CN112142263B - Surface quasi-class II drinking water source water replenishment regeneration treatment system and method - Google Patents
Surface quasi-class II drinking water source water replenishment regeneration treatment system and method Download PDFInfo
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 194
- 239000003651 drinking water Substances 0.000 title claims abstract description 33
- 235000020188 drinking water Nutrition 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 27
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Classifications
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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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
本发明公开了一种地表准二类饮用水水源补水再生处理系统及方法，包括曝气沉砂池、生物处理段、MBR池、臭氧氧化段、污泥浓缩分解池、消毒段和人工湿地段；生物处理段包括预缺氧区、厌氧区、一级好氧区、一级缺氧区、二级好氧区和二级缺氧区；曝气沉砂池的出水口分别与预缺氧区、厌氧区、一级缺氧区和二级缺氧区的进水口连通；二级好氧区的出水口与预缺氧区的进水口连通；MBR池的污泥出口与一级好氧区的污泥进口连通；MBR的污泥出口与污泥浓缩分解池的污泥进口连通，污泥浓缩分解池的污泥溶胞产物出口与预缺氧区连通，污泥浓缩分解池的剩余污泥处理成泥饼进入工湿地。本发明地表准二类饮用水水源补水再生处理系统具有处理效果好和运行成本低等优点。
The invention discloses a surface quasi-class II drinking water source water replenishment and regeneration treatment system and method, comprising an aerated grit chamber, a biological treatment section, an MBR tank, an ozone oxidation section, a sludge concentration and 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 aerated grit chamber is respectively connected 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 connected with the water inlet of the pre-anoxic zone; the sludge outlet of the MBR tank is connected with the sludge inlet of the primary aerobic zone; the sludge outlet of the MBR is connected with the sludge inlet of the sludge concentration and decomposition tank, the sludge lysate outlet of the sludge concentration and decomposition tank is connected with the pre-anoxic zone, and the residual sludge of the sludge concentration and decomposition tank is processed into a mud cake and enters the artificial wetland. The surface quasi-class II drinking water source water replenishment and regeneration treatment system of the invention has the advantages of good treatment effect and low operation cost.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, in particular to a drinking water source water supplementing and regenerating treatment system based on a surface quasi-second-class water quality standard, and further relates to a drinking water source water supplementing and regenerating treatment method based on the surface quasi-second-class water quality standard.
Background
The national people can utilize insufficient fresh water resources, but the water pollution is increasingly serious, the health and ecological environment of people are influenced, the water treatment emission standard is also more and more strict, the standard A standard of Beijing standard (DB 11890-2012) of the discharge standard of the water pollutants of urban sewage treatment plants reaches the III class water quality standard of surface water except TN, the opinion about accelerating the construction of ecological civilization, which is printed by the middle center and the national institutes, clearly proposes double limitation of the discharge standard and the total limit of the pollutants, namely ' region limitation ' is uniformly carried out in all areas which do not finish the control task of the total amount of the main pollutant emission ', particularly, the environmental sensitive regions such as natural protection areas, holiday villages and drinking water source protection areas are pushed, and the III class standard of the surface water (except TN) or higher standard is pushed to have practical significance for the water resource protection.
The prior art has difficulties in deep denitrification and dephosphorization and removal of refractory organic matters in a conventional water treatment process system, so that the sewage treatment effect is not ideal, the operation cost is high, and the invention is particularly provided in view of the problems.
Disclosure of Invention
The invention provides a drinking water source water supplementing treatment and regenerating system with standard surface quasi-second water quality aiming at municipal sewage, and aims to solve the problems of deep denitrification and dephosphorization and difficult degradation of organic matters in the conventional water treatment process system at present and realize an integrated system under the standard surface quasi-second discharge of municipal sewage. The invention also provides a treatment method for supplementing and regenerating the drinking water source with the standard of the surface quasi-second-class water quality, which has good treatment effect and low operation cost.
In order to achieve the aim, the surface quasi-class II drinking water source water supplementing and regenerating treatment system comprises an aeration sand setting tank, a biological treatment section, an MBR tank, a sludge concentration 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 a water inlet of the primary anoxic zone and a water inlet of 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 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 sludge return inlet of the primary aerobic zone, and the residual sludge outlet of the MBR tank is communicated with the sludge concentration decomposition tank. And a sludge lysate outlet of the sludge concentration decomposition tank is communicated with the pre-anoxic zone, and a filter cake generated by residual sludge of the MBR tank is used for artificial wetland filler. The ozone generator is characterized in that an ozone outlet of the ozone generator is respectively communicated with the sludge concentration and decomposition tank and the ozone reaction tank, and compressed air generated by an air compressor is used 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 constructed wetland, and a filter cake obtained by dewatering and filter pressing sludge is used as a filler of the constructed wetland.
Further, the aeration sand setting device further comprises a coarse grid, a fine grid and a membrane grid, wherein the coarse grid is positioned at the upstream of the aeration sand setting tank, the fine grid is positioned between the coarse grid and the aeration sand setting tank, and the membrane grid is positioned at the downstream of the aeration sand setting tank.
Further, the device comprises a water inlet automatic control device, a water inlet of the water inlet automatic control device is communicated with a water outlet of the aeration sand basin, 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.
Further, the water outlet of the secondary aerobic zone is communicated with the water inlet of the pre-anoxic zone.
Further, the device comprises an ozone reaction tank, and COD catalytic oxidation filling materials are arranged in the ozone reaction tank.
The invention also provides a surface quasi-class II drinking water source water supplementing and regenerating treatment method, which comprises the following steps:
a) Raw water passes through the coarse grille and the fine grille and enters the aeration sand basin.
B) The first part of water is mixed with the return sludge of the second-stage aerobic zone and lysate in the pre-anoxic zone to carry out denitrification and denitrification, and meanwhile, a dephosphorization reagent is added to carry out dephosphorization.
C) In the anaerobic zone, the treated first portion of effluent is mixed with the second portion of effluent for anaerobic phosphorus release.
D) In the first-stage aerobic zone, the treated first part of effluent, the treated second part of effluent and the return sludge of the MBR pool are mixed, aerobic nitrification reaction is carried out to remove ammonia nitrogen, and meanwhile, aerobic phosphorus absorption is carried out, so that the total phosphorus is transferred from liquid to sludge.
E) In the primary anoxic zone, the treated first partial effluent, the treated second partial effluent and the treated third partial effluent are mixed, and denitrification continues to remove total nitrogen.
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 carried out continuously.
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 treated fourth part of effluent are mixed, and then the external carbon source is added for deep denitrification.
H) In an MBR tank, 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 are mixed, biological enzyme modified activated carbon is added into the MBR tank to remove refractory organic matters, SS is removed through membrane filtration, residual phosphorus-containing sludge is discharged, and finally ozone is added into the MBR tank to reduce membrane silk blockage and restore the adsorption capacity of the biological enzyme modified activated carbon.
I) And (3) adding an obligate COD catalyst into the ozone reaction tank, and treating the residual ozone after the reaction in the ozone reaction tank by an ozone tail gas destruction device.
J) The effluent treated by the ozone reaction tank enters a disinfection tank for disinfection, and bacteria such as escherichia coli and the like are killed, so that the effluent fungus is qualified.
K) And performing ozone oxidation and concentration on the residual sludge in the MBR tank, and finally press-filtering to form a mud cake as a wetland filler.
Further, in the step B), the mass percentage of the first part of water is 10% -30%, the mass percentage of the second part of water is 30% -50%, the mass percentage of the third part of water is 30% -50%, and the mass percentage of the fourth part of water is 10%.
Further, in the step H), the sludge reflux ratio of the MBR tank-primary aerobic zone is 300% -500%, the mixed liquor reflux ratio of the secondary aerobic zone-pre-anoxic zone is 200% -400%, the biological enzyme modified activated carbon of the MBR tank is powdery activated carbon loaded with biological enzymes in pores, is specific refractory organic matters aiming at municipal sewage, has the particle size of 10 mu m-100 mu m, and the adding dosage of the biological enzyme modified activated carbon is 20 mg/L-40 mg/L.
Further, in the step I), the mass ratio of ozone addition amount to COD removal is 3:1-1:1, the ozone tail gas addition amount is 5-10 mg/L, and the ozone addition amount of the residual sludge tail gas is 0.01-0.2 gO 3/gVSS in the MBR.
The invention has the following beneficial effects:
the surface quasi-class II drinking water source water supplementing and regenerating treatment system and method have the following advantages:
(1) In the improved multistage AO-MBR process, the dephosphorization agent is added into the inlet water to remove part of TP in the raw water, so that the C/P ratio of the raw water is improved, conditions are created for removing TP by a biochemical system, TP is removed more effectively, consumption is reduced compared with the traditional method of adding carbon source, a subsequent removal system is omitted, and the water outlet effect is better;
(2) The whole process adopts an improved multistage AO-MBR-biological enzyme modified activated carbon process, the integrity is emphasized more, firstly, COD is removed, easily degradable organic matters are removed by using activated sludge, the difficultly degradable organic matters gradually diffuse into the biological enzyme modified activated carbon and are removed under the action of proprietary enzyme, the biological enzyme modified activated carbon system has a synergistic effect on organic matter degradation, an adsorption-degradation-adsorption mode is formed, different organic matter removal strategies are different, the aim of reasonably utilizing microorganisms is fulfilled, in addition, the anaerobic environment is protected by pre-denitrification, the phosphorus removal effect is higher, and the utilization of the segmented water inlet carbon source is more efficient. On one hand, the sludge residence time of the MBR tank is prolonged, so that different microorganisms of the multi-stage AO are easily strengthened, and microorganisms applicable to different water qualities are more easily cultured. The multi-stage AO-MBR-modified biological enzyme process plays the original multi-stage AO denitrification advantage, and simultaneously utilizes a modified biological enzyme-activated sludge system to realize the removal of refractory organic matters, wherein the MBR can intercept SS and remove TP high standards;
(3) And proper biological enzyme modified activated carbon is added into the MBR tank 3, and the biological enzyme modified activated carbon and the microorganism and the ozone are combined to form a virtuous circle of adsorption-analysis-adsorption, so that COD removal is enhanced, and meanwhile, a proper amount of ozone reaction tank tail gas is introduced into the membrane tank to be combined with the powdery biological enzyme modified activated carbon, so that membrane silk pollution and blockage caused by extracellular polymeric organic matters are reduced.
(4) On one hand, the residual sludge concentration and decomposition tank utilizes the ozone reaction generated by the ozone generator to break the cell wall of the sludge, a cell-dissolving substance is used as a carbon source for denitrification, meanwhile, the sludge after ozone treatment is easier to dehydrate, and a dehydrated mud cake is used as a filler of the constructed wetland for recycling the sludge;
(5) The ozone reaction tank further reduces refractory organic matters in the sewage by utilizing ozone, improves the biodegradability of the sewage, and creates conditions for further biochemical degradation of COD (chemical oxygen demand) in the constructed wetland. Meanwhile, the ozone tail gas is used as a medicament for inhibiting membrane silk fouling of a membrane tank, so that the treatment effect is obvious, and the recycling of waste can be realized;
(6) The constructed wetland is used as a means for advanced treatment to further deeply absorb nutrient elements such as nitrogen and phosphorus in sewage, meanwhile, the constructed wetland utilizes sludge as a filler, and fully utilizes substances containing nitrogen and phosphorus in the sludge, so that waste is changed into valuable, and sludge recycling is realized. Meanwhile, the artificial landscape can be constructed, the natural combination of sewage treatment and the artificial landscape is realized, and the ecological environment protection and restoration method has positive significance.
Drawings
FIG. 1 is a schematic diagram of a surface quasi-class II potable water source water replenishing and regenerating treatment system.
FIG. 2 is a flow chart of the surface quasi-class II drinking water source water replenishing and regenerating 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 by referring to the drawings are illustrative and intended to explain the present invention and should not be construed as limiting the invention.
Example 1
As shown in figure 1, the surface quasi-class II drinking water source water supplementing and regenerating treatment system comprises an aeration sand basin 1, a biological treatment section 2, an MBR (membrane bioreactor) basin 3, a sludge concentration decomposition basin 4, an ozone generator 5, an ozone reaction basin 6, a disinfection basin 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 a filter cake generated by the sludge concentration and decomposition tank 4 is used for the constructed 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 wetland water inlet 8. 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 destroying device 61 and the ozone tail gas inlet of the MBR tank 3.
The ozone outlet of the ozone generator 5 is respectively communicated with the ozone inlets of the sludge concentration decomposition tank 4 and the ozone reaction tank 6, wherein the ozone generator takes 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 quantity of municipal sewage can be distributed, and the carbon source utilization rate in the sewage can be improved. Specifically, municipal sewage flowing out of the aeration grit chamber 1 is divided into a first part of water (flowing into the pre-anoxic zone 21), a second part of water (flowing into the anaerobic zone 22), a third part of water (flowing into the primary anoxic zone 24), and a fourth part of water (flowing into the secondary anoxic zone 26).
The municipal sewage in China has lower C/N, and the organic carbon source in the municipal sewage is insufficient to support denitrification reaction. In the existing A2/O process, in order to ensure that effluent TN reaches the standard, an additional carbon source (such as methanol or ethanol and the like) is required to be added during denitrification, so that the treatment cost is greatly increased. According to the surface quasi-class two 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 used as a carbon source for denitrification reaction to be put into the pre-anoxic zone 21, and the denitrification reaction is carried out on municipal sewage, so that the additional carbon source is reduced, the treatment cost is reduced, the obvious sludge reduction effect is achieved, the sludge treatment cost is reduced, and meanwhile, the phosphorous removal agent is added, the redundant TP is eliminated, and the biochemical phosphorous removal of the residual total phosphorous is facilitated.
According to the surface quasi-class II drinking water source water supplementing 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 performing this anoxic treatment, further denitrification reactions can be performed on the municipal wastewater to further remove inorganic nitrogen from the municipal wastewater. The aeration treatment can blow off the residual nitrogen, and simultaneously can improve the sedimentation performance of the sludge through aeration, so as to further remove organic matters.
According to the surface quasi-class II drinking water source water supplementing treatment system, the pre-anoxic zone 21 is arranged at the upstream of the anaerobic zone 22, and the sludge from the arranged secondary anoxic zone 26 to the pre-anoxic zone 21 flows back, so that the protection of the subsequent anaerobic environment is ensured, denitrification and denitrification are carried out in anoxic treatment, NO 3 -N can be effectively removed, the subsequent phosphorus release reaction can be ensured to be fully carried out, and the biochemical phosphorus removal capability can be exerted to the greatest 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 microbial extracellular polymeric organic matters adhered to the surfaces of membrane wires can be degraded, and the membrane wires can be effectively blocked by dephosphorization agents and pollutants by being matched with biological enzyme modified activated carbon aeration scrubbing, and the tail gas waste utilization is realized.
According to the invention, the residual sludge of the MBR tank 3 is subjected to ozone treatment in the sludge concentration decomposition tank, a lysis substance is used as a carbon source, the sludge is easy to dehydrate, and the sludge after press filtration contains substances such as activated carbon, alumina and the like which are easy to support and expand pores and contains rich nitrogen and phosphorus substances, so that the sludge has the functions of containing water, ventilation, fixing support and providing nutrient elements as the filler of the subsequent constructed wetland 8.
According to the treatment of the constructed wetland 8, the aim of deeply removing nitrogen and phosphorus can be achieved, meanwhile, the 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 and the aim of deeply purifying is achieved.
Therefore, the surface quasi-class II drinking water source water supplementing treatment system has the advantages of good treatment effect, low running cost and the like. The effluent can meet the requirements of the A standard in the discharge standard of water pollutants in urban sewage treatment plants (DB 11/890-2012) in table 1, and the requirements of the standard on BOD 5、COD、NH3 -N and TP are the same as the water quality standard of II-type water bodies in the quality standard of surface water environments (GB 3838-2002).
Example 2
In this embodiment, the surface quasi-class II drinking water source water supplementing treatment system sequentially comprises a coarse grid (not shown in the figure), a fine grid (not shown in the figure), an aeration grit chamber 1, a water inflow automatic control device (not shown in the figure), a biological treatment section 2, an MBR tank 3, a sludge concentration decomposition tank 4, an ozone generator 5, an ozone reaction tank 6, a disinfection tank 7 and an artificial wetland 8.
The coarse grille is positioned at the upstream of the aeration grit chamber 1, and the fine grille is positioned between the coarse grille and the aeration grit chamber 1. In other words, municipal sewage flows through the coarse grid, the fine grid, and the aeration grit chamber 1 in this order. Wherein, the net distance of the grid bars of the coarse grid is 20mm, the flow rate of the municipal sewage passing the grid is 0.8m/s, the grid gap of the fine grid is 3mm, and the flow rate of the municipal sewage passing the grid is 0.8m/s.
Municipal wastewater enters the aeration grit chamber 1 after being simply pretreated by the coarse grille and the fine grille, and most inorganic particles in the municipal wastewater can be removed by carrying out aeration grit on the municipal wastewater, and organic matters adhered to the inorganic particles can enter the municipal wastewater, so that the organic carbon source content in the municipal wastewater can be improved. Wherein the hydraulic retention time of the aeration grit chamber 1 is 8 minutes.
Advantageously, the surface quasi-class two-drinking water source water supplementing and regenerating 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 the subsequent enhancement of biological denitrification and dephosphorization.
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 inflow automatic control device is a flow monitoring and adjusting device arranged among the water outlet of the aeration 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. Therefore, the municipal sewage can be split, and the utilization rate of the organic carbon source in the municipal sewage can be improved.
Wherein municipal wastewater is split into a first portion of effluent flowing into pre-anoxic zone 21, a second portion of effluent flowing into anaerobic zone 22, a third portion of effluent flowing into primary anoxic zone 24, and a fourth portion of effluent flowing into secondary anoxic zone 26. That is, the municipal sewage advanced treatment regeneration recycling system adopts a multi-point water inlet mode. The volume percentage of the first part of water outlet is 10% -30%, the volume percentage of the second part of water outlet is 30% -50%, the volume percentage of the third part of water outlet is 30% -50%, the volume percentage of the fourth part of water outlet is about 10%, and the water inlet automatic control device can automatically adjust the volume percentages of the first part of water outlet, the second part of water outlet, the third part of water outlet and the fourth part of water outlet according to the total water inlet amount, so that the water inlet flow distribution is more flexible and accurate. 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 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 sequentially connected. 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 dephosphorization and denitrification reaction tank consisting of an independent and separately controllable 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 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 technology, a large amount of NO 3 -N is carried by sludge discharged from a sedimentation tank (namely return sludge) to directly return to an anaerobic zone, so that the phosphorus release effect of the anaerobic zone is seriously affected, and the phosphorus removal capacity of the anaerobic zone is severely 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 lysis substance as the carbon source to strengthen the denitrification effect. Advantageously, the return sludge has a sludge return ratio of 200% -400%. Meanwhile, the dephosphorization reagent is added, part of TP is removed, the C/P ratio of the whole system is improved, and dephosphorization is facilitated. Advantageously, the dephosphorization 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 mixes with a second portion of the effluent. Within the anaerobic zone 22, the first portion of effluent and the second portion of effluent are subjected to anaerobic treatment for phosphorus release reactions. By adding new municipal sewage, i.e., municipal sewage which has not been subjected to anoxic treatment, when 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 after anaerobic treatment, the second part of effluent and MBR pool reflux sludge enter a primary aerobic zone 23 for nitration reaction to remove ammonia nitrogen and absorb sludge TP, preferably, the dissolved oxygen is 0.5-3 mg/L, and the sludge concentration is 3500-5000 mg/L.
After the primary aerobic zone 23 is treated, the first part of effluent and the second part of effluent treatment liquid enter a primary anoxic zone and are mixed with the third part of effluent, the third part of effluent is utilized to bring carbon sources in raw water in the primary anoxic zone 24, and the first part of effluent and the second part of effluent are subjected to nitrate nitrogen denitrification to be removed. Preferably, the concentration of the reaction sludge is 3500 mg/L-5000 mg/L, and the reflux ratio of the MBR tank 3 to the primary aerobic tank is 300% -500%.
After the first-stage anoxic zone 24 reacts, the first part of effluent, the second part of effluent and the third part of effluent enter the second-stage anoxic zone 25, the nitrification reaction and phosphorus absorption are continued, and the residual ammonia nitrogen in the first part of effluent and the second part of effluent and the ammonia nitrogen generated by the third part of effluent are removed, preferably, the required dissolved oxygen is 0.5-3 mg/L, and the sludge concentration is 3500-5000 mg/L.
And then, carrying out 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 carbon. Simultaneously, the input amount of the external carbon source is timely adjusted according to the requirement, the input amount/removed nitrate nitrogen of the external carbon source is 4:1-8:1, and the sludge concentration is 3500-5000 mg/L.
After the treatment of the secondary anoxic zone 26, the mixed liquid of the effluent water of the first part, the effluent water of the second part, the effluent water of the third part and the effluent water of the fourth part enters the MBR tank 3, and under the aeration condition, residual ammonia nitrogen is removed to reach the standard, and meanwhile, the biological activated carbon is added to remove deep degradation-resistant organic matters to reach the standard, so that COD reaches the standard.
And (3) introducing the tail gas of the ozone reaction tank into the MBR tank 3 to act together with the biological enzyme modified activated carbon, removing organic matters adhered to the surface of the membrane wires, and delaying the fouling degree of the membrane wires. And meanwhile, ozone reacts with organic matters in the activated carbon to recover the adsorption performance of the biological enzyme modified activated carbon. Ozone breaks the hard-to-degrade organic matters into smaller organic matters which are easy to decompose, and the COD removing capacity is enhanced.
Preferably, the biological enzyme modified activated carbon is powdered activated carbon with the particle size of 10-100 mu m and the adding dosage of the biological enzyme modified activated carbon is 20-40 mg/L. In the MBR tank, the ozone tail gas dosage is 5-10 mg/L, the sludge concentration is 6000-12000 mg/L, and the sludge age is 10-25 d.
The MBR excess sludge enters a sludge concentration decomposition tank 4, ozone is introduced into the sludge concentration decomposition tank by an ozone generator 5 to carry out decomposition reaction, and preferably, the ozone is added with the concentration of 0.01-0.2 g O3/gVSS. The water content after dehydration is less than 80 percent, and the sludge is used as the artificial wetland filler after being detected to be qualified. The extracellular dissolution liquid enters the pre-anoxic tank 21.
The effluent of the MBR tank 3 enters an ozone reaction tank 6, a catalyst filler is arranged in the ozone reaction tank 6, the filtering speed is set to be 3-6 m/h, the ozone adding amount is 20-30 mg/L, and the residence time is 1-2 h. Preferably, the mass ratio of ozone addition amount to COD removal 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 residence time is 4-8 h. The concentration of the sodium hypochlorite is 5-10 mg/L.
The water discharged from the disinfection tank 7 enters the artificial wetland 8, the hydraulic load of the artificial wetland is checked to be 0.45m 3/m2 d, the total hydraulic retention time is 3.1d, and the plants such as reed, typha, iris coreana and arundo donax are selected, and have developed root systems, strong pollution resistance and strong decontamination capability and are suitable for local environments.
Table 1-quality of incoming water and quality of outgoing water of quasi-two-class drinking water source make-up water regeneration treatment system.
| Project | CODcr | BOD5 | SS | TN | NH3-N | TP | Coli-like |
| Water quality of water inlet (mg/L) | 400 | 250 | 300 | 50 | 35 | 6.5 | 2000 |
| Water quality of outlet water (mg/L) | 15 | 3 | 5 | 10 | 0.5 | 0.1 | --- |
Example 3
As shown in fig. 2, the method for regenerating and treating the surface quasi-class II drinking water source comprises the following steps:
a) Municipal wastewater passes through the coarse grid and the fine grid and is subjected to aeration sand setting. 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 to on the inorganic granule get into municipal sewage moreover to can improve the organic carbon source content in the municipal sewage.
B) The water is discharged from the membrane grid after aeration sand setting, and is respectively discharged from the first part, the second part, the third part and the fourth part. In the pre-anoxic zone 21, the first part of effluent is mixed with the return sludge of the secondary aerobic zone 25 to perform denitrification and denitrification, and meanwhile, a dephosphorization reagent is added to remove phosphorus.
C) In the anaerobic zone 22, the treated first portion of the effluent is mixed with the second portion of the effluent for anaerobic phosphorus release.
D) In the first-stage aerobic zone, the treated first part of effluent, the treated second part of effluent and the return sludge of the MBR tank 3 are mixed, aerobic nitrification reaction is carried out to remove ammonia nitrogen, and meanwhile, aerobic phosphorus absorption is carried out, so that the total phosphorus is transferred from liquid to sludge.
E) In the primary anoxic zone 24, the treated first portion of effluent, the treated second portion of effluent, and the third portion of effluent are mixed and denitrification continues to remove total nitrogen.
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 to continue ammonia nitrogen removal and deep phosphorus removal.
G) In the secondary anoxic zone 26, the treated first portion of effluent, the treated second portion of effluent, the treated third portion of effluent, and the fourth portion of effluent are mixed and then fed with an external carbon source for deep denitrification.
H) In the MBR tank 3, 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 are mixed, biological enzyme modified activated carbon is added into the MBR tank 3 for removing refractory organic matters, SS is removed through membrane filtration, residual phosphorus-containing sludge is discharged, finally ozone is added into the MBR tank 3, membrane silk blockage is reduced, and the adsorption capacity of the biological enzyme modified activated carbon is recovered.
I) The ozone reaction tank 6 further removes refractory organic matters under the action of a catalyst, so that COD reaches the standard, redundant tail gas after reaction is treated by the ozone tail gas destruction device 61, and the rest of the tail gas is introduced into the MBR tank 3.
J) The effluent treated by the ozone reaction tank enters a disinfection tank 7 for disinfection, and bacteria such as escherichia coli and the like are killed, so that the effluent fungus is qualified.
K) In the constructed wetland 8, residual sludge in the MBR tank 3 is subjected to ozone oxidation treatment, and then is subjected to concentration, pressure filtration and the like to generate qualified mud cakes as wetland fillers, wherein the first part of effluent, the second part of effluent, the third part of effluent and the fourth part of effluent are intercepted, residual SS is continuously absorbed by nitrogen, phosphorus and the like, and the water quality is purified.
Compared with the traditional six-stage method-ultrafiltration process, the system has the following advantages:
Firstly, adding a proper amount of biological enzyme modified activated carbon into a membrane tank, and establishing a new symbiotic system by the biological enzyme modified activated carbon and activated sludge, wherein the biological enzyme modified activated carbon and the activated sludge are mutually promoted, so that the membrane tank has stronger removal capacity compared with the traditional process. 1) the activated sludge has higher concentration than biological enzyme modified activated carbon, firstly, the organic matters which are easy to degrade are decomposed to complete various functional metabolism (such as denitrification and dephosphorization and microorganism growth), 2) the subsequent organic matters which are difficult to degrade gradually diffuse into the biological enzyme-activated carbon to continue to carry out the special degradation along with the gradual progress of the reaction, the pre-degradation of the activated sludge provides conditions for the special degradation of the biological enzyme modified activated carbon, the agent is saved, the biological enzyme modified activated carbon can deeply remove the organic matters, inhibit aerobic heterotrophic bacteria and promote nitrifying bacteria to grow, and facilitate ammonia nitrogen removal, and 3) the organic matters which are difficult to degrade are subjected to the dynamic balance process of adsorption, degradation and adsorption in the biological enzyme-activated carbon system, so that the removal capacity of the organic matters which are difficult to degrade is improved, and the synergistic effect is achieved.
And secondly, a proper amount of tail gas of 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 wire on organic matters such as extracellular polymers and the like is enhanced, the viscosity of the organic matters is reduced, and the anti-fouling capacity of the membrane wire is greatly improved. Meanwhile, under the combined action of a proper amount of active carbon scouring, the membrane silk fouling degree is reduced, and the ozone is input to degrade organic matters adsorbed in the active carbon, so that the recovery capability of the active carbon is improved.
Thirdly, the residual sludge is subjected to ozone treatment, the cell walls of the sludge are damaged, partial sludge lysate is used as a denitrification carbon source, the carbon source is saved, the sludge is easier to filter-press and dewater after the ozone treatment, the sludge reduction is obvious, and meanwhile, bacteria and heavy metals are subjected to oxidation harmless treatment by ozone.
Fourth, the formed filter cake contains rich elements such as nitrogen and phosphorus, the property of the sludge can be changed by the aluminum salt added in dehydration, a porous structure is formed, the sludge cake is used for the constructed wetland 8, waste is changed into valuable, and sludge recycling is realized.
Fifth, the utilization rate of the organic carbon source of the raw water can be improved by water inlet in a sectional manner.
Sixthly, the anaerobic treatment is carried out in advance, the denitrification capability of nitrate is improved, and a good anaerobic environment is ensured.
Therefore, the drinking water source water supplementing treatment method based on the surface quasi-class two-water quality standard has the advantages of good treatment effect, low running cost and the like. The municipal sewage is treated by the method for supplementing the drinking water source based on the surface quasi-two-class water quality standard, so that the effluent meets the requirement of the A standard in the table 1 of the discharge standard of water pollutants in urban sewage treatment plants (DB 11/890-2012), and the requirements of the standard on BOD 5、COD、NH3 -N and TP are the same as the water quality standard of II-class water bodies of the surface water environment standard (GB 3838-2002).
Specific examples are set forth herein to illustrate the invention in detail, and the description of the above examples is only for the purpose of aiding in understanding the core concept of the invention. It should be noted that any obvious modifications, equivalents, or other improvements to those skilled in the art without departing from the inventive concept are intended to be included in the scope of the present invention.
Claims (7)
1. The surface quasi-class II drinking water source water supplementing and regenerating treatment system is characterized by comprising an aeration sand basin, a biological treatment section, an MBR (membrane bioreactor) basin, a sludge concentration and decomposition basin, an ozone generator, an ozone tail gas destruction device, an ozone reaction basin, a disinfection basin 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 a water inlet of the primary anoxic zone and a water inlet of 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 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 sludge return inlet of the primary aerobic zone, the residual sludge outlet of the MBR tank is communicated with the sludge concentration decomposition tank, and biological enzyme modified activated carbon is added into the MBR tank;
the sludge lysate outlet of the sludge concentration decomposition tank is communicated with the pre-anoxic zone, and a filter cake generated by residual sludge of the MBR tank is used for artificial wetland filler;
The ozone generator comprises a sludge concentration decomposition tank, an ozone reaction tank water inlet, an ozone reaction tank water outlet, a disinfection tank, an ozone reaction tank tail gas and an ozone tail gas destruction device, wherein the ozone outlet of the ozone generator is respectively communicated with the sludge concentration decomposition tank and the ozone reaction 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 constructed wetland, and a filter cake obtained by dewatering and filter pressing sludge is used as a filler of the constructed wetland;
The water outlet of the aeration grit chamber is respectively communicated with 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, and the water outlet of the secondary aerobic zone is communicated with the water inlet of the pre-anoxic zone;
The aeration sand setting device further comprises a coarse grid, a fine grid and a membrane grid, wherein the coarse grid is positioned at the upstream of the aeration sand setting tank, the fine grid is positioned between the coarse grid and the aeration sand setting tank, and the membrane grid is positioned at the downstream of the aeration sand setting tank.
2. The surface quasi-class II drinking water source moisturizing regeneration treatment system according to claim 1, wherein the surface quasi-class II drinking water source moisturizing regeneration treatment system comprises a water inflow automatic control device, a water inlet of the water inflow automatic control device is communicated with a water outlet of the aeration grit chamber, and a water outlet of the water inflow 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.
3. The surface quasi-class II drinking water source water supplementing and regenerating treatment system according to claim 1, wherein the system comprises an ozone reaction tank, and COD catalytic oxidation filler is arranged in the ozone reaction tank.
4. A surface quasi-class II drinking water source water supplementing and regenerating treatment method is characterized by comprising the following steps:
A) Raw water passes through the coarse grille and the fine grille and enters an aeration sand basin;
B) The first part of water is mixed with the return sludge of the second-stage aerobic zone and lysate in the pre-anoxic zone to carry out denitrification and denitrification, and meanwhile, a dephosphorization reagent is added to carry out dephosphorization;
C) Mixing the treated first part of effluent with the treated second part of effluent in an anaerobic zone to perform anaerobic phosphorus release;
D) In the first-stage aerobic zone, the treated first part of effluent, the treated second part of effluent and the return sludge of the MBR pool are mixed to perform aerobic nitration reaction, so as to remove ammonia nitrogen;
E) In the primary anoxic zone, mixing the treated first partial effluent, the treated second partial effluent and the treated third partial effluent, and continuing denitrification to remove total nitrogen;
F) In the second-stage aerobic zone, mixing the treated first part of effluent with the treated second part of effluent and the treated third part of effluent, and continuing ammonia nitrogen removal;
J) 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 treated 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 residual phosphorus-containing sludge, and finally adding ozone into the MBR tank;
i) Adding an obligate COD catalyst into an ozone reaction tank, and treating the residual ozone after the reaction in the ozone reaction tank by an ozone tail gas destruction device;
J) The effluent treated by the ozone reaction tank enters a disinfection tank for disinfection;
K) And performing ozone oxidation and concentration on the residual sludge in the MBR tank, and finally press-filtering to form a mud cake as a wetland filler.
5. The method for supplementing and regenerating the surface quasi-class II drinking water source according to claim 4, wherein in the step B), the mass percentage of the first part of water is 10% -30%, the mass percentage of the second part of water is 30% -50%, the mass percentage of the third part of water is 30% -50%, and the mass percentage of the fourth part of water is 10%.
6. The method for regenerating and treating the surface quasi-secondary drinking water source according to claim 4, wherein in the step H), the reflux ratio of the sludge from the MBR pool to the primary aerobic zone is 300% -500%, the reflux ratio of the mixed liquid from the secondary aerobic zone to the pre-anoxic zone is 200% -400%, the bio-enzyme modified activated carbon of the MBR pool is powdery activated carbon with bio-enzyme loaded in pores, the particle size is 10 mu m-100 mu m, and the adding dosage of the bio-enzyme modified activated carbon is 20 mg/L-40 mg/L.
7. The method for regenerating and treating the surface quasi-class II drinking water source according to claim 4 is characterized in that in the ozone reaction tank in the step I), the mass ratio of ozone addition amount to COD removal is 3:1-1:1, the ozone tail gas addition amount in the MBR tank is 5-10 mg/L, and the ozone addition amount of residual sludge tail gas is 0.01-0.2 g O 3/g VSS.
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| 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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| 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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