CN111217496A - Tail water deep treatment device and treatment method - Google Patents
Tail water deep treatment device and treatment method Download PDFInfo
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- CN111217496A CN111217496A CN202010191086.6A CN202010191086A CN111217496A CN 111217496 A CN111217496 A CN 111217496A CN 202010191086 A CN202010191086 A CN 202010191086A CN 111217496 A CN111217496 A CN 111217496A
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- 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
- C02F2303/00—Specific treatment goals
- C02F2303/04—Disinfection
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- 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
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)
Abstract
The invention relates to the technical field of sewage treatment, in particular to a tail water advanced treatment device and a treatment method. The invention 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 excess sludge discharged by the sewage treatment device is hydrolyzed and acidified by the excess sludge liquefying device and is recycled as a carbon source, so that the defect of insufficient carbon source of the sewage in villages and towns is overcome. The tail water advanced treatment device provided by the invention can be used for automatically and efficiently carrying out denitration, denitrification and dephosphorization on tail water, and recovering nitrogen and phosphorus resources to obtain water to be discharged which meets the standard of surface quasi IV water.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a tail water advanced treatment device and a treatment method.
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.
Disclosure of Invention
The tail water advanced treatment device provided by the invention has the advantages of reasonable design, simple and convenient structure, capability of being directly connected to the existing rural sewage treatment facilities, no need of adding medicaments such as carbon sources, phosphorus removal agents and the like, and low operation cost.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a tail water deep treatment device, which comprises
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 invention provides a tail water advanced treatment method based on the tail water advanced treatment device, which comprises the following steps:
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.
Preferably, the dichromate index of the sewage 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.
Preferably, the dichromate index 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.
Preferably, the hydrolytic acidification is carried out under micro-aerobic conditions with a dissolved oxygen content <0.15 mg/L; the time for hydrolytic acidification was >20 h.
The invention provides a tail water deep treatment device, which comprises 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. In the invention, the excess sludge discharged by the sewage treatment device 2 is hydrolyzed and acidified by the excess sludge liquefying device 1 and is recycled as a carbon source, so that the defect of insufficient carbon source of the sewage in villages and towns is overcome; 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; according to the device provided by the invention, additional carbon source, PAC (polyaluminium chloride) and other medicaments are not required to be added, so that the sludge yield is reduced, the operation is simplified, the operation cost is reduced, and the remote control and unattended operation are realized; the tail water advanced treatment device provided by the invention can be used for carrying out efficient denitration, denitrification and dephosphorization on tail water and recovering nitrogen and phosphorus resources, so that water to be discharged meeting the standard of surface quasi IV water is obtained.
Drawings
FIG. 1 is a schematic view of an advanced tail water treatment apparatus according to 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 invention provides a tail water deep treatment device, which comprises:
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 tail water advanced treatment device provided by the invention comprises a sewage treatment device 2, and belongs to conventional biochemical treatment. In the present invention, the sewage treatment apparatus 2 includes an SBR-integrated sewage treatment apparatus or an MBR-integrated sewage treatment apparatus, and the like.
As an embodiment of the invention, 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 specific structures of the grating 2-1, the denitrification regulating tank 2-2, the biochemical reaction tank 2-3, the filtering tank 2-4 and the sludge concentration tank 2-5 are not specially limited, and the grating, the denitrification regulating tank, the biochemical reaction tank, the filtering tank and the sludge concentration tank which are well known by the technical personnel in the field can be adopted.
In a specific embodiment of the present invention, the filtration tanks 2-4 comprise MBR membrane filtration tanks or sedimentation tanks.
In a specific embodiment of the invention, the denitrification regulating tank 2-2 is used for denitrification. As an embodiment of the invention, the denitrification regulating reservoir 2-2 is formed by modifying a regulating reservoir, and an aeration head, a gallery or a stirrer is added on the basis of the original regulating reservoir to promote the uniform mixing of the hydrolysate and the sewage discharged by the excess sludge liquefaction device 1 and improve the denitrification efficiency. The specific structures of the aeration head, the gallery and the stirrer are not particularly limited in the invention, and the aeration head, the gallery and the stirrer which are well known to those skilled in the art can be adopted. In the invention, the Total Nitrogen (TN) load of the denitrification regulating reservoir 2-2 is preferably 0.3-0.6 kg/(m)3·d)。
The tail water deep treatment device provided by the invention also comprises an excess sludge liquefaction device 1, wherein a sewage discharge outlet of the sewage treatment device 2 is communicated with a 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 specific embodiment of the invention, the liquid outlet of the excess sludge liquefaction device 1 is communicated with the denitrification regulating reservoir 2-2, so as to improve the denitrification efficiency in the denitrification regulating reservoir. The excess sludge discharged by the sewage treatment device 2 is hydrolyzed and acidified by the excess sludge liquefying device 1 and is recycled as a carbon source, so that the defect of insufficient carbon source of the sewage in villages and towns is overcome; 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 invention, the excess sludge liquefaction device 1 is a micro-aerobic sludge hydrolysis acidification device, and is operated by adopting an intermittent aeration mode, and the invention has no special limitation on the specific process of the intermittent aeration, and preferably maintains DO <0.15mg/L and Hydraulic Retention Time (HRT) >20 h. In a specific embodiment of the invention, the intermittent aeration frequency is 10-15 min per 2h of aeration.
The tail water deep treatment device provided by the invention comprises an ammonia recovery device 3 with a water inlet communicated with a water outlet of the sewage treatment device 2, and is used for deep denitrification. In the embodiment of the present invention, the ammonia recovery unit 3 is filled with an ammonia recovery packing, and the ammonia recovery packing is preferably a selective cation exchange resin, and more preferably an ammonium selective Na-type cation exchange resin. In a specific embodiment of the invention, the selective cation exchange resin is soaked in a 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 means and a regeneration means; 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 tail water advanced treatment device provided by the invention comprises a phosphorus recovery device 4 with a water inlet communicated with a water outlet of the ammonia recovery device 3, and is used for deeply removing phosphorus. In the invention, 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 invention, when the total phosphorus concentration of the tail water is >3mg/L, selective anion exchange resin is used as a phosphorus recovery filler; 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 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 apparatus 4 has an automatic backwashing means and a regenerating means; 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.
The tail water advanced treatment device provided by the invention further 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 and are used for recovering and reusing regenerated waste liquid.
The tail water advanced treatment device provided by the invention comprises a denitration device 5 with a water inlet communicated with a water outlet of the phosphorus recovery device 4, and is used for high-efficiency denitration. In an embodiment of the present invention, when the denitrification apparatus 5 is fed with nitrate Nitrogen (NO)3Concentration 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 present invention, when elemental sulfur is used, elemental sulfur is usedDuring denitration by a reduction denitrification mode, sulfur filler and sulfur autotrophic bacteria attached to the sulfur filler are filled in the denitration device 5; 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; in the present invention, it is preferable that the regular replenishment or replacement of the sulfur filler is performed for 3 to 6 months.
The invention carries out high-efficiency denitration treatment under the action of sulfur simple substance and sulfur autotrophic bacteria or the adsorption of ion exchange resin. 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, which 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), the frequency is preferably 1 time per week. As an embodiment of the present invention, 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 denitrification regulating tank 2-2 of the sewage treatment device 2 to perform a cyclic treatment on the wastewater. In the invention, the back washing waste liquid discharged by the denitration device 5 mainly contains dead sulfur autotrophic bacteria, suspended pollutants and the like; and stopping normal water outlet when the denitration device 5 performs backwashing, and if continuous water outlet is kept, adopting a mode of alternately and intermittently operating two groups of adsorption columns, wherein the two groups of adsorption columns are alternately and intermittently operated in the specific embodiment of the invention.
The invention realizes deep nitrogen and phosphorus removal and resource recycling of nitrogen and phosphorus by using sulfur autotrophic bacteria, high-efficiency ion exchange resin and the like without adding a carbon source.
The tail water advanced treatment device provided by the invention comprises a back washing filter device 6, the water inlet of which is communicated with the water outlet of the denitration device 5, and the back washing filter device is used for filtering and removing suspended matters (SS) in water. As an embodiment of the present invention, the backwashing filter device 6 is preferably a quartz sand filter device; 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, which can perform automatic backwashing according to a set program, so as to improve the automation degree; 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 present invention, the backwash filter device 6 is provided with a fourth backwash waste liquid outlet, and the fourth backwash waste liquid outlet is communicated with the feed inlet of the excess sludge liquefaction device 1 to recycle the carbon source in the waste liquid. In the invention, the backwash waste liquid discharged by the backwash filter device 6 is mainly suspended matters and fine particles between a biological film attached to the quartz sand filler and the trapped quartz sand filler.
The tail water deep treatment device provided by the invention comprises a disinfection device 7 with a water inlet communicated with the backwashing filter device 6 for disinfection treatment. The sterilizing device 7 of the present invention is not particularly limited, and a sterilizing device 7 known to those skilled in the art may be used.
As an embodiment of the invention, the tail water deep treatment device provided by the invention further comprises a discharge port 8 connected with a water outlet of the disinfection device 7, and the treated tail water is discharged. In a particular embodiment of the invention, the discharge opening 8 is provided with a pasteurisation tank for registering the amount of water treated by the treatment device.
As an embodiment of the present invention, a schematic diagram of a tail water advanced treatment apparatus provided by the present invention is shown in fig. 1, and includes a surplus sludge liquefaction apparatus 1, a sewage treatment apparatus 2, an ammonia recovery apparatus 3, a phosphorus recovery apparatus 4, a denitrification apparatus 5, an automatic backwashing filter apparatus 6, a disinfection apparatus 7, a discharge port 8, and a compound fertilizer recovery apparatus 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 of the above devices are preferably communicated by a pipe.
As an embodiment of the invention, a schematic diagram of the sewage treatment device 2 is shown in FIG. 2, and 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.
In the specific embodiment of the 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 invention solves the problem of blockage by periodically backwashing the resin or the adsorption filler, and the prior art such as the artificial wetland has overlarge area, can not be backwashed and only can periodically replace the filler.
The invention also provides a tail water advanced treatment method based on the tail water advanced treatment device, which comprises the following steps:
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 invention conveys the excess sludge of the sewage treatment device 2 to the excess sludge liquefying device 1 for hydrolysis acidification to obtain 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 carried out under a micro-aerobic condition, and the dissolved oxygen content is preferably<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 present invention, the hydrolytic acidification is performed on aged and dead microorganisms in the excess sludge, microbial autoxidation residues, and undegraded or hardly degraded organic matters attached to the surface of the activated sludge, which are converted into soluble organic matters (SCOD) and Volatile Fatty Acids (VFAs) after hydrolytic acidification and returned to the sewage treatment system as a carbon source. Hair brushIt is clear that the carbon source in the excess sludge is recovered by hydrolytic acidification, the sulphate reduction in the excess sludge is inhibited, the Biochemical Oxygen Demand (BOD) is maintained in micro-aerobic environmental conditions5) 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 specific embodiment of the invention, the dichromate index (CODcr) in the hydrolysate is 3014-5155 mg/L, wherein SCOD is 2411-4890 mg/L, and 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 sewage and the hydrolysate are conveyed to a sewage treatment device for biochemical treatment to obtain tail water. In a specific embodiment of the invention, the dichromate index of the sewage 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 specific embodiment of the invention, 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 denitrification bacteria utilize the carbon sources of the sewage and the hydrolysate to carry out denitrification on nitrate nitrogen in the sewage and remove part of 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 present invention, the denitrification performed in the denitrification adjustment tank 2-2 is preferably performed in an anoxic state, and the dissolved oxygen content (DO) is preferably<0.2mg/L, more preferably 0.1 to 0.15 mg/L. In the specific embodiment of the invention, the TN load of the denitrification regulating reservoir 2-2 is kept to be 0.3-0.6 kg/(m)3·d)。
After the tail water is obtained, the tail water is conveyed to an ammonia recovery device for deep denitrification, and the first treated tail water is obtained. In the present invention, the deep denitrification is preferably performed by using a selective cation exchange resin. In a specific embodiment of the invention, the selective cation exchange resin is regenerated by using 5-10 wt.% of sodium chloride solution, and the regenerated solution enters a compound fertilizer recovery device 9 to be recycled as a liquid nitrogen fertilizer. In the invention, the regeneration period is preferably 1-3 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 is returned to the excess sludge liquefaction device 1, and the carbon source is recovered therein.
In a specific embodiment of the invention, 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 the first treated tail water is obtained, the first treated tail water is conveyed to a phosphorus recovery device for deep phosphorus removal, and second treated tail water is obtained. In the present invention, the deep phosphorus removal is preferably performed by using selective anion exchange resin or iron-based modified adsorption filter material, which is described in detail above and will not be described herein again. In a specific embodiment of the invention, the selective anion exchange resin is regenerated by using 5-10 wt.% of sodium hydroxide solution, and the iron-based modified adsorption filter materialAnd 5-10 wt.% of sodium hydroxide solution is adopted for regeneration, and the obtained regenerated liquid enters a compound fertilizer recovery device 9 to be recycled as liquid phosphate fertilizer. In the invention, the regeneration period is preferably 1-3 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 present invention, it is preferable to mix the liquid nitrogen fertilizer and the liquid phosphorus fertilizer to obtain a composite liquid fertilizer.
As an embodiment of the present invention, the backwash waste liquid generated in the phosphorus recovery apparatus 4 is returned to the excess sludge liquefaction apparatus 1, and the carbon source is recovered therein.
In a specific embodiment of the invention, 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 the second treated tail water is obtained, the second treated tail water is conveyed to a denitration device for denitration treatment, and third treated tail water is obtained. In the invention, 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 a specific embodiment of the present invention, during the high-efficiency denitration treatment, the alkaline substance added is preferably 5 to 10 wt.% NaOH, so as to ensure that the pH value during the high-efficiency denitration treatment is 6 to 8.
In the embodiment of the present invention, the water inlet mode of the denitration device 5 is preferably an up-flow mode, and the denitration device maintains an anaerobic state; 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 solution; 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 a specific embodiment of the invention, 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 third treated tail water is obtained, the third treated tail water is conveyed to a backwashing filter device for filtering to obtain fourth treated tail water. In the present invention, the filtration is preferably quartz sand filtration; the particle size of the quartz sand is preferably 0.3-3.5 mm. The present invention removes SS from water by filtration. As an embodiment of the present invention, the backwash waste liquid generated by the automatic backwash filter device is returned to the excess sludge liquefaction device 1, and a carbon source in the backwash waste liquid is recycled.
After the fourth treatment tail water is obtained, the fourth treatment tail water is conveyed to a disinfection device for disinfection, and the effluent is obtained. The specific mode of sterilization in the present invention is not particularly limited, and the sterilization mode known to those skilled in the art may be used.
In a specific embodiment of the invention, 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, the water to be discharged after the disinfection is preferably discharged through the discharge port 8, and the specific manner of the discharge is not particularly limited in the present invention, and may be a discharge manner known to those skilled in the art.
In the specific embodiment of the invention, CODcr of 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 tail water advanced treatment device and the tail water advanced treatment method provided by the invention are simple and convenient to operate, have less manual demands and high automation degree, and can realize remote control and unattended operation of sewage treatment facilities in villages and towns.
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 described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within 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: the hydrolysate, the backwash waste liquid of the denitration device 5 and the inlet water in the table 1 were mixed, and passed throughThe primary filtration of the grating 2-1 enters a denitrification adjusting tank 2-2 reformed by an original adjusting tank to carry out pre-denitrification, and 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; the ammonia recovery device 3 adopts selective cation exchange resin as a filler, the height of the filler is 3m, the double adsorption columns run intermittently (namely two recovery devices which are connected in parallel, one of the adsorption columns runs normally during back washing, and the other adsorption column runs normally so as to realize continuous running without stopping water during back washing), 5 wt.% of NaCl solution is used for regenerating the adsorption material every 3 months, the soaking time is 2 hours, and the regenerated waste liquid enters the 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 53The concentration of-N is 8-13 mg/L, selective anion exchange resin is adopted for adsorption denitration, HRT is 1.5h, and 5% NaCl solution is used for regenerationThe regenerated waste liquid flows back to the denitrification regulating tank 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 Table 2, the water quality obtained by the treatment of the device provided by the invention meets the standard of surface IV water, and no additional carbon source or phosphorus removal agent is needed in the treatment process.
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, 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, 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: 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 a denitration device 5, and the denitration device5 water feed NO3The 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, and the 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 treatment of the device provided by the invention 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, various 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 (10)
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).
7. The tail water advanced treatment method based on the tail water advanced treatment device of any one of claims 1 to 6, comprising the following steps:
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.
8. The tail water advanced treatment method according to claim 7, wherein the dichromate index of the sewage 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.
9. The tail water advanced treatment method according to claim 7 or 8, characterized in that the dichromate index of the tail water is 10-30 mg/L; the biochemical oxygen demand is 5-10 mg/L; the content of ammonia nitrogen is 5-100 mg/L; the total nitrogen content is 10-200 mg/L; the total phosphorus content is 0.5-10 mg/L.
10. The method for advanced tail water treatment according to claim 7, wherein the hydrolytic acidification is performed under micro-aerobic conditions, and the content of dissolved oxygen is less than 0.15 mg/L; the time for hydrolytic acidification was >20 h.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114349276A (en) * | 2021-12-30 | 2022-04-15 | 北控水务(中国)投资有限公司 | Sewage treatment system and method |
| NL2032892B1 (en) * | 2022-05-11 | 2023-11-20 | Green Environmental Tech Co Ltd | A high-salt and high-ammonia-nitrogen wastewater autotrophic denitrification and full quantification treatment device and method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102815841A (en) * | 2012-08-29 | 2012-12-12 | 成官文 | Reconstruction process of nitrogen and phosphorus removing by two-stage bio-contact oxidation |
| CN107473378A (en) * | 2017-06-25 | 2017-12-15 | 云南傲远环保科技有限公司 | The aerobic membrane module processing method of anoxic anaerobic/anoxic |
| CN110386736A (en) * | 2019-08-08 | 2019-10-29 | 芜湖沃泰环保科技有限公司 | A kind of sewage treatment nitrogen phosphorus advanced treatment system and its processing method |
-
2020
- 2020-03-18 CN CN202010191086.6A patent/CN111217496A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102815841A (en) * | 2012-08-29 | 2012-12-12 | 成官文 | Reconstruction process of nitrogen and phosphorus removing by two-stage bio-contact oxidation |
| CN107473378A (en) * | 2017-06-25 | 2017-12-15 | 云南傲远环保科技有限公司 | The aerobic membrane module processing method of anoxic anaerobic/anoxic |
| CN110386736A (en) * | 2019-08-08 | 2019-10-29 | 芜湖沃泰环保科技有限公司 | A kind of sewage treatment nitrogen phosphorus advanced treatment system and its processing method |
Non-Patent Citations (2)
| Title |
|---|
| 中国环境保护产业协会: "《国家重点环境保护实用技术及示范工程汇编 2009》", 31 December 2009, 中国环境科学出版社, pages: 220 * |
| 韩耀霞等: "《环境保护与可持续发展》", 30 June 2018, 北京工业大学出版社, pages: 272 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114349276A (en) * | 2021-12-30 | 2022-04-15 | 北控水务(中国)投资有限公司 | Sewage treatment system and method |
| NL2032892B1 (en) * | 2022-05-11 | 2023-11-20 | Green Environmental Tech Co Ltd | A high-salt and high-ammonia-nitrogen wastewater autotrophic denitrification and full quantification treatment device and method |
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