CN212559887U - Water body deep purification system based on electrolytic denitrification and MBR - Google Patents
Water body deep purification system based on electrolytic denitrification and MBR Download PDFInfo
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Abstract
A water deep purification system based on electrolytic denitrification and MBR relates to the technical field of water purification. The device comprises a pretreatment device, a coagulating sedimentation device, an electrolytic denitrification device, a membrane bioreactor and a sludge treatment system, wherein the pretreatment device comprises a coarse grating, a fine and coarse grating, an aeration grit chamber and a lift pump which are sequentially communicated; the coagulating sedimentation device comprises a coagulating basin, a coagulation aiding basin, a coagulating sedimentation basin, an intermediate water basin and a sludge basin which are sequentially communicated; the electrolytic denitrification device comprises an electrolytic denitrification host, a direct current power supply and a denitrification reaction tank. The sludge treatment device comprises a sludge pump, a gravity concentration tank, a physicochemical conditioning tank and a dehydrator. A micro-electrolysis device can be arranged in front of the membrane bioreactor, and an adsorption dephosphorization device can be arranged behind the membrane bioreactor. Can remove 80-95 percent of COD in the water body, overcomes the defects of poor quality of the existing effluent, large investment, long purification period and large occupied area, and leads the effluent to reach the quality standard of surface water environment.
Description
Technical Field
The utility model relates to a water purifies technical field, specifically relates to a water degree of depth clean system based on electrolysis denitrogenation and MBR.
Background
The eutrophication of the water body is mainly caused by the fact that the nitrogen and phosphorus content in the water body accumulates day by day and continuously and seriously exceeds the standard, and one of the main reasons for the result is that sewage is discharged from a municipal sewage plant, and a large amount of nitrogen and phosphorus are discharged into the water body along with the sewage. The eutrophication of water body causes the massive proliferation of algae and the repeated outbreak of water bloom, so the treatment of the eutrophication of water body is an important problem at home and abroad.
The urban domestic sewage is a polluted water body generated in the living process of people, and the common physical and chemical indexes are that COD is less than or equal to 800mg/L (mostly 280-500 mg/L), BOD is less than or equal to 350mg/L (mostly 150-300 mg/L), SS is less than or equal to 400mg/L, ammonia nitrogen is less than or equal to 50mg/L, total nitrogen is less than or equal to 70mg/L, and total phosphorus is less than or equal to 10mg/L, pH 7-9. At present, pollution treatment at home and abroad is divided into primary treatment, secondary treatment and advanced treatment. The main process of the first-stage treatment comprises sewage collection, coarse grid filtration and fine grid filtration to an aeration sand settling tank and a primary settling tank; the main process of the secondary treatment comprises the following steps: activated sludge treatment process, biofilm process and Membrane Bioreactor (MBR). The activated sludge treatment process applied to the urban sewage plant mainly comprises three series: (1) oxidation ditch series; (2) A/A/O series; (3) sequencing Batch Reactor (SBR) series. The biofilm process applied to the urban sewage treatment plant mainly comprises a Biological Aerated Filter (BAF) process and a Moving Bed Biofilm (MBBR) process. Membrane Bioreactors (MBR) are a new sewage treatment process developed in the nineties of the last century, and can be classified into tubular membranes, curtain membranes, plate membranes and the like according to different processing modes of membrane modules, and further classified into built-in or external MBRs according to different installation positions of the membrane modules and the bioreactors. The advanced treatment process mainly applied at home and abroad is a coagulation dephosphorization and denitrification process.
When the sewage treatment plant is constructed by adopting the process to treat the sewage, the retention time of the sewage is more than 17 hours, so that the sewage treatment plant has large occupied area, more structures, more investment, high operating cost and long construction time, the effluent quality is mostly the quasi IV class (mainly the total nitrogen can only reach about 10 mg/L) of the pollutant discharge standard (GB 18918-2002) of the urban sewage treatment plant or the surface water environment quality standard (GB3838-2002), and the water quality is poor, and most of the effluent cannot meet the utilization requirement of water resources. In addition, from the analysis of the existing standards, the pollutant discharge standard of urban sewage treatment plants (GB 18918-2002) is implemented in domestic urban sewage treatment plants at present, and compared with the main physicochemical indexes of the environmental quality standard of surface water (GB3838-2002), the total nitrogen, the total phosphorus and the dissolved oxygen can not meet the index requirements of the environmental quality standard of surface water (GB 3838-2002). Although the classical sewage treatment processes are applied for more than one hundred years, the quality of the effluent cannot meet the index requirements of the quality standard of surface water environment (GB3838-2002) without great change, so that a novel sewage treatment process which has the advantages of high effluent quality (meeting the requirement of water resource utilization), short sewage retention time, small occupied area, less structures, less investment, lower operation cost and greatly shortened construction time is urgently needed.
The poor V-class water body and the black and odorous water body are blackened and smelled due to the fact that the water body excessively receives dirt and exceeds the water environment capacity of the water body, and are generally lower than the V-class water quality standard of surface water environment quality standard (GB3838-2002), and the main characteristic indexes of the poor V-class water body and the black and odorous water body are that dissolved oxygen is less than 2.0mg/L, ammonia nitrogen is more than 2.0mg/L or total phosphorus is more than 0.4mg/L, the poor V-class water body and the black and odorous water body are located in areas with dense population, high pollution load intensity and incomplete infrastructure, and mainly comprise water bodies in urban built-up areas, urban and rural junctions. In order to strengthen water body treatment and improve water environment, the state institute reaches ten water in 2015. The method comprises the following steps: ' treating black and odorous water in cities. Measures such as source control and sewage interception, garbage cleaning, dredging, ecological restoration and the like are adopted, the treatment strength of the black and odorous water body is enhanced, and the treatment condition is published to the society every half year. The Ministry of urban and rural construction of housing, together with the Ministry of environmental protection, Water conservancy and agriculture, has set up the working guidelines for treating black and odorous water in cities. Therefore, the treatment of water pollution is an urgent task.
Disclosure of Invention
The utility model aims to provide a water deep purification system based on electrolytic denitrification and MBR, which has the defects of poor water quality, large investment, long purification time and large occupied area, and has the advantages of short process flow, short sewage treatment retention time, low operation cost, strong adaptability to water quality, good continuous effect and high water quality.
A deep water body purification system based on electrolytic denitrification and MBR comprises a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300), a membrane bioreactor (400) and a sludge treatment system (500):
the pretreatment device (100) comprises a coarse grating (110), a fine and coarse grating (120), an aeration grit chamber (130) and a lift pump (140) which are sequentially communicated; a water inlet of the coarse grating (110) is communicated with a water inlet pipeline of a polluted water body to be treated, raw water is introduced, and a water outlet of the coarse grating (110) is communicated with a water inlet of the fine grating (120); the water outlet of the fine grid (120) is communicated with the water inlet of the aeration grit chamber (130), the water outlet of the aeration grit chamber (130) is communicated with the water inlet of the lift pump (140), and the lift pump (140) is connected with the coagulating sedimentation device (200); the coarse grating (110) and the fine grating (120) are used for removing large-particle solids, the aeration grit chamber (130) is used for precipitating impurities such as silt in a water body, and the precipitated sludge enters the sludge treatment system (500).
The coagulating sedimentation device (200) comprises a coagulating basin (210), a coagulation aiding basin (220), a coagulating sedimentation basin (230), an intermediate water pool (240) and a sludge pool (250) which are communicated in sequence; the coagulating sedimentation tank (230) is provided with a clear water outlet (231) and a sludge outlet (232); a water inlet of the coagulation tank (210) is communicated with a water outlet of a lift pump (140) of the pretreatment device (100), and the coagulation tank (210), the coagulation aiding tank (220) and the coagulating sedimentation tank (230) are communicated in sequence; a clear water outlet (231) of the coagulating sedimentation tank (230) is communicated with a water inlet of the intermediate water tank (240), a water outlet (241) of the intermediate water tank (240) is communicated with a water inlet of an electrolytic denitrification host (310) of the electrolytic denitrification device (300), and a lift pump (311) is further arranged in a connecting pipeline between the clear water outlet and the electrolytic denitrification host (310); a sludge outlet (232) of the coagulating sedimentation tank (230) is communicated with an inlet (251) of a sludge tank (250) through a sludge pump (233) and a sludge discharge pipe (235), and an outlet of the sludge tank (250) is communicated with an inlet of a sludge dewatering system (500); the sludge outlet (232) of the coagulating sedimentation tank (230) is also communicated with the coagulation aiding tank (220) through a sludge pump (233), a sludge discharge pipe (235) and a return pump (234).
The coagulating sedimentation device (200) can adopt one of a high-efficiency sedimentation device, a magnetic coagulation device, a super-magnetic coagulating sedimentation device and the like. The coagulation tank (210) of the coagulation sedimentation device (200) also comprises a coagulant dosing device (211) and a stirrer (212); ferrous sulfate with the mass ratio of 5 to 10 percent or polyaluminium chloride solution with the mass ratio of 10 to 15 percent is stored in the coagulant dosing device (211); the coagulant aid tank (220) also comprises a coagulant aid dosing device (221) and a stirrer (222); PAM solution with the mass ratio of 1-2 per mill is stored in the coagulant aid dosing device (221).
The electrolytic denitrification device (300) comprises an electrolytic denitrification host (310), a direct current power supply (320) and a denitrification reaction tank (330); the effluent of the coagulating sedimentation device (200) is connected with the water inlet of the electrolytic denitrification host (310) through a lift pump (311), a flowmeter (312), a valve (313), a pipeline mixer (314), a valve (315) and a tee joint (316). The water outlet of the main electrolytic denitrification machine (310) is respectively communicated with the water inlet of the denitrification reaction tank (330) and the water inlet of the coagulation sedimentation tank (210) through a tee joint (317), a valve (318) and a tee joint (319).
Specifically, the working voltage of the electrolytic denitrification host (310) is 2-500V, and the current density can be 0.5-10 mA/cm2。
The electrolytic denitrification device can also comprise an electrolyte adding device (340), which is composed of an electrolyte solution preparation tank (342), an electrolyte solution storage tank (341), an electrolyte solution delivery pump (343) and an electrolyte solution flowmeter (344), wherein the electrolyte solution is delivered to the electrolyte solution storage tank (341) through the pump for storage and use after the electrolyte solution preparation tank (342) is prepared. When the electrolytic denitrification device works, an electrolyte solution delivery pump (343) is started and is input into the polluted water body through an electrolyte solution flowmeter (344) and a pipeline mixer (314), and then the polluted water body is electrolyzed in a main machine of the electrolytic denitrification system;
more specifically, the electrolyte adding device (340) is used for adding 3-12% of sodium hypochlorite solution or 2-6% of sodium chloride solution into the electrolytic denitrification device (300); the electrolyte solution preparation tank (342) is used for preparing 4-12% sodium hypochlorite solution or 2-6% sodium chloride solution;
preferably, when ammonia nitrogen and total nitrogen are removed, 3% -12% of sodium hypochlorite solution is added into the electrolytic denitrification device by an electrolyte adding device (340) according to the concentration of ammonia nitrogen in the water body;
more preferably, when ammonia nitrogen and total nitrogen are removed, 3-5% of sodium hypochlorite solution is added into the electrolytic denitrification device by an electrolyte adding device (340) according to the concentration of ammonia nitrogen in the water body;
specifically, the electrolytic denitrification device also comprises an electrolytic main machine pickling system (350) which is composed of a pickling solution preparation tank (351) and a pickling solution delivery pump (352). The acid washing solution adopts 2 to 3 percent hydrochloric acid solution or 3 to 5 percent citric acid solution. When the electrode of the electrolytic denitrification device is polluted and the electrolytic efficiency is reduced, the electrolytic denitrification device stops working, and the acid cleaning system (350) is started to remove the scale deposited on the surface of the electrode.
Furthermore, the waste water of the acid washing system (350) enters the coagulating sedimentation purification treatment through a tee joint (319).
The membrane bioreactor (400) is called MBR for short and comprises a biological reaction tank body (410), an aeration pipe (420), a membrane assembly (430), an aeration fan (440), a backwashing water pipe (450), a vacuum system (460) and a disinfection tank (470); the water inlet of the membrane bioreactor (400) is communicated with the water outlet of a denitrification reaction tank (330) of the electrolytic denitrification device (300) system, and the water outlet (411) of the membrane bioreactor (400) is communicated with the water outlet of the disinfector (460) and flows into the disinfection tank (470); the sludge outlet (412) of the membrane bioreactor (400) is connected with the sludge treatment system (500), and the outlet of the disinfection tank (470) is connected with the adsorption dephosphorization system (700) or the discharge port;
the sludge treatment device (500) comprises a sludge pump (510), a gravity concentration tank (520), a physicochemical conditioning tank (530) and a dehydrator (540), wherein the inlet of the sludge pump (510) is communicated with a sludge outlet (232) of the coagulation sedimentation tank (230) and a sludge outlet (414) of a biological tank (410) of a Membrane Bioreactor (MBR), the outlet of the sludge pump (510) is communicated with the inlet of the gravity concentration tank (520), a sludge outlet (521) of the gravity concentration tank (520) is communicated with an inlet (531) of the physicochemical conditioning tank (530), and a sewage outlet (522) of the gravity concentration tank (520) is communicated with a water inlet of the Membrane Bioreactor (MBR) (400); the outlet of the physicochemical conditioning tank (530) is communicated with the sludge inlet of the dehydrator (540), the sludge blocks of the dehydrator (540) are collected in the sludge collecting plateau, and the sewage of the dehydrator (540) is communicated with the water inlet of the biological reaction tank body (410) of the Membrane Bioreactor (MBR) (400).
A micro-electrolysis device (600) can be arranged in front of the Membrane Bioreactor (MBR), and the micro-electrolysis device (600) consists of a tank body (610), a support frame (620), a support layer (630), an iron-carbon layer (640) and a filter material layer (650); the micro-electrolysis device (600) is also provided with a water inlet (611), a water outlet (612), a sludge outlet (613), a backwashing pipe and a backwashing water outlet (614); the outlet of the backwashing water outlet (614) is connected with the water inlet of the coagulating sedimentation device (200); the water inlet (611) is connected with the water outlet of the denitrification reaction tank (330), and the water outlet (612) is connected with the water inlet of the Membrane Bioreactor (MBR) (400). The sludge outlet (613) is communicated with the inlet of the sludge dewatering device (500). The micro-electrolysis device (600) is mainly used for consuming excessive sodium hypochlorite during electrolytic denitrification to ensure the normal growth of microbial flora in a Membrane Bioreactor (MBR) biological pool.
An adsorption dephosphorization device (700) can be arranged behind the MBR (400). The adsorption dephosphorization system (700) can be arranged when the requirement on phosphorus is less than 0.1mg/L or a large amount of iron ions are contained in the water body. The adsorption dephosphorization device (700) at least comprises an adsorption tower (710), a desorption regeneration system (720) and a phosphorus precipitation recovery system (730);
further, the adsorption phosphorus removal device needs to be operated continuously, and at least comprises two adsorption towers (710), a desorption regeneration system (720) and a phosphorus precipitation recovery system (730);
the desorption regeneration system (720) is composed of a desorption regeneration liquid storage tank (721), a regeneration liquid delivery pump (722), a flow meter (723), a regeneration liquid inlet valve (724), an adsorption tower (710), a clear water tank (728), a clear water pump (729), an eluent water outlet valve (726) and an eluent storage tank (727); the adsorption tower (710) is composed of a valve (711), a water inlet (712), a lower supporting plate (713), adsorption packing (714), an upper supporting plate (715), a water outlet (716), a tee joint (717), a tee joint (718) and a valve (719); the desorption regeneration liquid storage tank (721) is connected to the adsorption tower (710) through a regeneration liquid delivery pump (722), a water inlet valve (724) and a water inlet tee joint; the clean water tank (728) is connected with the adsorption tower (710) through a clean water pump (729) and a tee joint (718) and a water outlet tee joint (717); the eluent storage tank (727) is connected with the adsorption tower (710) through an eluent outlet valve (726) and an outlet tee joint (717);
the phosphorus precipitation recovery system (730) consists of a desorption liquid delivery pump (731), an inlet valve (732), a precipitation reaction tank (733), a stirrer (734), a precipitant storage tank (735), a dosing pump (736), a precipitation tank (739), a delivery pump (738), a concentration tank (737) and a recovery pump; the inlet of the desorption liquid delivery pump (731) is connected with the water outlet of the eluent storage tank (727), the water outlet of the desorption liquid delivery pump (731) is connected with the inlet of a desorption liquid inlet valve (732), and the outlet of the desorption liquid inlet valve (732) is connected with the phosphorus precipitation reaction tank (733); the sedimentation reaction tank (733) is also provided with a stirrer (734) and a precipitator storage tank (735), the water outlet of the sedimentation reaction tank (733) is connected with the water inlet of a phosphorus sedimentation tank (739), the water outlet of the phosphorus sedimentation recovery tank (739) is connected with the inlet of a concentration tank (737) through a delivery pump (738), and the outlet of the concentration tank (737) is connected with a desorption regeneration liquid storage tank (721) through a recovery pump.
Specifically, a calcium hydroxide saturated solution is stored in the precipitant storage tank (735).
More specifically, as shown in fig. 1, the inlet of the sludge pump (510) is respectively communicated with the sludge outlets of the pretreatment device (100), the coagulating sedimentation device (200), the electrolytic denitrification device (300), the MBR (400), the iron-carbon micro-electrolysis device (600) and the adsorption dephosphorization device (700).
The utility model discloses a water clean system based on electrolysis denitrogenation and MBR adopts one of underground, semi-underground or aboveground formula.
Adopt the utility model relates to a water deep purification system carries out water deep purification based on electrolysis denitrogenation and MBR, can include following step:
1) pretreatment: the polluted water collected by the pipeline is filtered by a coarse grating (110) and a fine grating (120) to remove larger solid particles, and then is precipitated by an aeration grit chamber (130) to remove impurities such as silt and the like in the water;
2) coagulating sedimentation: lifting the pretreated water body into a coagulation tank (210) through a lifting pump (140), adding a ferrous sulfate solution or a polyaluminium chloride solution through a coagulation dosing device, adding electrolytic water, mixing and stirring, feeding the water body after coagulation reaction into a coagulation aiding tank (220), adding a PAM solution through the coagulation aiding dosing device for coagulation aiding reaction, feeding the sewage after coagulation aiding reaction into a coagulation sedimentation tank (230), and performing solid-liquid separation to form a supernatant liquid area (231) on the upper layer of the coagulation sedimentation tank (230), a sludge concentration area (233) at the bottom of the coagulation sedimentation tank (230) and a solid-liquid separation area (232) in the middle of the coagulation sedimentation tank (230); when the precipitation amount formed in the coagulation aiding tank (220) is insufficient, a sludge reflux pump (270) is started, and part of sludge flows back into the coagulation aiding tank (220) from the coagulation aiding tank (230) to promote the generation of precipitates;
3) electrolytic denitrification: conveying the polluted water body subjected to the coagulating sedimentation in the step 2) to an electrolytic denitrification host (310) through an intermediate water tank (240) and a lifting pump (311) for electrolysis; during electrolysis, 3-12% of sodium hypochlorite solution or 2-6% of sodium chloride solution is added through an electrolyte adding system; feeding electrolyzed effluent of an electrolytic denitrification host (310) into a denitrification reaction tank (330) and uniformly distributing the electrolyzed effluent at the bottom of the denitrification reaction tank (330) through a water distributor to enable a water body to flow from bottom to top, wherein the retention time is 30-150 min, and oxygen and hydrogen generated by sodium hypochlorite and electrolysis react with ammonia nitrogen and nitrate nitrogen in a polluted water body respectively in the denitrification reaction tank (330) to generate nitrogen and water, so that the ammonia nitrogen and the nitrate nitrogen in the water body are removed;
4) micro-electricity to remove sodium hypochlorite: allowing the water body subjected to electrolytic denitrification to flow into an iron-carbon micro-electro-removal sodium hypochlorite device and stay for 5-20 min, so that excessive sodium hypochlorite and iron carbon react during electrolytic denitrification to eliminate the interference of the sodium hypochlorite on the operation of a subsequent biological aerated filter;
5) membrane Bioreactor (MBR) purification: conveying the water subjected to micro-electricity sodium hypochlorite removal to a Membrane Bioreactor (MBR) (400) for biochemical treatment and membrane filtration treatment, wherein the retention time of the polluted water in the filter is 150-240 min, so as to fully remove COD, BOD and total nitrogen in the water;
6) and (3) disinfection: feeding the water body treated by the MBR into a contact disinfection tank for disinfection, and after reaching the III or IV class water quality standard of surface water environmental quality Standard (GB3838-2002), feeding bottom sludge into a sludge treatment device (500) through a sludge pump for sludge dehydration treatment;
7) sludge treatment: conveying sludge in the coagulating sedimentation tank (230) and sludge in the secondary sedimentation tank (420) which are subjected to coagulating sedimentation in the step 2) into a gravity concentration tank (520) through a sludge pump (510), stirring, performing gravity sedimentation separation by using density difference of water, organic matters and inorganic matters, and conveying liquid in a supernatant layer into a Membrane Bioreactor (MBR) (400) for purification; adding a physicochemical conditioner into the lower inorganic layer in a physicochemical conditioning tank (530), then conveying the inorganic layer into a dehydrator (540) for dehydration into organic sludge blocks and water, and conveying the effluent of the dehydrator (540) into a biological aerated filter (400) for purification; and dehydrating and drying the organic matter enrichment layer in the middle layer to obtain the carbon fertilizer.
In step 2), the concrete steps of the coagulating sedimentation may be:
coagulation: the pretreated water body is lifted by a lifting pump (140) to enter a coagulation tank (210), and 10-120 g/m of the pretreated water body is added by a coagulation dosing device3Ferrous sulfate solution or 15-150 g/m3The polyaluminium chloride solution is mixed with electrolytic water accounting for 3 to 5 percent of the total amount of the inlet water and is continuously stirred, the stirring speed is 50 to 300r/min, and the coagulation reaction time is 3 to 15 min;
secondly, coagulation aiding: the water body after coagulation reaction in the step (1) enters a coagulation aid tank (220), PAM is added through a coagulation aid dosing device, and the relation between the weight of the added PAM and the volume of the sewage is 0.1-1 g/m3Stirring and reacting for 1-5 min at a stirring speed of 10-80 r/min;
precipitation: enabling the sewage subjected to coagulation aiding reaction in the step (2) to enter a coagulating sedimentation tank (230) for solid-liquid separation, wherein the solid-liquid separation time is 3-10 min, and forming a supernatant liquid zone on the upper layer of the coagulating sedimentation tank (230), a sludge concentration zone at the bottom of the coagulating sedimentation tank (230) and a solid-liquid separation zone in the middle of the coagulating sedimentation tank (230) after the solid-liquid separation for 3-10 min; and (3) when the sediment amount formed in the coagulation aiding tank (220) in the step (2) is insufficient, starting a sludge return pump (234), and returning part of sludge from the coagulation aiding tank (230) into the coagulation aiding tank (220) to promote sediment generation.
In the processes of coagulation, coagulation aiding and precipitation, phosphate radicals and hydrogen phosphate radicals in the water body react with ferric ions to generate ferric phosphate precipitates, so that total phosphorus in the water body is removed;
3Fe3++2PO4 3-＝Fe3(PO4)2↓
in addition, as a large amount of generated floc precipitates have large specific surface area and are charged, organic matters in the water body can be adsorbed, and the chromaticity and COD in the water body can be removed simultaneously;
after coagulating sedimentation treatment, 80-95% of SS in the water body is removed, so that the SS in the water body is less than or equal to 50mg/L, 40-90% of total phosphorus in the water body is removed, so that the total phosphorus in the water body is less than or equal to 1mg/L, and 40-75% of COD in the water body is removed together, so that the COD in the water body is less than or equal to 150 mg/L;
in step 3), the specific steps of the electrolytic denitrification can be as follows:
electrolysis: conveying the polluted water body after coagulating sedimentation to an electrolytic denitrification host (310) through an intermediate water tank (240) and a lift pump (311) for electrolysis for 10-150 s, wherein the working voltage of electrolysis is 2-500V, and the current density can be 0.5-10 mA/cm2(ii) a During electrolysis, 3-12% of sodium hypochlorite solution or 2-6% of sodium chloride solution is added through an electrolyte adding system;
② denitrification reaction: feeding the electrolyzed effluent of the electrolysis denitrification host machine into a denitrification reaction tank (330) and uniformly distributing the electrolyzed effluent at the bottom of the denitrification reaction tank (330) through a water distributor so that the water body flows from bottom to top, wherein the retention time is 30-150 min, and the sodium hypochlorite and the oxygen and the hydrogen generated by electrolysis react with the ammonia nitrogen and the nitrate nitrogen in the polluted water body respectively in the denitrification reaction tank (330) for 10-150 min to generate nitrogen and water so as to remove the ammonia nitrogen and the nitrate nitrogen in the water body; the working voltage of the electrolytic denitrification host (310) is 2-500V, and the current density is 0.05-10 mA/cm2(ii) a Through electrolytic denitrification, 50mg/L of ammonia nitrogen in the water body is reduced to be less than or equal to 1mg/L, and the total nitrogen in the water body is reduced to be less than or equal to 5mg/L from 10-70 mg/L; the electrolytic denitrification reaction also removes 5 to 15 percent of COD and 5 to 10 percent of total phosphorus in the water bodyMeanwhile, the dissolved oxygen in the water body can be increased to more than 7 mg/L.
The principle of electrolysis of sodium hypochlorite solution to remove ammonia nitrogen is that hypochlorous acid reacts with ammonia to finally generate nitrogen.
NaOCl+H2O→HOCl+NaOH
NH3+HOCl→NH2Cl+H2O (monochloramine)
NH2Cl+HOCl→NHCl2+H2O (dichloramine)
2NHCl2+HOCl→N2↑+3HCl+H2O (denitrogenation main reaction one)
The main reaction formula is as follows:
2NH3+3NaOCl→N2↑+3NaCl+3H2O
principle of deammoniation (side reaction)
At the same time, the radical O.produced by electrolysis reacts with ammonia to produce nitrate radical.
2NH4 ++5O2→2NO3 -+4H2O
In addition, hydrogen generated by electrolysis reacts with nitrate and nitrite in the water body under the action of the catalyst to generate nitrogen, so that nitrate nitrogen in the water body is removed.
NO3 -+H2—→NO2 -+H2O
2NO2 -+2H2—→N2↑+2H2O (total nitrogen removal reaction)
In the step 4), when sodium hypochlorite is removed by microelectro, the retention time of iron-carbon microelectrolysis can be 10-30 min; the content of sodium hypochlorite in the micro-electrolysis effluent is less than or equal to 0.1 mg/L.
After the treatment of the method of the utility model, the effect prediction of removing main sewage in each step of water purification is as shown in the following table 1:
TABLE 1 prediction of the effectiveness of water purification steps in removing major waste materials
The residence time of each step after the above treatment is shown in Table 2.
Table 2 residence time units for the procedure: min
| Pretreatment of | Coagulating sedimentation | Electrolytic denitrification | Micro-electrolysis | MBR | Deep phosphorus removal | Total up to |
| 10～15 | 25～30 | 30～40 | 10～20 | 120～300 | 10～15 | 235～420 |
After the water body purification system combining the electrolytic denitrification and the membrane bioreactor is adopted and treated by the steps, the COD in the water body can be removed by 80-95%, so that the COD of the effluent is less than or equal to 20 mg/L; BOD is removed by 95-99%, so that BOD of effluent is less than or equal to 4 mg/L; the total phosphorus is removed by 90-95 percent, so that the total phosphorus of the effluent is less than or equal to 0.1 mg/L; the ammonia nitrogen of the effluent is less than or equal to 1.0mg/L, the ammonia nitrogen is removed by 95-99.99%, the total nitrogen of the effluent is less than or equal to 1mg/L, and the total nitrogen is removed by 80-95%; the chroma is removed by 80 to 95 percent, and the dissolved oxygen is increased to more than 7 mg/L. Is particularly suitable for the purification treatment of water bodies with poor V-class water quality or black and odorous water bodies, so that the water bodies reach the III-class or IV-class water quality standard of surface water environmental quality standard (GB 3838-2002). The main indexes of inlet and outlet water for deep purification of sewage or water are shown in table 3.
TABLE 3 Main indices of inlet and outlet water for purifying sewage or water
| Serial number | Item | Unit of | Inflow water | Discharging water | Removal Rate (%) |
| 1 | pH | Dimensionless | 6～9 | 6～9 | - |
| 2 | Dissolved oxygen is not less than | mg/L | - | 7 | -600 |
| 3 | Chemical Oxygen Demand (COD) is less than or equal to | mg/L | 800 | 20 | 97.5 |
| 4 | Biochemical Oxygen Demand (BOD) less than or equal to five days | mg/ |
350 | 4 | 98.9 |
| 5 | Ammonia Nitrogen (NH)3-N)≤ | mg/L | 50 | 1 | 98.0 |
| 6 | Total phosphorus (measured as P) is less than or equal to | mg/L | 10 | 0.1 | 99.0 |
| 7 | Total nitrogen (calculated by N) is less than or equal to | mg/L | 70 | 1 | 98.57 |
| 8 | Less than or equal to petroleum | mg/L | - | 0.5 | - |
| 9 | Anionic surfactant is less than or equal to | mg/L | 0.3 | - | |
| 10 | Fecal coliform group | Per L | 3 |
The utility model overcomes the defects of poor effluent quality, large investment, long purification period and large occupied area of the treatment process or the water body purification technology of the existing sewage treatment plant, so that the effluent of the sewage treatment plant reaches the IV-class or even III-class water quality standard of the surface water environment quality standard (GB3838-2002), the water quality is improved, the water ecological system is recovered, and the reconstruction and the healthy sustainable development of the river and lake ecological system are realized. Compared with the prior art, the utility model discloses following outstanding effect has:
1. high water quality and changing sewage into water resource
Adopt the utility model discloses water clean system and method based on electrolytic denitrification and membrane bioreactor all reach "surface water environmental quality standard" (GB3838-2002) III class or IV water quality standard including total nitrogen after purifying the water, and dissolved oxygen content is greater than 7mg/L, has directly been transformed into the water resource with sewage, in discharging the natural water, can effectively improve the dissolved oxygen of water, restrain the growth of alga, improve quality of water comprehensively, can regard as industrial and agricultural production and commercial water simultaneously.
2. Eliminate nitrogen and phosphorus pollution from source
At present, nitrogen and phosphorus in water body seriously exceed the standard, and eutrophication of water bodies such as rivers and lakes is caused, so that blue algae in many lakes in China explode year after year. In order to radically treat blue algae, China invests a large amount of manpower and material resources, but the effect is not high. As the discharge standard of pollutants for municipal wastewater treatment plants (GB 18918 + 2002) executed by the existing wastewater treatment plants is that the total nitrogen is less than or equal to 15mg/L and the total phosphorus is less than or equal to 0.5mg/L, and a large amount of nitrogen and phosphorus enter a water body along with the discharge water of the wastewater treatment plants, so that the nitrogen and phosphorus in the water body are greatly enriched, the discharge water of the wastewater treatment plants is one of the main sources of the nitrogen and phosphorus in the water body. After the sewage purification system and the method thereof based on the electrolytic denitrification and the membrane bioreactor of the utility model are used for purifying sewage, the total nitrogen of the water body is less than or equal to 1mg/L, and the total phosphorus is less than or equal to 0.1mg/L, which all reach the III or IV water quality standard of the environmental quality standard of surface water (GB3838-2002), and the nitrogen and phosphorus pollution of the water body can be thoroughly eradicated from the source.
3. Simple process flow
Adopt the utility model discloses only handle main processes such as coagulation, electrolytic denitrification and MBR to sewage, the production process flow is more simple than current sewage treatment production process flow, and building structures still less.
4. Investment saving
At present, the investment of construction of fixed assets of ten thousand tons per day sewage treatment plants of the mainstream urban sewage treatment process at home and abroad is about 3500-5000 ten thousand yuan, and the investment of construction of fixed assets of ten thousand tons per day sewage treatment plants of the deep water purification system of the utility model is about 3300-4500 ten thousand yuan, which can save the investment by about 10-20% compared with the prior art.
5. Low running cost
Adopt the utility model discloses a running cost that deep purification of water degree of depth clean system carried out deep purification to sewage is 15% ~ 20% than current sewage town sewage treatment plant's running cost.
6. Saving a lot of land
At present, when sewage treatment plants constructed by an activated sludge method are adopted at home and abroad to treat sewage, the retention time is more than 17 hours, some sewage treatment plants even can reach more than 20 hours, the occupied area of each ten thousand tons of sewage treatment facilities is between 0.6 and 1 hectare, and the occupied area is large. Adopt the utility model discloses a when water degree of depth clean system handled the water, the dwell time of water only has 5 ~ 7 hours, and device area only has traditional sewage treatment plant's third, and area is little, can save land resource in a large number, is particularly suitable for the nervous city of land resource.
7. Short construction period
The utility model discloses a water deep purification system's essential element coagulating sedimentation device, electrolytic denitrification device, MBR device, absorption phosphorus removal device etc. all are the modular equipment, and the essential equipment is all produced at the mill, when adopting these equipment construction sewage treatment plant, as long as assemble these modular equipment at sewage treatment plant, need not a large amount of construction structures, so, the construction period of sewage treatment plant's construction period than traditional sewage treatment plant will shorten more than half, and construction period is short.
Drawings
FIG. 1 is a schematic diagram of the water body purification device based on electrolytic denitrification and MBR
FIG. 2 is a schematic view of the pretreatment apparatus (100) of the present invention;
fig. 3 is a schematic view of the coagulating sedimentation device (200) of the present invention;
FIG. 4 is a schematic view of an electrolytic denitrification apparatus (300) according to the present invention;
fig. 5 is a schematic diagram of the MBR apparatus (400) of the present invention;
FIG. 6 is a schematic view of the sludge dehydrating apparatus (500) of the present invention
Fig. 7 is a schematic diagram of a microelectrolysis sodium hypochlorite residue removing device (600) of the present invention;
fig. 8 is a schematic view of the adsorption phosphorus removal device (700) of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by a person of ordinary skill in the art without creative efforts belong to the protection scope of the present invention.
Referring to fig. 1, the embodiment of the present invention provides a water deep purification system, include: pretreatment device (100), coagulating sedimentation device (200), electrolysis denitrification device (300), indisputable carbon microelectrolysis device (600), MBR device (400), adsorb phosphorus removal device (700) and sludge treatment device (500):
a pretreatment device (100), referring to fig. 2, the pretreatment device (100) comprises a coarse grating (110), a fine and coarse grating (120), an aeration grit chamber (130) and a lift pump (140) which are sequentially communicated; the water inlet of the coarse grating (110) is communicated with a water inlet pipeline of a polluted water body to be treated, the water outlet of the coarse grating (110) is communicated with the water inlet of the fine and coarse grating (120), the water outlet of the fine and coarse grating (120) is communicated with the water inlet of the aeration grit chamber (130), and the water outlet of the aeration grit chamber (130) is communicated with the water inlet of the lift pump (140);
(II) a coagulating sedimentation device (200), referring to fig. 3, the coagulating sedimentation device (200) comprises a coagulating basin (210), a coagulation aiding basin (220), a coagulating sedimentation basin (230), an intermediate water pool (240) and a sludge pool (250) which are communicated in sequence; the coagulating sedimentation tank (230) is provided with a clear water outlet (231) and a sludge outlet (232); the water inlet of the coagulation tank (210) is communicated with the water outlet of a lift pump (140) of the pretreatment device (100), the water outlet of the coagulation tank (210) is communicated with the water inlet of a coagulation aiding tank (220), and the water outlet of the coagulation aiding tank (220) is communicated with the water inlet of a coagulation sedimentation tank (230); a clear water outlet (231) of the coagulation sedimentation tank (230) is communicated with a water inlet of the intermediate water tank (240), a water outlet of the intermediate water tank (240) is communicated with a water inlet of an electrolytic denitrification host (310) of the electrolytic denitrification device (300), and a lifting pump (311) is further arranged in a connecting pipeline between the clear water outlet and the electrolytic denitrification host (310); a sludge outlet (232) of the coagulation sedimentation tank (230) is communicated with an inlet of a sludge collection tank (250), and an outlet of the sludge collection tank (250) is communicated with an inlet of a sludge dewatering device (500);
(III) an electrolytic denitrification device (300), referring to FIG. 4, the electrolytic denitrification device (300) comprises an electrolytic denitrification host (310), a direct current power supply (320) and a denitrification reaction tank (330), wherein a water inlet of the electrolytic denitrification host (310) is used for clear water entering after coagulating sedimentation, and a water outlet of the electrolytic denitrification host (310) is respectively communicated with a water inlet (331) of the denitrification reaction tank (330) and a water inlet of the coagulating sedimentation tank (210) through a tee joint (311);
(IV) a membrane bioreactor (400), referring to FIG. 5, the membrane bioreactor is abbreviated as MBR, and is composed of a biological reaction tank body (410), an aeration pipe (420), a membrane module (430), an aeration fan (440), a backwashing water pipe (450), a water outlet (411), a sludge outlet (412) and a disinfection tank (460); the water inlet of the membrane bioreactor (400) is communicated with the water outlet of a denitrification reaction tank (330) of the electrolytic denitrification device (300) system, and the water outlet of the membrane bioreactor (400) is communicated with the water outlet of the disinfector (460) and flows into the disinfection tank (470) or a drainage system;
(V) a sludge treatment device (500), referring to FIG. 6, the sludge treatment device (500) comprises a sludge pump (510), a gravity concentration tank (520), a physicochemical conditioning tank (530) and a dewatering machine (540), wherein the inlet of the sludge pump (510) is communicated with a sludge outlet (232) of the coagulation sedimentation tank (230) and a sludge outlet (414) of a Membrane Bioreactor (MBR) biological tank (410), the outlet of the sludge pump (510) is communicated with the inlet of the gravity concentration tank (520), the sludge outlet (521) of the gravity concentration tank (520) is communicated with the inlet (531) of the physicochemical conditioning tank (530), and the sewage outlet (522) of the gravity concentration tank (520) is communicated with the water inlet of the membrane bioreactor (410); the outlet of the physicochemical conditioning pool (530) is communicated with the sludge inlet of the dehydrator (540), the sludge blocks of the dehydrator (540) are collected in the sludge collecting plateau, and the sewage of the dehydrator (540) is communicated with the water inlet of the Membrane Bioreactor (MBR) (410).
The coagulating sedimentation device (200) is one of a high-efficiency sedimentation device, a magnetic coagulation device and a supermagnetic coagulating sedimentation device.
Specifically, the coagulation tank (210) of the coagulation sedimentation device (200) further comprises a coagulant dosing device (211) and a stirrer (212).
Furthermore, ferrous sulfate with the mass ratio of 5-10% or polyaluminium chloride solution with the mass ratio of 10-15% is stored in the coagulant dosing device (211).
Specifically, the coagulant aid tank (220) further comprises a coagulant aid dosing device (221) and a stirrer (222).
Furthermore, a PAM solution with the mass ratio of 1-2 per mill is stored in the coagulant aid dosing device (221).
Specifically, the electrolytic denitrification device also comprises an electrolyte adding device (340), which is composed of an electrolyte solution storage tank (341), an electrolyte solution preparation tank (342), an electrolyte solution delivery pump (343) and an electrolyte solution flowmeter (344), wherein the electrolyte solution is delivered to the electrolyte solution storage tank (341) through the pump (345) for storage after the electrolyte solution preparation tank (342) is prepared. When the electrolytic denitrification device works, an electrolyte solution delivery pump (343) is started and is input into a polluted water body pipeline through an electrolyte solution flowmeter (344), and then the polluted water body pipeline enters a main machine of the electrolytic denitrification device for electrolysis;
more specifically, the electrolyte adding device (340) is used for adding 3-12% of sodium hypochlorite solution or 2-6% of sodium chloride solution into the electrolytic denitrification device; the electrolyte solution preparation tank (342) is used for preparing 4-12% sodium hypochlorite solution or 2-6% sodium chloride solution;
preferably, when ammonia nitrogen and total nitrogen are removed, an electrolyte adding device (340) is adopted to add 3% -12% of sodium hypochlorite solution into the electrolytic denitrification device according to the concentration of ammonia nitrogen in the water body;
more preferably, when ammonia nitrogen and total nitrogen are removed, an electrolyte adding device (340) is adopted to add 3% -5% of sodium hypochlorite solution into the electrolytic denitrification device according to the concentration of ammonia nitrogen in the water body;
specifically, the electrolytic denitrification device also comprises an electrolytic main machine pickling system (350) which is composed of a pickling solution preparation tank (351) and a pickling solution delivery pump (352). The acid washing solution adopts 2 to 3 percent hydrochloric acid solution or 3 to 5 percent citric acid solution. When the electrode of the electrolytic denitrification device is polluted and the electrolytic efficiency is reduced, the electrolytic denitrification device stops working, and the acid cleaning system (350) is started to remove the scale deposited on the surface of the electrode.
Furthermore, the wastewater of the acid washing system (350) enters the coagulating sedimentation purification treatment.
Specifically, a micro-electrolysis device (600) can be arranged in front of the Membrane Bioreactor (MBR), referring to fig. 7, the micro-electrolysis device (600) is composed of a tank body (610), a support frame (620), a support layer (630), an iron-carbon layer (640) and a filter material layer (650); the micro-electrolysis device (600) is also provided with a water inlet (611), a water outlet (612), a sludge outlet (613), a backwashing pipe and a backwashing water outlet (614); the outlet of the backwashing water outlet (614) is connected with the water inlet of the coagulating sedimentation device (200). The micro-electrolysis device (600) is mainly used for consuming excessive sodium hypochlorite during electrolytic denitrification to ensure the normal growth of bacteria in the biological aerated filter.
Specifically, a deep phosphorus removal device can be arranged behind the Membrane Bioreactor (MBR), and the deep phosphorus removal device is an adsorption phosphorus removal device.
Specifically, referring to fig. 8, the adsorption phosphorus removal device (700) at least comprises an adsorption tower (710), a desorption regeneration system (720) and a phosphorus precipitation recovery system (730).
Further, the continuous operation is needed, and the adsorption phosphorus removal device at least comprises two adsorption towers (710), a desorption regeneration system (720) and a phosphorus precipitation recovery system (730).
The adsorption tower (710) is composed of a valve (711), a water inlet (712), a lower supporting plate (713), adsorption packing (714), an upper supporting plate (715), a water outlet (716), a tee joint (717), a tee joint (718) and a valve (719); the desorption regeneration system (720) is composed of a desorption regeneration liquid storage tank (721), a regeneration liquid delivery pump (722), a flow meter (723), a regeneration liquid inlet valve (724), an adsorption tower (710), a clear water tank (728), a clear water pump (729), an eluent water outlet valve (726) and an eluent storage tank (727); the desorption regeneration liquid storage tank (721) is connected to the adsorption tower (710) through a regeneration liquid delivery pump (722), a water inlet valve (724) and a water inlet tee joint; the clean water tank (728) is connected with the adsorption tower (710) through a clean water pump (729) and a tee joint (718) and a water outlet tee joint (717); the eluent storage tank (727) is connected with the adsorption tower (710) through an eluent outlet valve (726) and an outlet tee joint (717);
the phosphorus precipitation recovery system (730) consists of a desorption liquid delivery pump (731), an inlet valve (732), a precipitation reaction tank (733), a stirrer (734), a precipitant storage tank (735), a dosing pump (736), a precipitation tank (739), a delivery pump (738), a concentration tank (737) and a recovery pump; the inlet of the desorption liquid delivery pump (731) is connected with the water outlet of the eluent storage tank (727), the water outlet of the desorption liquid delivery pump (731) is connected with the inlet of a desorption liquid inlet valve (732), and the outlet of the desorption liquid inlet valve (732) is connected with the phosphorus precipitation reaction tank (733); the sedimentation reaction tank (733) is also provided with a stirrer (734) and a precipitator storage tank (735), the water outlet of the sedimentation reaction tank (733) is connected with the water inlet of a phosphorus sedimentation tank (739), the water outlet of the phosphorus sedimentation recovery tank (739) is connected with the inlet of a concentration tank (737) through a delivery pump (738), and the outlet of the concentration tank (737) is connected with a desorption regeneration liquid storage tank (721) through a recovery pump.
Specifically, a calcium hydroxide saturated solution is stored in the precipitant storage tank (735).
Specifically, an inlet of a sludge pump (510) is respectively communicated with sludge outlets of the coagulating sedimentation device (200) and a Membrane Bioreactor (MBR) (400), an outlet of the sludge pump (510) is communicated with an inlet of the gravity concentration tank (520), an upper layer area, a middle layer area and a lower layer area from top to bottom are arranged in the gravity concentration tank (520), a water outlet of the upper layer area is used for being communicated with a water inlet of the MBR, an outlet of the lower layer area is communicated with an inlet of the dehydrator (540), and the middle layer area, the physicochemical conditioning tank (530) and the dehydrator (540) are sequentially communicated in sequence; the gravity concentration tank (520) is also provided with a stirrer.
The application is given, the utility model discloses carry out the method of water deep purification, including following step:
1) pretreatment: the polluted water collected by the pipeline is filtered by a coarse grating (110) and a fine grating (120) to remove larger solid particles, and then is precipitated by an aeration grit chamber (130) to remove impurities such as silt and the like in the water;
2) coagulating sedimentation: lifting the pretreated water body into a coagulation tank (210) through a lifting pump (140), adding a ferrous sulfate solution or a polyaluminium chloride solution through a coagulation dosing device, adding electrolytic water, mixing and stirring, feeding the water body after coagulation reaction into a coagulation aiding tank (220), adding a PAM solution through the coagulation aiding dosing device for coagulation aiding reaction, feeding the sewage after coagulation aiding reaction into a coagulation sedimentation tank (230), and performing solid-liquid separation to form a supernatant liquid area (231) on the upper layer of the coagulation sedimentation tank (230), a sludge concentration area (233) at the bottom of the coagulation sedimentation tank (230) and a solid-liquid separation area (232) in the middle of the coagulation sedimentation tank (230); when the precipitation amount formed in the coagulation aiding tank (220) is insufficient, a sludge reflux pump (270) is started, and part of sludge flows back into the coagulation aiding tank (220) from the coagulation aiding tank (230) to promote the generation of precipitates;
3) electrolytic denitrification: conveying the polluted water body subjected to the coagulating sedimentation in the step 2) to an electrolytic denitrification host (310) through an intermediate water tank (240) and a lift pump (311) for electrolysis, wherein the working voltage of the electrolysis is 2-500V, and the current density can be 0.5-10 mA/cm2(ii) a During electrolysis, 3-12% of sodium hypochlorite solution or 2-6% of sodium chloride solution is added through an electrolyte adding system; feeding electrolyzed effluent of an electrolytic denitrification host (310) into a denitrification reaction tank (330) and uniformly distributing the electrolyzed effluent at the bottom of the denitrification reaction tank (330) through a water distributor to enable a water body to flow from bottom to top, wherein the retention time is 30-150 min, and oxygen and hydrogen generated by sodium hypochlorite and electrolysis react with ammonia nitrogen and nitrate nitrogen in a polluted water body respectively in the denitrification reaction tank (330) to generate nitrogen and water, so that the ammonia nitrogen and the nitrate nitrogen in the water body are removed;
4) micro-electricity to remove sodium hypochlorite: allowing the water body subjected to electrolytic denitrification to flow into an iron-carbon micro-electro-removal sodium hypochlorite device and stay for 5-20 min, so that excessive sodium hypochlorite and iron carbon react during electrolytic denitrification to eliminate the interference of the sodium hypochlorite on the operation of a subsequent biological aerated filter;
5) membrane Bioreactor (MBR) purification: conveying the water subjected to micro-electricity sodium hypochlorite removal to a Membrane Bioreactor (MBR) (400) for biochemical treatment and membrane filtration treatment, wherein the retention time of the polluted water in the filter is 120-300 min, so as to fully remove COD, BOD and total nitrogen in the water;
6) and (3) disinfection: feeding the water body treated by the MBR into a contact disinfection tank for disinfection, and after reaching the III or IV class water quality standard of surface water environmental quality Standard (GB3838-2002), feeding bottom sludge into a sludge treatment device (500) through a sludge pump for sludge dehydration treatment;
7) sludge treatment: conveying sludge in the coagulating sedimentation tank (230) and sludge in the secondary sedimentation tank (420) which are subjected to coagulating sedimentation in the step 2) into a gravity concentration tank (520) through a sludge pump (510), stirring, performing gravity sedimentation separation by using density difference of water, organic matters and inorganic matters, and conveying liquid in a supernatant layer into a Membrane Bioreactor (MBR) (400) for purification; adding a physicochemical conditioner into the lower inorganic layer in a physicochemical conditioning tank (530), then conveying the inorganic layer into a dehydrator (540) for dehydration into organic sludge blocks and water, and conveying the effluent of the dehydrator (540) into a biological aerated filter (400) for purification; and dehydrating and drying the organic matter enrichment layer in the middle layer to obtain the carbon fertilizer.
In step 2), the concrete steps of the coagulating sedimentation may be:
coagulation: the pretreated water body is lifted by a lifting pump (140) to enter a coagulation tank (210), and 10-120 g/m of the pretreated water body is added by a coagulation dosing device3Ferrous sulfate solution or 15-150 g/m3The polyaluminium chloride solution is mixed with electrolytic water accounting for 3 to 5 percent of the total amount of the inlet water and is continuously stirred, the stirring speed is 50 to 300r/min, and the coagulation reaction time is 3 to 15 min;
secondly, coagulation aiding: the water body after coagulation reaction in the step (1) enters a coagulation aid tank (220), PAM is added through a coagulation aid dosing device, and the relation between the weight of the added PAM and the volume of the sewage is 0.1-1 g/m3Stirring and reacting for 1-5 min at a stirring speed of 10-80 r/min;
precipitation: enabling the sewage subjected to coagulation aiding reaction in the step (2) to enter a coagulating sedimentation tank (230) for solid-liquid separation, wherein the solid-liquid separation time is 3-10 min, and forming a supernatant liquid zone on the upper layer of the coagulating sedimentation tank (230), a sludge concentration zone at the bottom of the coagulating sedimentation tank (230) and a solid-liquid separation zone in the middle of the coagulating sedimentation tank (230) after the solid-liquid separation for 3-10 min; and (3) when the sediment amount formed in the coagulation aiding tank (220) in the step (2) is insufficient, starting a sludge return pump (234), and returning part of sludge from the coagulation aiding tank (230) into the coagulation aiding tank (220) to promote sediment generation.
In the processes of coagulation, coagulation aiding and precipitation, phosphate radicals and hydrogen phosphate radicals in the water body react with ferric ions to generate ferric phosphate precipitates, so that total phosphorus in the water body is removed;
3Fe3++2PO4 3-＝Fe3(PO4)2↓
in addition, as a large amount of generated floc precipitates have large specific surface area and are charged, organic matters in the water body can be adsorbed, and the chromaticity and COD in the water body can be removed simultaneously;
after coagulating sedimentation treatment, 80-95% of SS in the water body is removed, so that the SS in the water body is less than or equal to 50mg/L, 40-90% of total phosphorus in the water body is removed, so that the total phosphorus in the water body is less than or equal to 1mg/L, and 40-75% of COD in the water body is removed together, so that the COD in the water body is less than or equal to 150 mg/L;
in the electrolytic denitrification, the method comprises the following steps:
electrolysis: conveying the polluted water body after coagulating sedimentation to an electrolytic denitrification host (310) through an intermediate water tank (240) and a lift pump (311) for electrolysis for 10-150 s, wherein the working voltage of electrolysis is 2-500V, and the current density can be 0.5-10 mA/cm2(ii) a During electrolysis, 3-12% of sodium hypochlorite solution or 2-6% of sodium chloride solution is added through an electrolyte adding system;
② denitrification reaction: feeding the electrolyzed effluent of the electrolysis denitrification host machine into a denitrification reaction tank (330) and uniformly distributing the electrolyzed effluent at the bottom of the denitrification reaction tank (330) through a water distributor (331) to enable the water body to flow from bottom to top, wherein the retention time is 30-150 min, and the oxygen and the hydrogen generated by sodium hypochlorite and electrolysis respectively react with the ammonia nitrogen and the nitrate nitrogen in the polluted water body in a denitrification reaction tank (330) for 10-150 min to generate nitrogen and water, so that the ammonia nitrogen and the nitrate nitrogen in the water body are removed; the working voltage of the electrolytic denitrification host (310) is 35-90V, and the current density is 3-50 mA/cm2(ii) a Through electrolytic denitrification, 50mg/L of ammonia nitrogen in the water body is reduced to be less than or equal to 1mg/L, and the total nitrogen in the water body is reduced to be less than or equal to 5mg/L from 10-70 mg/L;and removing 5-15% of COD and 5-10% of total phosphorus in the water body through the electrolytic denitrification reaction, and simultaneously increasing the dissolved oxygen in the water body to be more than 7 mg/L.
The principle of electrolysis of sodium hypochlorite solution to remove ammonia nitrogen is that hypochlorous acid reacts with ammonia to finally generate nitrogen.
NaOCl+H2O→HOCl+NaOH
NH3+HOCl→NH2Cl+H2O (monochloramine)
NH2Cl+HOCl→NHCl2+H2O (dichloramine)
2NHCl2+HOCl→N2↑+3HCl+H2O (denitrogenation main reaction one)
The main reaction formula is as follows:
2NH3+3NaOCl→N2↑+3NaCl+3H2O
principle of deammoniation (side reaction)
At the same time, the radical O.produced by electrolysis reacts with ammonia to produce nitrate radical.
2NH4 ++5O2→2NO3 -+4H2O
In addition, hydrogen generated by electrolysis reacts with nitrate and nitrite in the water body under the action of the catalyst to generate nitrogen, so that nitrate nitrogen in the water body is removed.
NO3 -+H2—→NO2 -+H2O
2NO2 -+2H2—→N2↑+2H2O (total nitrogen removal reaction)
Specific examples are given below.
Example 1
A certain municipal sewage treatment plant adopts the production process of the utility model, which mainly comprises pretreatment (coarse grid, fine grid, aeration desilting tank), coagulating sedimentation, electrolytic denitrification, micro electrolysis, MBR, adsorption dephosphorization and disinfection.
TABLE 4 Water quality index of influent water from certain Sewage treatment plant
| Serial number | Basic control items | Measured value (mg/L) |
| 1 | |
521 |
| 2 | BOD | 236 |
| 3 | |
200 |
| 4 | Total nitrogen (in N) | 47.2 |
| 5 | Ammonia nitrogen (in N) | 42.7 |
| 6 | Total phosphorus (in terms of P) | 8 |
| 7 | Chroma (dilution multiple) | 80 |
| 8 | pH | 6～9 |
And the domestic sewage enters a water body purification system of the sewage treatment plant. The water body purification system comprises a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300) and a Membrane Bioreactor (MBR) (400). The purification system of the sewage treatment plant also comprises a sludge treatment device (500).
The sewage sequentially enters a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300) and a Membrane Bioreactor (MBR) (400).
Adding a ferrous sulfate coagulant into the coagulating sedimentation device, wherein the adding amount is 45mg/L, adding 1mg/L of coagulant aid PAM after coagulation reaction under the condition of 100 revolutions, reacting under the condition of 20 revolutions, and then feeding the mixture into a sedimentation tank for separation, wherein the water quality of the coagulating sedimentation effluent is shown in Table 5.
TABLE 5 Water quality index after coagulating sedimentation treatment of certain municipal wastewater
| Serial number | Basic control items | Sewage plant influent (mg/L) | Coagulation water (mg/L) | Removal Rate (%) |
| 1 | |
521 | 182.05 | 65.06 |
| 2 | BOD | 236 | 86.51 | 63.34 |
| 3 | |
200 | 35 | 82.50 |
| 4 | Animal and vegetable oil | - | 0.5 | |
| 5 | Petroleum products | - | 0.3 | |
| 6 | Total nitrogen (in N) | 47.2 | 45.31 | 4.00 |
| 7 | Ammonia nitrogen (in N) | 42.7 | 40.09 | 6.11 |
| 8 | Total phosphorus (in terms of P) | 8 | 0.95 | 88.13 |
| 9 | Dissolved oxygen | - | 2.5 | - |
| 10 | Chroma (dilution multiple) | 80 | 20 | 75.00 |
| 11 | pH | 6～9 | 6-9 | - |
The water body after coagulating sedimentation enters an electrolytic denitrification device (300) for treatment, the treated water body enters a denitrification reaction tank (330) for denitrification reaction, and the effluent indexes are shown in table 6. The working voltage of the electrolytic denitrification host (310) is 36.5V, and the current density is 3mA/cm2。
TABLE 6 Water quality index of a certain wastewater after coagulating sedimentation and electrolytic denitrification
| Serial number | Basic control items | Coagulation water (mg/L) | Denitrification effluent (mg/L) | Removal Rate (%) |
| 1 | COD | 182.05 | 101.35 | 44.33 |
| 2 | BOD | 86.51 | Not detected out | - |
| 3 | SS | 35 | 19 | 45.71 |
| 4 | Animal and vegetable oil | 0.5 | 0.4 | 20 |
| 5 | Petroleum products | 0.3 | 0.2 | 33.33 |
| 6 | Total nitrogen (in N) | 45.31 | 1.93 | 95.74 |
| 7 | Ammonia nitrogen (in N) | 40.09 | 1.12 | 97.21 |
| 8 | Total phosphorus (in terms of P) | 0.44 | 0.41 | 6.82 |
| 9 | Dissolved oxygen | 2.5 | 8.91 | - |
| 10 | Chroma (dilution multiple) | 20 | 5 | - |
| 11 | pH | 6～9 | 6～9 | - |
The effluent treated by the electrolytic denitrification device (300) is subjected to biochemical treatment and filtration by a Membrane Bioreactor (MBR) (400), and the quality of the purified effluent is shown in Table 7.
TABLE 7 Water quality index of a certain sewage after electrolytic denitrification and MBR system treatment
| Serial number | Basic control items | Denitrification effluent (mg/L) | MBR effluent (mg/L) | Removal Rate (%) |
| 1 | COD | 101.35 | 16.35 | 83.82 |
| 2 | BOD | 2 | - | |
| 3 | SS | 19 | 7 | 63.16 |
| 4 | Animal and vegetable oil | 0.4 | 0.2 | - |
| 5 | Petroleum products | 0.2 | 0.1 | - |
| 6 | Total nitrogen (in N) | 1.93 | 0.94 | 51.03 |
| 7 | Ammonia nitrogen (in N) | 1.12 | 0.81 | 27.68 |
| 8 | Total phosphorus (in terms of P) | 0.41 | 0.33 | 19.51 |
| 9 | Dissolved oxygen | 8.91 | 8.02 | - |
| 10 | Chroma (dilution multiple) | 5 | 1 | 80 |
| 11 | pH | 7～9 | 7～9 | - |
As can be seen from Table 7, the effluent index of a certain sewage after being purified by the sewage treatment process based on electrolytic denitrification and membrane bioreactor of the utility model completely meets the III-class water quality standard of the quality standard of surface water environment (GB 3838-2002).
Example 2
TABLE 8 Water quality index of certain sewage plant
| Serial number | Basic control items | Measured value (mg/L) |
| 1 | COD | 282.43 |
| 2 | BOD | 125.08 |
| 3 | SS | 155 |
| 4 | Total nitrogen (in N) | 42.22 |
| 5 | Ammonia nitrogen (in N) | 39.66 |
| 6 | Total phosphorus (in terms of P) | 8.1 |
| 7 | Chroma (dilution multiple) | 120 |
| 8 | pH | 7～9 |
| 9 | Dissolved oxygen | 2.3 |
And the water body enters the water body deep purification system. The water body purification system comprises a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300), a Membrane Bioreactor (MBR) (400) and adsorption dephosphorization (600). The water body purification system also comprises a sludge treatment device.
The water body enters a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300), a Membrane Bioreactor (MBR) (400) and an adsorption dephosphorization device (600) in sequence.
Adding 15% PAC solution into the coagulating sedimentation device (200), wherein the adding amount is 200mg/L, after coagulating reaction under the condition that the rotating speed is 100 revolutions, adding coagulant aid PAM according to 1mg/L, reacting under the condition that the rotating speed is 20 revolutions, and then entering a sedimentation tank for separation, wherein the water quality of coagulating sedimentation effluent is shown in Table 9.
TABLE 9 Water quality index of a certain wastewater after coagulating sedimentation treatment
| Serial number | Basic control items | Certain sewage intake (mg/L) | Coagulation water (mg/L) | Removal Rate (%) |
| 1 | COD | 282.43 | 93.11 | 67.03 |
| 2 | BOD | 125.08 | 71.55 | 42.80 |
| 3 | SS | 155 | 16 | 89.68 |
| 4 | Animal and vegetable oil | 0.9 | 0.5 | 44.44 |
| 5 | Petroleum products | 1.2 | 0.7 | 41.67 |
| 6 | Total nitrogen (in N) | 42.22 | 37.51 | 11.16 |
| 7 | Ammonia nitrogen (in N) | 39.66 | 37.09 | 6.48 |
| 8 | Total phosphorus (in terms of P) | 8.1 | 0.91 | 88.76 |
| 9 | Dissolved oxygen | 2.3 | 2.5 | - |
| 10 | Chroma (dilution multiple) | 120 | 30 | 75.00 |
| 11 | pH | 7～9 | 7～9 | - |
The water body after coagulating sedimentation enters an electrolytic denitrification device (300) for treatment, the treated water body enters a denitrification reaction tank (330) for denitrification reaction, and the effluent indexes are shown in the table 10. The working voltage of the electrolytic denitrification host (310) is 90V, and the current density is 0.5mA/cm2。
TABLE 10 Water quality index of a certain wastewater after coagulating sedimentation and electrolytic denitrification device treatment
| Serial number | Basic control items | Coagulation water (mg/L) | Denitrification effluent (mg/L) | Removal Rate (%) |
| 1 | COD | 93.11 | 66.21 | 7.62 |
| 2 | BOD | 71.55 | - | - |
| 3 | SS | 16 | 13 | 18.75 |
| 4 | Animal and vegetable oil | 0.5 | 0.1 | 80.00 |
| 5 | Petroleum products | 0.7 | 0.2 | 71.43 |
| 6 | Total nitrogen (in N) | 37.51 | 3.72 | 90.08 |
| 7 | Ammonia nitrogen (in N) | 37.09 | 0.57 | 98.46 |
| 8 | Total phosphorus (in terms of P) | 0.91 | 0.82 | 9.89 |
| 9 | Dissolved oxygen | 2.5 | 8.1 | - |
| 10 | Chroma (dilution multiple) | 30 | 20 | - |
| 11 | pH | 7～9 | 7.3 | - |
The effluent treated by the electrolytic denitrification device (300) is subjected to micro-electrolysis to remove residual sodium hypochlorite and then enters the MBR (400) for purification treatment; the quality of the effluent after the effluent treated by the electrolytic denitrification device (300) is treated by the MBR (400) and is adsorbed by the dephosphorization device (600) is shown in Table 11.
TABLE 11 Water quality index of a certain wastewater after electrolytic denitrification, MBR and adsorption dephosphorization
| Serial number | Basic control items | Denitrification effluent (mg/L) | MBR effluent (mg/L) | Removal Rate (%) |
| 1 | COD | 66.21 | 14.55 | 78.02 |
| 2 | BOD | - | 2 | |
| 3 | |
13 | 3 | 76.92 |
| 4 | Animal and vegetable oil | 0.1 | Not detected out | 100 |
| 5 | Petroleum products | 0.2 | Not detected out | 100 |
| 6 | Total nitrogen (in N) | 3.72 | 1.93 | 48.12 |
| 7 | Ammonia nitrogen (in N) | 0.57 | 0.35 | 38.60 |
| 8 | Total phosphorus (in terms of P) | 0.82 | 0.04 | 95.12 |
| 9 | Dissolved oxygen | 8.1 | 7.9 | |
| 10 | Chroma (dilution multiple) | 20 | 1 | 95 |
| 11 | pH | 7～9 | 7～9 |
As can be seen from Table 11, the effluent indexes of the sewage after pretreatment, coagulating sedimentation, electrolytic denitrification, micro-electrolysis, MBR and adsorption dephosphorization completely meet the III-class water quality standard of the quality Standard of surface Water Environment (GB 3838-2002).
Example 3
TABLE 12 Water quality index of a certain black and odorous water body
| Serial number | Basic control items | Measured value (mg/L) |
| 1 | COD | 449.47 |
| 2 | BOD | 219.84 |
| 3 | SS | 360.21 |
| 4 | Total nitrogen (in N) | 43.61 |
| 5 | Ammonia nitrogen (in N) | 27.96 |
| 6 | Total phosphorus (in terms of P) | 8.43 |
| 7 | Chroma (dilution multiple) | 29.59 |
| 8 | pH | 7.5 |
| 9 | Dissolved oxygen | 1.2 |
And the black and odorous water body enters the water body deep purification system. The water body purification system comprises a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300), a micro-electrolysis device (600) and a membrane bioreactor MBR (400). The water body purification system also comprises a sludge treatment device (500).
The water body enters a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300), a micro-electrolysis device (600) and a membrane bioreactor MBR (400) in sequence.
Adding a ferrous sulfate coagulant into the coagulating sedimentation device, wherein the adding amount is 50mg/L, adding 1mg/L of coagulant aid PAM after coagulation reaction under the condition of 100 revolutions, reacting under the condition of 20 revolutions, and then feeding the mixture into a sedimentation tank for separation, wherein the quality of the coagulating sedimentation effluent is as shown in Table 13.
TABLE 13 Water quality index after coagulating sedimentation treatment of certain black and odorous water body
| Serial number | Basic control items | Certain river channel water intake (mg/L) | Coagulation water (mg/L) | Removal Rate (%) |
| 1 | COD | 449.47 | 195.84 | 56.43 |
| 2 | BOD | 219.84 | 144.44 | 34.30 |
| 3 | SS | 360.21 | 18 | 95.00 |
| 4 | Animal and vegetable oil | 5 | 0.3 | 94.00 |
| 5 | Petroleum products | 2.3 | 0.2 | 91.30 |
| 6 | Total nitrogen (in N) | 43.61 | 29.42 | 32.52 |
| 7 | Ammonia nitrogen (in N) | 27.96 | 25.12 | 10.14 |
| 8 | Total phosphorus (in terms of P) | 8.43 | 0.18 | 97.86 |
| 9 | Dissolved oxygen | 1.20 | 2.1 | - |
| 10 | Chroma (dilution multiple) | 29.59 | 4.46 | 84.92 |
| 11 | pH | 7.5 | 7.6 | - |
The water body after coagulating sedimentation enters an electrolytic denitrification purification device (300) for treatment, the treated water body enters a denitrification reaction tank (330) for denitrification reaction, and the effluent indexes are shown in the table 14. The working voltage of the electrolytic denitrification host (310) is 39V, and the current density is 10mA/cm2. When the electrolytic denitrification host works, 4% sodium hypochlorite solution is mixed into the water body, and the adding amount is seven to ten per thousand (volume ratio).
TABLE 14 Water quality index of a black and odorous water after coagulating sedimentation and electrolytic denitrification device treatment
| Serial number | Basic control items | Coagulation water (mg/L) | Denitrification effluent (mg/L) | Removal Rate (%) |
| 1 | COD | 195.84 | 176.21 | 10.02 |
| 2 | BOD | 144.44 | Not detected out | - |
| 3 | SS | 18 | 13 | 27.78 |
| 4 | Animal and vegetable oil | 0.5 | 0.1 | 80.00 |
| 5 | Petroleum products | 0.5 | 0.2 | 60.00 |
| 6 | Total nitrogen (in N) | 29.37 | 3.72 | 87.33 |
| 7 | Ammonia nitrogen (in N) | 21.09 | 0.39 | 98.15 |
| 8 | Total phosphorus (in terms of P) | 0.81 | 0.69 | 14.81 |
| 9 | Dissolved oxygen | 2.5 | 8.1 | - |
| 10 | Chroma (dilution multiple) | 20 | 20 | - |
| 11 | pH | 7.6 | 7.3 | - |
The effluent treated by the plasma denitrification device (300) is purified by micro-electrolysis (600) and a membrane bioreactor MBR (400). The quality of the effluent water treated by the electrolytic denitrification device (300) after the advanced purification treatment by the micro-electrolysis (600) is shown in the table 15.
TABLE 15 Water quality index after plasma denitrification and MBR treatment of a certain black and odorous water body
| Serial number | Basic control items | Denitrification effluent (mg/L) | MBR effluent (mg/L) | Removal Rate (%) |
| 1 | COD | 176.21 | 17.64 | 89.99 |
| 2 | BOD | Not detected out | 2 | - |
| 3 | |
13 | 7 | 46.15 |
| 4 | Animal and vegetable oil | 0.1 | Not detected out | - |
| 5 | Petroleum products | 0.2 | Not detected out | - |
| 6 | Total nitrogen (in N) | 3.72 | 0.93 | 75.00 |
| 7 | Ammonia nitrogen (in N) | 0.39 | 0.35 | 10.26 |
| 8 | Total phosphorus (in terms of P) | 0.69 | 0.09 | 87.00 |
| 9 | Dissolved oxygen | 8.1 | 7.9 | -2.47 |
| 10 | Chroma (dilution multiple) | 20 | 1 | 95.00 |
| 11 | pH | 7.3 | 7.4 | - |
As can be seen from Table 15, the effluent indexes of the treated black and odorous water body of the severely polluted river completely meet the III-class water quality standard of the Water environmental quality Standard (GB 3838-2002).
Example 4
TABLE 16 Water quality index after precipitation in secondary sedimentation tank of certain sewage treatment plant
| Serial number | Basic control items | Measured value (mg/L) |
| 1 | COD | 57 |
| 2 | BOD | 19 |
| 3 | SS | 23 |
| 4 | Animal and vegetable oil | 3 |
| 5 | Petroleum products | 1.5 |
| 6 | Anionic surfactants | 1.2 |
| 7 | Total nitrogen (in N) | 23 |
| 8 | Ammonia nitrogen (in N) | 12 |
| 9 | Total phosphorus (in terms of P) | 1.0 |
| 10 | Chroma (dilution multiple) | 40 |
| 11 | pH | 7 |
After the effluent of the sewage treatment plant enters a coagulating sedimentation device (200) of a water body purification system for coagulation treatment, the effluent is subjected to denitrification treatment by an electrolytic denitrification host (310), the electrolytic working voltage is 500V, and the current density can be 0.5mA/cm2. The effluent treated by the main electrolytic denitrification machine enters a denitrification reaction tank (330) for denitrification reaction, and the effluent of the denitrification reaction tank (330) flows through water micro-electrolysis (600) for deep purification treatment.
When the mixed solution enters a coagulating sedimentation device (200) for coagulation treatment, as the total phosphorus in the water body is only 1mg/L and the concentration is low, a polyaluminum chloride (usually called PAC) solution is added according to 5mg/L, a 5% sodium hydroxide solution is added to adjust the pH to 7-8 (as the pH is 6-7), the mixed solution enters a coagulation tank after coagulation reaction at the rotation speed of 200 revolutions, a coagulant aid PAM is added according to 1mg/L, the mixed solution enters a coagulating sedimentation tank (230) for solid-liquid separation after coagulation at the rotation speed of 60 revolutions, and the effluent quality is as shown in Table 17.
TABLE 17 Water quality index of water precipitated in secondary precipitation tank of certain sewage treatment plant after coagulating sedimentation
| Serial number | Basic control items | Sewage plant influent (mg/L) | Coagulation water (mg/L) | Removal Rate (%) |
| 1 | COD | 57 | 34.2 | 40.00 |
| 2 | BOD | 19 | 13.00 | 31.58 |
| 3 | SS | 23 | 9 | 60.87 |
| 4 | Animal and vegetable oil | 3 | 0.5 | 83.33 |
| 5 | Petroleum products | 1.5 | 0.2 | 86.67 |
| 6 | Total nitrogen (in N) | 23 | 22.07 | 4.04 |
| 7 | Ammonia nitrogen (in N) | 12 | 11.51 | 4.08 |
| 8 | Total phosphorus (in terms of P) | 1.0 | 0.41 | 59.00 |
| 9 | Dissolved oxygen | 4.6 | 4.8 | - |
| 10 | Chroma (dilution multiple) | 40 | 20 | 50 |
| 11 | pH | 7 | 7.2 | - |
The effluent water treated by the coagulating sedimentation (200) enters an electrolytic denitrification host (310), the working voltage of the electrolytic denitrification host (310) is 56V, and the current density is 6mA/cm2. The effluent after the electrolytic denitrification (310) enters a denitrification reaction tank (330) for denitrification reaction, and the water quality of the effluent after the denitrification treatment is shown in the table 15.
TABLE 18 Water quality index of effluent from certain sewage plant after coagulating sedimentation and denitrification device treatment
| Serial number | Basic control items | Coagulation water (mg/L) | Denitrification effluent (mg/L) | Removal Rate (%) |
| 1 | COD | 34.2 | 32.31 | 5.56 |
| 2 | BOD | 15.00 | Not detected out | 100 |
| 3 | SS | 9 | 7 | 22.22 |
| 4 | Animal and vegetable oil | 0.5 | 0 | 100 |
| 5 | Petroleum products | 0.2 | 0 | 100 |
| 6 | Total nitrogen (in N) | 22.07 | 9 | 59.22 |
| 7 | Ammonia nitrogen (in N) | 11.51 | 1.32 | 88.53 |
| 8 | Total phosphorus (in terms of P) | 0.41 | 0.35 | 14.63 |
| 9 | Dissolved oxygen | 4.8 | 7.93 | - |
| 10 | Chroma (dilution multiple) | 20 | 20 | 0 |
| 11 | pH | 7.2 | 7.1 | - |
The effluent treated by the electrolytic denitrification device (300) is subjected to deep purification by micro-electrolysis (600).
The quality of the effluent water treated by the electrolytic denitrification device (300) after the advanced purification treatment by the micro-electrolysis (600) is shown in the table 19.
TABLE 19 Water quality index of effluent from certain sewage plant after electrolytic denitrification and micro-electrolysis treatment
| Serial number | Basic control items | Denitrification effluent (mg/L) | Micro-electrolysis water (mg/L) | Removal Rate (%) |
| 1 | COD | 32.31 | 18.75 | 41.97 |
| 2 | BOD | Not detected out | 1 | - |
| 3 | SS | 7 | 5 | 28.57 |
| 4 | Animal and vegetable oil | 0 | 0 | - |
| 5 | Petroleum products | 0 | 0 | - |
| 6 | Total nitrogen (in N) | 9 | 1.45 | 83.89 |
| 7 | Ammonia nitrogen (in N) | 1.32 | 0.76 | 42.42 |
| 8 | Total phosphorus (in terms of P) | 0.35 | 0.11 | 68.57 |
| 9 | Dissolved oxygen | 7.93 | 7.71 | - |
| 10 | Chroma (dilution multiple) | 20 | 20 | - |
| 11 | pH | 7.1 | 7.1 | - |
As can be seen from Table 19, the effluent indexes of the treated effluent of the sewage treatment plant completely meet IV-class water quality standards of surface water environment quality Standard (GB 3838-2002).
Example 5
TABLE 20 Water quality index of a slightly polluted Water body
| Serial number | Basic control items | Measured value (mg/L) |
| 1 | COD | 89.56 |
| 2 | BOD | 29.88 |
| 3 | SS | 69.67 |
| 4 | Total nitrogen (in N) | 43.61 |
| 5 | Ammonia nitrogen (in N) | 27.96 |
| 6 | Total phosphorus (in terms of P) | 5.44 |
| 7 | Chroma (dilution multiple) | 29.59 |
| 8 | pH | 7.5 |
| 9 | Dissolved oxygen | 1.2 |
And the micro-polluted water enters the water body purification system. The water body purification system comprises a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300) and a micro-electrolysis device (600). The water body purification system also comprises a sludge treatment device (500).
The water body enters a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300) and a micro-electrolysis device (600) in sequence.
Adding 10% of polyaluminium solution into the coagulating sedimentation device, wherein the adding amount is 40mg/L, after coagulating reaction at the rotating speed of 100 revolutions, adding 1mg/L of PAM (Polyacrylamide) as a coagulant aid, reacting at the rotating speed of 20 revolutions, and then separating in a sedimentation tank, wherein the water quality of coagulating sedimentation effluent is shown in Table 21.
TABLE 21 Water quality index after coagulating sedimentation treatment of a slightly polluted Water body
| Serial number | Basic control items | Certain river channel water intake (mg/L) | Coagulation water (mg/L) | Removal Rate (%) |
| 1 | COD | 89.56 | 25.81 | 72.30 |
| 2 | BOD | 29.88 | 14.45 | 51.64 |
| 3 | SS | 69.67 | 13 | 81.34 |
| 4 | Animal and vegetable oil | 5 | 0.3 | 94.00 |
| 5 | Petroleum products | 2.3 | 0.2 | 91.30 |
| 6 | Total nitrogen (in N) | 43.61 | 29.42 | 32.52 |
| 7 | Ammonia nitrogen (in N) | 27.96 | 25.12 | 10.14 |
| 8 | Total phosphorus (in terms of P) | 8.43 | 0.18 | 97.86 |
| 9 | Dissolved oxygen | 1.20 | 2.1 | - |
| 10 | Chroma (dilution multiple) | 29.59 | 4.46 | 84.92 |
| 11 | pH | 7.5 | 7.6 | - |
The water body after coagulating sedimentation enters an electrolytic denitrification purification device (300) for treatment, the treated water body enters a denitrification reaction tank (330) for denitrification reaction, and the effluent indexes are shown in a table 22. The working voltage of the electrolytic denitrification host (310) is 39V, and the current density is 7mA/cm2. When the electrolytic denitrification host works, 4% sodium hypochlorite solution is mixed into the water body, and the adding amount is seven to ten per thousand (volume ratio).
TABLE 22 Water quality index after coagulating sedimentation and electrolytic denitrification of a slightly polluted water body
| Serial number | Basic control items | Coagulation water (mg/L) | Denitrification effluent (mg/L) | Removal Rate (%) |
| 1 | COD | 25.81 | 16.21 | 37.19 |
| 2 | BOD | 14.45 | Not detected out | |
| 3 | |
13 | 11 | 15.38 |
| 4 | Animal and vegetable oil | 0.5 | 0.1 | 80.00 |
| 5 | Petroleum products | 0.5 | 0.2 | 60.00 |
| 6 | Total nitrogen (in N) | 29.37 | 3.72 | 87.33 |
| 7 | Ammonia nitrogen (in N) | 21.09 | 0.39 | 98.15 |
| 8 | Total phosphorus (in terms of P) | 0.81 | 0.69 | 14.81 |
| 9 | Dissolved oxygen | 2.5 | 8.1 | - |
| 10 | Chroma (dilution multiple) | 20 | 20 | - |
| 11 | pH | 7.6 | 7.3 | - |
The effluent treated by the plasma denitrification device (300) is subjected to deep purification by micro-electrolysis (600). The quality of the effluent water after the effluent water treated by the electrolytic denitrification device (300) is subjected to deep purification treatment by micro-electrolysis (600) is shown in a table 23.
TABLE 23 Water quality index after plasma Denitrification and micro-electrolysis treatment of a certain slightly polluted Water
| Serial number | Basic control items | Denitrification effluent (mg/L) | Micro-electrolysis water (mg/L) | Removal Rate (%) |
| 1 | COD | 16.21 | 12.10 | 25.35 |
| 2 | BOD | Not detected out | 2 | - |
| 3 | SS | 11 | 5 | 54.55 |
| 4 | Animal and vegetable oil | 0.1 | Not detected out | - |
| 5 | Petroleum products | 0.2 | Not detected out | - |
| 6 | Total nitrogen (in N) | 3.72 | 0.93 | 75.00 |
| 7 | Ammonia nitrogen (in N) | 0.39 | 0.35 | 10.26 |
| 8 | Total phosphorus (in terms of P) | 0.69 | 0.09 | 87.00 |
| 9 | Dissolved oxygen | 8.1 | 7.9 | -2.47 |
| 10 | Chroma (dilution multiple) | 20 | 1 | 95.00 |
| 11 | pH | 7.3 | 7.4 | - |
As can be seen from Table 23, the effluent indexes of the slightly polluted riverway water body after treatment completely meet the III-class water quality standard of the quality standard of surface water environment (GB 3838-2002).
Example 6
TABLE 24 Water quality index of a slightly polluted Water body
| Serial number | Basic control items | Measured value (mg/L) |
| 1 | COD | 69.51 |
| 2 | BOD | 27.80 |
| 3 | SS | 39.50 |
| 4 | Animal and vegetable oil | 4.6 |
| 5 | Petroleum products | 0.5 |
| 6 | Total nitrogen (in N) | 23.00 |
| 7 | Ammonia nitrogen (with N)Meter) | 12.95 |
| 8 | Total phosphorus (in terms of P) | 1.41 |
| 9 | Chroma (dilution multiple) | 50 |
| 10 | pH | 7.1 |
| 11 | Dissolved oxygen | 2.9 |
The micro-polluted water enters a water body purification system for experiment. The water body purification system comprises a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300) and a micro-electrolysis device (600).
The water body enters a pretreatment device (100), a coagulating sedimentation device (200), an electrolytic denitrification device (300) and a micro-electrolysis device (600) in sequence.
Adding 10% of polyaluminium solution into the coagulating sedimentation device, wherein the adding amount is 20mg/L, after coagulating reaction at the rotating speed of 100 revolutions, adding 1mg/L of PAM (Polyacrylamide) as a coagulant aid, reacting at the rotating speed of 20 revolutions, and then separating in a sedimentation tank, wherein the water quality of coagulating sedimentation effluent is shown in Table 25.
TABLE 25 Water quality index after coagulating sedimentation treatment of a slightly polluted Water body
| Serial number | Basic control items | Certain river channel water intake (mg/L) | Coagulation water (mg/L) | Removal Rate (%) |
| 1 | COD | 69.51 | 33.50 | 51.81 |
| 2 | BOD | 27.80 | 15.50 | 44.24 |
| 3 | SS | 39.50 | 11 | 72.15 |
| 4 | Animal and vegetable oil | 4.6 | 0.3 | 93.48 |
| 5 | Petroleum products | 0.5 | 0.2 | 60.00 |
| 6 | Total nitrogen (in N) | 23.00 | 21.49 | 6.57 |
| 7 | Ammonia nitrogen (in N) | 12.95 | 12.31 | 4.94 |
| 8 | Total phosphorus (in terms of P) | 1.41 | 0.18 | 87.23 |
| 9 | Dissolved oxygen | 2.9 | 2.8 | - |
| 10 | Chroma (dilution multiple) | 50 | 4 | 92.00 |
| 11 | pH | 7.1 | 7.1 | - |
The water body after coagulating sedimentation enters an electrolytic denitrification purification device (300) for treatment, the treated water body enters a denitrification reaction tank (330) for denitrification reaction, and the effluent indexes are shown in the table 26. The working voltage of the electrolytic denitrification host (310) is 2V, and the current density is 0.5mA/cm2. When the electrolytic denitrification host works, 4% sodium hypochlorite solution is mixed into the water body, and the adding amount is seven to ten per thousand (volume ratio).
TABLE 26 Water quality index after coagulating sedimentation and electrolytic denitrification of a slightly polluted water body
| Serial number | Basic control items | Coagulation water (mg/L) | Denitrification effluent (mg/L) | Removal Rate (%) |
| 1 | COD | 33.50 | 26.25 | 21.70 |
| 2 | BOD | 15.50 | Not detected out | - |
| 3 | SS | 11 | 11 | 0 |
| 4 | Animal and vegetable oil | 0.3 | 0.1 | 66.67 |
| 5 | Petroleum products | 0.2 | 0.05 | 75.00 |
| 6 | Total nitrogen (in N) | 21.49 | 1.42 | 93.39 |
| 7 | Ammonia nitrogen (in N) | 12.31 | 0.75 | 93.91 |
| 8 | Total phosphorus (in terms of P) | 0.18 | 0.17 | 5.56 |
| 9 | Dissolved oxygen | 2.8 | 8.1 | - |
| 10 | Chroma (dilution multiple) | 4 | 2 | - |
| 11 | pH | 7.1 | 7.0 | - |
The effluent treated by the plasma denitrification device (300) is subjected to deep purification by micro-electrolysis (600). The quality of the effluent water after the effluent water treated by the electrolytic denitrification device (300) is subjected to deep purification treatment by micro-electrolysis (600) is shown in a table 27.
TABLE 27 Water quality index after plasma Denitrification and micro-electrolysis treatment of a slightly polluted Water
| Serial number | Basic control items | Denitrification effluent (mg/L) | Micro-electrolysis water (mg/L) | Removal Rate (%) |
| 1 | COD | 26.25 | 13.55 | 48.38 |
| 2 | BOD | Not detected out | 2 | - |
| 3 | SS | 11 | 5 | 54.55 |
| 4 | Animal and vegetable oil | 0.1 | Not detected out | - |
| 5 | Petroleum products | 0.05 | Not detected out | - |
| 6 | Total nitrogen (in N) | 1.42 | 1.13 | 20.00 |
| 7 | Ammonia nitrogen (in N) | 0.75 | 0.65 | 13.33 |
| 8 | Total phosphorus (in terms of P) | 0.17 | 0.09 | 47.06 |
| 9 | Dissolved oxygen | 8.1 | 7.9 | -2.47 |
| 10 | Chroma (dilution multiple) | 2 | 2 | - |
| 11 | pH | 7.0 | 7.1 | - |
As can be seen from Table 27, the effluent indexes of the slightly polluted riverway water body after treatment completely meet the III-class water quality standard of the quality standard of surface water environment (GB 3838-2002).
The utility model discloses a system and a method for deeply purifying water body based on electrolytic denitrification and MBR, which can remove 80% -95% of COD in the water body and make the COD of the effluent less than or equal to 20mg/L after the polluted water body is treated by a pretreatment device, a coagulation device, an electrolytic denitrification device, a Membrane Bioreactor (MBR) and an adsorption phosphorus removal device in sequence; BOD is removed by 95-99%, so that BOD of effluent is less than or equal to 4 mg/L; 60-98% of total phosphorus is removed, so that the total phosphorus of effluent is less than or equal to 0.1 mg/L; 95-99.99% of ammonia nitrogen is removed, the ammonia nitrogen content of the effluent is less than or equal to 1.0mg/L, the total nitrogen content of the effluent is 95-99.00%, the total nitrogen content of the effluent is less than or equal to 1mg/L, the chromaticity is removed by 80-95%, and the dissolved oxygen content in the water body is increased to more than 7 mg/L. The method is particularly suitable for deep purification treatment and recycling of sewage, purification treatment of surface water or black and odorous water with quality lower than poor V-class water quality or upgrading and reconstruction of sewage treatment plants, so that the purified water reaches the III or IV class water quality standard of surface water environmental quality standard (GB3838-2002), and sewage and wastewater are changed into water resources.
Claims (10)
1. The utility model provides a water deep purification system based on electrolysis denitrogenation and MBR which characterized in that includes: the pretreatment device (100), the coagulating sedimentation device (200), the electrolytic denitrification device (300), the membrane bioreactor (400) and the sludge treatment system (500):
the pretreatment device (100) comprises a coarse grating (110), a fine and coarse grating (120), an aeration grit chamber (130) and a 1 st lifting pump (140) which are sequentially communicated; the water inlet of the coarse grating (110) is communicated with a water inlet pipeline of a polluted water body to be treated, the water outlet of the coarse grating (110) is communicated with the water inlet of the fine and coarse grating (120), the water outlet of the fine and coarse grating (120) is communicated with the water inlet of the aeration grit chamber (130), and the water outlet of the aeration grit chamber (130) is communicated with the water inlet of the lift pump 1 (140);
the coagulating sedimentation device (200) comprises a coagulating basin (210), a coagulation aiding basin (220), a coagulating sedimentation basin (230), an intermediate water basin (240) and a sludge collecting basin (250) which are communicated in sequence; the coagulating sedimentation tank (230) is provided with a clear water outlet (231) and a sludge outlet (232); the water inlet of the coagulation tank (210) is communicated with the water outlet of a 1 st lifting pump (140) of the pretreatment device (100), the water outlet of the coagulation tank (210) is communicated with the water inlet of the coagulation aiding tank (220), and the water outlet of the coagulation aiding tank (220) is communicated with the water inlet of the coagulation sedimentation tank (230); a clear water outlet (231) of the coagulation sedimentation tank (230) is communicated with a water inlet of the intermediate water tank (240), a water outlet of the intermediate water tank (240) is communicated with a water inlet of an electrolytic denitrification host (310) of the electrolytic denitrification device (300), and a 2 nd lift pump (311) is further arranged in a connecting pipeline between the clear water outlet and the electrolytic denitrification host (310); a sludge outlet (232) of the coagulation sedimentation tank (230) is communicated with an inlet of a sludge collection tank (250), and an outlet of the sludge collection tank (250) is communicated with an inlet of a sludge treatment system (500);
the electrolytic denitrification device (300) comprises an electrolytic denitrification host (310), a direct-current power supply (320) and a denitrification reaction tank (330), wherein a water inlet of the electrolytic denitrification host (310) is used for allowing clear water after coagulating sedimentation to enter, and a water outlet of the electrolytic denitrification host (310) is respectively communicated with a water inlet of the denitrification reaction tank (330) and a water inlet of the coagulation tank (210) through a tee joint (319);
the membrane bioreactor (400) consists of a biological reaction tank (410), an aeration pipe (420), a membrane module (430), an aeration fan (440), a backwashing water pipe (450), a No. 1 water outlet (411), a sludge outlet (412) and a disinfection tank (460); the water inlet of the membrane bioreactor (400) is communicated with the water outlet of a denitrification reaction tank (330) of the electrolytic denitrification device (300) system, and the water outlet of the membrane bioreactor (400) is communicated with the water outlet of the disinfection tank (460) and flows into the disinfection tank (470);
the sludge treatment system (500) comprises a sludge pump (510), a gravity concentration tank (520), a physicochemical conditioning tank (530) and a dehydrator (540), wherein the inlet of the sludge pump (510) is communicated with the sludge outlet of the aeration grit chamber (130), the sludge outlet (232) of the coagulation sedimentation tank (230) and the sludge outlet (414) of the biological reaction tank (410) of the membrane bioreactor (400), the outlet of the sludge pump (510) is communicated with the inlet of the gravity concentration tank (520), the sludge outlet (521) of the gravity concentration tank (520) is communicated with the inlet (531) of the physicochemical conditioning tank (530), and the sewage outlet (522) of the gravity concentration tank (520) is communicated with the water inlet of the biological reaction tank (410) of the membrane bioreactor (400); the outlet of the physicochemical conditioning pool (530) is communicated with the sludge inlet of the dehydrator (540), the sludge blocks of the dehydrator (540) are collected in the sludge collecting plateau, and the sewage of the dehydrator (540) is communicated with the water inlet of the biological reaction pool (410) of the membrane bioreactor (400).
2. The system of claim 1, wherein the coagulation sedimentation device (200) is one of a high efficiency sedimentation device, a magnetic coagulation device and a super magnetic coagulation sedimentation device.
3. The system for deep purification of water body based on electrolytic denitrification and MBR (membrane bioreactor) according to claim 1, wherein the coagulation tank (210) of the coagulation sedimentation device (200) further comprises a coagulant dosing device (211) and a No. 1 stirring machine (212), wherein the coagulant dosing device (211) is stored with 5-10% ferrous sulfate or 10-15% polyaluminium chloride solution by mass ratio; the coagulant aid tank (220) also comprises a coagulant aid dosing device (221) and a No. 2 stirrer (222).
4. The system for deep purification of water body based on electrolytic denitrification and MBR (membrane bioreactor) according to claim 1, wherein the electrolytic denitrification device further comprises an electrolyte adding device (340) which is composed of an electrolyte solution preparation tank (342), an electrolyte solution storage tank (341), an electrolyte solution delivery pump (343) and an electrolyte solution flow meter (344), wherein the electrolyte solution is delivered to the electrolyte solution storage tank (341) through the pump after the preparation of the electrolyte solution preparation tank (342) is completed, the electrolyte solution delivery pump (343) is started and is delivered to the polluted water body through the electrolyte solution flow meter (344), and then the polluted water body is electrolyzed in the main machine of the electrolytic denitrification system; the electrolyte adding device (340) is used for adding 3-12% of sodium hypochlorite solution or 2-6% of sodium chloride solution into the electrolytic denitrification device; the electrolyte solution preparation tank (342) is used for preparing 4-12% sodium hypochlorite solution or 2-6% sodium chloride solution.
5. The system of claim 1, wherein the apparatus further comprises a main pickling system (350) consisting of a pickling solution preparation tank (351) and a pickling solution delivery pump (352).
6. The system for deep purification of water body based on electrolytic denitrification and MBR (membrane bioreactor) according to claim 1, wherein a micro-electrolysis device (600) is arranged in front of the membrane bioreactor (400), and the micro-electrolysis device (600) is composed of a tank body (610), a support frame (620), a support layer (630), an iron-carbon layer (640) and a filter material layer (650).
7. The system of claim 1, wherein the membrane bioreactor (400) is followed by a deep phosphorus removal device, and the deep phosphorus removal device is one of an adsorption phosphorus removal device and a chemical precipitation phosphorus removal device.
8. The system of claim 7, wherein the apparatus for removing phosphorus by adsorption comprises at least one adsorption tower (710), a desorption regeneration system (720) and a phosphorus precipitation recovery system (730);
the adsorption phosphorus removal device needs to be operated continuously and at least comprises two adsorption towers (710), a desorption regeneration system (720) and a phosphorus precipitation recovery system (730); the adsorption tower (710) is composed of a valve (711), a water inlet (712), a lower supporting plate (713), adsorption packing (714), an upper supporting plate (715), a No. 2 water outlet (716), a water outlet tee joint (717), a tee joint (718) and a valve (719); the desorption regeneration system (720) is composed of a desorption regeneration liquid storage tank (721), a regeneration liquid delivery pump (722), a flow meter (723), a regeneration liquid inlet valve (724), an adsorption tower (710), a clear water tank (728), a clear water pump (729), an eluent water outlet valve (726) and an eluent storage tank (727); the desorption regeneration liquid storage tank (721) is connected to the adsorption tower (710) through a regeneration liquid delivery pump (722), a regeneration liquid inlet valve (724) and a water inlet tee joint; the clean water tank (728) is connected with the adsorption tower (710) through a clean water pump (729) and a tee joint (718) and a water outlet tee joint (717); the eluent storage tank (727) is connected with the adsorption tower (710) through an eluent outlet valve (726) and an outlet tee joint (717); the phosphorus precipitation recovery system (730) consists of a desorption liquid delivery pump (731), an inlet valve (732), a precipitation reaction tank (733), a stirrer (734), a precipitant storage tank (735), a dosing pump (736), a precipitation tank (739), a delivery pump (738), a concentration tank (737) and a recovery pump; the inlet of the desorption liquid delivery pump (731) is connected with the water outlet of the eluent storage tank (727), the water outlet of the desorption liquid delivery pump (731) is connected with the inlet of a desorption liquid inlet valve (732), and the outlet of the desorption liquid inlet valve (732) is connected with the phosphorus precipitation reaction tank (733); the sedimentation reaction tank (733) is also provided with a stirrer (734) and a precipitator storage tank (735), the water outlet of the sedimentation reaction tank (733) is connected with the water inlet of a sedimentation tank (739), the water outlet of the sedimentation tank (739) is connected with the inlet of a concentration tank (737) through a delivery pump (738), and the outlet of the concentration tank (737) is connected with a desorption regeneration liquid storage tank (721) through a recovery pump.
9. The system for deep purification of water body based on electrolytic denitrification and MBR (membrane bioreactor) according to claim 1, wherein the inlet of the sludge pump (510) is respectively communicated with the sludge outlet of the pretreatment device (100), the coagulating sedimentation device (200), the electrolytic denitrification device (300), the membrane bioreactor (400) and the iron-carbon micro-electrolysis device (600).
10. The system of claim 1, wherein the system is one of underground, semi-underground or above ground.
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| CN115108680A (en) * | 2022-06-25 | 2022-09-27 | 广西七彩环境科技有限公司 | Targeting method water quality upgrading process system |
| CN115108680B (en) * | 2022-06-25 | 2023-11-03 | 广西七彩环境科技有限公司 | Water quality upgrading process system adopting targeting method |
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