CN212315842U - Tail water advanced treatment device - Google Patents
Tail water advanced treatment device Download PDFInfo
- Publication number
- CN212315842U CN212315842U CN202020342403.5U CN202020342403U CN212315842U CN 212315842 U CN212315842 U CN 212315842U CN 202020342403 U CN202020342403 U CN 202020342403U CN 212315842 U CN212315842 U CN 212315842U
- Authority
- CN
- China
- Prior art keywords
- water
- outlet
- sludge
- communicated
- sewage treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The utility model relates to a sewage treatment technical field, concretely relates to tail water advanced treatment unit. The utility model provides a tail water deep treatment device, which comprises a sewage treatment device, an ammonia recovery device, a phosphorus recovery device, a denitration device, a backwashing filter device and a disinfection device which are sequentially communicated; the sewage treatment device is characterized by also comprising a residual sludge liquefying device, wherein a sewage outlet of the sewage treatment device is communicated with a feed inlet of the residual sludge liquefying device; and the liquid outlet of the residual sludge liquefying device is communicated with the water inlet of the sewage treatment device. The utility model discloses an excess sludge liquefaction device carries out hydrolytic acidification with sewage treatment plant exhaust excess sludge, retrieves as the carbon source, has compensatied the not enough shortcoming of village and town sewage carbon source. Adopt the utility model provides a tail water advanced treatment unit can carry out automatic high-efficient denitration, denitrogenation and dephosphorization to the tail water, retrieves nitrogen phosphorus resource, obtains the drainage of treating that accords with the accurate IV class water standard in earth's surface.
Description
Technical Field
The utility model relates to a sewage treatment technical field, concretely relates to tail water advanced treatment unit.
Background
The prior dispersed village and town sewage treatment process mainly comprises an oxidation ditch, SBR and A/O, A2O or "A/O, A2The technology of/O + MBR is mainly, and the problem of low C/N of inlet water generally exists. The nitrogen and phosphorus removal effect of the sewage treatment facility in the villages and towns is poor due to insufficient carbon source of inlet water, and medicaments such as carbon source, PAC and the like are usually required to be continuously added to improve the nitrogen and phosphorus removal effect, so that the cost is high; and the use of phosphorus removing agents such as PAC can cause the problems of large mud production yield and the like.
Aiming at the problems of low C/N of inlet water and low nitrogen and phosphorus removal efficiency of sewage treatment facilities in villages and towns, Chinese patents CN209259896U and CN108101222A advocate that the artificial wetland is used for carrying out advanced treatment on tail water after sewage treatment in villages and towns, but the artificial wetland advanced treatment method has the disadvantages of large occupied area, easy blockage and inconvenient maintenance and management.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a tail water advanced treatment unit, the utility model provides a tail water advanced treatment unit reasonable in design, the structure is simple and convenient, can directly insert current villages and towns sewage treatment facility, need not to throw and adds medicaments such as carbon source and dephosphorization agent, and the operation cost is lower.
In order to realize the purpose of the utility model, the utility model provides a following technical scheme:
the utility model provides a tail water advanced treatment device, include
A sewage treatment device 2;
the water inlet of the ammonia recovery device 3 is communicated with the water outlet of the sewage treatment device 2;
a phosphorus recovery device 4 with a water inlet communicated with the water outlet of the ammonia recovery device 3;
a denitration device 5 with a water inlet communicated with the water outlet of the phosphorus recovery device 4;
a back washing filter device 6 with a water inlet communicated with the water outlet of the denitration device 5;
the water inlet of the sterilizing device 7 is communicated with the backwashing filter device 6;
the device also comprises a residual sludge liquefying device 1, wherein a sewage outlet of the sewage treatment device 2 is communicated with a feed inlet of the residual sludge liquefying device 1; and the liquid outlet of the excess sludge liquefying device 1 is communicated with the water inlet of the sewage treatment device 2.
Preferably, the sewage treatment device 2 comprises a grid 2-1, a denitrification regulating tank 2-2, a biochemical reaction tank 2-3 and a filtering tank 2-4 which are communicated in sequence; the denitrification adjusting tank 2-2 is provided with a first sludge outlet, the biochemical reaction tank 2-3 is provided with a second sludge outlet, the filter tank 2-4 is provided with a third sludge outlet, and the first sludge outlet, the second sludge outlet and the third sludge outlet are independently communicated with a feed inlet of the sludge concentration tank 2-5; and the sewage outlet of the sludge concentration tank 2-5 is communicated with the feed inlet of the residual sludge liquefying device 1.
Preferably, the device also comprises a compound fertilizer recovery device 9, wherein the ammonia recovery device 3 is provided with a first regenerated waste liquid outlet, the phosphorus recovery device 4 is provided with a second regenerated waste liquid outlet, and the first regenerated waste liquid outlet and the second regenerated waste liquid outlet are independently communicated with a feed inlet of the compound fertilizer recovery device 9.
Preferably, the ammonia recovery device 3 is provided with a first backwash waste liquid outlet, the phosphorus recovery device 4 is provided with a second backwash waste liquid outlet, and the first backwash waste liquid outlet and the second backwash waste liquid outlet are independently communicated with the feed inlet of the residual sludge liquefaction device 1.
Preferably, the denitration device 5 is provided with a third backwash waste liquid outlet, and the third backwash waste liquid outlet is communicated with the water inlet of the sewage treatment device 2.
Preferably, the backwashing filter device 6 is provided with a fourth backwashing waste liquid outlet, and the fourth backwashing waste liquid outlet is communicated with the feed inlet of the residual sludge liquefaction device 1.
The utility model provides a tail water deep treatment device, a sewage treatment device 2; the water inlet of the ammonia recovery device 3 is communicated with the water outlet of the sewage treatment device 2; a phosphorus recovery device 4 with a water inlet communicated with the water outlet of the ammonia recovery device 3; a denitration device 5 with a water inlet communicated with the water outlet of the phosphorus recovery device 4; a back washing filter device 6 with a water inlet communicated with the water outlet of the denitration device 5; the water inlet of the sterilizing device 7 is communicated with the backwashing filter device 6; the device also comprises a residual sludge liquefying device 1, wherein a sewage outlet of the sewage treatment device 2 is communicated with a feed inlet of the residual sludge liquefying device 1; and the liquid outlet of the excess sludge liquefying device 1 is communicated with the water inlet of the sewage treatment device 2. The utility model carries out hydrolysis and acidification on the excess sludge discharged by the sewage treatment device 2 through the excess sludge liquefaction device 1, and recovers the excess sludge as a carbon source, thereby overcoming the defect of insufficient carbon source of sewage in villages and towns; the hydrolysate obtained after hydrolytic acidification is introduced into the sewage treatment device 2, so that the nitrogen and phosphorus removal capability of the original sewage treatment device is enhanced, the sludge yield is reduced, and the near zero emission of the sludge is realized; the device provided by the utility model does not need to add extra carbon source, PAC and other medicaments, reduces the sludge yield, simplifies the operation, reduces the operation cost and realizes remote control and unattended operation; adopt the utility model provides a tail water advanced treatment unit can carry out high-efficient denitration, denitrogenation and dephosphorization and retrieve the nitrogen phosphorus resource to the tail water, obtains the drainage of treating that accords with the accurate IV class water standard in earth's surface.
Drawings
Fig. 1 is a schematic view of a tail water deep treatment device provided by an embodiment of the present invention; wherein 1 is a residual sludge liquefying device, 2 is a sewage treatment device, 3 is an ammonia recovering device, 4 is a phosphorus recovering device, 5 is a denitration device, 6 is a back washing filtering device, 7 is a sterilizing device, 8 is a discharge port, and 9 is a compound fertilizer recovering device;
FIG. 2 is a schematic view of the sewage treatment apparatus 2; wherein 2-1 is a grating, 2-2 is a denitrification adjusting tank, 2-3 is a biochemical reaction tank, 2-4 is a filter tank, and 2-5 is a sludge concentration tank.
Detailed Description
The utility model provides a tail water advanced treatment unit, include:
a sewage treatment device 2;
the water inlet of the ammonia recovery device 3 is communicated with the water outlet of the sewage treatment device 2;
a phosphorus recovery device 4 with a water inlet communicated with the water outlet of the ammonia recovery device 3;
a denitration device 5 with a water inlet communicated with the water outlet of the phosphorus recovery device 4;
a back washing filter device 6 with a water inlet communicated with the water outlet of the denitration device 5;
the water inlet of the sterilizing device 7 is communicated with the backwashing filter device 6;
the device also comprises a residual sludge liquefying device 1, wherein a sewage outlet of the sewage treatment device 2 is communicated with a feed inlet of the residual sludge liquefying device 1; and the liquid outlet of the excess sludge liquefying device 1 is communicated with the water inlet of the sewage treatment device 2.
The utility model provides a tail water advanced treatment unit includes sewage treatment plant 2, belongs to conventional biochemical treatment. The utility model discloses in, sewage treatment plant 2 includes SBR integration sewage treatment device or MBR integration sewage treatment device etc..
As an embodiment of the utility model, the sewage treatment device 2 comprises a grid 2-1, a denitrification adjusting tank 2-2, a biochemical reaction tank 2-3 and a filtering tank 2-4 which are communicated in sequence; the denitrification adjusting tank 2-2 is provided with a first sludge outlet, the biochemical reaction tank 2-3 is provided with a second sludge outlet, the filter tank 2-4 is provided with a third sludge outlet, and the first sludge outlet, the second sludge outlet and the third sludge outlet are independently communicated with a feed inlet of the sludge concentration tank 2-5; and the sewage outlet of the sludge concentration tank 2-5 is communicated with the feed inlet of the residual sludge liquefying device 1. The utility model discloses it does not have special limited to right the concrete structure of grid 2-1, denitrification equalizing basin 2-2, biochemical reaction pond 2-3, filtering ponds 2-4 and sludge concentration pond 2-5, adopt grid, denitrification equalizing basin, biochemical reaction pond, filtering ponds and sludge concentration pond that technical personnel in the field are familiar with can.
In the embodiment of the present invention, the filtration tank 2-4 comprises an MBR membrane filtration tank or a sedimentation tank.
In the embodiment of the present invention, the denitrification regulating tank 2-2 is used for denitrification. As an embodiment of the utility model, denitrification equalizing basin 2-2 is reformed transform by the equalizing basin and is formed, increases aeration head, corridor or agitator on the basis of former equalizing basin to promote surplus sludge liquefaction device 1 exhaust hydrolysis liquid and sewage misce bene, improve denitrification efficiency. The utility model discloses it is right the concrete structure of aeration head, corridor and agitator does not have special restriction, adopt aeration head, corridor and agitator that technical personnel in the field are familiar with can. In the utility model, the Total Nitrogen (TN) load of the denitrification regulating tank 2-2 is preferably 0.3-0.6 kg/(m)3·d)。
The tail water deep treatment device provided by the utility model also comprises an excess sludge liquefaction device 1, wherein the drain outlet of the sewage treatment device 2 is communicated with the feed inlet of the excess sludge liquefaction device 1; and the liquid outlet of the excess sludge liquefying device 1 is communicated with the water inlet of the sewage treatment device 2. In the embodiment of the present invention, the liquid outlet of the excess sludge liquefaction device 1 is communicated with the denitrification regulating reservoir 2-2 to improve the denitrification efficiency in the denitrification regulating reservoir. The utility model utilizes the excess sludge liquefying device 1 to hydrolyze and acidify the excess sludge discharged by the sewage treatment device 2, and the excess sludge is recovered as a carbon source to make up the defect of insufficient carbon source of the sewage in villages and towns; and introducing the hydrolysate obtained after hydrolysis acidification into a sewage treatment device for backflow, so that the nitrogen and phosphorus removal capability of the sewage treatment device 2 is enhanced, the sludge yield is reduced, and near zero emission of sludge is realized. As an embodiment of the utility model, the excess sludge liquefaction device 1 is a micro-aerobic sludge hydrolysis acidification device, and the intermittent aeration mode is adopted for operation, the utility model discloses it is right the concrete technology of intermittent aeration does not have special restriction to keep DO <0.15mg/L, Hydraulic Retention Time (HRT) >20h is suitable. In the embodiment of the present invention, the intermittent aeration frequency is 10-15 min per 2h of aeration.
The utility model provides a tail water advanced treatment unit include the water inlet with the ammonia recovery unit 3 that sewage treatment plant 2's delivery port is linked together for degree of depth denitrogenation. In the embodiment of the present invention, the ammonia recovery device 3 is filled with an ammonia recovery filler, and the ammonia recovery filler is preferably a selective cation exchange resin, and more preferably an ammonium selective Na type cation exchange resin. In a specific embodiment of the present invention, the selective cation exchange resin is soaked in 5-10 wt.% sodium chloride solution for regeneration, so as to realize recycling; the soaking time is preferably 2 hours.
As an embodiment of the present invention, the ammonia recovery device 3 has an automatic backwashing part and a regeneration part; the back washing part is a long-handle filter head gas and water distribution system or a filter brick gas and water distribution system, and is arranged at the bottom of the ammonia recovery filler; the regeneration part comprises a water pump for conveying sodium chloride regeneration liquid, a water pipe and a medicine inlet. The ammonia recovery device 3 is provided with a first backwashing waste liquid outlet which is communicated with the feed inlet of the residual sludge liquefaction device 1, and carbon sources in waste liquid are recycled.
The utility model provides a tail water advanced treatment unit include the water inlet with the phosphorus recovery unit 4 that the delivery port of ammonia recovery unit 3 is linked together for degree of depth dephosphorization. In the utility model, the phosphorus recovery device 4 is filled with phosphorus recovery filler, and the phosphorus recovery filler is preferably selective anion exchange resin or iron-based modified adsorption filter material; the selective anion exchange resin is preferably a phosphate selective anion exchange resin; the iron-based modified adsorption filter material is preferably iron-based modified activated carbon, iron-based modified hydrotalcite or modified layered iron oxide; the modification method is preferably chemical soaking or burning. In a specific embodiment of the present invention, when the total phosphorus concentration of the tail water is >3mg/L, selective anion exchange resin is used as a phosphorus recovery packing; when the total phosphorus concentration of the tail water is below 5mg/L, an iron-based modified adsorption filter material is used as a phosphorus recovery filler; when the total phosphorus concentration of the sewage is 3-5 mg/L, the selective anion exchange resin or the iron-based modified adsorption filter material is adopted as the phosphorus recovery filler. In a specific embodiment of the present invention, the selective anion exchange resin and the iron-based modified adsorbent filter material are periodically regenerated; the regeneration method of the selective anion exchange resin is preferably to perform soaking regeneration by adopting 5-10 wt.% of sodium hydroxide solution, and the soaking time is preferably 2 hours; the regeneration method of the iron-based modified adsorption filter material is preferably to soak and regenerate the iron-based modified adsorption filter material by adopting 5-10 wt.% of sodium hydroxide solution; the soaking time is preferably 2 hours.
As an embodiment of the present invention, the phosphorus recovery device 4 has an automatic back-washing part and a regeneration part; the back washing part is a long-handle filter head gas and water distribution system or a filter brick gas and water distribution system, and is arranged at the bottom of the phosphorus recovery filler; the regeneration part comprises a water pump for conveying sodium chloride regeneration liquid, a water pipe and a medicine inlet. The phosphorus recovery device 4 is provided with a second backwashing waste liquid outlet which is communicated with the feed inlet of the residual sludge liquefaction device 1, and carbon sources in waste liquid are recycled.
As an embodiment of the utility model, the utility model provides an end water advanced treatment unit still includes compound fertilizer recovery unit 9, ammonia recovery unit 3 is provided with first regeneration waste liquid export, phosphorus recovery unit 4 is provided with second regeneration waste liquid export, first regeneration waste liquid export and second regeneration waste liquid export independently with compound fertilizer recovery unit 9's feed inlet is linked together for retrieve the recycle to the regeneration waste liquid.
The utility model provides a tail water advanced treatment unit include the water inlet with denitrification facility 5 that the delivery port of phosphorus recovery unit 4 is linked together for high-efficient denitration. In the embodiment of the present invention, the nitrate Nitrogen (NO) is fed into the denitration device 53Concentration of-N)>When the concentration is 20mg/L, adopting a sulfur simple substance self-reduction denitrification mode for denitration; when water is fed into the denitration device 53When the concentration of N is less than 25mg/L, selective anion exchange resin is adopted for adsorption denitration; when nitrate Nitrogen (NO)3and-N) when the concentration is 20-25 mg/L, adopting a sulfur simple substance self-reduction denitrification mode for denitration or selective anion exchange resin for adsorption denitration. In the utility model, when the denitration is carried out by adopting the sulfur simple substance self-reduction denitrification mode, the inside of the denitration device 5 is filled with sulfur filler and sulfur autotrophic bacteria attached to the sulfur filler; the sulfur filler is preferably a combined filler of elemental sulfur and limestone particles, the particle size of the elemental sulfur is preferably 5-15 mm, the particle size of the limestone particles is preferably 10-20 mm, and the mass ratio of the elemental sulfur to the limestone particles is preferably 2: 1-1: 1; the utility model discloses in, preferably 3 ~ 6 months carry out the regular replenishment or the change of sulphur packing.
The utility model discloses under sulphur simple substance and sulphur autotrophy fungus effect or ion exchange resin adsorption, carry out high-efficient denitration treatment. In the present invention, the selective anion exchange resin is preferably a nitrate selective anion exchange resin.
As an embodiment of the present invention, the denitration device 5 includes a back-washing kit, and can perform automatic back-washing according to a set program; the backwashing matching component is a conventional long-handle filter head gas and water distribution system or a filter brick gas and water distribution system in the field and is arranged at the bottom of a packing layer of the denitration device 5; the back flushing gas amount is preferably 3-5L/(m)2S) preferably 2 to 3L/(m) of water2S), frequencyPreferably 1 time per week. As an embodiment of the present invention, the denitration device 5 is provided with a third back-washing waste liquid outlet, which is communicated with the water inlet of the denitrification regulating tank 2-2 of the sewage treatment device 2, so as to circularly treat the waste water. In the utility model, the back washing waste liquid discharged from the denitration device 5 mainly contains dead sulfur autotrophic bacteria, suspended pollutants and the like; work as denitrification facility 5 stops normal play water when carrying out the back flush, if keep going out water in succession, adopts two sets of adsorption columns intermittent operation's mode in turn, the utility model discloses an in the embodiment adopt two sets of adsorption columns intermittent operation in turn to go on.
The utility model discloses under the condition of not throwing the feeder carbon source, utilize sulphur autotrophy fungus, high-efficient ion exchange resin etc. to realize the resource recovery who degree of depth nitrogen and phosphorus removal and nitrogen phosphorus.
The utility model provides a tail water advanced treatment unit include the water inlet with back flush filter equipment 6 that denitrification facility 5's delivery port is linked together for the Suspended Solid (SS) in filtration detaching aquatic. As an embodiment of the present invention, the backwashing filter 6 is preferably a quartz sand filter; the particle size of the quartz sand is preferably 0.3-3.5 mm.
As an embodiment of the present invention, the backwashing filter device 6 is preferably an automatic backwashing filter device, and can perform automatic backwashing according to a set program, so as to improve the degree of automation; the back flushing gas amount is preferably 5-7L/(m)2S) and the amount of water is preferably 4 to 10L/(m)2S), the frequency is preferably 1 time of automatic back flushing every 1-2 weeks. As an embodiment of the utility model, back flush filter equipment 6 is provided with fourth back flush waste liquid delivery port, fourth back flush waste liquid delivery port with excess sludge liquefaction device 1's feed inlet is linked together, the carbon source in the recycle waste liquid. The utility model discloses in, the back flush waste liquid of back flush filter equipment 6 exhaust is mainly attached to the biomembrane on the quartz sand packs and holds back suspended solid and tiny granule between the quartz sand packs.
The utility model provides a tail water advanced treatment unit include the water inlet with degassing unit 7 that back flush filter equipment 6 is linked together carries out disinfection. The present invention is not limited to the disinfection device 7, and a disinfection device 7 known to those skilled in the art may be used.
As an embodiment of the utility model, the tail water deep treatment device provided by the utility model also comprises a discharge port 8 connected with the water outlet of the disinfection device 7, and the tail water after treatment is discharged. In a particular embodiment of the invention, the discharge opening 8 is provided with a pasteurisation tank for recording the amount of water treated by the treatment device.
As an embodiment of the present invention, the schematic diagram of the tail water deep treatment device provided by the present invention is shown in fig. 1, and includes a residual sludge liquefaction device 1, a sewage treatment device 2, an ammonia recovery device 3, a phosphorus recovery device 4, a denitration device 5, an automatic backwashing filter device 6, a disinfection device 7, a discharge port 8 and a compound fertilizer recovery device 9; wherein, the liquid outlet of the excess sludge liquefying device 1 is communicated with the water inlet of the sewage treatment device 2; the water outlet of the sewage treatment device 2 is communicated with the water inlet of the ammonia recovery device 3, and the water outlet of the ammonia recovery device 3 is communicated with the water inlet of the phosphorus recovery device 4; the regeneration waste liquid outlets of the ammonia recovery device 3 and the phosphorus recovery device 4 are communicated with the feed inlet of the compound fertilizer recovery device 9, and the backwashing waste liquid outlets of the ammonia recovery device 3 and the phosphorus recovery device 4 are communicated with the feed inlet of the residual sludge liquefaction device 1; the water outlet of the phosphorus recovery device 4 is communicated with the water inlet of the denitration device 5, and the backwashing waste liquid outlet of the denitration device 5 is communicated with the water inlet of the sewage treatment device 2; the water outlet of the denitration device 5 is communicated with the water inlet of the automatic backwashing filter; the water outlet of the automatic backwashing filter is communicated with the water inlet of the disinfecting device 7; the water outlet of the disinfection device 7 is communicated with the discharge port 8; and a sewage discharge port of the sewage treatment device 2 is communicated with a feed port of the residual sludge liquefying device 1. In the present invention, all the above devices are preferably communicated through a pipe.
As an embodiment of the present invention, a schematic view of the sewage treatment device 2 is shown in fig. 2, and the sewage treatment device 2 includes a grid 2-1, a denitrification adjusting tank 2-2, a biochemical reaction tank 2-3 and a filtering tank 2-4 which are sequentially connected; the denitrification adjusting tank 2-2 is provided with a first sludge outlet, the biochemical reaction tank 2-3 is provided with a second sludge outlet, the filter tank 2-4 is provided with a third sludge outlet, and the first sludge outlet, the second sludge outlet and the third sludge outlet are independently communicated with a feed inlet of the sludge concentration tank 2-5; and the sewage outlet of the sludge concentration tank 2-5 is communicated with the feed inlet of the residual sludge liquefying device 1.
In the embodiment of the present invention, the design flow of the tail water deep treatment device is preferably 800-1000 m3The daily average treated water amount is preferably 500-800 m3And d. The utility model discloses a carry out regular back flush to resin or absorption filler and solve the jam problem, prior art like constructed wetland, the area is too big, can not the back flush, can only regularly change the filler.
The utility model also provides a tail water advanced treatment method based on above-mentioned technical scheme tail water advanced treatment unit, including following step:
conveying the excess sludge of the sewage treatment device to an excess sludge liquefying device, and carrying out hydrolytic acidification to obtain a hydrolysate;
conveying the sewage and the hydrolysate to a sewage treatment device for biochemical treatment to obtain tail water;
conveying the tail water to an ammonia recovery device for deep denitrification to obtain first treated tail water;
conveying the first treated tail water to a phosphorus recovery device for deep phosphorus removal to obtain second treated tail water;
conveying the second treated tail water to a denitration device for denitration treatment to obtain third treated tail water;
conveying the third treated tail water to a backwashing filter device for filtering to obtain fourth treated tail water;
and conveying the fourth treated tail water to a disinfection device for disinfection to obtain outlet water.
The utility model discloses carry sewage treatment plant 2's excess sludge to excess sludge liquefaction device 1, carry out the hydrolytic acidification, obtain the hydrolysate. In the present invention, the substances contained in the excess sludge preferably include: microorganisms having activity or death by aging, microorganism autoxidation residues, organic and inorganic substances attached to the surface of activated sludge that have not been degraded or are difficult to degrade; among them, microorganisms having activity including bacteria and fungi are the most important components.
In the present invention, the hydrolytic acidification is preferably performed under a micro-aerobic condition, and the dissolved oxygen content is preferably selected<0.15mg/L, more preferably 0.10-1.15 mg/L; the time for the hydrolytic acidification is preferably>20h, more preferably 24-48 h; the height of the hydrolytically acidified mud layer is preferably 3 m. In the utility model discloses in, hydrolytic acidification's object is the dead microorganism of ageing among the excess sludge, microorganism autoxidation residue, attaches the organic matter that has not degraded or be difficult to degrade on the activated sludge surface, and above-mentioned these materials can be converted into soluble organic matter (SCOD) and Volatile Fatty Acid (VFAs) after hydrolytic acidification, return in sewage treatment system as the carbon source. The utility model recovers the carbon source in the excess sludge through hydrolytic acidification, and the reduction of sulfate in the excess sludge is inhibited and the Biochemical Oxygen Demand (BOD) is controlled in the micro-aerobic environmental condition5) More accumulation in the wastewater, more sufficient carbon source recovery, and S2-The sulfide concentration in the sludge liquefaction recovery device is reduced, the generation of malodorous substances is reduced, and the surrounding environment is effectively protected.
In the embodiment of the utility model, the dichromate index (CODcr) in the hydrolysate is 3014-5155 mg/L, wherein SCOD is 2411-4890 mg/L, VFAs is 1446-3912 mg/L; biochemical Oxygen Demand (BOD)5) 1989-3866 mg/L; content of Ammonia Nitrogen (NH)3-N) is 301-430 mg/L; the total nitrogen amount (TN) is 363-460 mg/L; the total phosphorus amount (TP) is 12-33 mg/L.
After obtaining the hydrolysate, the utility model discloses with sewage with the hydrolysate is carried to sewage treatment plant in, carries out biochemical treatment, obtains the tail water. In an embodiment of the present invention, the contaminated water isThe dichromate index is 50-400 mg/L; the biochemical oxygen demand is 30-300 mg/L; the ammonia nitrogen content is 10-100 mg/L; the total nitrogen amount is 20-200 mg/L; the total phosphorus content is 0.5-10 mg/L. The CODcr of the tail water is 10-30 mg/L; biochemical Oxygen Demand (BOD)5) 5-10 mg/L; ammonia Nitrogen (NH)3-N) content of 5-100 mg/L; the Total Nitrogen (TN) content is 10-200 mg/L; the Total Phosphorus (TP) content is 0.5-10 mg/L.
In the embodiment of the utility model, the sewage passes through the grating 2-1 to remove garbage and large-particle pollutants, enters the denitrification regulating tank 2-2 to be mixed with the hydrolysate discharged by the residual sludge liquefying device, and the denitrifying bacteria utilizes the carbon source of the sewage and the hydrolysate to carry out denitrification on nitrate nitrogen in the sewage and remove partial organic matters; the effluent of the denitrification regulating tank 2-2 enters a biochemical reaction tank 2-3 to further remove organic pollutants, nitrogen and phosphorus; the biochemical reaction tank 2-3 comprises an anaerobic tank, an anoxic tank and an aerobic tank which are communicated in sequence; the effluent of the denitrification regulating tank 2-2 enters an anaerobic tank, phosphorus is released by phosphorus-removing bacteria, and meanwhile, part of organic matters are aminated; the effluent of the anaerobic tank and the reflux mixed liquid of the aerobic tank enter an anoxic tank, and nitrate nitrogen is removed through denitrification; the effluent of the anoxic tank enters an aerobic tank to remove BOD, nitrification and phosphorus absorption are carried out, and finally, pollutants are further removed through a filter tank 2-4 and tail water is obtained through mud-water separation; and the residual sludge in the denitrification regulating tank, the biochemical reaction tank and the filter tank enters a sludge concentration tank.
In the utility model, the denitrification performed in the denitrification adjusting tank 2-2 is preferably performed in an anoxic state, and the Dissolved Oxygen (DO) content is preferably selected<0.2mg/L, more preferably 0.1 to 0.15 mg/L. In the embodiment of the utility model, the TN load of the denitrification adjusting tank 2-2 is kept to be 0.3-0.6 kg/(m)3·d)。
After obtaining the tail water, the utility model discloses will the tail water is carried to ammonia recovery unit, carries out degree of depth denitrogenation, obtains first processing tail water. In the present invention, the deep denitrification preferably employs a selective cation exchange resin for deep denitrification. In the specific embodiment of the utility model, selective cation exchange resin adopts 5 ~ 10 wt.% sodium chloride solution to regenerate, and the regeneration liquid gets into compound fertilizer recovery unit 9 and utilizes as liquid nitrogen fertilizer recycle. In the present invention, the regeneration period is preferably 1 to 3 months; the liquid nitrogen fertilizer in the regeneration liquid is mainly ammonium chloride, and the concentration of the ammonium chloride is preferably 1500 mg/L-3500 mg/L.
As an embodiment of the present invention, the backwash waste liquid generated in the ammonia recovery device 3 flows back to the excess sludge liquefaction device 1 to recover the carbon source therein.
In the specific embodiment of the utility model, CODcr of the first treated tail water is 6-14 mg/L; BOD54-6 mg/L; NH (NH)3N is 0.1-0.2 mg/L; TN is 8-34 mg/L; TP is 0.02-6.2 mg/L.
After obtaining first processing tail water, the utility model discloses will first processing tail water is carried to phosphorus recovery unit, carries out degree of depth dephosphorization, obtains second processing tail water. In the utility model discloses in, the degree of depth dephosphorization preferably adopts selective anion exchange resin or iron-based modified adsorption filter material to carry out degree of depth dephosphorization, see in detail earlier herein, no longer give unnecessary details here. In the specific embodiment of the utility model, selectivity anion exchange resin adopts 5 ~ 10 wt.% sodium hydroxide solution to regenerate, the modified adsorption filter material of iron-based adopts 5 ~ 10 wt.% sodium hydroxide solution regeneration, and gained regeneration liquid gets into compound fertilizer recovery unit 9 and recycles as liquid phosphorus fertilizer. In the present invention, the regeneration period is preferably 1 to 3 months; na in the regeneration liquid3PO4The concentration of (b) is preferably more than 15mg/L, more preferably 15 to 20mg/L, and further preferably 16 to 17 mg/L.
As an embodiment of the utility model, preferably will liquid nitrogen fertilizer and liquid phosphorus fertilizer mix, obtain compound liquid fertilizer.
As an embodiment of the present invention, the back washing waste liquid generated in the phosphorus recovery device 4 flows back to the excess sludge liquefaction device 1 to recover the carbon source therein.
In the specific embodiment of the utility model, the CODcr of the second treated tail water is 5-13 mg/L; BOD53-7 mg/L; NH (NH)3N is 0.1-0.2 mg/L; TN is 8 &31 mg/L; TP is 0.01-0.03 mg/L.
After obtaining the second and handling the tail water, the utility model discloses will the second is handled the tail water and is carried to denitrification facility, carries out denitration treatment, obtains the third and handles the tail water. In the utility model, the high-efficiency denitration treatment is preferably sulfur autotrophic denitrification denitration; the sulfur autotrophic denitrification denitration is a continuous H production+The pH value of the system is reduced, the suitable pH value for the survival of the thiobacillus denitrificans is 6-8, and the efficiency of the sulfur autotrophic denitrification can be improved by adding the alkaline substance into the system. In the embodiment of the utility model, going on in the high-efficient denitration treatment process, the alkaline material of addition is preferably 5 ~ 10 wt.% NaOH to pH value when guaranteeing high-efficient denitration treatment is 6 ~ 8.
In the embodiment of the present invention, the water inlet mode of the denitration device 5 is preferably an up-flow type, and the anaerobic state is maintained; the HRT of the elemental sulfur self-reduction denitrification is preferably 0.5-2.0 h.
As an embodiment of the present invention, the selective anion exchange resin is regenerated by using nitrate radical selective anion exchange resin to obtain a regenerated liquid; the regenerated liquid and the back-flushing waste liquid generated by the denitration device 5 independently flow back to the denitrification regulating tank 2-2 for circular treatment.
In the specific embodiment of the utility model, CODcr of the third treated tail water is 3-8 mg/L; BOD51-5 mg/L; NH (NH)3N is 0.02-0.1 mg/L; TN is 0.2-0.3 mg/L; TP is 0.01-0.03 mg/L.
After the tail water is treated by the third treatment, the utility model discloses will the tail water is treated by the third and is carried to back flush filter equipment, filters, obtains the fourth treatment tail water. In the utility model, the filtration is preferably quartz sand filtration; the particle size of the quartz sand is preferably 0.3-3.5 mm. The utility model discloses a SS of filtration detach aquatic. As an embodiment of the present invention, the backwash waste liquid generated by the automatic backwash filter device flows back to the excess sludge liquefaction device 1, and the carbon source in the backwash waste liquid is recycled.
After the fourth treatment tail water is obtained, the utility model discloses will fourth treatment tail water is carried to degassing unit, disinfects, obtains out water. The specific way of disinfection is not specifically limited in the present invention, and the disinfection method known to those skilled in the art can be adopted.
In the specific embodiment of the utility model, CODcr of the effluent is 3-8 mg/L; BOD51-5 mg/L; NH (NH)3N is 0.02-0.1 mg/L; TN is 0.2-0.3 mg/L; TP is 0.01-0.03 mg/L.
In the embodiment of the present invention, it is preferable to discharge the water to be discharged obtained by disinfection through the discharge port 8, and the present invention is not limited to the specific discharge manner, and the discharge manner known to those skilled in the art can be adopted.
In the embodiment of the present invention, the CODcr of the water discharged from the discharge port 8 is 3-7 mg/L; BOD51-4 mg/L; NH (NH)3N is 0.02-0.1 mg/L; TN is 0.2-0.3 mg/L; TP is 0.01-0.03 mg/L and meets the standard of surface standard IV water.
The utility model provides a tail water advanced treatment unit and method easy and simple to handle, artifical demand is few, and degree of automation is high, can realize villages and towns sewage treatment facility's remote control and unmanned on duty.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the embodiments described are only some embodiments of the invention, and not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Example 1
Carrying out village and town sewage treatment by adopting a tail water deep treatment device shown in figure 1; wherein the design flow is 1000m3D, daily average treated water amount is 800m3/d；
The sewage treatment device 2 is a DMBR double-membrane integrated device based on an MBR process, and comprises a grid 2-1, a denitrification adjusting tank 2-2, a biochemical reaction tank 2-3 and a filter tank 2-4 which are communicated in sequence as shown in figure 2; the denitrification adjusting tank 2-2 is provided with a first sludge outlet, the biochemical reaction tank 2-3 is provided with a second sludge outlet, the filter tank 2-4 is provided with a third sludge outlet, and the first sludge outlet, the second sludge outlet and the third sludge outlet are independently communicated with a feed inlet of the sludge concentration tank 2-5; and the sewage outlet of the sludge concentration tank 2-5 is communicated with the feed inlet of the residual sludge liquefying device 1. The water quality of the influent water in FIG. 1 is shown in Table 1;
table 1 example 1 quality of influent water
The tail water deep treatment method comprises the following steps:
(1) and (3) liquefying the sludge to recover a carbon source: the excess sludge of the sludge concentration tank 2-5 of the sewage treatment device 2 enters the excess sludge liquefying device 1 for hydrolysis and acidification to obtain hydrolysate; the hydrolytic acidification is operated in an intermittent aeration mode and is automatically controlled by adopting a PLC (programmable logic controller); the main parameters include: the height of the hydrolyzed and acidified mud layer is 3m, the intermittent aeration frequency of the liquefaction pool is 10min per 2h, and the DO concentration is ensured to be 0.10-0.15 mg/L;
(2) denitrification: mixing the hydrolysate and the backwash waste liquid of the denitration device 5 with the inlet water in the table 1, primarily filtering the mixture through a grating 2-1, and entering a denitrification regulating tank 2-2 reformed from an original regulating tank to carry out pre-denitrification and denitrification, wherein the main reforming is as follows: an aeration head and a sludge discharge pump are added, so that pollutants can be mixed with activated sludge conveniently, and the sludge concentration can be regulated and controlled; the effluent of the denitrification regulating tank 2-2 enters a biochemical reaction tank 2-3 for conventional biochemical treatment, the residual sludge provides a carbon source, and the nitrogen and phosphorus removal efficiency of a primary system is improved; wherein, the TN load of the denitrification regulating reservoir 2-2 is as follows: 0.3 to 0.6 kg/(m)3D) the main parameter is DO<0.2mg/L；
(3) Deep denitrification and dephosphorization: effluent of the sewage treatment device 2 sequentially enters an ammonia recovery device 3 and a phosphorus recovery device 4 for deep denitrification and dephosphorization; wherein the ammonia recovery device 3 adoptsThe selective cation exchange resin is used as a filler, the height of the filler is 3m, the double adsorption columns run intermittently (namely two sets of recovery devices are connected in parallel, when one set of adsorption columns are backwashed, the other set of adsorption columns run normally, so that the backwashing can be realized, the continuous operation without stopping water is realized), 5 wt.% of NaCl solution is used for regenerating the adsorption materials every 3 months, the soaking time is 2h, and the regenerated waste liquid enters a compound fertilizer recovery device 9; the concentration of feed water TP to the phosphorus recovery apparatus 4<3mg/L, the phosphorus recovery device 4 uses an iron-based adsorption filter material as a filler, the height of the filter material is 2.5m, and the double adsorption columns operate intermittently; after the adsorption saturation, 5 wt.% of NaOH solution is used for soaking and regenerating the iron-based resin with the adsorption saturation every 3 months for 2 hours, and Na obtained from the regenerated waste liquid3PO4The concentration is 15-17 mg/L, and the obtained regenerated waste liquid enters a compound fertilizer recovery device 9 for storage and recovery; the back washing waste liquid of the ammonia recovery device 3 and the phosphorus recovery device 4 flows back to the residual sludge liquefaction device 1; the back washing is air-water back washing, and the parameters are as follows: gas amount of 2-4L/(m)2S) water content of 1.5-3L/(m)2S) with a frequency of 1 time per month.
(4) High-efficiency denitration: after the ammonia nitrogen and the total phosphorus in the tail water are deeply removed, the effluent of the phosphorus recovery device 4 enters the denitration device 5, and the NO of the influent of the denitration device 53N concentration is 8-13 mg/L, selective anion exchange resin is adopted for adsorption denitration, HRT is 1.5h, 5% NaCl solution is used for regeneration, and regenerated waste liquid flows back to the denitrification regulating reservoir 2-2; the backwashing of the denitration device 5 is also air-water backwashing, and the parameters are as follows: gas amount of 2-4L/(m)2S) water content of 1.5-3L/(m)2S) frequency of 1 time per month;
(5) filtering and sterilizing, and discharging after reaching standards: the effluent of the denitration device 5 enters an automatic backwashing filter 6 for filtering, and SS and the like are removed; the quartz sand filtering device is characterized in that the quartz sand filtering device automatically performs backwashing once every 2 weeks, and the backwashing parameters are as follows: gas amount of 5-7L/(m)2S) and water amount of 4-10L/(m)2S); the filtered water is disinfected by the original disinfection device 7 and finally discharged through the discharge port 8 after reaching the standard; after running for a period of time, the effluent quality conditions of each treatment device are shown in Table 2 below.
Table 2 example 1 effluent quality of each treatment apparatus
As can be seen from the table 2, the water quality obtained by the device provided by the utility model meets the ground surface IV water standard, and in the treatment process, no additional carbon source or phosphorus removing agent is needed.
Example 2
Carrying out village and town sewage treatment by adopting a tail water deep treatment device shown in figure 1; wherein the design flow is 800m3D, daily average treated water amount is 500m3/d；
The sewage treatment device 2 is a DMBR double-membrane integrated device based on an MBR process, as shown in FIG. 2. Because slaughtering wastewater is discharged into a pipe network, the concentrations of ammonia nitrogen and total phosphorus pollutants in water are high, and the water quality of inlet water in the graph 1 is shown in a table 3;
table 3 quality of influent water of example 2
The tail water deep treatment method comprises the following steps:
(1) and (3) liquefying the sludge to recover a carbon source: the excess sludge of the sludge concentration unit of the sewage treatment device 2 enters the excess sludge liquefying device 1 for hydrolysis acidification to obtain hydrolysate; the hydrolytic acidification is operated in an intermittent aeration mode and is automatically controlled by adopting a PLC (programmable logic controller); the main parameters include: the height of the hydrolyzed and acidified mud layer is 3m, the intermittent aeration frequency of the liquefaction pool is 15min per 2h, and the DO concentration is ensured to be 0.10-0.15 mg/L;
(2) pre-denitrification: mixing the hydrolysate, the backwash waste liquid of the denitration device 5 and the inlet water of the table 3, and performing primary filtration through a grating 2-1 to enter the original mixerThe denitrification regulating tank 2-2 reformed by the save tank is used for pre-denitrification and denitrification, and mainly comprises the following steps: an aeration head and a sludge discharge pump are added, so that pollutants can be mixed with activated sludge conveniently, and the sludge concentration can be regulated and controlled; the effluent of the denitrification regulating tank 2-2 enters a biochemical reaction tank 2-3 for conventional biochemical treatment, the residual sludge provides a carbon source, and the nitrogen and phosphorus removal efficiency of a primary system is improved; wherein, the TN load of the denitrification regulating reservoir 2-2 is as follows: 0.3 to 0.6 kg/(m)3D) the main parameter is DO<0.2mg/L；
(3) Deep denitrification and dephosphorization: the effluent of the sewage treatment device 2 enters an ammonia recovery device 3 and a phosphorus recovery device 4 respectively to carry out deep nitrogen and phosphorus removal; the ammonia recovery device 3 adopts selective cation exchange resin as a filler, the height of the filler is 3m, the double adsorption columns operate intermittently, 5 wt.% of NaCl solution is used for regenerating the adsorption material every 1 month, the soaking time is 2 hours, and the regenerated waste liquid enters a compound fertilizer recovery device 9; as the concentration of inlet water TP of the phosphorus recovery device 4 is more than 3mg/L, the phosphorus recovery device 4 uses selective anion exchange resin as a filler, the height of a filter material is 2.5m, and the double adsorption columns operate intermittently; after the adsorption saturation, 10 wt.% of NaOH solution is used for soaking and regenerating the selective anion exchange resin with saturated adsorption every 1 month, the soaking time is 2h, and Na obtained from the regenerated waste liquid3PO4The concentration is 16-20 mg/L, and the obtained regenerated waste liquid enters a compound fertilizer recovery device 9 for storage and recovery; the back washing waste liquid of the ammonia recovery device 3 and the phosphorus recovery device 4 flows back to the residual sludge liquefaction device 1;
(4) high-efficiency denitration: after the ammonia nitrogen and the total phosphorus in the tail water are deeply removed, the effluent of the phosphorus recovery device 4 enters the denitration device 5, and the NO of the influent of the denitration device 53The concentration of N is 20-31 mg/L, a sulfur simple substance self-reduction denitrification mode is adopted for denitration, sulfur autotrophic denitrification is carried out under the action of the sulfur simple substance and sulfur autotrophic bacteria, the simple substance sulfur and limestone particles are used as combined fillers, the particle size of the simple substance sulfur is 10mm, the particle size of the limestone particles is 15mm, the mass ratio of the simple substance sulfur to the limestone particles is 2:1, and the combined fillers are properly supplemented every 3 months; the water inlet mode of the denitration device 5 is an up-flow mode, the anaerobic state is kept,HRT is 2.0 h; the denitration device 5 is provided with a back washing device, uses clear water for back washing to prevent blockage, and uses a PLC (programmable logic controller) to set a program for control, wherein the back washing parameters are as follows: gas amount of 3-5L/(m)2S) water content of 2-3L/(m)2S) at a frequency of 1 time per week;
(5) filtering and sterilizing, and discharging after reaching standards: the effluent of the denitration device 5 enters an automatic backwashing filter 6 for filtering, and SS and the like are removed; the quartz sand filtering device is characterized in that the quartz sand filtering device automatically performs backwashing once every 1 week, and the backwashing parameters are as follows: gas amount of 5-7L/(m)2S) and water amount of 4-10L/(m)2S); the filtered water is disinfected by the original disinfection device 7 and finally discharged through the discharge port 8 after reaching the standard; after running for a period of time, the effluent quality conditions of each treatment device are shown in Table 4 below.
TABLE 4 quality of effluent from treatment apparatus of example 2
As can be seen from Table 4, the water quality obtained by the device provided by the utility model is superior to the surface IV water standard, and no additional carbon source or phosphorus removing agent is needed in the treatment process; the whole system has high automation degree, and can realize unattended operation during operation.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (6)
1. An advanced treatment device for tail water is characterized by comprising
A sewage treatment device (2);
the water inlet of the ammonia recovery device (3) is communicated with the water outlet of the sewage treatment device (2);
a phosphorus recovery device (4) with a water inlet communicated with the water outlet of the ammonia recovery device (3);
a denitration device (5) with a water inlet communicated with the water outlet of the phosphorus recovery device (4);
a back washing filter device (6) with a water inlet communicated with the water outlet of the denitration device (5);
a disinfecting device (7) with a water inlet communicated with the backwashing filter device (6);
the device is characterized by also comprising a residual sludge liquefying device (1), wherein a sewage outlet of the sewage treatment device (2) is communicated with a feed inlet of the residual sludge liquefying device (1); and the liquid outlet of the excess sludge liquefying device (1) is communicated with the water inlet of the sewage treatment device (2).
2. The tail water deep treatment device according to claim 1, characterized in that the sewage treatment device (2) comprises a grating (2-1), a denitrification adjusting tank (2-2), a biochemical reaction tank (2-3) and a filtering tank (2-4) which are communicated in sequence; the denitrification adjusting tank (2-2) is provided with a first sludge outlet, the biochemical reaction tank (2-3) is provided with a second sludge outlet, the filter tank (2-4) is provided with a third sludge outlet, and the first sludge outlet, the second sludge outlet and the third sludge outlet are independently communicated with a feed inlet of the sludge concentration tank (2-5); and a drain outlet of the sludge concentration tank (2-5) is communicated with a feed inlet of the residual sludge liquefaction device (1).
3. An advanced tail water treatment device according to claim 1, further comprising a compound fertilizer recovery device (9), wherein the ammonia recovery device (3) is provided with a first regenerated waste liquid outlet, the phosphorus recovery device (4) is provided with a second regenerated waste liquid outlet, and the first regenerated waste liquid outlet and the second regenerated waste liquid outlet are independently communicated with a feed inlet of the compound fertilizer recovery device (9).
4. The tail water advanced treatment device according to claim 1 or 3, characterized in that the ammonia recovery device (3) is provided with a first backwash waste water outlet, the phosphorus recovery device (4) is provided with a second backwash waste water outlet, and the first backwash waste water outlet and the second backwash waste water outlet are independently communicated with the feed inlet of the residual sludge liquefaction device (1).
5. The tail water advanced treatment device according to claim 1, characterized in that the denitration device (5) is provided with a third backwash waste water outlet which is communicated with a water inlet of the sewage treatment device (2).
6. The tail water advanced treatment device according to claim 1, characterized in that the back flush filtering device (6) is provided with a fourth back flush waste water outlet which is communicated with the feed inlet of the residual sludge liquefaction device (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020342403.5U CN212315842U (en) | 2020-03-18 | 2020-03-18 | Tail water advanced treatment device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020342403.5U CN212315842U (en) | 2020-03-18 | 2020-03-18 | Tail water advanced treatment device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212315842U true CN212315842U (en) | 2021-01-08 |
Family
ID=74017655
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202020342403.5U Active CN212315842U (en) | 2020-03-18 | 2020-03-18 | Tail water advanced treatment device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212315842U (en) |
-
2020
- 2020-03-18 CN CN202020342403.5U patent/CN212315842U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105906142B (en) | A kind of landfill leachate advanced treatment system and processing method | |
| CN106927628A (en) | Light electrolysis-Fenton-EGSB-A/O-BCO-BAF-coagulating treatment pharmacy waste water technique | |
| KR100906742B1 (en) | Treatment method and the apparatus including ultasonic-electrolysis-precipitator and complexed upper filter isolator for domestic sewage or wasted water | |
| CN106673373A (en) | Sustainable and efficient sewage treatment system | |
| CN101172729A (en) | Physciochemical treatment technique for remained aqueous ammonia of coke-oven plant | |
| CN106256787A (en) | A kind of refinery sewage O3 catalytic oxidation processing method | |
| KR101198334B1 (en) | Apparatus and Method for Treating Wastewater Using Zeolites Having Media | |
| CN110526504B (en) | System and method for treating regenerated waste liquid of targeted denitrification and dephosphorization resin | |
| CN106396191A (en) | Emergency treatment process and device of waste water with high COD and high NH3-N | |
| CN111217496A (en) | Tail water deep treatment device and treatment method | |
| KR102171918B1 (en) | Recycling and water quality purification treatment system of livestock manure | |
| CN110342750A (en) | Sewage treatment device and process for synchronously realizing sludge in-situ reduction and nitrogen and phosphorus removal | |
| CN107324606B (en) | Sewage treatment system and method for recycling iron-rich excess sludge dephosphorization membrane bioreactor | |
| KR101360015B1 (en) | Method of reusing treated wastewater and system using the same | |
| CN212315842U (en) | Tail water advanced treatment device | |
| KR100432437B1 (en) | Method and Apparatus for Treating N-containing Wastewater Using Granular Zeolites | |
| CN106430846A (en) | Efficient treatment integrated process for recalcitrant wastewater with low organic matter content | |
| CN103224311A (en) | Advanced treatment system for sewage and wastewater | |
| KR100825518B1 (en) | Device and method for Biological Treatment of Wastewater using MBR and Zeolite Powder | |
| CN206624744U (en) | Light electrolysis Fenton EGSB A/O BCO BAF coagulating treatment pharmacy waste water systems | |
| CN101830611A (en) | System and method for treating sewage containing high-proportion industrial waste water | |
| KR100583904B1 (en) | High intergated Biological Nutrient Removal System | |
| CN211078800U (en) | System for treating regenerated waste liquid of targeted nitrogen and phosphorus removal resin | |
| CN114409207A (en) | Printing ink effluent disposal system | |
| KR100243729B1 (en) | Method for treating wastewater biologically by continuously cycling and regenerating powdered zeolite in the bioreactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |