CN112142263A - Surface quasi-class II drinking water source water replenishing regeneration treatment system and method - Google Patents

Surface quasi-class II drinking water source water replenishing regeneration treatment system and method Download PDF

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CN112142263A
CN112142263A CN202011039092.6A CN202011039092A CN112142263A CN 112142263 A CN112142263 A CN 112142263A CN 202011039092 A CN202011039092 A CN 202011039092A CN 112142263 A CN112142263 A CN 112142263A
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effluent
sludge
tank
zone
ozone
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张强
卢东昱
张薛龙
赵有生
骆平
马效贤
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Beijing Enfi Environmental Protection Co ltd
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Beijing Enfi Environmental Protection Co ltd
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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
    • 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
    • C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
    • 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
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • 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
    • C02F2101/30—Organic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/308—Biological phosphorus removal
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F7/00—Aeration of stretches of water

Abstract

The invention discloses a surface quasi-class II drinking water source water replenishing regeneration treatment system and a method, comprising an aeration grit chamber, a biological treatment section, an MBR (membrane bioreactor) tank, an ozone oxidation section, a sludge concentration decomposition tank, a disinfection section and an artificial wetland section; the biological treatment section comprises a pre-anoxic zone, an anaerobic zone, a primary aerobic zone, a primary anoxic zone, a secondary aerobic zone and a secondary anoxic zone; the water outlet of the aeration grit chamber is respectively communicated with the water inlets of the pre-anoxic zone, the anaerobic zone, the primary anoxic zone and the secondary anoxic zone; the water outlet of the secondary aerobic zone is communicated with the water inlet of the pre-anoxic zone; a sludge outlet of the MBR tank is communicated with a sludge inlet of the primary aerobic zone; the sludge outlet of the MBR is communicated with the sludge inlet of the sludge concentration decomposition pool, the sludge lysate outlet of the sludge concentration decomposition pool is communicated with the pre-anoxic zone, and the residual sludge in the sludge concentration decomposition pool is treated into a sludge cake to enter the industrial wetland. The surface quasi-second type drinking water source water replenishing regeneration treatment system has the advantages of good treatment effect, low operation cost and the like.

Description

Surface quasi-class II drinking water source water replenishing regeneration treatment system and method
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a drinking water source water replenishing regeneration treatment system based on a surface quasi-second water quality standard, and further relates to a drinking water source water replenishing regeneration treatment method based on the surface quasi-second water quality standard.
Background
The available fresh water resources of all people in China are insufficient, water pollution is increasingly serious, the health and ecological environment of people are affected, and the water treatment discharge standard is increasingly strict, and in the standard A of the Jing Standard (DB11890-2012) of discharge Standard of Water pollutants of urban Sewage treatment plants, the standard reaches the III-class water quality standard of surface water except TN; in 2015, the opinion on accelerating the development of ecological civilization released by the common center and the state department clearly proposes two limitations: the method has the advantages that pollutant emission standards and total amount limitation are realized, and 'regional batch limitation' is uniformly implemented in regions where main pollutant emission total amount control tasks are not completed, and particularly, surface water III standards (except TN) or higher standards are pushed to have practical significance for water resource protection in environment sensitive regions such as natural protection regions, resorts and drinking water source protection places.
The invention provides a method for deeply removing nitrogen and phosphorus and refractory organic matters in a conventional water treatment process system, which aims to solve the problems that the effect of sewage treatment is not ideal and the operation cost is high due to the difficulties in the aspects of deep nitrogen and phosphorus removal and refractory organic matter removal in the prior art.
Disclosure of Invention
The invention provides a drinking water source water replenishing treatment regeneration treatment system with a surface standard of two types of water quality aiming at municipal sewage, aiming at solving the difficulties of deep nitrogen and phosphorus removal and removal of refractory organics of the conventional water treatment process system at present and realizing an integrated system under the surface standard of the municipal sewage of two types of discharge standards. The invention also provides a treatment method for the water replenishing and regeneration of the drinking water source with the surface standard class II water quality standard, which has good treatment effect and low operation cost.
In order to achieve the above object, the present invention provides a surface standard class two drinking water source water replenishing regeneration treatment system, comprising: the system comprises an aeration grit chamber, a biological treatment section, an MBR (membrane bioreactor) tank, a sludge concentration and decomposition tank, an ozone reactor, an ozone tail gas destruction device, an air compressor, an ozone reaction tank, a disinfection tank and an artificial wetland. The biological treatment section comprises a pre-anoxic zone, an anaerobic zone, a primary aerobic zone, a primary anoxic zone, a secondary aerobic zone and a secondary anoxic zone which are sequentially connected, wherein each of a water inlet of the pre-anoxic zone, a water inlet of the anaerobic zone, and water inlets of the primary anoxic zone and the secondary anoxic zone is communicated with a water outlet of the aeration grit chamber, and a water outlet of the secondary aerobic zone is communicated with a water inlet of the pre-anoxic zone. The water inlet of the MBR tank is communicated with the water outlet of the second-stage anoxic zone, the water outlet of the MBR tank is communicated with the inlet of the ozone reaction tank, the return sludge outlet of the MBR tank is communicated with the return aerobic sludge inlet of the first-stage anoxic zone, and the residual sludge outlet of the MBR tank is communicated with the sludge concentration decomposition tank. The sludge lysate outlet of the sludge concentration decomposition pool is communicated with the pre-anoxic zone; and filter cakes generated by the residual sludge in the MBR tank are used for artificial wetland packing. The ozone outlet of the ozone generator is respectively communicated with the sludge concentration and decomposition tank and the ozone reaction tank; the ozone generator uses compressed air generated by an air compressor as an air source. The water inlet of the ozone reaction tank is communicated with the water outlet of the MBR tank, the water outlet of the ozone reaction tank is communicated with the disinfection tank, and the tail gas of the ozone reaction tank is respectively connected with the ozone tail gas destruction device and the MBR tank.
The water inlet of the disinfection tank is communicated with the water outlet of the ozone reaction tank, the outlet of the disinfection tank is communicated with the water inlet of the artificial wetland, and a filter cake obtained by dewatering and filter pressing sludge is used as a filler of the artificial wetland.
Further, the device further comprises a coarse grid, a fine grid and a membrane grid; the coarse grating is positioned at the upstream of the aeration grit chamber, the fine grating is positioned between the coarse grating and the aeration grit chamber, and the membrane grating is positioned at the downstream of the aeration grit chamber.
And the water inlet of the water inlet automatic control device is communicated with the water outlet of the aeration grit chamber, and the water outlet of the water inlet automatic control device is communicated with each of the water inlet of the pre-anoxic zone, the water inlet of the anaerobic zone, the water inlet of the primary anoxic zone and the water inlet of the secondary anoxic zone.
Furthermore, a water outlet of the secondary aerobic zone is communicated with a water inlet of the pre-anoxic zone.
Further, the device comprises an ozone reaction tank, wherein a COD catalytic oxidation filler is arranged in the ozone reaction tank.
The invention also provides a surface quasi-second class drinking water source water replenishing regeneration treatment method, which comprises the following steps:
A) raw water enters the aeration grit chamber through the coarse grids and the fine grids.
B) After aeration and sand setting, dividing the effluent into four parts, namely a first part effluent, a second part effluent, a third part effluent and a fourth part effluent through a membrane grid; in the pre-anoxic zone, the first part of effluent is mixed with return sludge and lysate of the secondary aerobic zone for denitrification and dephosphorization, and simultaneously, a dephosphorization agent is added for dephosphorization.
C) In the anaerobic zone, the treated first part of effluent and the second part of effluent are mixed for anaerobic phosphorus release.
D) In the primary aerobic zone, mixing the treated first part of effluent, the treated second part of effluent and return sludge of an MBR tank, and carrying out aerobic nitration reaction to remove ammonia nitrogen; simultaneously, aerobic absorption of phosphorus is carried out, and total phosphorus is transferred from the liquid to the sludge.
E) In the first-stage anoxic zone, the treated first part of effluent, the treated second part of effluent and the third part of effluent are mixed, and total nitrogen is continuously removed by denitrification.
F) In the secondary aerobic zone, the treated first part of effluent is mixed with the treated second part of effluent and the treated third part of effluent, and ammonia nitrogen removal is continuously carried out.
G) In the secondary anoxic zone, the treated first part of effluent, the treated second part of effluent, the treated third part of effluent and the fourth part of effluent are mixed, and then an external carbon source is added for deep denitrification.
H) In an MBR tank, mixing the treated first part of effluent, the treated second part of effluent, the treated third part of effluent and the treated fourth part of effluent, adding biological enzyme modified activated carbon into the MBR tank to remove refractory organic matters, performing membrane filtration to remove SS, discharging residual phosphorus-containing sludge, and finally adding ozone into the MBR tank to reduce membrane silk fouling and restore the adsorption capacity of the biological enzyme modified activated carbon.
I) And adding an obligate COD catalyst into the ozone reaction tank, and treating residual ozone after reaction in the ozone reaction tank by an ozone tail gas destruction device.
J) And the effluent treated by the sampling reaction tank enters a disinfection tank for disinfection, and bacteria such as escherichia coli and the like are killed, so that the effluent bacteria are qualified.
K) The effluent disinfected by the disinfection tank enters the artificial wetland; and performing ozone oxidation and concentration on the residual sludge in the MBR tank, and finally performing filter pressing to obtain a mud cake as wetland filler.
Further, in the step B), the mass percent of the first part of effluent is 10-30%, the mass percent of the second part of effluent is 30-50%, the mass percent of the third part of effluent is 30-50%, and the mass percent of the fourth part of effluent is 10%.
Further, the sludge reflux ratio of the MBR tank to the primary aerobic zone in the step H) is 300-500 percent; the reflux ratio of the mixed liquid of the secondary aerobic zone and the pre-anoxic zone is 200 to 400 percent; the MBR tank biological enzyme modified activated carbon is powdered activated carbon with biological enzyme loaded in pores, is a special refractory organic matter for municipal sewage, and has a particle size of 10-100 mu m, and the dosage of the biological enzyme modified activated carbon is 20-40 mg/L.
Further, in the ozone reaction tank in the step I), the mass ratio of the added amount of ozone to the mass of COD removed is 3: 1-1: 1; in the MBR tank, the dosage of ozone tail gas is 5-10 mg/L; the ozone dosage of the residual sludge tail gas is as follows: 0.01 to 0.2g O3/g VSS。
The invention has the following beneficial effects:
the surface quasi-second class drinking water source water replenishing regeneration treatment system and the method have the following advantages:
(1) in the improved multi-stage AO-MBR process, a phosphorus removal agent is added into the inlet water, part of TP in the raw water is removed, the C/P ratio of the raw water is improved, conditions are created for removing TP in a biochemical system, the consumption is reduced, a subsequent removal system is omitted, and the water outlet effect is better compared with a traditional method for removing TP by adding a carbon source;
(2) the whole process adopts an improved multistage AO-MBR-biological enzyme modified activated carbon process, the integrity is more emphasized, COD is removed, easily degradable organic matters are removed by using activated sludge, and difficultly degradable organic matters are gradually diffused into the biological enzyme modified activated carbon and are removed under the action of an obligate enzyme; and the biological enzyme modified active carbon system has a synergistic effect on the degradation of organic matters, and forms: the adsorption-degradation-adsorption mode is different in different organic matter removal strategies, so that the aim of reasonably utilizing microorganisms is fulfilled; in addition, the pre-denitrification protects the anaerobic environment, the dephosphorization effect is higher, and the utilization of the carbon source by the sectional inflow is more efficient. On one hand, the MBR tank is adopted, so that the sludge retention time is prolonged, the multistage AO different microorganisms are easily strengthened, and the microorganisms suitable for different water qualities are easier to culture. Meanwhile, as a water outlet guarantee unit, SS and most of phosphorus-containing sludge can be removed, so that the water quality is better; the multi-stage AO-MBR-modified biological enzyme process plays the original multi-stage AO denitrification advantages, meanwhile, the modified biological enzyme-activated sludge system is utilized to remove refractory organic matters, the MBR can intercept SS, and TP is removed at a high standard;
(3) proper bio-enzyme modified activated carbon is added into the MBR tank 3, and the bio-enzyme modified activated carbon and the microorganisms and the ozone jointly act to form a virtuous cycle of adsorption-desorption-adsorption, so that COD removal is enhanced, and simultaneously, a proper amount of tail gas of the ozone reaction tank is introduced into the membrane tank to jointly act with the powdery bio-enzyme modified activated carbon, so that membrane silk fouling and blocking caused by extracellular polymeric organic matters are reduced.
(4) On one hand, the residual sludge concentration decomposition tank utilizes the ozone reaction generated by the ozone generator to destroy the sludge cell wall, cell dissolving substances are used as a carbon source for denitrification, meanwhile, the sludge after ozone treatment is easier to dehydrate, and the dehydrated sludge cake is used as the filler of the artificial wetland for sludge resource utilization;
(5) the ozone reaction tank further reduces the organic matters which are difficult to degrade in the sewage by using ozone, improves the biodegradability of the wastewater, and creates conditions for further biochemical degradation of COD by the artificial wetland. Meanwhile, the ozone tail gas is used as a medicament for inhibiting membrane silk fouling and blocking of the membrane tank, the treatment effect is obvious, and waste recycling can be realized;
(6) the artificial wetland is used as a means for advanced treatment, so that nutrient elements such as nitrogen and phosphorus in the sewage are further absorbed deeply, meanwhile, the artificial wetland utilizes the sludge as a filler, nitrogen and phosphorus substances contained in the sludge are fully utilized, waste is turned into treasure, and sludge recycling is realized. Meanwhile, artificial landscape can be built, natural combination of sewage treatment and artificial landscape is realized, and the ecological environment protection and restoration has positive significance.
Drawings
Fig. 1 is a schematic structural diagram of a surface level two-type drinking water source water replenishing regeneration treatment system.
FIG. 2 is a flow chart of the surface level two drinking water source water replenishing regeneration treatment method of the invention.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the invention and are not to be construed as limiting the invention.
Example 1
As shown in figure 1, the surface quasi-second type drinking water source water replenishing regeneration treatment system comprises an aeration grit chamber 1, a biological treatment section 2, an MBR (membrane biological reactor) chamber 3, a sludge concentration and decomposition tank 4, an ozone generator 5, an ozone reaction tank 6, a disinfection tank 7 and an artificial wetland 8.
The biological treatment section 2 comprises a pre-anoxic zone 21, an anaerobic zone 22, a primary aerobic zone 23, a primary anoxic zone 24, a secondary aerobic zone 25 and a secondary anoxic zone 26 which are connected in sequence. Wherein, the water outlet of the aeration grit chamber 1 is respectively communicated with the water inlet of the pre-anoxic zone 21, the water inlet of the anaerobic zone 22, the water inlet of the primary anoxic zone 24 and the water inlet of the secondary anoxic zone 26, and the water outlet of the secondary aerobic zone 25 is communicated with the water inlet of the pre-anoxic zone 21.
The sludge outlet of the MBR tank 3 is communicated with the sludge inlet of the primary aerobic zone 23. The sludge inlet of the sludge concentration and decomposition tank 4 is communicated with the sludge outlet of the MBR tank 3, the sludge lysate outlet of the sludge concentration and decomposition tank 4 is communicated with the pre-anoxic zone 21, and the filter cake produced by the sludge concentration and decomposition tank 4 is used for the artificial wetland 8.
The water outlet of the MBR tank 3 is communicated with the water inlet of the ozone reaction tank 6, the water outlet of the ozone reaction tank 6 is communicated with the water inlet of the disinfection tank 7, and the water outlet of the disinfection tank 7 is communicated with the water inlet 8 of the wetland. The gas inlet of the ozone reaction tank 6 is communicated with the outlet of the ozone generator 4, and the tail gas outlet of the ozone reaction tank 6 is respectively communicated with the ozone tail gas destruction device 61 and the ozone tail gas inlet of the MBR tank 3.
An ozone outlet of the ozone generator 5 is respectively communicated with an ozone inlet of the sludge concentration decomposition tank 4 and an ozone inlet of the ozone reaction tank 6, wherein the ozone generator uses compressed air generated by an air compressor as an air source.
According to the municipal sewage advanced treatment system provided by the embodiment of the invention, the water outlet of the aeration grit chamber 1 is respectively communicated with the water inlet of the pre-anoxic zone 21, the water inlet of the anaerobic zone 22, the water inlet of the primary anoxic zone 24 and the water inlet of the secondary anoxic zone 26, so that the water distribution of municipal sewage can be realized, and the utilization rate of a carbon source in the sewage can be improved. Specifically, the municipal wastewater exiting the aerated grit chamber 1 is divided into a first portion of effluent (flowing into the pre-anoxic zone 21), a second portion of effluent (flowing into the anaerobic zone 22), a third portion of effluent (flowing into the primary anoxic zone 24), and a fourth portion of effluent (flowing into the secondary anoxic zone 26).
The C/N of municipal sewage in China is low, and organic carbon sources in the municipal sewage are not enough to support denitrification reaction. In the existing A2/O process, in order to ensure that the TN of the discharged water reaches the standard, an additional carbon source (such as methanol or ethanol and the like) needs to be added during the denitrification reaction, thereby greatly increasing the treatment cost. According to the ground surface quasi-second type drinking water source water supplementing treatment system, the sludge lysate outlet of the sludge concentration decomposition tank 4 is communicated with the pre-anoxic zone 21, so that the sludge lysate can be fed into the pre-anoxic zone 21 as a carbon source for denitrification reaction, so that the denitrification reaction is performed on municipal sewage, and extra added carbon sources are reduced, so that the treatment cost is reduced, the obvious sludge reduction effect is achieved, and the sludge treatment cost is reduced; and meanwhile, a phosphorus removal agent is added to eliminate redundant TP, so that biochemical phosphorus removal of residual total phosphorus is facilitated.
According to the ground surface quasi-second-class drinking water source water replenishing treatment system, the secondary aerobic zone 25 and the secondary anoxic zone 26 are arranged, so that after the municipal sewage is subjected to aerobic treatment, the municipal sewage can be subjected to anoxic treatment and aeration treatment. By carrying out the anoxic treatment, the municipal sewage can be subjected to further denitrification reaction so as to further remove inorganic nitrogen in the municipal sewage. The aeration treatment can blow off the residual nitrogen, and simultaneously, the sedimentation performance of the sludge can be improved through aeration, so that organic matters are further removed.
According to the surface quasi-class II drinking water source water replenishing treatment system, the pre-anoxic zone 21 is arranged at the upstream of the anaerobic zone 22, and the sludge from the secondary anoxic zone 26 to the pre-anoxic zone 21 flows back, so that the protection of the subsequent anaerobic environment is ensured, the anoxic treatment is performed for denitrification, and NO can be effectively removed3And N, thereby ensuring that the subsequent phosphorus release reaction is fully performed and exerting the biochemical phosphorus removal capability to the maximum extent.
According to the invention, a proper amount of ozone tail gas of the ozone reaction tank 6 is added into the MBR tank 3, so that the microorganism extracellular polymer organic matters adhered to the surface of the membrane wires can be degraded, and the aeration scrubbing is carried out by matching with the biological enzyme modified activated carbon, so that the pollution blockage of a phosphorus removal agent and pollutants to the membrane wires can be effectively reduced, and the tail gas waste utilization can be realized.
According to the invention, the residual sludge in the MBR tank 3 is subjected to ozone treatment in the sludge concentration and decomposition tank, the lysate is used as a carbon source, the sludge is easy to dehydrate, the sludge after filter pressing contains substances such as activated carbon, alumina and the like which are easy to support and expand and rich nitrogen and phosphorus substances, and the sludge is used as a filler of a subsequent artificial wetland 8 and has the functions of containing water, ventilating, fixing and supporting and providing nutrient elements.
According to the invention, the constructed wetland 8 can be treated to achieve the purpose of deeply removing nitrogen and phosphorus, and SS and COD are treated by the wetland, so that the toxicity of microorganisms and water quality is further reduced, and the water quality is soft to achieve the purpose of deeply purifying.
Therefore, the surface quasi-second type drinking water source water replenishing treatment system has the advantages of good treatment effect, low operation cost and the like. Can make the effluent meet the requirements of the A standard in the Table 1 of the discharge Standard of Water pollutants for municipal wastewater treatment plant (DB11/890-5、COD、NH3The requirements of-N and TP are the same as the water quality standard of class II water body of the environmental quality standard of surface water (GB 3838-2002).
Example 2
In this embodiment, the surface quasi-second type drinking water source water replenishing treatment system of the present invention sequentially comprises a coarse grating (not shown in the figure), a fine grating (not shown in the figure), an aeration grit chamber 1, a water inlet automatic control device (not shown in the figure), a biological treatment section 2, an MBR chamber 3, a sludge concentration and decomposition chamber 4, an ozone generator 5, an ozone reaction chamber 6, a disinfection chamber 7 and an artificial wetland 8.
The coarse grid is positioned at the upstream of the aeration grit chamber 1, and the fine grid is positioned between the coarse grid and the aeration grit chamber 1. In other words, the municipal sewage flows through the coarse grating, the fine grating, and the aeration grit chamber 1 in this order. Wherein, the clear distance of the grid bars of the coarse grid is 20 mm, and the flow velocity of the municipal sewage passing through the grid is 0.8 m/s; the gap between the grids of the fine grid is 3 mm, and the flow velocity of municipal sewage passing through the grids is 0.8 m/s.
Municipal sewage gets into in the aeration grit chamber 1 through carrying out the aeration grit to municipal sewage after the simple preliminary treatment of thick grid and thin grid, not only can get rid of most inorganic granule in the municipal sewage, can make the organic matter that adheres on inorganic granule get into in the municipal sewage moreover to can improve the organic carbon source content in the municipal sewage. Wherein the hydraulic retention time of the aeration grit chamber 1 is 8 minutes.
Advantageously, the surface quasi-second type drinking water source water replenishing regeneration treatment system is not provided with a primary sedimentation tank, so that the loss of organic carbon sources can be reduced, and carbon sources as much as possible are provided for subsequent enhanced biological nitrogen and phosphorus removal.
The water outlet of the aeration grit chamber 1 is communicated with the water inlet of a water inlet automatic control device, and the water outlet of the water inlet automatic control device is respectively communicated with the water inlet of the pre-anoxic zone 21, the water inlet of the anaerobic zone 22, the water inlet of the primary anoxic zone 24 and the water inlet of the secondary anoxic zone 26. In other words, the water inlet automatic control device is flow monitoring and adjusting equipment arranged among the water outlet of the aerated grit chamber 1, the water inlet of the pre-anoxic zone 21, the water inlet of the anaerobic zone 22, the water inlet of the primary anoxic zone 24 and the water inlet of the secondary anoxic zone 26. Can shunt municipal sewage from this to can improve the utilization ratio of the organic carbon source in the municipal sewage.
Wherein the municipal wastewater is split into a first portion of effluent flowing into the pre-anoxic zone 21, a second portion of effluent flowing into the anaerobic zone 22, a third portion of effluent flowing into the primary anoxic zone 24, and a fourth portion of effluent flowing into the secondary anoxic zone 26. That is to say, municipal wastewater advanced treatment regeneration recycling system adopts the mode of multiple spot water inflow. The volume percentage of the first part of the discharged water is 10-30%, the volume percentage of the second part of the discharged water is 30-50%, the volume percentage of the third part of the discharged water is 30-50%, and the volume percentage of the fourth part of the discharged water is about 10%. That is, the volume distribution can be realized according to the water inlet automatic control device.
As shown in fig. 1, the biological treatment section 2 includes a pre-anoxic zone 21, an anaerobic zone 22, a primary aerobic zone 23, a primary anoxic zone 24, a secondary aerobic zone 25, and a secondary anoxic zone 26, which are connected in sequence. A first portion of the effluent flows into the pre-anoxic zone 21.
Specifically, the biological treatment and membrane tank can be designed into a rectangular tank, and a biological phosphorus and nitrogen removal reaction tank consisting of a pre-anoxic zone 21, an anaerobic zone 22, a primary aerobic zone 23, a primary anoxic zone 24, a secondary aerobic zone 25, a secondary anoxic zone 26 and an MBR tank 3 which are independent and can be controlled respectively is adopted. The hydraulic retention time of the biological treatment section 2 is 26.5 hours, and the volume ratio of the pre-anoxic zone 21, the anaerobic zone 22, the primary aerobic zone 23, the primary anoxic zone 24, the secondary aerobic zone 25 and the secondary anoxic zone 26 can be 1:1:2:1.27:1.7:1.12: 0.88.
In the existing A2/O process, the sludge discharged from the sedimentation tank (i.e. return sludge) carries a large amount of NO3the-N directly flows back to the anaerobic zone, and the phosphorus release effect of the anaerobic zone is seriously influenced, so that the phosphorus removal capability of the anaerobic zone is seriously limited. In the process, the pre-anoxic zone 21 preferentially utilizes a carbon source to remove nitrate nitrogen in the return sludge, protects the environment of the subsequent anaerobic zone 22 from being damaged, and utilizes a lysate as the carbon source to enhance the denitrification effect. Advantageously, the return sludge has a sludge return ratio of 200% to 400%. And meanwhile, a phosphorus removal agent is added to remove part of TP, so that the C/P ratio of the whole system is improved, and phosphorus removal is facilitated. Advantageously, the phosphorus removal agent is PFS and PAC, and the dosage is 20 mg/L-40 mg/L.
After the pre-anoxic zone 21 reaction, a first portion of the effluent flows into the anaerobic zone 22 and is mixed with a second portion of the effluent. In the anaerobic zone 22, the first portion of the effluent and the second portion of the effluent are anaerobically treated to effect a phosphorus release reaction. By adding new municipal sewage, that is, municipal sewage which is not subjected to anoxic treatment, while the phosphorus release reaction is performed, it is possible to ensure that the phosphorus release reaction is sufficiently performed.
Then, the first part of effluent water after the anaerobic treatment and the second part of effluent water and return sludge of the MBR tank enter a primary aerobic zone 23 to carry out nitration reaction to remove ammonia nitrogen and absorb the sludge TP, preferably, the dissolved oxygen is 0.5-3 mg/L, and the sludge concentration is 3500 mg/L-5000 mg/L.
After the first-stage aerobic zone 23 is treated, the first part of effluent and the second part of effluent treatment liquid enter the first-stage anoxic zone and are mixed with the third part of effluent, and the third part of effluent is used for bringing carbon sources in raw water in the first-stage anoxic zone 24 to generate nitrate nitrogen for denitrification removal. Preferably, the concentration of the reaction sludge is 3500 mg/L-5000 mg/L, and the reflux ratio of the MBR tank from 3 to the first-stage aerobic tank is 300-500%.
After the reaction in the first-stage anoxic zone 24, the first part of effluent, the second part of effluent and the third part of effluent enter a second-stage aerobic zone 25, the nitration reaction and phosphorus absorption are continuously carried out, residual ammonia nitrogen in the first part of effluent and the second part of effluent and ammonia nitrogen generated in the third part of effluent are removed, preferably, the required dissolved oxygen is 0.5-3 mg/L, and the sludge concentration is 3500 mg/L-5000 mg/L.
And then, performing secondary anoxic reaction on the first part of effluent, the second part of effluent, the third part of effluent and the fourth part of effluent, and deeply denitrifying nitrate nitrogen contained in the first part of effluent, the second part of effluent and the third part of effluent under the condition that the fourth part of effluent raw water provides a carbon source. And simultaneously, adjusting the input amount of the external carbon source in time according to the requirement, wherein the input amount/removal amount of the external carbon source is 4: 1-8: 1, the sludge concentration is 3500 mg/L-5000 mg/L.
After the treatment in the second-stage anoxic zone 26, the sludge-water mixed liquid of the first part of effluent, the second part of effluent, the third part of effluent and the fourth part of effluent enters the MBR tank 3, under the aeration condition, the residual ammonia nitrogen is removed to reach the standard, and meanwhile, the biological activated carbon is added to remove deeply difficultly-degraded organic matters to reach the standard of COD.
And introducing the tail gas of the ozone reaction tank into the MBR tank 3 to act together with the biological enzyme modified activated carbon, so as to remove organic matters adhered to the surface of the membrane filaments and delay the fouling and blocking degree of the membrane filaments. Meanwhile, the ozone reacts with organic matters in the active carbon to recover the adsorption performance of the biological enzyme modified active carbon. The ozone breaks the chains of the organic matters which are difficult to degrade into smaller organic matters which are easy to decompose, and the COD removal capability is enhanced.
Preferably, the biological enzyme modified activated carbon is powdered activated carbon, the particle size is 10-100 μm, and the dosage of the biological enzyme modified activated carbon is 20-40 mg/L. In the MBR tank, the ozone tail gas input amount is as follows: 5-10 mg/L; the sludge concentration is 6000 mg/L-12000 mg/L, and the sludge age is 10 d-25 d.
And (3) allowing residual sludge of the MBR to enter a sludge concentration decomposition tank 4, and introducing ozone from an ozone generator 5 to perform decomposition reaction on the sludge, wherein preferably, the ozone adding concentration is 0.01-0.2 gO 3/gVSS. The water content of the dewatered sludge is less than 80 percent, and the sludge is used as the artificial wetland filler after being detected to be qualified. The extracellular lysate enters the pre-anoxic tank 21.
And (3) enabling the effluent of the MBR tank 3 to enter an ozone reaction tank 6, arranging catalyst filler in the ozone reaction tank 6, setting the filtering speed to be 3-6 m/h, setting the adding amount of ozone to be 20-30 mg/L, and keeping the ozone for 1-2 h. Preferably, the mass ratio of the ozone addition amount to the COD removed is 3: 1-1: 1;
the effluent of the ozone reaction tank 6 enters a disinfection tank 7, the disinfectant used in the disinfection tank 7 is sodium hypochlorite, and the retention time is 4-8 h. The concentration of sodium hypochlorite is 5-10 mg/L.
The effluent enters an artificial wetland 8 after passing through a disinfection tank 7, and the artificial wetland ground check hydraulic load is 0.45m3/m2d, total hydraulic retention time: and 3.1d, selecting the plants such as reed, cattail, yellow iris, giant reed and the like which have developed root systems, strong pollution resistance and strong dirt-removing power and are suitable for local environments.
Table 1-surface water quality of inlet water and outlet water of the quasi-second class drinking water source water replenishing regeneration treatment system.
Item CODcr BOD5 SS TN NH3-N TP Coliform bacteria
Quality of inlet water (mg/L) 400 250 300 50 35 6.5 2000
Effluent water quality (mg/L) 15 3 5 10 0.5 0.1 ---
Example 3
As shown in fig. 2, a surface level two-type drinking water source water replenishing regeneration treatment method includes the following steps:
A) municipal sewage passes through the coarse grating and the fine grating, and aeration and sand setting are carried out on the sewage. Through carrying out aeration sand setting to municipal sewage, not only can get rid of most inorganic granule in the municipal sewage, can make the organic matter that adheres on inorganic granule get into in the municipal sewage moreover to can improve the organic carbon source content in the municipal sewage.
B) And after aeration and sand setting, water is separated into four parts, namely first part effluent, second part effluent, third part effluent and fourth part effluent. In the pre-anoxic zone 21, the first part of effluent is mixed with the return sludge of the secondary aerobic zone 25 for denitrification and dephosphorization, and a dephosphorization agent is added for dephosphorization at the same time.
C) In the anaerobic zone 22, the treated first part of the effluent is mixed with the second part of the effluent to carry out anaerobic phosphorus release.
D) In the primary aerobic zone, mixing the treated first part of effluent, the treated second part of effluent and return sludge in the MBR tank 3, and carrying out aerobic nitration reaction to remove ammonia nitrogen; simultaneously, aerobic absorption of phosphorus is carried out, and total phosphorus is transferred from the liquid to the sludge.
E) In the first-stage anoxic zone 24, the treated first part of effluent, the treated second part of effluent and the third part of effluent are mixed, and total nitrogen is continuously removed by denitrification.
F) In the secondary aerobic zone 25, the treated first part of effluent is mixed with the treated second part of effluent and the treated third part of effluent, and ammonia nitrogen removal and deep phosphorus removal are continuously carried out.
G) In the secondary anoxic zone 26, the treated first part of effluent, the treated second part of effluent, the treated third part of effluent and the fourth part of effluent are mixed, and then an external carbon source is added for deep denitrification.
H) In the MBR tank 3, mixing the treated first part of effluent, the treated second part of effluent, the treated third part of effluent and the treated fourth part of effluent, adding biological enzyme modified activated carbon into the MBR tank 3 to remove refractory organic matters, filtering by a membrane to remove SS (suspended substances), discharging the residual phosphorus-containing sludge, and finally adding ozone into the MBR tank 3 to reduce membrane silk fouling and restore the adsorption capacity of the biological enzyme modified activated carbon.
I) The ozone reaction tank 6 further removes organic matters difficult to degrade under the action of a catalyst, so that COD reaches the standard, excessive tail gas after reaction is treated by the ozone tail gas destruction device 61, and the rest is introduced into the MBR tank 3.
J) The effluent treated by the sampling reaction tank enters a disinfection tank 7 for disinfection, and bacteria such as escherichia coli and the like are killed, so that the effluent bacteria are qualified.
K) In the artificial wetland 8, the residual sludge in the MBR tank 3 is subjected to ozone oxidation treatment and then is subjected to concentration, filter pressing and the like to generate qualified mud cakes as wetland fillers; the first part of effluent, the second part of effluent, the third part of effluent and the fourth part of effluent, the residual SS is intercepted, nitrogen, phosphorus and the like are continuously absorbed, and the water quality is purified.
Compared with the traditional six-stage method-ultrafiltration process, the system has the following advantages:
firstly, a proper amount of biological enzyme modified activated carbon is added into the membrane tank, a new symbiotic system is established between the biological enzyme modified activated carbon and the activated sludge, the biological enzyme modified activated carbon and the activated sludge are mutually promoted, and the removal capacity is stronger than that of the traditional process. 1) The activated sludge has higher concentration than the biological enzyme modified activated carbon, and firstly decomposes easily degradable organic matters to complete various functional metabolisms (such as nitrogen and phosphorus removal and microorganism growth); 2) along with the gradual progress of the reaction, the subsequent refractory organic matters are gradually diffused into the biological enzyme-activated carbon for continuous obligate degradation, the pre-degradation of the activated sludge provides conditions for the obligate degradation of the biological enzyme modified activated carbon, the medicament is saved, and the biological enzyme modified activated carbon deeply removes the organic matters, inhibits aerobic heterogeneous bacteria, promotes the growth of nitrifying bacteria and is beneficial to removing ammonia nitrogen; 3) in a biological enzyme-activated carbon system, the difficultly degraded organic matters are subjected to an adsorption-degradation-adsorption dynamic balance process, so that the removal capacity of the difficultly degraded organic matters is improved, and a synergistic effect is achieved.
Secondly, a proper amount of tail gas in the ozone reaction tank 6 is introduced into the MBR tank 3, so that the degradation and mineralization capacity of the surface of the membrane yarn on organic matters such as extracellular polymers is enhanced, the viscosity of the organic matters is reduced, and the anti-fouling and anti-blocking capacity of the membrane yarn is greatly improved. Simultaneously under the combined action of appropriate amount of activated carbon scouring, the dirty stifled degree of membrane silk is reduced, and the input of ozone degrades the organic matter that adsorbs in the activated carbon, improves the activated carbon recovery ability.
And thirdly, the residual sludge is subjected to ozone treatment to destroy the sludge cell wall, part of sludge lysate is used as a denitrification carbon source, the carbon source is saved, the sludge is subjected to filter pressing and dehydration more easily after the ozone treatment, the sludge reduction is obvious, and meanwhile, the ozone is subjected to oxidation harmless treatment on bacteria and heavy metals.
Fourthly, the formed filter cake contains rich elements such as nitrogen and phosphorus, the aluminum salt added by dehydration can change the property of the sludge to form a porous structure, and the sludge cake is used for the artificial wetland 8, thereby changing waste into valuable and realizing the recycling of the sludge.
Fifthly, the water is fed in stages, so that the utilization rate of the organic carbon source in the raw water can be improved.
And sixthly, the oxygen deficiency is preposed, so that the denitrification capability of the nitrate is improved, and a good anaerobic environment is ensured.
Therefore, the drinking water source water replenishing treatment method based on the surface standard II water quality standard has the advantages of being good in treatment effect, low in operation cost and the like. By treating municipal sewage by using the drinking water source water replenishing treatment method based on the surface standard II water quality standard according to the embodiment of the invention, the outlet water can meet the requirements of the A standard in the Table 1 of the discharge Standard of Water pollutants for urban Sewage treatment plants (DB11/890-5、COD、NH3The requirements of-N and TP are the same as the water quality standard of class II water body of the environmental quality standard of surface water (GB 3838-2002).
The inventive concept is explained in detail herein using specific examples, which are given only to aid in understanding the core concepts of the invention. It should be understood that any obvious modifications, equivalents and other improvements made by those skilled in the art without departing from the spirit of the present invention are included in the scope of the present invention.

Claims (9)

1. A surface quasi-class II drinking water source water replenishing regeneration treatment system is characterized by comprising an aeration grit chamber, a biological treatment section, an MBR tank, a sludge concentration and decomposition tank, an ozone reactor, an ozone tail gas destruction device, an ozone reaction tank, a disinfection tank and an artificial wetland;
the biological treatment section comprises a pre-anoxic zone, an anaerobic zone, a primary aerobic zone, a primary anoxic zone, a secondary aerobic zone and a secondary anoxic zone which are sequentially connected, wherein a water inlet of the pre-anoxic zone, a water inlet of the anaerobic zone, a water inlet of the primary anoxic zone and a water inlet of the secondary anoxic zone are communicated with a water outlet of the aeration grit chamber, and a water outlet of the secondary aerobic zone is communicated with a water inlet of the pre-anoxic zone;
the water inlet of the MBR tank is communicated with the water outlet of the secondary anoxic zone, the water outlet of the MBR tank is communicated with the inlet of the ozone reaction tank, the return sludge outlet of the MBR tank is communicated with the return inlet of the primary aerobic sludge, and the residual sludge outlet of the MBR tank is communicated with the sludge concentration decomposition tank;
the sludge lysate outlet of the sludge concentration decomposition pool is communicated with the pre-anoxic zone; filter cakes generated by the residual sludge in the MBR tank are used for artificial wetland filler;
the ozone outlet of the ozone generator is respectively communicated with the sludge concentration and decomposition tank and the ozone reaction tank;
the water inlet of the ozone reaction tank is communicated with the water outlet of the MBR tank, the water outlet of the ozone reaction tank is communicated with the disinfection tank, and the tail gas of the ozone reaction tank is respectively connected with the ozone tail gas destruction device and the MBR tank;
the water inlet of the disinfection tank is communicated with the water outlet of the ozone reaction tank, the outlet of the disinfection tank is communicated with the water inlet of the artificial wetland, and a filter cake obtained by dewatering and filter pressing sludge is used as a filler of the artificial wetland.
2. The surface level two type drinking water source water replenishing regeneration treatment system according to claim 1, characterized by further comprising a coarse grid, a fine grid and a membrane grid; the coarse grating is positioned at the upstream of the aeration grit chamber, the fine grating is positioned between the coarse grating and the aeration grit chamber, and the membrane grating is positioned at the downstream of the aeration grit chamber.
3. The surface level two-class drinking water source water replenishing regeneration treatment system of claim 1, which comprises a water inlet automatic control device, wherein a water inlet of the water inlet automatic control device is communicated with a water outlet of the aeration grit chamber, and a water outlet of the water inlet automatic control device is communicated with each of a water inlet of the pre-anoxic zone, a water inlet of the anaerobic zone, a water inlet of the primary anoxic zone and a water inlet of the secondary anoxic zone.
4. The surface level two-class drinking water source water replenishing and regeneration treatment system as claimed in claim 1, wherein a water outlet of the secondary aerobic zone is communicated with a water inlet of the pre-anoxic zone.
5. The surface level two type drinking water source water replenishing regeneration treatment system according to claim 1, which is characterized by comprising an ozone reaction tank, wherein a COD catalytic oxidation filler is arranged in the ozone reaction tank.
6. A surface quasi-second class drinking water source water replenishing regeneration treatment method is characterized by comprising the following steps:
A) raw water enters an aeration grit chamber through a coarse grid and a fine grid;
B) after aeration and sand setting, dividing the effluent into four parts, namely a first part effluent, a second part effluent, a third part effluent and a fourth part effluent through a membrane grid; mixing the first part of effluent in the pre-anoxic zone with return sludge and lysate in the secondary aerobic zone for denitrification, and simultaneously adding a phosphorus removal agent for phosphorus removal;
C) in the anaerobic zone, mixing the treated first part of effluent with the second part of effluent to carry out anaerobic phosphorus release;
D) in the primary aerobic zone, mixing the treated first part of effluent, the treated second part of effluent and return sludge of an MBR tank, and carrying out aerobic nitration reaction to remove ammonia nitrogen; simultaneously carrying out aerobic absorption of phosphorus, and transferring total phosphorus from the liquid to sludge;
E) in the first-stage anoxic zone, mixing the treated first part of effluent, the treated second part of effluent and the third part of effluent, and continuously removing total nitrogen through denitrification;
F) in the secondary aerobic zone, mixing the treated first part of effluent with the treated second part of effluent and the treated third part of effluent, and continuously removing ammonia nitrogen;
G) in the secondary anoxic zone, mixing the treated first part of effluent, the treated second part of effluent, the treated third part of effluent and the fourth part of effluent, and adding an external carbon source for deep denitrification;
H) mixing the treated first part of effluent, the treated second part of effluent, the treated third part of effluent and the treated fourth part of effluent in an MBR tank, adding biological enzyme modified activated carbon into the MBR tank, discharging the residual phosphorus-containing sludge, and finally adding ozone into the MBR tank;
I) adding an obligate COD catalyst into the ozone reaction tank, and treating residual ozone after reaction in the ozone reaction tank by an ozone tail gas destruction device;
J) the effluent treated by the sampling reaction tank enters a disinfection tank for disinfection;
K) the effluent disinfected by the disinfection tank enters the artificial wetland; and performing ozone oxidation and concentration on the residual sludge in the MBR tank, and finally performing filter pressing to obtain a mud cake as wetland filler.
7. The surface level two drinking water source water replenishing regeneration treatment method according to claim 6, characterized in that: in the step B), the mass percent of the first part of effluent is 10-30%, the mass percent of the second part of effluent is 30-50%, the mass percent of the third part of effluent is 30-50%, and the mass percent of the fourth part of effluent is 10%.
8. The surface level two drinking water source water replenishing regeneration treatment method according to claim 6, characterized in that: in the step H), the sludge reflux ratio from the MBR tank to the primary aerobic zone is 300-500 percent; the reflux ratio of the mixed liquid from the secondary aerobic zone to the pre-anoxic zone is 200-400 percent; the biological enzyme modified activated carbon of the MBR tank is powdered activated carbon loaded with biological enzyme in pores, the particle size is 10-100 mu m, and the adding dosage of the biological enzyme modified activated carbon is 20-40 mg/L.
9. The surface level two-class drinking water source water replenishing and regeneration treatment method according to claim 6, which is characterized in that: in the ozone reaction tank in the step I), the mass ratio of the added amount of ozone to the removed COD is 3: 1-1: 1; in the MBR tank, the dosage of ozone tail gas is 5-10 mg/L; the ozone dosage of the residual sludge tail gas is as follows: 0.01 to 0.2g O3/g VSS。
CN202011039092.6A 2020-09-28 2020-09-28 Surface quasi-class II drinking water source water replenishing regeneration treatment system and method Pending CN112142263A (en)

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2583752A1 (en) * 2004-10-12 2006-04-20 Biocast Systems, Inc. Integrated multi-zone wastewater treatment system and method
CN102276121A (en) * 2011-07-26 2011-12-14 中冶南方工程技术有限公司 Process and system for treating reverse osmosis concentrated water of cold rolling steel mill
CN103359893A (en) * 2013-08-06 2013-10-23 山东建筑大学 A sewage treatment and reclaimed-water reuse coupled system for landscape energy-efficient residential areas
CN105621814A (en) * 2016-03-07 2016-06-01 北京恩菲环保股份有限公司 High-quality regenerated recycle water treatment system and method
CN214400149U (en) * 2020-09-28 2021-10-15 北京恩菲环保股份有限公司 Surface quasi-second-class drinking water source water replenishing regeneration treatment system

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2583752A1 (en) * 2004-10-12 2006-04-20 Biocast Systems, Inc. Integrated multi-zone wastewater treatment system and method
CN102276121A (en) * 2011-07-26 2011-12-14 中冶南方工程技术有限公司 Process and system for treating reverse osmosis concentrated water of cold rolling steel mill
CN103359893A (en) * 2013-08-06 2013-10-23 山东建筑大学 A sewage treatment and reclaimed-water reuse coupled system for landscape energy-efficient residential areas
CN105621814A (en) * 2016-03-07 2016-06-01 北京恩菲环保股份有限公司 High-quality regenerated recycle water treatment system and method
CN214400149U (en) * 2020-09-28 2021-10-15 北京恩菲环保股份有限公司 Surface quasi-second-class drinking water source water replenishing regeneration treatment system

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