CN113493274A - Deep and efficient purification method for water body - Google Patents

Deep and efficient purification method for water body Download PDF

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Publication number
CN113493274A
CN113493274A CN202010267212.1A CN202010267212A CN113493274A CN 113493274 A CN113493274 A CN 113493274A CN 202010267212 A CN202010267212 A CN 202010267212A CN 113493274 A CN113493274 A CN 113493274A
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water
phosphorus
tank
water body
coagulation
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Inventor
孔玲芬
谢小青
王宝臣
魏炎光
郭春勇
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Xiamen Shuihui Environmental Technology Co ltd
Dayuan Environmental Technology Xiamen Co ltd
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Xiamen Shuihui Environmental Technology Co ltd
Dayuan Environmental Technology Xiamen Co ltd
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Priority to CN202010267212.1A priority Critical patent/CN113493274A/en
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/30—Treatment of water, waste water, or sewage by irradiation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/105—Phosphorus compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/16—Regeneration of sorbents, filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/02—Specific form of oxidant
    • C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical

Abstract

The invention discloses a deep and efficient purification method of a water body, wherein a polluted water body is coagulated, precipitated, subjected to plasma denitrification treatment, adsorbed phosphorus removal and phosphorus precipitation recovery sequentially through a coagulation precipitation device, a plasma denitrification device and an adsorbed phosphorus removal and phosphorus recovery device. The deep and efficient purification method for the water body has strong phosphorus adsorption capacity, so that the total phosphorus in the water body is less than or equal to 0.1mg/L, COD and chroma in the water body are also adsorbed, the water quality is further improved, 80-95% of the COD in the water body can be removed after the phosphorus adsorption, and the COD of the effluent is less than or equal to 20mg/L, BOD and less than or equal to 6 mg/L; 95-99% of total phosphorus is removed, so that the total phosphorus of 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 5mg/L, and the total nitrogen is removed by 80-95%; and removing 90-99% of chroma.

Description

Deep and efficient purification method for water body
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a deep and efficient purification method for a water body.
Background
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 contains 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 joints, county cities, central towns and other areas. Therefore, the treatment of water pollution is an urgent task.
Disclosure of Invention
The invention provides a device and a method for purifying and treating a water body, which have the advantages of short process flow, low operation cost, strong adaptability to water quality and good continuous effect, and aims to overcome the defect of difficulty in removing ammonia nitrogen, total nitrogen and total phosphorus in the existing water body purification technology, deeply remove nitrogen and phosphorus in the water body, improve the water quality and realize the survival and healthy sustainable development of ecological systems of rivers and lakes.
The invention is realized by the following technical scheme: a deep and efficient purification method of a water body is characterized by comprising the following steps:
(1) coagulation: the polluted water is input into a coagulation tank and is added into the coagulation tank by a coagulation feeding device at a ratio of 5-80 g/m3Mixing the ferrous sulfate solution and plasma treatment water accounting for 3-5% of the total amount of inlet water, and continuously stirring at the stirring speed of 50-300 r/min for 2-15 min;
(2) coagulation aiding: the water body after the coagulation reaction in the step (1) enters a coagulation aiding poolAdding a PAM flocculating agent through a coagulation aid and medicine adding device, wherein the weight of the added PAM is 0.1-1 g/m3Stirring and reacting for 1-5 min at a stirring speed of 10-80 r/min;
(3) and (3) precipitation: enabling the sewage subjected to the coagulation aiding reaction in the step (2) to enter a sedimentation tank for solid-liquid separation, wherein the solid-liquid separation time is 3-10 min, and a supernatant area on the upper layer of the sedimentation tank, a sludge concentration area on the bottom and a solid-liquid separation middle area in the middle are formed;
(4) plasma treatment: conveying the sewage into a plasma generator to stay for 1-10 s, and enabling plasmas generated by the plasma generator to collide with each other to generate free radicals; the pulse working voltage of the plasma generator is 0.01-30 KV, and the current density is 1-10 mA/cm2The frequency is 2400-2600 MHz;
(5) and (3) denitrification reaction: the effluent in the step (4) is uniformly distributed in a denitrification reaction tank through a water distributor for reaction, and the retention time is 10-150 min;
(6) and (3) adsorption dephosphorization: and (3) enabling the effluent water obtained in the step (4) to flow into an adsorption tower through a water inlet of the adsorption tower, wherein adsorption filler in the adsorption tower comprises metal oxyhydroxide, the metal oxyhydroxide is grafted on a carrier, the total phosphorus in the effluent water after adsorption and dephosphorization is less than or equal to 0.1mg/L, and the phosphorus removal rate is 95-99.5%.
(7) Elution of phosphorus and regeneration of adsorption packing: when the adsorption saturation of the phosphorus reaches 80-90%, closing a water inlet valve and a water outlet valve of the adsorption tower, opening a water inlet valve and a regenerated liquid outlet valve of the eluent, desorbing the adsorption filler to desorb phosphate radicals adsorbed in the filler, and storing the phosphate radicals in a phosphorus recovery liquid storage tank along with the elution flow; and after the desorption is finished, closing the eluent water inlet valve and the regenerated liquid outlet valve, opening the clear water inlet valve and the clear water valve, washing the mixture to be neutral by using clear water, and finishing the regeneration of the adsorption filler.
Preferably, when the amount of sediment formed in the coagulation basin in the step (2) is insufficient, the sludge reflux pump is started, and part of sludge flows back into the coagulation basin from the sedimentation basin.
Preferably, the method further comprises the step (8) of recovering the phosphorus through precipitation: pumping the phosphorus eluent stored in the phosphorus recovery liquid storage tank into a precipitation reaction tank, starting a dosing pump, pumping the calcium hydroxide saturated solution stored in the phosphorus precipitation solution storage tank into the phosphorus precipitation reaction tank for reaction, starting a stirrer to generate calcium phosphate precipitate, pumping the calcium phosphate precipitate into the phosphorus precipitation recovery tank, pumping the supernatant into a concentration tank for concentration, and then, pumping the concentrated supernatant into a regeneration liquid storage tank for recycling.
Preferably, the regeneration liquid storage tank stores 1-5% of sodium hydroxide solution.
Preferably, the step (3) further comprises a sludge treatment step: conveying the sludge in the sludge concentration zone in the sedimentation tank in the step (3) into a gravity concentration tank of a sludge treatment device through a sludge pump, and performing gravity sedimentation separation by using density differences of water, organic matters and inorganic matters to form a supernatant layer, a middle organic matter enrichment layer and a lower inorganic layer; conveying the liquid in the supernatant layer to a coagulation and precipitation device for further purification, conveying the substances in the middle-layer organic matter enrichment layer to a conditioning tank for conditioning, and conveying the conditioned substances to a dehydrator for dehydration; the lower inorganic layer is directly dehydrated by a dehydrator.
Preferably, in the step (4), when the plasma generator needs to be descaled, the water body valve is closed, the check valve, the inlet valve and the water outlet valve are opened, the cleaning pump is started, and the descaling liquid is pumped into the plasma generator for circular cleaning.
Preferably, the coagulation tank comprises a coagulant feeding device, a ferrous sulfate solution with the mass ratio of 5-10% is stored in the coagulant feeding device, and the dosage of the coagulant is 5-80 g/m3(ii) a The coagulation aiding pool comprises a coagulation aiding agent feeding device, and a PAM solution with the mass ratio of 1-2 per mill is stored in the coagulation aiding agent feeding device.
Preferably, COD (chemical oxygen demand) of effluent in the treated water body is less than or equal to 20mg/L, BOD (biochemical oxygen demand) is less than or equal to 6mg/L, total phosphorus of the effluent is less than or equal to 0.1mg/L, ammonia nitrogen is less than or equal to 1.0mg/L, and total nitrogen is less than or equal to 5 mg/L.
Preferably, when the total phosphorus is less than or equal to 1mg/L, 15mg/L ferrous sulfate solution is added, and the PH value in the coagulation tank is adjusted to 8-9.
Preferably, in the step (6), the retention time of the effluent after plasma denitrification in the adsorption tower is 200-800 s.
The deep and efficient purification system and the deep and efficient purification method for the water body have the following action principles:
first, adding coagulant, Fe2+With radicals Cl, O, OH or Cl generated by the plasma generator2Reaction to form Fe3+，Fe3+And PO4 3-Reacting to generate ferric phosphate precipitate to remove phosphorus in the sewage and OH-Reaction to Fe (OH)3The precipitate is coagulated to remove organic substances such as petroleum and animal and vegetable oil by adsorption.
Next, phosphorus in sewage generally exists in three forms, i.e., inorganic phosphate, biological phosphorus (e.g., biological phosphate of DNA and RNA of an organism), organic phosphorus, and the like. Under the action of plasma and free radicals, biological phosphate radicals of DNA and RNA of organisms are released into inorganic PO4 3-Conversion of organic phosphorus to inorganic PO4 3-So as to be convenient for precipitation in the form of ferric phosphate and remove organic matters such as petroleum, animal and vegetable oil and the like through the adsorption effect of the precipitation. Meanwhile, through coagulation, redundant free radicals can be consumed, and the influence of the free radicals on COD determination is eliminated.
Fe2++Cl·—→Fe3++Cl﹣
Fe2++OH·—→Fe3++OH﹣
Fe3++PO43-—→FePO4↓ (phosphorus removal main reaction)
Fe3++3OH﹣—→Fe(HO)3↓
Furthermore, after coagulation, a coagulant aid is added, namely 0.1-1 g PAM/m3Stirring the solution at the rotating speed of 30-80 r/min to promote the generation of large-particle flocs (alum flocs), and performing solid-liquid separation in a sedimentation tank; when the formed precipitation amount is small and alum floc is small, a sludge reflux pump is started to enable the sludge part of the sedimentation tank to reflux into the coagulation aiding tank, and alum floc formation is promoted.
Finally, the sewage after the coagulation aiding reaction enters a sedimentation tank for solid-liquid separation, and clear liquid moves to the upper part and flows into a water tank through a weir plate; the sludge is settled downwards, accumulated in a sludge hopper at the bottom of the sedimentation tank and input into a sludge treatment device through a sludge pump.
Further, slurry generated by coagulating sedimentation is pumped into a gravity sedimentation separation tank to be subjected to gravity concentration, and supernatant liquid subjected to gravity separation in the gravity sedimentation separation tank is pumped into a biochemical tank to be treated; conveying the middle organic matter to a conditioning pool, and dehydrating the organic matter by a dehydrator to form mud blocks; the lower layer is directly conveyed to a dehydrator for dehydration to form a mud block.
Secondly, a large amount of plasmas are generated when the plasma generator works, the plasmas act with a water body to generate a large amount of free radicals with strong activity, wherein O & OH & can react with organic molecules of the plasmas to generate water and carbon dioxide; o.and NH3Reaction to form water and NO3 ﹣(ii) a Cl and H with NO3 ﹣Reacts with ammonia nitrogen to generate N2And H2And O. H generated by the plasma effect and not participating in the reaction in time generates hydrogen to form a large amount of micro bubbles; in addition,. H and NO3 ﹣And NO2 ﹣Reaction to form N2A large number of microbubbles are also formed. Along with the floating of the hydrogen and nitrogen microbubbles, a large amount of solid suspended matters can be carried out, the effect of solid-liquid separation is achieved, the air flotation effect is formed, and the pollution indexes such as COD (chemical oxygen demand), chroma, turbidity and the like in the wastewater are further reduced. The free radicals generated by the action of the plasma and the odor-producing substances in the polluted water body can eliminate odor, so the plasma denitrification device has the effect of eliminating odor.
1. Principle of removing COD and BOD
RH+O·—→CO2↑+H2O
RH+HO·—→CO2↑+H2O
·Cl+H2O—→HClO—→O·+HCl
RH-means organic matter.
2. Decolorization (deodorization) principle
R-R＇+O·—→CO2↑+H2O
R' -represents an organic chromophore.
3. Principle of removing ammonia nitrogen
NH3+O·—→NO3 ﹣+H2O
4. Principle for removing nitrate nitrogen
NO2 ﹣+O·—→NO3 ﹣
NO3 ﹣+H·—→NO2 ﹣+H2O
NO2 ﹣+H·—→N2↑+H2Main reaction of O denitrogenation
5. Principle for increasing dissolved oxygen in water body
The plasma generator is adopted to carry out plasma treatment on the water body, a large number of oxygen radicals and hydroxyl radicals can be generated, in the water body treatment process, oxygen radicals or hydroxyl radicals which are not completely consumed are combined with each other, water molecules and oxygen molecules are generated, and dissolved oxygen in the water is increased.
O·+O·—→O2↑
2HO·+2HO·—→2H2O+O2↑
Thirdly, the effluent treated by the plasma denitrification device flows into a phosphorus adsorption tower through a water inlet of the adsorption tower, and phosphate ions in the water body are adsorbed by a special phosphorus adsorption filler in the phosphorus adsorption tower, so that the phosphate in the water body is removed.
Reaction formula (adsorption reaction):
Fe-OOH+H2PO4 -＝Fe-O-HPO4 -+H2O
then, when the adsorption saturation of phosphorus reaches 80-90%, closing a water inlet valve and a water outlet discharge valve, opening a water inlet valve of eluent and a regenerated liquid outlet valve, starting an eluent dosing pump, cleaning the phosphorus adsorption filler, desorbing phosphate radicals adsorbed in the filler, flowing out along with the eluent, and storing in a phosphorus recovery liquid storage tank; and after the desorption is finished, closing the eluent water inlet valve and the regenerated liquid outlet valve, opening the clean water inlet valve and the clean water valve, and washing the mixture to be neutral by using clean water, thus finishing the regeneration of the adsorption filler.
Reaction formula (desorption reaction):
Fe-O-HPO4-+3OH-＝Fe-OOH+PO4 3-+OH-+H2O
pumping the phosphorus eluent stored in the phosphorus recovery liquid storage tank into a phosphorus precipitation reaction tank, starting a dosing pump and a stirrer, pumping the calcium hydroxide saturated solution stored in the precipitant storage tank into the phosphorus precipitation reaction tank, reacting to generate calcium phosphate precipitate, separating the precipitate, recycling the supernatant into a coagulation process, and precipitating to obtain the recovered calcium phosphate.
Reaction formula (precipitation crystallization reaction):
PO4 3-+3/2Ca(OH)2＝1/2Ca3(PO4)2+3OH-
the deep and efficient purification system and method for the water body have the following remarkable effects:
1. the deep and efficient purification system for the water body is further provided with a phosphorus adsorption device after coagulation precipitation and plasma purification, residual phosphorus in the water body is further removed through a phosphorus adsorption filler with a strong phosphate radical selecting effect, so that the total phosphorus in the water body is less than or equal to 0.1mg/L, COD and chromaticity in the water body are also adsorbed, the water quality is further improved, the COD in the water body can be removed by 80-95% after adsorption and phosphorus removal, and the COD of the effluent is less than or equal to 20mg/L, BOD and less than or equal to 6 mg/L; 95-99% of total phosphorus is removed, so that the total phosphorus of 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 5mg/L, and the total nitrogen is removed by 80-95%; and removing 90-99% of chroma. Is particularly suitable for the purification treatment of surface water bodies or black and odorous water bodies with poor V-class water quality and the upgrading and reconstruction of sewage treatment plants, so that the water bodies reach the II or III class water quality standards of the environmental quality standard GB3838-2002 for surface water.
2. The deep and efficient purification system for the water body integrates coagulation precipitation, plasma purification and adsorption dephosphorization, and can remove COD and BOD in the water body simultaneously while coagulating dephosphorization, so that the COD of the effluent is less than or equal to 20mg/L, BOD and less than or equal to 6 mg/L; during plasma denitrification, 95-99.99% of ammonia nitrogen and 80-95% of total nitrogen in the water body are removed together, so that the ammonia nitrogen content of the effluent is less than or equal to 1.0mg/L and the total nitrogen content is less than or equal to 5mg/L, and the COD in the water body can be further reduced.
3. According to the invention, water which is treated by the plasma generator and contains a large number of free radicals flows back to the coagulation tank through the tee joint and the pipeline to oxidize ferrous iron, so that polyaluminium chloride (PAC) is replaced by ferrous sulfate, the usage amount of a medicament is reduced by more than one third under the same condition, the sludge amount is reduced by one third, the medicament cost is greatly reduced by two thirds, and the operation cost of a coagulation process is greatly reduced.
4. The floor area of the device is only one tenth of that of the traditional device, the floor area is small, and the process steps are simple.
5. The invention can remove phosphorus more thoroughly, so that biological phosphorus and organic phosphorus in water can generate inorganic phosphate under the action of generating free radicals by plasma, the inorganic phosphate and iron ions can form iron phosphate precipitate, and the total phosphorus content is less than or equal to 0.1mg/L after phosphorus removal by coagulation.
6. According to the invention, water is decomposed to generate oxygen by impacting water molecules through plasma, the content of dissolved oxygen in the purified water body is higher than 7mg/L, the dissolved oxygen in the water body can be effectively increased, the growth of algae is effectively inhibited, and the water quality is comprehensively improved.
Drawings
In order to more clearly illustrate the technical solution of the present invention, the drawings needed for the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
FIG. 1 is a flow chart of a plasma denitrification adsorption dephosphorization process of the invention.
FIG. 2 is a schematic diagram of the adsorption dephosphorization of the invention.
Fig. 3 is a schematic view of the apparatus of the present invention.
Fig. 4 is a schematic view of a coagulating sedimentation device of the present invention.
FIG. 5 is a schematic structural view of the coagulating sedimentation device of the present invention.
FIG. 6 is a schematic view showing the structure of the plasma denitrification apparatus according to the present invention.
FIG. 7 is a schematic structural diagram of the apparatus for phosphorus removal by adsorption and recovery according to 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 a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments of the present invention without making an invasive task, fall within the scope of protection of the present invention.
Referring to the attached drawings 1-7 of the specification, the invention provides a deep purification system of a water body, which comprises a coagulating sedimentation device 100, a plasma denitrification device 200 and an adsorption dephosphorization and phosphorus recovery device 300; wherein, the coagulating sedimentation device 100 is communicated with the sewage inlet water, and the pretreatment device 100, the plasma denitrification device 200 and the adsorption dephosphorization and phosphorus recovery device 300 are connected in sequence.
1. Coagulating sedimentation device
The coagulating sedimentation device comprises a water collecting well 110, a grating 120, a lifting pump 130, a precise filter 140, a coagulating basin 150, a coagulation aiding basin 160, a sedimentation basin 170 and an intermediate water basin 180 which are sequentially communicated; the water inlet of the water collecting well 110 is communicated with sewage to be treated, the input end of the grating 120 is communicated with the water outlet of the water collecting well 110, the water outlet of the grating 120 is communicated with the water inlet of the lift pump 130, the water outlet of the lift pump 130 is connected with the inlet of the precision filter 140, the water outlet of the precision filter 140 is communicated with the water inlet of the coagulation basin 150, the water outlet of the coagulation basin 150 is communicated with the water inlet of the coagulation basin 160, the water outlet of the coagulation basin 160 is communicated with the water inlet of the sedimentation basin 170, the sedimentation basin 170 is provided with a clear water outlet 178 and a sludge outlet 179, the clear water outlet is communicated with the water inlet of the middle water basin 180, the water outlet of the middle water basin 180 is communicated with the input end of the plasma generator 210, and a circulating water pump is further arranged in a connecting pipeline between the clear water outlet and the plasma generator 210.
The coagulation tank 150 comprises a coagulant feeding device 152 and a coagulation stirrer 153, wherein a ferrous sulfate solution with the mass ratio of 5-10% is stored in the coagulant feeding device; the dosage of the coagulant is 5-80 g/m3(ii) a Preferably, the coagulant feeding device comprises a metering feeding pump and a coagulant feeding tank which are connected. Further, the coagulation tank 150 and the outlet of the plasma generator 210 are communicated with each other by a tee joint.
The coagulant aid tank 160 comprises a tank body, a coagulant aid feeding device 162 and a coagulant aid stirrer 163, wherein a PAM solution with the mass ratio of 1-2 per mill is stored in the coagulant aid feeding device 162; preferably, the coagulant aid feeding device comprises a coagulant aid feeding tank and a metering feeding pump which are connected.
The sedimentation tank 170 comprises a supernatant area 171, a solid-liquid separation middle area 172 and a sludge concentration area 173 at the bottom, the upper end of the supernatant area 171 is provided with a weir plate and a water tank, water in the supernatant area 171 flows into an intermediate water tank 180 from a clear water outlet 178 for subsequent treatment, and a sludge outlet 179 is arranged at the bottom of the sludge concentration area 173. Preferably, the sedimentation tank 170 includes a high-density sedimentation tank or an inclined plate sedimentation tank, and the lower inclined plate can effectively and rapidly guide out the sludge, which is very convenient.
Preferably, the sludge generated at the sludge outlet 179 is delivered to a sludge treatment device for corresponding treatment, for example, another three-way device 181 is connected to a pipeline of the sludge outlet 179, one of water paths of the three-way device 181 is communicated with the sludge treatment device, and the other water path is communicated with the coagulation-aiding tank 160, wherein a valve 174 and a sludge reflux pump 190 are disposed between the three-way device 181 and the coagulation-aiding tank 160, and the sludge reflux pump 190 is configured to reflux a portion of the sludge in the sedimentation tank 170 to the coagulation-aiding tank 160, increase the sludge concentration, promote the formation of large-particle sludge, and improve the sludge separation effect in the sedimentation tank 170. The sludge treatment device comprises a sludge pump 41, a gravity concentration tank, a physicochemical conditioning tank and a dehydrator, wherein the input end of the sludge pump is communicated with the sludge outlet 179, the output end of the sludge pump is communicated with the input end of the gravity concentration tank, the gravity concentration tank comprises an upper layer area, a middle layer area and a lower layer area from top to bottom, the output end of the upper layer area is used for communicating the biochemical tank, the output end of the lower layer area is communicated with the input end of the dehydrator, and the middle layer area, the physicochemical conditioning tank and the dehydrator are sequentially communicated in sequence; preferably, a stirrer is further arranged in the gravity concentration tank. Wherein, the dehydrator can comprise a plate-and-frame filter press, a bag type dehydrator or a centrifugal dehydrator.
In another preferred embodiment, the coagulating sedimentation device 100 further comprises a pH value adding device, wherein sodium hydroxide or sodium carbonate is stored in the pH value adding device, and when the pH of the sewage in the coagulating process is less than 7, the pH of the sewage can be adjusted to 7-9 by adding drugs.
In a preferred embodiment, the coagulating sedimentation device is an integrated vertical coagulating device comprising a coagulating zone, a separating zone, a coagulation promoting zone and a sedimentation zone, wherein the height ratio of the coagulating zone to the separating zone to the coagulation promoting zone to the sedimentation zone is 1.5: 4: 1.8: 1.7, this vertical coagulating sedimentation device of integration, the outward appearance is cylinder or cuboid, and its diameter is 1 ~ 7 with the ratio of height: 8-11, preferably, the ratio of the diameter to the height is 1.6: and 9, separating the coagulation area from the separation area by using a partition plate, preferably, the partition plate is a carbon steel anti-corrosion partition plate, and more preferably, the thickness of the partition plate is 10 mm.
2. Plasma denitrification device
The plasma denitrification device 200 comprises a plasma generator 210, a pulse power supply 220 and a denitrification reaction tank 230, wherein a water inlet pipeline of the plasma generator 210 is communicated with the intermediate water tank 180 by a water taking pump 211 and a water inlet valve 212, so that clear water after coagulating sedimentation is input into the plasma generator, and preferably, a flow sensor 213 is also arranged in the water inlet pipeline of the plasma generator 210; the outlet 215 of the plasma generator 210 is respectively communicated with the water inlet 231 of the denitrification reaction tank 230 and the water inlet of the coagulation tank 150, for example, they are communicated with each other by a tee joint, so that the free radicals in the plasma generator can be input into the coagulation tank to promote flocculation.
In a specific embodiment, the denitrification reaction tank 230 comprises a tank body and an ammonia nitrogen oxidation tank 233 and a nitrate nitrogen reduction tank 237 which are adjacently arranged in the tank body, a water inlet 231 of the denitrification reaction tank is arranged on the side wall of the ammonia nitrogen oxidation tank 233, a water outlet 238 of the denitrification reaction tank is arranged on the side wall of the nitrate nitrogen reduction tank 237, a lower partition plate 234 and an upper partition plate 236 which are provided with a water flow passage 235 are arranged between the ammonia nitrogen oxidation tank 233 and the nitrate nitrogen reduction tank 237, and the ammonia nitrogen oxidation tank 233 and the nitrate nitrogen reduction tank 237 are communicated through the water flow passage 235.
Preferably, the lower partition plate 234 is adjacent to the ammonia nitrogen oxidation tank 233, the upper partition plate 236 is adjacent to the nitrate nitrogen reduction tank 237, a first water passing opening b1 is formed at the top end of the lower partition plate, a second water passing opening b2 is formed at the bottom end of the upper partition plate 236, and a water passing channel 235 is formed in the space between the lower partition plate 234 and the upper partition plate 236.
Preferably, the plasma generator 210 includes at least one electrode set therein, optionally, the electrode is one of graphite, iron, aluminum, zinc, copper, lead, nickel, alloy and inert electrode with noble metal oxide coating; preferably, the inert electrode has a noble metal oxide coating.
Preferably, the pulse operating voltage of the plasma generator 210 is 0.01-30 KV, and the current density is 1-10 mA/cm2The frequency is 2400-2600 MHz, and the residence time of the water body in the plasma generator 210 is 1-10 s.
Further, a water distributor 232 is arranged at the lower part of the denitrification reaction tank 230 and used for uniformly distributing the polluted water body output by the plasma generator 210 in the ammonia nitrogen oxidation tank 233, and the input end of the water distributor 232 is communicated with the water inlet 231 of the denitrification reaction tank.
Preferably, the residence time of the polluted water body in the ammonia nitrogen oxidation pond 233 is 10-150 min.
In another preferred embodiment, the plasma denitrification apparatus 200 further comprises a descaling system of a plasma generator, the descaling system comprises a descaling agent storage tank 240, a one-way valve 241, a cleaning pump 242, an inlet valve 243 and an outlet valve 244, the cleaning pump 242 and the inlet valve 243 are installed between the output end of the descaling agent storage tank 240 and the water inlet 214 of the plasma generator, and the outlet valve 244 is installed on the outlet pipeline of the plasma generator; when the plasma generator 210 needs to be descaled, the water inlet and water outlet valves are closed, the check valve 241, the inlet valve 243 and the water outlet valve 244 are opened, the cleaning pump 242 is started, and the descaling liquid is pumped into the plasma generator 210 for circular cleaning.
3. Phosphorus adsorption and removal and phosphorus recovery device
The device 300 for removing phosphorus by adsorption and recovering phosphorus is composed of an adsorption tower 310, a desorption regeneration system 320 and a phosphorus precipitation recovery system 330.
Specifically, the adsorption tower 310 comprises a water inlet 311, a lower support plate 315, adsorption filler 316, an upper support plate 317 and a water outlet 318, wherein the adsorption filler 316 is positioned between the upper support plate 317 and the lower support plate 315 and is used for adsorbing phosphorus components in the water body entering the adsorption tower, and preferably, when adsorption and phosphorus removal are performed, the retention time of the water body after denitrification reaction treatment in the adsorption tower 310 is 200-800 s; the inlet water is communicated with a first water path of the inlet four-way 312 after passing through the inlet valve 313, and the inlet valve 313 is used for controlling the communication between the adsorption tower and the water body of the plasma denitrification device; the water outlet 318 is communicated with the first waterway of the water outlet four-way 319 and discharges the effluent after the absorption and the dephosphorization through the effluent discharge valve.
The desorption regeneration system 320 comprises a regeneration liquid storage tank 321, a regeneration liquid delivery pump 322, a regeneration liquid outlet valve 323, a clean water tank 324, a clean water pump 325, a clean water valve 326, a phosphorus recovery liquid outlet valve 327 and a phosphorus recovery liquid storage tank 328, wherein the regeneration liquid storage tank 321 is communicated with the second water path of the water inlet four-way 312 through the regeneration liquid delivery pump 322 and the regeneration liquid outlet valve 323 and is connected to the water inlet 311 of the adsorption tower through the second water path of the water inlet four-way 312; the clean water tank 324 is communicated with a second waterway of the water outlet cross 319 through a clean water pump 325 and a clean water valve 326, and is further connected with the water outlet 318 of the adsorption tower 310 through the second waterway of the water outlet cross 319; the water inlet of the phosphorus recovery liquid storage tank 328 is connected with the water outlet 318 of the adsorption tower 310 through a water way of a phosphorus recovery liquid outlet valve 327 and a water outlet four-way 319, and the water outlet of the phosphorus recovery liquid storage tank 328 is connected with a phosphorus precipitation recovery system 330. Wherein, the regenerated liquid storage tank 321 stores 1-5% sodium hydroxide solution as eluent (regenerated liquid) of phosphate radical, and is connected to the adsorption tower 310 through a regenerated liquid outlet valve 323 and a water inlet four-way 312; more preferably, the eluent stored in the regeneration liquid storage tank 321 is a 3-5% sodium hydroxide solution.
The phosphorus precipitation recovery system 330 comprises a phosphorus precipitation reaction tank 333, a precipitator storage tank 335, a phosphorus precipitation recovery tank 337 and a concentration tank 339, wherein the water outlet of the phosphorus recovery liquid storage tank 328 enters the phosphorus precipitation reaction tank 333 through an eluent water inlet valve 332; the phosphorus precipitation reaction tank 333 is provided with a stirrer 334, and the phosphorus precipitation reaction tank 333 is connected with a precipitator storage tank 335, preferably, the precipitator storage tank 335 is stored with calcium hydroxide saturated solution, and more preferably, the phosphorus precipitation solution storage tank is stored with calcium chloride solution; the water inlet of the phosphorus precipitation reaction tank 333 is communicated with the water outlet of the phosphorus recovery liquid storage tank 328, and the water outlet of the phosphorus precipitation reaction tank 333 is connected with the phosphorus precipitation recovery tank 337; the water outlet of the phosphorus precipitation recovery tank 337 is connected to the concentration tank 339, and the water outlet of the concentration tank 339 is connected to the regenerated liquid storage tank 321. When the device works, the phosphorus eluent in the phosphorus recovery liquid storage tank 328 is pumped into the phosphorus precipitation reaction tank 333, the dosing pump 336 is started, the calcium hydroxide saturated solution stored in the precipitator storage tank 335 is pumped into the phosphorus precipitation reaction tank 333, the stirrer 334 is started to accelerate the reaction to generate calcium phosphate precipitate, the calcium phosphate precipitate is pumped into the phosphorus precipitation recovery tank 337, and the supernatant in the phosphorus precipitation recovery tank enters the concentration tank 339 for concentration under the action of the pump 338 and is pumped into the regeneration liquid storage tank 321 by the recovery pump 340 for recycling.
In a preferred embodiment, the water body nitrogen and phosphorus removal deep purification system further comprises an automatic control device which comprises a controller, an electric conductivity sensor, a flow sensor, a potential sensor, a stirring rotation speed sensor, a temperature sensor, a chlorine sensor, a hydrogen sensor, a pH value sensor, a PLC (programmable logic controller) value sensor and a valve group, wherein the valve group comprises an electric valve or a pneumatic valve. Specifically, the controller comprises a control unit, a fault detection unit, a data receiving unit and a data processing unit, wherein the data processing unit comprises a calculation module and a judgment module, and the fault detection unit can receive a fault signal and transmit the fault signal to the control unit; the data receiving unit can receive working signals such as water quality, system operation, valve group switch states and pump operation states acquired by the sensors, transmit the working signals to the data processing unit, and transmit the working signals to the control unit after the working signals are processed by the computing module and the module. The control unit can send out an instruction to control the water body plasma purification, the coagulating sedimentation process and the sludge treatment process in the system, namely, the reflux repurification. The automatic operation of the plasma coagulation integrated sewage treatment system is realized through the automatic control device, and the automatic purification of the polluted water body is further realized.
The invention also provides a deep and efficient purification method of the water body, which comprises the following steps:
(1) coagulation: the water body passing through the lift pump 130 enters a coagulation tank 150, and 5-80 g/m is added through a coagulation feeding device3Mixing and continuously stirring the ferrous sulfate solution and plasma treatment water accounting for 3-5% of the total amount of inlet water, wherein the stirring speed is 50-300 r/min, and the coagulation reaction time is 2-15 min; in the process, the ferrous ions and oxygen free radicals or hydroxyl free radicals in the water body generate ferric ions, and the ferric ions and the hydroxyl react to generate ferric hydroxide particles (flocs);
(2) coagulation aiding: the water body after the coagulation reaction in the step (1) enters a coagulation aiding pool 160, a PAM flocculating agent is added through a coagulation aiding and dosing device, and the weight of the added PAM is 0.1-1 g/m3Stirring and reacting for 1-5 min at a stirring speed of 10-80 r/min;
(3) and (3) precipitation: enabling the sewage subjected to coagulation aiding reaction in the step (2) to enter a sedimentation tank 170 for solid-liquid separation, wherein the solid-liquid separation time is 3-10 min, and after 3-10 min of solid-liquid separation, forming a supernatant area 171 on the upper layer of the sedimentation tank 170, a sludge concentration area 173 at the bottom of the sedimentation tank 170 and a solid-liquid separation middle area 172 in the middle of the sedimentation tank 170; when the precipitation amount formed in the coagulation-aiding tank 160 in the step (2) is insufficient, the sludge reflux pump 190 is started, and part of sludge flows back into the coagulation-aiding tank 160 from the precipitation tank 170 to promote the generation of precipitates;
in the coagulation, coagulation aiding and precipitation processes, 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; 50-70% of COD, 60-96% of total phosphorus and 70-90% of chroma in the water body can be removed through coagulating sedimentation.
Further, the method also comprises the following sludge treatment steps: conveying the sludge in the sludge concentration zone 163 in the sedimentation tank 160 in the step (3) to a gravity concentration tank of a sludge treatment device through a sludge pump, stirring, and performing gravity sedimentation separation by using density difference of water, organic matters and inorganic matters to form an upper supernatant layer, a middle organic matter enrichment layer and a lower inorganic layer; conveying the liquid in the supernatant layer to a coagulating sedimentation device for purification; conveying the substances in the middle-layer organic matter enrichment layer to a conditioning pool for conditioning, and then conveying the conditioned substances to a dehydrator for dehydration; the substance formed by dehydrating the lower inorganic layer can be used as a building material raw material for producing building bricks or ceramsite.
(4) Plasma treatment: conveying the sewage into a plasma generator 210 and staying for 1-10 s, wherein plasmas generated by the plasma generator 210 collide with each other to generate free radicals; the pulse working voltage of the plasma generator 210 is 0.01-30 KV, and the current density is 1-10 mA/cm2The frequency is 2400-2600 MHz;
(5) and (3) denitrification reaction: the effluent in the step (4) is uniformly distributed in the denitrification reaction tank 230 through a water distributor 232, the retention time is 10-150 min, and the effluent is subjected to the catalytic action of a catalystThen, the oxygen free radical (O.cndot.) and hydroxyl oxygen free radical (OH) in the water react with ammonia nitrogen in the water to generate nitrate nitrogen, nitrite nitrogen and water; meanwhile, hydrogen free radicals (. H) in the water body react with nitrate nitrogen and nitrite nitrogen to generate nitrogen and water; in addition, oxygen free radicals (O.OH) and hydroxyl free radicals (OH) in the water body react with BOD in the water body to generate CO2Water is blended to reduce COD, oxygen free radicals (O.OH) and hydroxyl oxygen free radicals (OH) in the water body can also react with organic phosphorus and biological phosphorus in the water body to generate phosphate radicals, nitrogen generated in the denitrification reaction process and oxygen generated by the action of plasma play a role in air flotation and can remove small particle solid matters in the water body; through denitrification reaction, 85-99.9% of ammonia nitrogen, 80-95% of total nitrogen, 90-100% of BOD, 99-100% of fecal coliform, 5-15% of COD and 5-10% of total phosphorus in the water body can be removed together, and meanwhile, the dissolved oxygen in the water body can be increased to be more than 7 mg/L;
the reaction to remove ammonia nitrogen is:
NH4 ++10O·→2NO3 -+4H2O
the reaction of the denitrified nitrogen is as follows:
NO2 -+O·→NO3 -
NO3 -+H·→NO2 -+H2O
NO2 -+H·→N2↑+H2O
(6) and (3) adsorption dephosphorization: the effluent water after the plasma denitrification step flows into the adsorption tower 310 for phosphorus through a water inlet 311 of the adsorption tower, phosphate ions in the water body are adsorbed by the special filler for phosphorus adsorption in the adsorption tower 310, so that phosphate in the water body is removed, and the main principle is as follows: part of metal oxyhydroxide has extremely strong selective adsorption capacity to phosphorus in water with neutral pH, and the adsorbed phosphorus can be rapidly desorbed when the pH is changed into strong alkali; the support of the metal oxyhydroxide is, for example, polyethylene or polystyrene, and the metal oxyhydroxide is grafted to the support. The total phosphorus in the effluent is less than or equal to 0.1mg/L, and the removal rate of phosphorus is 95-99.5%.
Reaction formula (adsorption reaction):
Fe-OOH+H2PO4 -＝Fe-O-HPO4 -+H2O
(7) elution of phosphorus and regeneration of adsorption packing: when the adsorption saturation of phosphorus reaches 80-90%, closing a water inlet valve 313 and a water outlet discharge valve of the adsorption tower, opening a water inlet valve of eluent (regenerated liquid) and a regenerated liquid outlet valve 323, starting an eluent dosing pump, cleaning the phosphorus adsorption filler in the adsorption tower 310, desorbing phosphate radicals adsorbed in the filler, flowing out along with the eluent and storing in a phosphorus recovery liquid storage tank 328; after desorption, closing the eluent water inlet valve and the regenerated liquid outlet valve, opening the clear water inlet valve and the clear water valve 326, and washing with clear water to be neutral, namely, completing the regeneration of the adsorption filler; the eluent is 1-5% sodium hydroxide solution.
Reaction formula (desorption reaction):
Fe-O-HPO4 -+3OH-＝Fe-OOH+PO4 3-+OH-+H2O
(8) and (3) recovering the phosphorus through precipitation: pumping the phosphorus recovery solution stored in the phosphorus recovery solution storage tank 328 into the phosphorus precipitation reaction tank 333, starting the dosing pump 336, pumping the calcium hydroxide saturated solution stored in the precipitant storage tank 335 into the phosphorus precipitation reaction tank 333, starting the stirrer 334 to react to generate calcium phosphate precipitate, pumping the calcium phosphate precipitate into the phosphorus precipitation recovery tank 337, pumping the supernatant into the concentration tank 339 for concentration through the pump 338, pumping the concentrated supernatant into the regeneration solution storage tank 321 for recycling, and obtaining the recovered calcium phosphate precipitate.
Reaction formula (precipitation crystallization reaction):
PO4 3-+3/2Ca(OH)2＝1/2Ca3(PO4)2+3OH-
preferably, when the plasma generator in the plasma denitrification apparatus needs to be descaled, the water inlet valve 212 and the water outlet valve 216 are closed, the check valve 241, the inlet valve 243 and the water outlet valve 244 are opened, the cleaning pump 242 is started, and the descaling liquid is pumped into the plasma generator 210 for circular cleaning.
After the deep high-efficiency purification system of the water body is adopted for treatment and the treatment is carried out through the steps, the COD in the water body can be removed by 80-95%, and the COD of the effluent is less than or equal to 20 mg/L; removing 95-99% of BOD, and enabling the BOD of the effluent to be less than or equal to 6 mg/L; 95-99% of total phosphorus is removed, so that the total phosphorus of 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 5mg/L, and the total nitrogen is removed by 80-95%; the chroma is removed by 90-99%, and the method is particularly suitable for purification treatment of surface water bodies or black and odorous water bodies with poor V-class water quality and upgrading transformation of sewage treatment plants, so that the water bodies reach the water quality standards of class II or class III in the environmental quality standard GB3838-2002 for surface water.
Example one
The method comprises the following steps of (1) enabling a slightly polluted water body of a river to enter a deep high-efficiency purification system of the water body for treatment; the polluted water sequentially enters the coagulating sedimentation device 100, the plasma denitrification device 200 and the adsorption dephosphorization and phosphorus recovery device 300 for treatment.
Firstly, in the steps 1-3, adding a ferrous sulfate coagulant into the coagulating sedimentation device 100, wherein the addition amount is 5mg/L, after coagulation reaction at the rotation speed of 100 revolutions, adding a coagulant aid PAM at the ratio of 1mg/L, reacting at the rotation speed of 20 revolutions, and then separating in a sedimentation tank 170, wherein the quality of the coagulating sedimentation effluent is shown as the coagulating effluent in the table 1;
then, the coagulated and precipitated water enters the plasma generator 210 in the step 4 for treatment, the treated water enters the denitrification reaction tank 230 in the step 5 for denitrification reaction, the effluent index is shown as denitrification effluent in the table 1, the working voltage of the plasma generator 210 is 10V, and the current density is 1mA/cm2；
Finally, the effluent treated by the plasma denitrification device 200 flows through the adsorption dephosphorization system in step 6 for advanced purification, and the quality of the effluent after the effluent treated by the plasma denitrification device 200 is subjected to the advanced purification treatment by the adsorption dephosphorization system is shown in the adsorption effluent in table 1.
TABLE 1 Water quality index of slightly polluted water in river course after each step
Figure BDA0002441719050000151
Figure BDA0002441719050000161
As can be seen from Table 1, 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 two
The untreated water body of a river water body enters a deep high-efficiency purification system of the water body for treatment; the polluted water body sequentially enters the coagulating sedimentation device 100, the plasma denitrification device 200 and the adsorption phosphorus removal and recovery device 300 for treatment.
Firstly, in the steps 1 to 3, adding a ferrous sulfate coagulant into the coagulation sedimentation device 100, wherein the adding amount is 20mg/L, after coagulation reaction at the rotation speed of 100 revolutions, adding a coagulant aid PAM at the ratio of 1mg/L, reacting at the rotation speed of 20 revolutions, and then separating in a sedimentation tank 170, wherein the quality of the coagulation sedimentation effluent is shown as the coagulation effluent in the table 2:
then, the coagulated and precipitated water enters the plasma generator 210 in the step 4 for treatment, the treated water enters the denitrification reaction tank 230 in the step 5 for denitrification reaction, the effluent index is shown as denitrification effluent in the table 2, the working voltage of the plasma generator 210 is 60V, and the current density is 2mA/cm2；
Finally, the effluent treated by the plasma denitrification device 200 flows through the adsorption dephosphorization system in step 6 for advanced purification, and the quality of the effluent after the effluent treated by the plasma denitrification device 200 is subjected to the advanced purification treatment by the adsorption dephosphorization system is shown in the adsorption effluent in table 2.
TABLE 2 Water quality index of untreated water in river course
Figure BDA0002441719050000162
Figure BDA0002441719050000171
As can be seen from Table 2, the effluent index of a river water body after treatment completely meets the III-class water quality standard of 'surface water environment quality Standard' (GB 3838-2002).
Example 3
A certain black and odorous water body enters a deep and efficient purification system of the water body for treatment; the polluted water body sequentially enters the coagulating sedimentation device 100, the plasma denitrification device 200 and the adsorption dephosphorization and phosphorus recovery device 300 for treatment.
Firstly, in the steps 1 to 3, adding a ferrous sulfate coagulant into the coagulation sedimentation device 100, wherein the adding amount is 80mg/L, after coagulation reaction at the rotation speed of 100 revolutions, adding a coagulant aid PAM at the ratio of 1mg/L, reacting at the rotation speed of 20 revolutions, and then separating in a sedimentation tank 170, wherein the quality of the coagulation sedimentation effluent is shown as the coagulation effluent in the table 3:
then, the coagulated and precipitated water enters the plasma generator 210 in the step 4 for treatment, the treated water enters the denitrification reaction tank 230 in the step 5 for denitrification reaction, the effluent index is shown as denitrification effluent in the table 3, the working voltage of the plasma generator 210 is 30KV, and the current density is 10mA/cm2；
Finally, the effluent treated by the plasma denitrification apparatus 200 flows through the adsorption dephosphorization system in step 6 for advanced purification, and the quality of the effluent after the effluent treated by the plasma denitrification apparatus 200 is subjected to the advanced purification treatment by the adsorption dephosphorization system is shown in the adsorption effluent in table 3.
TABLE 3 Water quality index of a certain black and odorous water body after treatment in each step
Figure BDA0002441719050000172
Figure BDA0002441719050000181
As can be seen from Table 3, the effluent index of the treated black and odorous water completely meets the III-class water quality standard of the quality Standard of Water surface Environment (GB 3838-2002).
Example 4
Firstly, water precipitated in a secondary sedimentation tank of a certain sewage treatment plant enters a deep high-efficiency purification system of the water for treatment; the polluted water body sequentially enters the coagulating sedimentation device 100, the plasma denitrification device 200 and the adsorption dephosphorization and phosphorus recovery device 300 for treatment.
Firstly, in the step 1-3, when the water body enters the coagulating sedimentation device 100 for coagulation treatment, because the total phosphorus in the water body is only 1mg/L and the concentration is low, a ferrous sulfate solution is added according to 15mg/L, a 5% sodium hydroxide solution is added to adjust the pH value to 8-9 (because the pH value is 6-7), after coagulation reaction is carried out under the condition that the rotating speed is 200 revolutions, the water body enters a coagulation tank, a coagulant aid PAM is added according to 1mg/L, and after coagulation is carried out under the condition that the rotating speed is 60 revolutions, the water body enters a sedimentation tank 230 for solid-liquid separation, and the water quality of effluent is as the coagulated effluent in the table 4:
then, the water body after coagulating sedimentation enters a plasma generator 210 for treatment, the working voltage of the plasma generator 210 is 50V, and the current density is 10mA/cm2(ii) a The treated water body enters a denitrification reaction tank 230 for denitrification reaction, and the effluent indexes are as the denitrification effluent in the table 4;
finally, the effluent treated by the plasma denitrification device 200 flows through the adsorption dephosphorization system for deep purification, and the quality of the effluent treated by the plasma denitrification device 200 through the adsorption dephosphorization system for deep purification is shown in the adsorption effluent in table 4.
TABLE 4 Water quality index of water precipitated in secondary sedimentation tank of certain sewage treatment plant after treatment in each step
Figure BDA0002441719050000182
Figure BDA0002441719050000191
As can be seen from Table 4, the effluent indexes of the treated effluent of the sewage treatment plant completely meet IV-class water quality standards of environmental quality Standard of surface Water (GB 3838-2002).
While the foregoing specification illustrates and describes the preferred embodiments of this invention, it is to be understood that the invention is not limited to the forms disclosed herein, but is not intended to be exhaustive or to exclude other embodiments and may be used in various other combinations, modifications, and environments and may be modified within the scope of the inventive concept described herein by the teachings or the skill or knowledge of the relevant art. And that modifications and variations may be effected by those skilled in the art without departing from the spirit and scope of the invention as defined by the appended claims.

Claims (10)

1. A deep and efficient purification method of a water body is characterized by comprising the following steps:
(1) coagulation: the polluted water is input into a coagulation tank and is added into the coagulation tank by a coagulation feeding device at a ratio of 5-80 g/m3Mixing and continuously stirring the ferrous sulfate solution and plasma treatment water accounting for 3-5% of the total amount of inlet water, wherein the stirring speed is 50-300 r/min, and the coagulation reaction time is 2-15 min;
(2) coagulation aiding: the water body after the coagulation reaction in the step (1) enters a coagulation aiding pool, a PAM flocculating agent is added through a coagulation aiding and dosing device, and the weight of the added PAM is 0.1-1 g/m3Stirring and reacting for 1-5 min at a stirring speed of 10-80 r/min;
(3) and (3) precipitation: enabling the sewage subjected to the coagulation aiding reaction in the step (2) to enter a sedimentation tank for solid-liquid separation, wherein the solid-liquid separation time is 3-10 min, and a supernatant area on the upper layer of the sedimentation tank, a sludge concentration area on the bottom and a solid-liquid separation middle area in the middle are formed;
(4) plasma treatment: conveying the sewage to a plasma generator to stay for 1-10 s, and generating plasma by the plasma generatorThe bodies collide with each other to generate free radicals; the pulse working voltage of the plasma generator is 0.01-30 KV, and the current density is 1-10 mA/cm2The frequency is 2400-2600 MHz;
(5) and (3) denitrification reaction: the effluent in the step (4) is uniformly distributed in a denitrification reaction tank through a water distributor for reaction, and the retention time is 10-150 min;
(6) and (3) adsorption dephosphorization: and (3) enabling the effluent water obtained in the step (4) to flow into an adsorption tower through a water inlet of the adsorption tower, wherein adsorption filler in the adsorption tower comprises metal oxyhydroxide, the metal oxyhydroxide is grafted on a carrier, the total phosphorus in the effluent water after adsorption and dephosphorization is less than or equal to 0.1mg/L, and the phosphorus removal rate is 95-99.5%.
(7) Elution of phosphorus and regeneration of adsorption packing: when the adsorption saturation of the phosphorus reaches 80-90%, closing a water inlet valve and a water outlet valve of the adsorption tower, opening a water inlet valve and a regenerated liquid outlet valve of the eluent, desorbing the adsorption filler to desorb phosphate radicals adsorbed in the filler, and flowing out along with the eluent to be stored in a phosphorus recovery liquid storage tank; and after the desorption is finished, closing the eluent water inlet valve and the regenerated liquid outlet valve, opening the clear water inlet valve and the clear water valve, washing the mixture to be neutral by using clear water, and finishing the regeneration of the adsorption filler.
2. The method for deeply and efficiently purifying the water body according to claim 1, wherein when the precipitation amount formed in the coagulation basin in the step (2) is insufficient, a sludge reflux pump is started, and part of sludge flows back into the coagulation basin from the precipitation basin.
3. The deep and efficient purification method of the water body according to claim 1, characterized by further comprising the step (8) of precipitating and recovering phosphorus: pumping the phosphorus eluent stored in the phosphorus recovery liquid storage tank into a precipitation reaction tank, starting a dosing pump, pumping the calcium hydroxide saturated solution stored in the phosphorus precipitation solution storage tank into the phosphorus precipitation reaction tank for reaction, starting a stirrer to generate calcium phosphate precipitate, pumping the calcium phosphate precipitate into the phosphorus precipitation recovery tank, pumping the supernatant into a concentration tank for concentration, and then, pumping the concentrated supernatant into a regeneration liquid storage tank for recycling.
4. The method according to claim 3, wherein the regeneration liquid storage tank stores 1-5% sodium hydroxide solution.
5. The deep and efficient purification method of water body according to claim 1, characterized in that the step (3) further comprises a sludge treatment step: conveying the sludge in the sludge concentration zone in the sedimentation tank in the step (3) to a gravity concentration tank of a sludge treatment device through a sludge pump, and performing gravity sedimentation separation by using density differences of water, organic matters and inorganic matters to form a supernatant layer, a middle organic matter enrichment layer and a lower inorganic layer; conveying the liquid in the supernatant layer to a coagulating sedimentation device for further purification, conveying the substances in the middle layer organic matter enrichment layer to a conditioning tank for conditioning, and conveying the conditioned substances to a dehydrator for dehydration; the lower inorganic layer is directly dehydrated by a dehydrator.
6. The deep and efficient purification method of the water body according to claim 1, characterized in that in the step (4), when the plasma generator needs to be descaled, the water body valve is closed, the check valve, the inlet valve and the water outlet valve are opened, the cleaning pump is started, and the descaling liquid is pumped into the plasma generator for circular cleaning.
7. The deep and efficient water body purification method according to claim 1, wherein the coagulation tank comprises a coagulant feeding device, a ferrous sulfate solution with a mass ratio of 5-10% is stored in the coagulant feeding device, and the amount of the coagulant is 5-80 g/m3(ii) a The coagulant aid tank comprises a coagulant aid feeding device, and a PAM solution with the mass ratio of 1-2 per mill is stored in the coagulant aid feeding device.
8. The method for deeply and efficiently purifying the water body according to claim 1, wherein COD and BOD of the effluent in the treated water body are less than or equal to 20mg/L and 6mg/L, total phosphorus and ammonia nitrogen of the effluent are less than or equal to 0.1mg/L, 1.0mg/L and 5mg/L, respectively.
9. The deep and efficient purification method of the water body according to claim 1, characterized in that when the total phosphorus is less than or equal to 1mg/L, 15mg/L ferrous sulfate solution is added, and the PH in the coagulation tank is adjusted to 8-9.
10. The method for deeply and efficiently purifying the water body according to claim 1, wherein in the step (6), the retention time of the effluent after the plasma denitrification in the adsorption tower is 200-800 s.
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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2011255341A (en) * 2010-06-11 2011-12-22 Asahi Kasei Chemicals Corp Recovered phosphorus and method for recovering phosphorus
CN108911318A (en) * 2018-09-03 2018-11-30 大渊环境技术（厦门）有限公司 A kind of purification device and purification method of black and odorous water
CN109081467A (en) * 2018-08-02 2018-12-25 北京水汇物源环境科技有限公司 The method that the dephosphorization of urban wastewater treatment firm tail water, phosphorus recovery system and adsorption and dephosphorization, phosphorus recycle
CN109650589A (en) * 2019-01-02 2019-04-19 北京北华中清环境工程技术有限公司 A kind of Emergency management method and system recycled with nitrogen, phosphorus
CN110770175A (en) * 2017-06-16 2020-02-07 高桥金属株式会社 Adsorption process

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2011255341A (en) * 2010-06-11 2011-12-22 Asahi Kasei Chemicals Corp Recovered phosphorus and method for recovering phosphorus
CN110770175A (en) * 2017-06-16 2020-02-07 高桥金属株式会社 Adsorption process
CN109081467A (en) * 2018-08-02 2018-12-25 北京水汇物源环境科技有限公司 The method that the dephosphorization of urban wastewater treatment firm tail water, phosphorus recovery system and adsorption and dephosphorization, phosphorus recycle
CN108911318A (en) * 2018-09-03 2018-11-30 大渊环境技术（厦门）有限公司 A kind of purification device and purification method of black and odorous water
CN109650589A (en) * 2019-01-02 2019-04-19 北京北华中清环境工程技术有限公司 A kind of Emergency management method and system recycled with nitrogen, phosphorus

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
肖羽堂: "环境微生物学", 中国建材工业出版社, pages: 257 - 258 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115259555A (en) * 2022-07-26 2022-11-01 安徽久吾天虹环保科技有限公司 Powerful combination method for treating micro-polluted water body

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