus removal system consists of a synchronous desulfurization denitrification system (7), an electrochemical phosphorus removal system (8) and a precipitation system (9), and the temperature control system (10) consists of a temperature control center (10-1), An aerobic temperature controller (10-2), an anoxic temperature controller (10-3) and a desulfurization denitrification temperature controller (10-4);
the water inlet system (1) is connected with the ceramic membrane-activated carbon adsorber (2), the activated carbon dosing system (3) is communicated with the ceramic membrane-activated carbon adsorber (2), the activated carbon recycling system (4) is connected with the ceramic membrane-activated carbon adsorber (2), the water outlet of the ceramic membrane-activated carbon adsorber (2) is connected with the water inlet of the aerobic biological filler system (5), the water outlet of the aerobic biological filler system (5) is communicated with the water inlet of the anoxic biological filler system (6), the water outlet of the anoxic biological filler system (6) is communicated with the synchronous desulfurization denitrification system (7), the synchronous desulfurization denitrification system (7) is communicated with the electrochemical dephosphorization system (8), and the electrochemical dephosphorization system (8) is communicated with the precipitation system (9); the aerobic biological filler system (5), the anoxic biological filler system (6) and the synchronous desulfurization denitrification system (7) are respectively provided with an aerobic temperature controller (10-2), an anoxic temperature controller (10-3) and a desulfurization denitrification temperature controller (10-4), and the aerobic temperature controller (10-2), the anoxic temperature controller (10-3) and the desulfurization denitrification temperature controller (10-4) are all connected to a temperature control center (10-1).
2. The system of claim 1, wherein the system comprises a synchronous desulfurization denitrification coupled with electrochemical phosphorus removal, the system is characterized in that the water inlet system (1) comprises a grating (1-1), a water inlet pipeline (1-2), a pressurizing lift pump (1-3), a first valve (1-4) and a connecting pipeline (1-5), the ceramic membrane-activated carbon adsorber (2) comprises a tank body (2-1) and a ceramic membrane (2-2), the activated carbon dosing system (3) consists of an activated carbon dosing barrel (3-1), a first stirrer (3-2), a first dosing pump (3-3) and a second valve (3-4), and the activated carbon recycling system (4) consists of a third valve (4-1), a recycling pump (4-2), an activated carbon collecting pool (4-3) and a first sludge pump (4-4); the device comprises a water inlet system (1), a grid (1-1), a water inlet, a pressurizing lift pump (1-3), a connecting pipeline (1-5), a first valve (1-4), a ceramic membrane (2-2), an active carbon dosing barrel (3-1), a second valve (3-4), a first stirrer (3-2), a first dosing pump (3-3), a second stirrer, a water inlet pipe (1-2), a connecting pipeline (1-5), a first valve (1-4), a ceramic membrane (2-1), a ceramic membrane (2-2), an active carbon dosing barrel (3-1), a second dosing pump (3-4), a first stirrer (3-2), a second stirring pump, a first dosing pump, a second dosing pump, a first stirring pump, a second stirring pump, a stirring tank, a first stirring pump, a second stirring tank, a second stirring pump, a second stirring tank, a second stirring device, a second stirring device and a second stirring device, a stirring device and a stirring device, a stirring device and a stirring device, wherein the stirring device and a stirring device, a stirring device and a stirring device, wherein the stirring device, a stirring device, wherein the stirring device, a stirring device and a stirring device, a stirring device and a stirring device, wherein the stirring device, a stirring device and a stirring device, wherein the, the activated carbon sewage treatment device is characterized in that the tank body (2-1) is connected to the activated carbon collecting tank (4-3) through a third valve (4-1) and a recovery pump (4-2), a first sludge pump (4-4) is installed in the activated carbon collecting tank (4-3), and the first sludge pump (4-4) is connected to the activated carbon dosing barrel (3-1).
3. The system as claimed in claim 2, wherein the ceramic membrane-activated carbon adsorber (2) has a ceramic membrane (2-2) with a pore size of 1 μm, and the added activated carbon has a particle size of 800-1000 mesh.
4. The synchronous desulfurization denitrification coupling electrochemical phosphorus removal system according to claim 1, wherein the aerobic biological filler system (5) is composed of a nano aeration device (5-1), a fourth valve (5-2), an aerobic reaction tank (5-3), an aerobic biological filler (5-4) and an aeration head (5-5), the aerobic reaction tank (5-3) is connected with a water outlet of a tank body (2-1) in the ceramic membrane-activated carbon adsorber (2) through the fourth valve (5-2), the aerobic reaction tank (5-3) is internally provided with the aeration head (5-5) and the aerobic biological filler (5-4), the aeration head (5-5) is connected with the nano aeration device (5-1), the nano aeration device (5-1) is further connected with the tank body (2-1), an aerobic temperature controller (10-2) is also arranged in the aerobic reaction tank (5-3); the anaerobic biological filler system (6) consists of an anaerobic reaction tank (6-1), an anaerobic biological filler (6-2) and a fifth valve (6-3), the anaerobic reaction tank (6-1) is connected to a water outlet of the aerobic reaction tank (5-3) through the fifth valve (6-3), the anaerobic biological filler (6-2) is arranged in the anaerobic reaction tank (6-1), and an anaerobic temperature controller (10-3) is further arranged in the anaerobic reaction tank (6-1).
5. The system of claim 4, wherein the aerobic biological filler (5-4) and the anoxic biological filler (6-2) adopt carbon fiber biological fillers with strong adsorption effect.
6. The synchronous desulfurization denitrification coupling electrochemical phosphorus removal system as claimed in claim 1, wherein the synchronous desulfurization denitrification system (7) comprises a synchronous desulfurization denitrification reactor (7-1), a multi-tooth stirrer (7-2), an exhaust hole (7-3), a first water pump (7-4), a sixth valve (7-5), an FeS ore filler (7-6) and a spherical biological filler (7-7), the synchronous desulfurization denitrification reactor (7-1) adopts a water inlet mode of top inlet and bottom outlet, the synchronous desulfurization denitrification reactor (7-1) is filled with the FeS ore filler (7-6) and the spherical biological filler (7-7), and the synchronous desulfurization denitrification reactor (7-1) is provided with the multi-tooth stirrer (7) for fully stirring the FeS ore filler (7-6) and the spherical biological filler (7-7) -2), an exhaust hole (7-3) for discharging nitrogen generated by denitrification is arranged at the top end of the synchronous desulfurization denitrification reactor (7-1), and a water inlet of the synchronous desulfurization denitrification reactor (7-1) is connected to a water outlet of an anoxic reaction tank (6-1) in the anoxic biological filler system (6) through a first water pump (7-4) and a sixth valve (7-5); the synchronous desulfurization denitrification reactor (7-1) is also provided with a desulfurization denitrification temperature controller (10-4).
7. The synchronous desulfurization denitrification coupling electrochemical dephosphorization system according to claim 6, wherein the filler inside the synchronous desulfurization denitrification reactor (7-1) is divided into two parts, the upper layer is provided with FeS ore filler (7-6), the lower layer is provided with spherical biological filler (7-7), the two layers of fillers are separated by stainless steel metal grids (7-8), the side wall of the synchronous desulfurization denitrification reactor (7-1) is provided with a FeS ore inlet (7-9) and a FeS ore outlet (7-10) at the corresponding position of the upper layer FeS ore filler (7-6), the side wall of the synchronous desulfurization denitrification reactor (7-1) is provided with a spherical biological filler inlet (7-11) at the corresponding position of the lower layer spherical biological filler (7-7), and a spherical biological filler outlet (7-12).
8. The synchronous desulfurization denitrification coupling electrochemical phosphorus removal system of claim 1, wherein the electrochemical phosphorus removal system (8) comprises an electrochemical phosphorus removal reactor (8-1), an Fe anode plate (8-2), an AL cathode plate (8-3), a second stirrer (8-4), a current stabilizer (8-5), a third stirrer (8-6), a PAM dosing barrel (8-7), a second dosing pump (8-8), a seventh valve (8-9) and an eighth valve (8-10), the electrochemical phosphorus removal reactor (8-1) is connected to a water outlet of the synchronous desulfurization denitrification reactor (7-1) in the synchronous desulfurization denitrification system (7) through the eighth valve (8-10), the electrochemical phosphorus removal reactor (8-1) is provided with the second stirrer (8-4), fe anode plates (8-2) and AL cathode plates (8-3) which are uniformly arranged at intervals are arranged in the electrochemical phosphorus removal reactor (8-1), the electrochemical phosphorus removal reactor (8-1) is connected with a current stabilizer (8-5), the electrochemical phosphorus removal reactor (8-1) is connected to a PAM dosing barrel (8-7) through a second dosing pump (8-8) and a seventh valve (8-9), and a third stirrer (8-6) is arranged on the PAM dosing barrel (8-7).
9. The system of claim 8, wherein the Fe anode plate (8-2) and the AL cathode plate (8-3) are uniformly arranged at intervals, and the interval between the Fe anode plate (8-2) and the AL cathode plate (8-3) is 2 cm.
10. The system of claim 1, wherein the system comprises a synchronous desulfurization denitrification coupled with electrochemical phosphorus removal, the device is characterized in that the sedimentation system (9) consists of a ninth valve (9-1), a second water pump (9-2), a sedimentation tank (9-3), a tenth valve (9-4), an eleventh valve (9-5) and a second sludge pump (9-6), a water outlet of the electrochemical phosphorus removal reactor (8-1) in the electrochemical phosphorus removal system (8) is connected to the sedimentation tank (9-3) through the ninth valve (9-1) and the second water pump (9-2), the sedimentation tank (9-3) is connected with the tenth valve (9-4) for treating water discharge, and the bottom of the sedimentation tank (9-3) is connected with the eleventh valve (9-5) through the second sludge pump (9-6).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122993217.5U CN216687821U (en) | 2021-12-02 | 2021-12-02 | Synchronous desulfurization denitrification nitrogen removal coupling electrochemistry dephosphorization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122993217.5U CN216687821U (en) | 2021-12-02 | 2021-12-02 | Synchronous desulfurization denitrification nitrogen removal coupling electrochemistry dephosphorization system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216687821U true CN216687821U (en) | 2022-06-07 |
Family
ID=81836238
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122993217.5U Active CN216687821U (en) | 2021-12-02 | 2021-12-02 | Synchronous desulfurization denitrification nitrogen removal coupling electrochemistry dephosphorization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216687821U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115745098A (en) * | 2022-11-14 | 2023-03-07 | 中国科学院地球化学研究所 | Method for recycling phosphorus in acidic phosphorus-containing wastewater through spontaneous anoxic and ferroelectric flocculation |
-
2021
- 2021-12-02 CN CN202122993217.5U patent/CN216687821U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115745098A (en) * | 2022-11-14 | 2023-03-07 | 中国科学院地球化学研究所 | Method for recycling phosphorus in acidic phosphorus-containing wastewater through spontaneous anoxic and ferroelectric flocculation |
| CN115745098B (en) * | 2022-11-14 | 2023-08-11 | 中国科学院地球化学研究所 | Method for recycling phosphorus in acidic phosphorus-containing wastewater through spontaneous anoxic ferroelectric flocculation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106830573B (en) | Low-energy-consumption urban sewage denitrification method based on enhanced carbon capture and anaerobic ammonia oxidation | |
| CN100509664C (en) | Method for treating percolation liquid of water deficiency area garbage embedding field | |
| CN101244883B (en) | High-efficiency low-consumption retexture method for urban sewage | |
| CN108503026B (en) | Urban secondary effluent sulfur matrix circulating autotrophic nitrogen removal method | |
| CN109336325B (en) | Device and method for zero-emission treatment of late landfill leachate | |
| CN105481208B (en) | A kind of high-efficiency sewage treatment process and device based on electron stream orientation regulation and control | |
| CN106277555B (en) | High-efficiency low-cost treatment method and system for coking wastewater | |
| WO2019169610A1 (en) | Method for upgrading and expanding sewage biological treatment process | |
| CN110395851B (en) | High-altitude town sewage treatment method based on nitrogen and phosphorus capture and completely autotrophic nitrogen removal | |
| CN112979065A (en) | Garbage transfer station leachate full-treatment system | |
| CN100482599C (en) | Biological sponge iron preparation and its uses in water disposal | |
| CN109912145B (en) | Aerobic granular sludge power generation device | |
| CN112744912A (en) | Sulfur autotrophic denitrification biological filter, sewage treatment system and treatment method thereof | |
| CN110606626B (en) | Synchronous nitrogen and phosphorus removal sewage treatment process | |
| CN109912128B (en) | Synchronous nitrogen and phosphorus removal system for continuous flow aerobic granular sludge with low carbon-nitrogen ratio | |
| CN111333175A (en) | Method for coupling treatment of wastewater containing DMAC (dimethylacetamide) and DMF (dimethyl formamide) by adopting iron-carbon and aerobic granular sludge | |
| CN216687821U (en) | Synchronous desulfurization denitrification nitrogen removal coupling electrochemistry dephosphorization system | |
| CN210481144U (en) | Sewage treatment device for synchronously realizing sludge in-situ reduction and nitrogen and phosphorus removal | |
| CN109231673B (en) | A/O combined micro-electric field-Fe/C reinforced dephosphorization device and application thereof | |
| CN215365360U (en) | System for treating rural domestic sewage by utilizing A2O + modified filter material biological filter | |
| CN204779236U (en) | Coking wastewater's high -efficient low -cost processing system | |
| CN212532677U (en) | Landfill leachate treatment system | |
| CN204550200U (en) | Municipal effluent denitrogenation dephosphorizing treatment system | |
| CN113998846A (en) | Efficient carbon adsorption coupled biological nitrogen and phosphorus removal sewage treatment device and method | |
| CN116282609A (en) | Synchronous desulfurization, denitrification and denitrification coupling electrochemical dephosphorization system and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |