CN214142033U

CN214142033U - Nitrogen and phosphorus removal combined process system

Info

Publication number: CN214142033U
Application number: CN202023056789.2U
Authority: CN
Inventors: 徐成; 玄小立; 赵馨
Original assignee: Suez Water Treatment Co Ltd
Current assignee: Suez Environmental Technology Beijing Co Ltd
Priority date: 2020-12-17
Filing date: 2020-12-17
Publication date: 2021-09-07
Anticipated expiration: 2030-12-17

Abstract

A combined process system for nitrogen and phosphorus removal is characterized in that the process system is provided with a pre-anoxic zone, an anaerobic zone, an anoxic zone, an aeration zone, a degassing zone and a precipitation zone; the pre-anoxic zone, the anaerobic zone and the anoxic zone are arranged in the middle; the aeration zone, degassing zone and settling zone are disposed on either side of the pre-anoxic zone, anaerobic zone and anoxic zone.

Description

Nitrogen and phosphorus removal combined process system

Technical Field

The disclosure relates to a combined nitrogen and phosphorus removal process system, in particular to a compact integrated nitrogen and phosphorus removal aeration process system.

Background

Generally, a nitrogen and phosphorus removal aeration process system is constructed by separating an anoxic aerobic tank and a secondary sedimentation tank, the aerobic tank utilizes activated sludge to perform carbon removal and nitrification treatment, and the system has large volume, large occupied area and high civil engineering cost. The common denitrification and dephosphorization aeration process system has the problem of not compact structure. Although the existing compact process (such as MSBR) has the functions of biological phosphorus removal, carbon removal and nitrification and has a compact structure, the anoxic zone has small volume, short denitrification time and insufficient denitrification capability, and the aerobic tank has small volume and weak nitrification capability.

SUMMERY OF THE UTILITY MODEL

In order to solve one or more defects in the prior art, according to one aspect of the disclosure, a combined denitrification and dephosphorization process system is provided with a pre-anoxic zone, an anaerobic zone, an anoxic zone, an aeration zone, a degassing zone and a precipitation zone.

The pre-anoxic zone, the anaerobic zone and the anoxic zone are arranged in the middle.

The aeration zone, degassing zone and settling zone are arranged (side by side) on either side of the pre-anoxic zone, anaerobic zone and anoxic zone.

According to the above aspect of the disclosure, the pre-anoxic zone is arranged for receiving a portion of the influent water and return sludge from the settling zone and is arranged to remove nitrate from the return sludge.

According to the above aspects of the present disclosure, 30% to 50% of the feed water enters the front end of the pre-anoxic zone.

And return sludge channels or return sludge pipes are arranged on two sides of the pre-anoxic zone.

And refluxing sludge to the front end of the pre-anoxic zone through the refluxing sludge channel or the refluxing sludge pipe.

The effluent of the pre-anoxic zone enters the anaerobic zone from the upper part of the partition wall at the tail end of the pre-anoxic zone.

According to the above aspects of the present disclosure, a submersible agitator is installed in the pre-anoxic zone for mixing and preventing sludge from settling.

And a water inlet ammonia nitrogen instrument, a sludge concentration meter and an oxidation reduction potential instrument are arranged in the pre-anoxic zone.

In the pre-anoxic zone, the dissolved oxygen is controlled to be below 0.5 mg/l.

In accordance with the above aspects of the present disclosure, the anaerobic zone is configured to receive another portion of the influent water and the influent water from the pre-anoxic zone and to perform biological phosphorus removal.

According to the above aspects of the present disclosure, 50% to 70% of the influent water enters the upper portion of the anaerobic zone through the influent pipe.

And a hole is formed in the bottom of the end partition wall of the anaerobic zone, and the effluent of the anaerobic zone enters the anoxic zone from the bottom of the anaerobic zone.

According to the above aspects of the present disclosure, a submersible agitator is installed in the anaerobic zone for mixing and preventing sludge sedimentation.

And an oxidation-reduction potentiometer is arranged in the anaerobic zone.

In the anaerobic zone, dissolved oxygen is controlled to be below 0.2 mg/l.

According to the above aspects of the disclosure, a nitrified liquid return channel is arranged in the middle of the anoxic zone.

And a nitrifying liquid reflux pump is arranged in the nitrifying liquid reflux channel, and the nitrifying liquid reflux pump is a wall-penetrating pump.

And a nitrifying liquid return pipe is arranged at the outlet of the nitrifying liquid return pump.

And the outlet of the nitrifying liquid return pipe reaches the front end of the anoxic zone.

According to the above aspects of the disclosure, a return sludge well is arranged on each of two sides of the anoxic zone and near the sedimentation zone.

And a return sludge pump is arranged in each return sludge well, and the return sludge pump adopts an axial flow pump.

According to the above aspects of the present disclosure, return sludge canals or return sludge pipes are provided on both sides of the anoxic zone.

The return sludge pump sends sludge to the return sludge channel or the return sludge pipe.

And the sludge flows back to the front end of the pre-anoxic zone through the return sludge channel or the return sludge pipe.

According to the above aspects of the present disclosure, at the front end of the anoxic zone, sewage, return sludge, and nitrified liquid are mixed.

Nitrate in the nitrifying liquid takes BOD in inlet water as a carbon source to carry out denitrification reaction in the anoxic zone.

According to the above aspects of the present disclosure, an external carbon source feeding point is provided at the water inlet end of the anoxic zone, so that when the carbon/nitrogen ratio of the inlet water is insufficient, denitrification is ensured by feeding the external carbon source.

According to the above aspects of the disclosure, water outlets are arranged on the side walls on both sides of the water outlet end of the anoxic zone, and the water outlets are connected to the water inlet channel of the aeration zone.

And the water outlet of the anoxic zone enters the aeration zone through the water outlet and the water inlet channel.

According to the above aspects of the present disclosure, a submersible agitator is installed in the anoxic zone for mixing and preventing sludge from settling.

And a sludge concentration meter and an oxidation-reduction potential meter are arranged in the anoxic zone.

In the anoxic zone, dissolved oxygen is controlled to be less than 0.5 mg/l.

According to the above aspects of the present disclosure, the aeration zone is two, and the two aeration zones are respectively arranged on two sides of the anoxic zone.

And adding a suspension carrier filler into the aeration zone, and performing carbonization and nitration reaction by using the suspension activated sludge and the biological film attached to the suspension carrier filler.

According to the above aspects of the present disclosure, the depth of water in the aeration zone is 6 m.

A mesoporous aerator is installed in the aeration zone, and the mesoporous aerator is maintenance-free and replacement-free.

According to the above aspects of the present disclosure, a dissolved oxygen meter is installed in the aeration zone.

And an ammonia nitrogen instrument and a nitrate nitrogen instrument are arranged at the outlet end of the aeration zone.

In the aeration zone, the value of dissolved oxygen is controlled to be 4 to 6 mg/l.

According to the above aspects of the present disclosure, a water inlet channel is provided at the water inlet end of the aeration zone.

The delivery port is evenly seted up to the channel of intaking, the delivery port graticule mesh is installed to the delivery port for prevent that the interior suspension carrier of pond packs to follow through the channel of intaking the delivery port material of running. Or a partition wall is arranged at the water outlet of the water inlet channel of the aeration zone to prevent the suspended carrier filler in the aeration zone from entering the water inlet channel, a water outlet weir is arranged on the partition wall, and sewage in the water inlet channel turns over the water outlet weir to enter the aeration zone.

According to the various aspects of the disclosure, a concrete partition wall is arranged at the tail end of the aeration zone, circular water outlets are uniformly formed in the concrete partition wall, and each circular water outlet is provided with a columnar filler intercepting grid.

And the effluent of the aeration zone enters the degassing zone through the columnar filler interception grid and the water outlet.

The columnar filler intercepting grid is made of stainless steel, the diameter of the columnar filler intercepting grid is 700-900 mm, and a plurality of circular holes are formed in the columnar filler intercepting grid.

According to the above aspects of the present disclosure, a U-shaped aeration pipe is installed under each of the columnar filler intercepting grids, and the fillers are prevented from being accumulated at the columnar filler intercepting grids by aeration.

According to the above aspects of the present disclosure, the process system is provided with a process aeration blower room in which an aeration blower is installed.

The U-shaped aeration pipe is connected with the process air pipe.

An automatic air regulating valve and an air flow meter are arranged on the air inlet pipe of each aeration area and used for regulating the process air to uniformly and equivalently enter each aeration area.

According to the above aspects of the present disclosure, the degassing zone is two, and is disposed on two sides of the anoxic zone.

The degassing zone has a water depth of 2.5m to 3 m.

According to the above aspects of the present disclosure, the lower space of the degassing zone communicates with the nitrification liquid reflux channel in the anoxic zone.

And a water inlet weir is arranged at the water inlet end of the degassing area.

And the effluent of the aeration zone overflows into the degassing zone through the water inlet weir.

According to the above aspects of the present disclosure, a mesoporous aerator is installed in the degassing zone, and aeration is performed to form turbulent flow, so as to remove nitrogen in water.

And a plurality of water outlet pipes are arranged at the bottom of the outlet of each degassing area.

The outlet of the water outlet pipe is the water inlet end of the settling zone.

The degassed effluent enters the settling zone through the water outlet pipe.

And the sewage in the bottom space of the degassing zone enters the nitrifying liquid return channel through a communication port of the degassing zone.

According to the above aspects of the disclosure, two degassing areas are provided with one degassing fan, and the degassing fan adopts a roots fan.

According to the above aspects of the present disclosure, the settling zone is two, and is disposed on two sides of the anoxic zone.

Each settling zone is divided into two compartments.

The settling zone is rectangular, a sludge hopper is arranged at the bottom of the water inlet end of the settling zone, and the depth of the sludge hopper is 1 m.

And a slope is smeared at the bottom of the water inlet end of the settling zone, and the slope of the slope is 0.5% towards the sludge hopper.

The water depth in the settling zone is 4.7m to 5.5 m.

The bottom of each grid of the settling zone is provided with a chain type mud scraper, the middle part is provided with an inclined plate, and the upper part is provided with a clear water collecting tank.

According to the above aspects of the present disclosure, a suspended solids meter is installed at an outlet of the settling zone.

According to the above aspects of the present disclosure, a phosphorus removal agent feeding point is provided at an inlet of the settling zone, and chemical phosphorus removal is performed by feeding phosphorus removal agent, so as to improve the removal rate of total phosphorus.

According to the above aspects of the present disclosure, the settling zone is a horizontal flow inclined plate settling tank.

And the inlet water of the settling zone is guided by the guide wall to enter the lower part of the inclined plate for mud-water separation.

And scraping the separated sludge to the sludge hopper through the chain type sludge scraper.

The inclined plate is of a frame structure and is arranged on a transverse steel beam or a concrete beam.

According to the above aspects of the present disclosure, the sludge hopper is provided with a sludge collecting pipe, and sludge in the sludge hopper is discharged to the return sludge well by gravity.

The sludge hopper is provided with excess sludge pump pits, and two excess sludge pumps are arranged in each excess sludge pump pit and used for discharging excess sludge.

According to the aspects of the disclosure, the swash plate automatic flushing device is installed below the swash plate, and the swash plate is automatically cleaned periodically at regular time intervals.

According to the above aspects of the disclosure, the swash plate automatic flushing device adopts a gas washing mode.

The automatic flushing device of the inclined plate comprises a transverse air pipe, two longitudinal steel beams, two walking trolleys and two winches.

Two winches are respectively arranged at two ends of the top of the tank in the settling zone, one winch provides a steel wire rope to pull the travelling trolley to travel along the steel beam in a reciprocating manner, and the other winch provides a gas washing hose.

The air source of the inclined plate automatic flushing device is from the aeration blower or the degassing blower.

According to the above aspects of the present disclosure, the clarified water collection tank is uniformly distributed at the upper portion of the inclined plate.

The clear water collecting tank is U-shaped and made of stainless steel.

And the water outlet groove of the clarified water collecting groove adopts a rectangular weir crest.

According to the above aspects of the present disclosure, a common clear water channel is provided between the two settling zones, and the common clear water channel converges to collect and discharge the clear water in the clear water collecting tank to the outside.

In accordance with the above aspects of the present disclosure, the pre-anoxic zone, the anaerobic zone, and the anoxic zone are each rectangular.

The water depth of the pre-anoxic zone, the water depth of the anaerobic zone and the water depth of the anoxic zone are all 6-8 m.

The general idea of the present disclosure is to provide a combined denitrification and dephosphorization process system, which is provided with a pre-anoxic zone to remove nitrate in the return sludge, so as to ensure the biological dephosphorization effect; an anaerobic zone is arranged to enhance biological phosphorus removal; setting an anoxic zone, wherein the residence time of the anoxic zone is sufficient to ensure an anoxic reaction, and the total nitrogen of effluent reaches 10 mg/l; adding suspended carrier filler into an aeration zone (aerobic zone), and performing decarbonization and nitrification treatment by using activated sludge and a biological film attached to the filler, wherein the ammonia nitrogen in the effluent reaches 1.5mg/l (3mg/l) (the value of water temperature lower than 12 ℃ in brackets), the aeration volume is small, the occupied area is small, the construction cost is saved, and the decarbonization and nitrification capabilities are strong; the inclined plates are arranged in the sedimentation zone (secondary sedimentation tank), and the inclined plate sedimentation is adopted to ensure that the hydraulic load reaches 2 m/h. In addition, in order to prevent nitrogen released in water from floating in the sedimentation zone after aeration, a degassing zone is arranged behind the aeration zone, and the nitrogen in the water is removed by aeration.

The nitrogen and phosphorus removal aeration process system according to the disclosure is a compact biological treatment process system integrating a pre-anoxic zone, an oxygen-pressing zone, an anoxic zone, an aeration zone, a degassing zone and a settling zone, and has the functions of biological carbon removal, nitrification, denitrification nitrogen removal and phosphorus removal. The process system is matched with a complete Motor Control Center (MCC) and a Programmable Logic Controller (PLC). The process system adopts a rectangular pool shape and side-by-side arrangement, has compact structure, neat appearance and modular arrangement, thereby being easy to overall layout.

So that the manner in which the disclosure is made in detail herein can be better understood, and in which the contributions to the art may be better appreciated, the disclosure has been summarized rather broadly. There are, of course, embodiments of the disclosure that will be described below and which will form the subject matter of the claims appended hereto.

As such, those skilled in the art will appreciate that the conception upon which this disclosure is based may readily be utilized as a basis for the designing of other structures, methods and systems for carrying out the several purposes of the present disclosure. It is important, therefore, that the appended claims be regarded as including such equivalent constructions insofar as they do not depart from the spirit and scope of the present disclosure.

Drawings

The present disclosure will be better understood and its advantages will become more apparent to those skilled in the art from the following drawings. The drawings described herein are for illustrative purposes only of selected embodiments and not all possible implementations and are not intended to limit the scope of the present disclosure.

FIG. 1 shows a flow chart of a combined denitrification and dephosphorization process according to the present disclosure;

FIG. 2 is a schematic diagram of the overall layout of a combined denitrification and dephosphorization process system according to the disclosure.

Detailed Description

Specific embodiments according to the present disclosure are described in detail below with reference to the accompanying drawings.

A combined denitrification and dephosphorization process system according to the present disclosure comprises six parts, as shown in the process flow diagram of FIG. 1, namely a pre-anoxic zone 1, an anaerobic zone 2, an anoxic zone 3, an aeration zone 4, a degassing zone 5 and a precipitation zone 6 (secondary sedimentation tank). The sewage treatment process comprises the following steps: water intake → pre-anoxic zone 1 → anaerobic zone 2 → anoxic zone 3 → aeration zone 4 → degassing zone 5 → precipitation zone 6 → effluent. 30-50% of inlet water and return sludge enter the pre-anoxic zone 1, and nitrate in the return sludge is removed in the pre-anoxic zone 1. 70-50% of the inlet water enters the anaerobic zone 2. The effluent of the aeration zone 4 enters a degassing zone. Part of effluent (nitrified liquid) in the degassing zone 5 flows back to the anoxic zone 3, and nitrate is brought back to the anoxic zone 3 for denitrification treatment. The other part of the effluent of the degassing zone enters a precipitation zone 6. And refluxing the returned sludge in the settling zone 6 to the pre-anoxic zone 1, and discharging the residual sludge.

According to one embodiment of the present disclosure, as shown in fig. 2, a combined denitrification and dephosphorization process system is provided with a pre-anoxic zone 1, an anaerobic zone 2, an anoxic zone 3, an aeration zone 4, a degassing zone 5 and a precipitation zone 6.

The pre-anoxic zone 1, the anaerobic zone 2 and the anoxic zone 3 are all one and are arranged in the middle in series.

The aeration zone 4, degassing zone 5 and precipitation zone 6 are each two and arranged (side by side) on both sides of the pre-anoxic zone 1, anaerobic zone 2 and anoxic zone 3.

According to the above described embodiments of the present disclosure, the pre-anoxic zone 1 is arranged for receiving a portion of the influent water and return sludge from the settling zone 6 and arranged to remove nitrate from the return sludge.

According to the above various embodiments of the present disclosure, 30% to 50% of the feed water enters the front end of the pre-anoxic zone 1.

Return sludge canals or return sludge pipes (not shown) are provided on both sides of the pre-anoxic zone 1.

And the return sludge flows back to the front end of the pre-anoxic zone 1 through the return sludge channel or the return sludge pipe.

The effluent of the pre-anoxic zone 1 enters the anaerobic zone 2 from the upper part of its end partition (not shown).

According to the above-described various embodiments of the present disclosure, a submersible agitator (not shown) is installed in the pre-anoxic zone 1 for mixing and preventing sludge from settling.

An influent ammonia nitrogen instrument, a sludge concentration meter and an oxidation reduction potential instrument (not shown) are installed in the pre-anoxic zone 1.

In the pre-anoxic zone 1, the dissolved oxygen is controlled to be below 0.5 mg/l.

According to the above various embodiments of the present disclosure, the anaerobic zone 2 is arranged for receiving another portion of the feed water and the feed water from the pre-anoxic zone 1 and performing biological phosphorus removal.

According to the above various embodiments of the present disclosure, 50% to 70% of the influent water enters the upper portion of the anaerobic zone 2 through an influent pipe (not shown).

The bottom (not shown) of the end partition of the anaerobic zone 2 is perforated and the effluent of the anaerobic zone 2 enters the anoxic zone 3 from its bottom.

According to the above-described various embodiments of the present disclosure, a submersible agitator (not shown) is installed in the anaerobic zone 2 for mixing and preventing sludge sedimentation.

An oxidation-reduction potentiometer (not shown) is installed in the anaerobic zone 2.

In the anaerobic zone 2, the dissolved oxygen is controlled to be below 0.2 mg/l.

According to the above embodiments of the present disclosure, a nitrification liquid return channel (not shown) is provided at a middle position of the anoxic zone 3.

A nitrifying liquid reflux pump (not shown) is installed in the nitrifying liquid reflux channel, and the nitrifying liquid reflux pump is a wall-through pump.

A nitrifying liquid return pipe (not shown) is provided at an outlet of the nitrifying liquid return pump.

The outlet of the nitrifying liquid return pipe reaches the front end of the anoxic zone 3.

According to the above embodiments of the present disclosure, a return sludge well (not shown) is provided on each side of the anoxic zone 3 and near the settling zone 6.

One return sludge pump (not shown) is installed in each return sludge well, and the return sludge pump adopts an axial flow pump.

According to the above-described embodiments of the present disclosure, return sludge canals or return sludge pipes (not shown) are provided on both sides of the anoxic zone 3.

And the sludge flows back to the front end of the pre-anoxic zone 1 through the return sludge channel or the return sludge pipe.

In accordance with the above-described embodiments of the present disclosure, at the front end of the anoxic zone 3, sewage, return sludge, and nitrified liquid are mixed.

Nitrate in the nitrifying liquid takes BOD in inlet water as a carbon source to carry out denitrification reaction in the anoxic zone 3.

According to the above embodiments of the present disclosure, an external carbon source feeding point (not shown) is provided at the water inlet end of the anoxic zone 3, so that when the carbon/nitrogen ratio of the inlet water is insufficient, denitrification is ensured by feeding the external carbon source.

According to the above embodiments of the present disclosure, water outlets (not shown) are provided on the side walls of the anoxic zone 3 on both sides of the water outlet end, and the water outlets are connected to the water inlet channels (not shown) of the aeration zone 4.

The water outlet of the anoxic zone 3 enters the aeration zone 4 through the water outlet and the water inlet channel.

According to the above-described various embodiments of the present disclosure, a submersible agitator (not shown) is installed in the anoxic zone 3 for mixing and preventing sludge from settling.

A sludge concentration meter and an oxidation-reduction potentiometer (not shown) are installed in the anoxic zone 3.

In the anoxic zone 3, dissolved oxygen is controlled to be less than 0.5 mg/l.

According to each of the above embodiments of the present disclosure, the pre-anoxic zone 1, the anaerobic zone 2 and the anoxic zone 3 are all rectangular.

The water depth of the pre-anoxic zone 1, the water depth of the anaerobic zone 2 and the water depth of the anoxic zone 3 are all 6-8 m.

According to the above embodiments of the present disclosure, the aeration zone 4 is two and rectangular, and is disposed on two sides of the anoxic zone 3.

Suspension carrier fillers (not shown) are added into the aeration zone 4, and carbonization and nitration are carried out by using suspension activated sludge and biological films attached to the suspension carrier fillers.

According to the above various embodiments of the present disclosure, the depth of water in the aeration zone 4 is 6 m.

A mesoporous aerator (not shown) is installed in the aeration zone 4, which is maintenance-free and replacement-free.

According to the above-described various embodiments of the present disclosure, a dissolved oxygen meter (not shown) is installed in the aeration zone 4.

An ammonia nitrogen meter and a nitrate nitrogen meter (not shown) are installed at the outlet end of the aeration zone 4.

In the aeration zone 4, the amount of dissolved oxygen is controlled to be 4 to 6 mg/l.

According to the above embodiments of the present disclosure, a water inlet channel (not shown) is provided at the water inlet end of the aeration zone 4.

The delivery port is evenly seted up to the channel of intaking, delivery port graticule mesh (not shown) is installed to the delivery port for prevent that the interior suspension carrier filler from following through the channel of intaking the delivery port is run the material, perhaps sets up the partition wall in the play water department of the channel of intaking in aeration zone, in order to prevent that the interior suspension carrier filler of aeration zone from getting into the inlet channel, is provided with out the mill weir on the partition wall, and the interior sewage of inlet channel turns over out the mill weir and gets into aeration zone.

According to the above embodiments of the present disclosure, a concrete partition (not shown) is disposed at the end of the aeration zone 4, circular water outlets are uniformly formed on the concrete partition, and each circular water outlet is provided with a columnar filler intercepting grid (not shown).

The effluent of the aeration zone 4 enters the degassing zone 5 through the columnar filler interception grid and the water outlet.

The columnar packing intercepting grid is made of stainless steel, the diameter of the columnar packing intercepting grid is 700-900 mm, and a plurality of circular holes (not shown) are formed in the columnar packing intercepting grid.

According to the above-described respective embodiments of the present disclosure, a U-shaped aeration pipe (not shown) is installed under each of the columnar filler-intercepting grids, and the fillers are prevented from being piled up at the columnar filler-intercepting grids by aeration.

According to the above-described embodiments of the present disclosure, the process system is provided with a process aeration blower room (not shown) in which the aeration blower 7 is installed.

The U-shaped aeration pipe is connected to a process aeration blower room through a process air pipe (not shown).

An automatic air regulating valve and an air flow meter (not shown) are arranged on the air inlet pipe of each aeration zone 4 and used for regulating the process air to uniformly and equivalently enter each aeration zone.

According to the above embodiments of the present disclosure, the degassing zone 5 is two and rectangular, and is disposed on both sides of the anoxic zone 3.

The degassing zone 5 has a water depth of 2.5m to 3 m.

According to the above-described embodiments of the present disclosure, the lower space of the degassing zone 5 communicates with a nitrifying liquid return channel (not shown) in the anoxic zone 3.

The water inlet end of the degassing zone 5 is provided with a water inlet weir (not shown).

The effluent of the aeration zone 4 overflows through the water inlet weir into a degassing zone 5.

According to the above embodiments of the present disclosure, a central control aerator (not shown) is installed in the degassing zone 5, and the aeration forms turbulence to remove nitrogen from the water.

A plurality of water outlet pipes (not shown) are arranged at the bottom of the outlet of each degassing zone 5.

The outlet of the water outlet pipe is the water inlet end of the settling zone 6.

The degassed effluent enters the settling zone 6 through the water outlet pipe.

The sewage in the bottom space of the degassing zone 5 enters the nitrifying liquid return channel through the communication port of the degassing zone 5.

According to the above embodiments of the present disclosure, two degassing zones 5 are provided with one degassing fan (not shown), and the degassing fan is a roots fan.

According to the above embodiments of the present disclosure, the settling zone 6 is two, and is respectively disposed at two sides of the anoxic zone 3.

The settling zone 6 is rectangular, and each settling zone 6 is divided into two grids.

The bottom of the water inlet end of the settling zone 6 is provided with a sludge hopper (not shown), and the depth of the sludge hopper is 1 m.

And a slope is smeared at the bottom of the water inlet end of the settling zone 6, and the slope of the slope is 0.5% towards the sludge hopper.

The water depth in the settling zone 6 is 4.7m to 5.5 m.

The bottom of each grid of the settling zone 6 is provided with a chain type mud scraper, the middle part is provided with an inclined plate, and the upper part is provided with a clear water collecting tank (not shown).

According to the above-described various embodiments of the present disclosure, a suspended solids meter (not shown) is installed at the outlet of the settling zone 6.

According to the above embodiments of the present disclosure, a phosphorus removal agent feeding point (not shown) is disposed at the inlet of the settling zone 6, and chemical phosphorus removal is performed by feeding phosphorus removal agent, so as to improve the removal rate of total phosphorus.

According to the above embodiments of the present disclosure, the settling zone 6 is a horizontal inclined plate settling tank.

The inlet water of the settling zone 6 is guided by a guide wall to enter the lower part of the inclined plate (not shown) for mud-water separation.

The swash plate is of a frame type construction and is mounted on a transverse steel or concrete beam (not shown).

According to the above-described various embodiments of the present disclosure, the sludge hopper is provided with a sludge collecting pipe (not shown), and sludge in the sludge hopper is discharged to the return sludge well by gravity.

The sludge hopper is provided with excess sludge pump pits (not shown), and two excess sludge pumps (not shown) are installed in each excess sludge pump pit for discharging excess sludge.

According to the above embodiments of the present disclosure, an automatic flushing device (not shown) is installed under the swash plate, and the swash plate is automatically cleaned periodically.

According to the above embodiments of the present disclosure, the swash plate automatic flushing device adopts a gas washing mode.

The automatic flushing device of the inclined plate comprises a transverse air pipe, two longitudinal steel beams, two walking trolleys and two winches (not shown).

Two winches are respectively arranged at two ends of the top of the tank of the settling zone 6, one winch provides a steel wire rope to pull the walking trolley to walk back and forth along the steel beam, and the other winch provides a gas washing hose (not shown).

The air source of the inclined plate automatic flushing device is from the aeration blower or the degassing blower (not shown).

According to the above-described respective embodiments of the present disclosure, at the upper portion of the inclined plate is the clarified water collection tank (not shown) which is uniformly distributed.

The clear water collecting tank is U-shaped and made of stainless steel.

The outlet trough of the clarified water collection trough employs a rectangular weir (not shown).

According to the above-described respective embodiments of the present disclosure, a common clarified water channel (not shown) is provided between the two sedimentation zones 6, and the common clarified water channel converges to collect the clarified water in the clarified water collecting tank and is discharged outside.

The foregoing disclosure provides illustration and description, but is not intended to be exhaustive or to limit the embodiments to the precise form disclosed. Modifications and variations are possible in light of the above disclosure or may be acquired from practice of the embodiments.

Even though particular combinations of features are recited in the claims and/or disclosed in the specification, these combinations are not intended to limit the disclosure of the various embodiments. In fact, many of these features may be combined in ways not specifically recited in the claims and/or disclosed in the specification. Although each dependent claim listed below may depend directly on only one claim, the disclosure of various embodiments includes each dependent claim in combination with every other claim in the claim set.

No element, act, or instruction used herein should be construed as critical or essential unless explicitly described as such. In addition, as used herein, the articles "a" and "an" are intended to include one or more items, and may be used interchangeably with "one or more". Further, as used herein, the article "the" is intended to include the incorporation of one or more items referenced by the article "the" and may be used interchangeably with "one or more". Further, as used herein, the term "set" is intended to include one or more items (e.g., related items, unrelated items, combinations of related and unrelated items, etc.) and may be used interchangeably with "one or more". Where only one item is intended, the phrase "only one item" or similar language is used. In addition, as used herein, the term "having," variants thereof, and the like are intended to be open-ended terms. Further, the phrase "based on" is intended to mean "based, at least in part, on" unless explicitly stated otherwise. In addition, as used herein, the term "or" when used in series is intended to be inclusive and may be used interchangeably with "and/or" unless specifically stated otherwise (e.g., if used in conjunction with "or" only one of ").

Claims

1. A combined process system for nitrogen and phosphorus removal, which is characterized in that,

the process system is provided with a pre-anoxic zone, an anaerobic zone, an anoxic zone, an aeration zone, a degassing zone and a precipitation zone;

the pre-anoxic zone, the anaerobic zone and the anoxic zone are arranged in the middle;

the aeration zone, degassing zone and settling zone are disposed on either side of the pre-anoxic zone, anaerobic zone and anoxic zone.

2. The process system of claim 1,

the pre-anoxic zone is arranged for receiving a portion of the influent water and return sludge from the settling zone and is arranged to remove nitrate from the return sludge.

3. The process system of claim 2,

30 to 50 percent of inlet water enters the front end of the pre-anoxic zone;

a return sludge channel or a return sludge pipe is arranged on two sides of the pre-anoxic zone;

returning sludge flows back to the front end of the pre-anoxic zone through the returning sludge channel or the returning sludge pipe;

4. The process system of claim 3,

installing a submersible agitator in the pre-anoxic zone for mixing and preventing sludge from settling;

a water inlet ammonia nitrogen instrument, a sludge concentration meter and an oxidation reduction potential instrument are arranged in the pre-anoxic zone;

5. The process system of claim 3,

the anaerobic zone is configured to receive another portion of the influent water and the influent water from the pre-anoxic zone and to perform biological phosphorus removal.

6. The process system of claim 5,

50 to 70 percent of inlet water enters the upper part of the anaerobic zone through a water inlet pipe;

7. The process system of claim 6,

installing a submersible agitator in the anaerobic zone for mixing and preventing sludge settling;

installing an oxidation-reduction potentiometer in the anaerobic zone;

in the anaerobic zone, dissolved oxygen is controlled to be below 0.2 mg/l.

8. The process system of claim 6,

a nitrifying liquid backflow channel is arranged at the middle position of the anoxic zone;

a nitrifying liquid reflux pump is installed in the nitrifying liquid reflux channel, and the nitrifying liquid reflux pump is a wall-through pump;

a nitrifying liquid return pipe is arranged at the outlet of the nitrifying liquid return pump;

9. The process system of claim 8,

a return sludge well is respectively arranged at the two sides of the anoxic zone and close to the sedimentation zone;

10. The process system of claim 9,

a return sludge channel or a return sludge pipe is arranged on two sides of the anoxic zone;

the return sludge pump sends sludge to the return sludge channel or the return sludge pipe;

11. The process system of claim 10,

mixing sewage, return sludge and nitrifying liquid at the front end of the anoxic zone;

12. The process system of claim 11,

and an external carbon source adding point is arranged at the water inlet end of the anoxic zone, so that when the carbon/nitrogen ratio of inlet water is insufficient, nitrogen removal is ensured by adding the external carbon source.

13. The process system of claim 12,

water outlets are arranged on the side walls on the two sides of the water outlet end of the anoxic zone and are connected to the water inlet channel of the aeration zone;

14. The process system of claim 13,

installing a submersible agitator in the anoxic zone for mixing and preventing sludge from settling;

a sludge concentration meter and an oxidation-reduction potential meter are arranged in the anoxic zone;

in the anoxic zone, dissolved oxygen is controlled to be less than 0.5 mg/l.

15. The process system of claim 13,

the aeration zone is divided into two parts which are respectively arranged at two sides of the anoxic zone;

16. The process system of claim 15,

the depth of water in the aeration zone is 6 m;

17. The process system of claim 16,

installing a dissolved oxygen instrument in the aeration zone;

an ammonia nitrogen instrument and a nitrate nitrogen instrument are arranged at the outlet end of the aeration zone;

18. The process system of claim 17,

a water inlet channel is arranged at the water inlet end of the aeration zone;

the delivery port is evenly seted up to the channel of intaking, delivery port graticule mesh is installed to the delivery port for prevent that the interior suspension carrier filler from following through the channel of intaking the delivery port material of running, perhaps set up the partition wall in the delivery water department of the channel of intaking in aeration zone, in order to prevent that the suspension carrier filler in the aeration zone from getting into the inlet channel, be provided with out the mill weir on the partition wall, the interior sewage of inlet channel turns over out the mill weir and gets into aeration zone.

19. The process system of claim 18,

arranging a concrete partition wall at the tail end of the aeration area, uniformly arranging round water outlets on the concrete partition wall, and mounting a columnar filler intercepting grid at each round water outlet;

the effluent of the aeration zone enters the degassing zone through the columnar filler interception grid and the water outlet;

20. The process system of claim 19,

and a U-shaped aeration pipe is arranged below each columnar filler interception grid, and fillers are prevented from being accumulated at the columnar filler interception grid through aeration.

21. The process system of claim 20,

the process system is provided with a process aeration blower room, and an aeration blower is arranged in the process aeration blower room;

the U-shaped aeration pipe is connected with a process air pipe;

22. The process system of claim 21,

the degassing area is divided into two parts which are respectively arranged at two sides of the anoxic area;

the degassing zone has a water depth of 2.5m to 3 m.

23. The process system of claim 22,

the lower space of the degassing zone is communicated with a nitrifying liquid return channel in the anoxic zone;

a water inlet weir is arranged at the water inlet end of the degassing area;

and the effluent of the aeration zone overflows into a degassing zone through the water inlet weir.

24. The process system of claim 23,

a mesoporous aerator is arranged in the degassing zone, and is aerated to form turbulent flow so as to remove nitrogen in water;

a plurality of water outlet pipes are arranged at the bottom of an outlet of each degassing area;

the outlet of the water outlet pipe is the water inlet end of the settling zone;

the degassed effluent enters the settling zone through the water outlet pipe;

25. The process system of claim 24,

and the two degassing areas are provided with a degassing fan which adopts a Roots fan.

26. The process system of claim 25,

the two sedimentation zones are respectively arranged at two sides of the anoxic zone;

each precipitation zone is divided into two grids;

the sedimentation zone is rectangular, a sludge hopper is arranged at the bottom of the water inlet end of the sedimentation zone, and the depth of the sludge hopper is 1 m;

a slope is smeared at the bottom of the water inlet end of the settling zone, and the slope of the slope is 0.5 percent towards the sludge hopper;

the water depth in the settling zone is 4.7m to 5.5 m;

27. The process system of claim 26,

and a suspended solid measuring instrument is arranged at the outlet of the settling zone.

28. The process system of claim 27,

and a phosphorus removing agent adding point is arranged at the inlet of the settling zone, and the phosphorus removing agent is added to carry out chemical phosphorus removal, so that the removal rate of the total phosphorus is improved.

29. The process system of claim 28,

the sedimentation zone is a horizontal flow type inclined plate sedimentation tank;

the inlet water of the settling zone is guided by a guide wall to enter the lower part of the inclined plate for mud-water separation;

the separated sludge is scraped to the sludge hopper through the chain type sludge scraper;

30. The process system of claim 29,

the sludge hopper is provided with a sludge collecting pipe, and sludge in the sludge hopper is discharged to a return sludge well through gravity;

31. The process system of claim 30,

an automatic inclined plate flushing device is arranged below the inclined plate, and the inclined plate is automatically cleaned regularly.

32. The process system of claim 31,

the automatic inclined plate flushing device adopts a gas washing mode;

the automatic flushing device of the inclined plate comprises a transverse air pipe, two longitudinal steel beams, two walking trolleys and two winches;

two winches are respectively arranged at two ends of the top of the tank in the settling zone, one winch provides a steel wire rope to pull the travelling trolley to travel back and forth along the steel beam, and the other winch provides a gas washing hose;

33. The process system of claim 32,

the upper part of the inclined plate is provided with the clarified water collecting tanks which are uniformly distributed;

the clear water collecting tank is U-shaped and made of stainless steel;

34. The process system of claim 33,

and a public clarifying channel is arranged between the two sedimentation areas, and the public clarifying channel converges and collects the clarified water in the clarified water collecting tank and discharges the clarified water outwards.

35. The process system of claim 1,

the pre-anoxic zone, the anaerobic zone and the anoxic zone are rectangular;