CN109354175B

CN109354175B - Efficient autotrophic nitrogen removal system for treating high-ammonia-nitrogen wastewater and operation method

Info

Publication number: CN109354175B
Application number: CN201811477781.8A
Authority: CN
Inventors: 韩文杰; 吴迪; 周家中; 管勇杰
Original assignee: Qingdao Si Purun Water Treatment Limited-Liability Co
Current assignee: Qingdao Si Purun Water Treatment Limited-Liability Co
Priority date: 2018-12-05
Filing date: 2018-12-05
Publication date: 2020-03-06
Anticipated expiration: 2038-12-05
Also published as: CN109354175A

Abstract

The invention discloses a high-efficiency autotrophic nitrogen removal system for treating high-ammonia-nitrogen wastewater and an operation method thereof, belonging to the technical field of biological nitrogen removal of wastewater. The method solves the problems that the related system in the prior art needs large occupied area, has excessive inoculation amount, long starting time, low denitrification load, poor impact resistance, is easily influenced by water inlet organic matters and the like. The invention combines pure membrane denitrification with one-stage autotrophic nitrogen removal of a sludge membrane, a denitrification tank is arranged in front, the autotrophic nitrogen removal is arranged in back, and effluent flows back; the invention can realize three operation modes, namely a parallel operation mode, a double-series A operation mode and a double-series B operation mode, and realizes the series, parallel or independent operation of the reaction tanks by controlling the water outlet directions of the four reaction tanks through the communicating valves; the rapid starting of the process is realized by means of inoculation, feeding and the like; different process arrangement forms are realized according to the treatment requirements. The invention has the advantages of small land occupation, small inoculation ratio, quick start, high denitrification load, strong impact resistance, good tolerance to influent organic matters and the like.

Description

Efficient autotrophic nitrogen removal system for treating high-ammonia-nitrogen wastewater and operation method

Technical Field

The invention belongs to the technical field of biological denitrification of wastewater, and particularly relates to a high-efficiency autotrophic denitrification system for treating high-ammonia-nitrogen wastewater and an operation method.

Background

The autotrophic nitrogen removal technology is a novel nitrogen removal process which is developed rapidly in recent years, and is concerned by researchers in the field of biological nitrogen removal of wastewater all over the world, and compared with the traditional nitrification and denitrification, the autotrophic nitrogen removal technology can save 62.5% of oxygen supply and energy consumption and 100% of organic carbon source addition, so that the autotrophic nitrogen removal technology is considered as the most economic and effective biological nitrogen removal mode for wastewater. In the one-stage autotrophic nitrogen removal process, nitrite oxidizing bacteria (AOB) and anaerobic ammonium oxidizing bacteria (AnAOB) are enriched in the same reactor through oxygen limitation, and efficient nitrogen removal is achieved through the synergistic effect of two functional microorganisms. However, AOB and AnAOB are autotrophic microorganisms, the generation cycle is long, the growth is slow, the actual starting time in engineering application is too long, in addition, the theoretical total nitrogen removal rate of the autotrophic nitrogen removal process is 89%, and the effluent water reaching the standard may not be guaranteed for projects with high requirements on the total nitrogen of the effluent water.

In order to further improve the total nitrogen removal rate, the denitrification coupling autotrophic nitrogen removal technology is widely concerned by people, the main process forms are pre-denitrification and post-denitrification, most of wastewater contains a part of organic carbon source in inlet water, when the post-combination form is utilized, organic matters enter the autotrophic nitrogen removal stage firstly, and may affect the autotrophic nitrogen removal stage, so that researchers can pre-arrange the denitrification stage and set outlet water backflow to realize the removal of nitrate and organic matters in the first stage, compared with the post-denitrification, the combination form is easier to control the outlet water organic matters, can remove most of organic matters through the regulation and control of aeration amount or dissolved oxygen in an autotrophic nitrogen removal zone and improve the total nitrogen removal rate, however, most of the prior pre-denitrification processes adopt granular sludge or anoxic sludge, and the outlet water needs to be subjected to mud-water separation, the long-term operation easily leads to the sludge output too big, needs often to arrange mud, and in addition, mud easily gets into follow-up processing system along with the play water and produces the influence to follow-up technology, and takes place the mud inflation phenomenon easily, therefore is difficult to long-term stable operation. Compared with the activated sludge process, the pre-denitrification process of the biofilm process has richer microbial community and more stable species diversity; after the biomembrane falls off, flocs with larger particles and good settling property are easily formed, and the biomembrane has good settling property and is easy to separate solid from liquid; in addition, the biofilm method generally does not need sludge backflow, has low energy consumption, is easy to maintain and manage and does not have the sludge bulking problem. Is limited by the technical bottleneck required by the starting and stable operation of the pure membrane denitrification process, and the pure membrane denitrification process is still lack of large-scale engineering application so far.

Because two functional microorganisms of autotrophic nitrogen removal, namely AOB and AnAOB, grow very slowly, have long multiplication time, are difficult to maintain high biological concentration, and the AnAOB is extremely easy to be influenced by inhibiting factors such as organic matters in inlet water and the like to reduce the activity, the current research on the one-stage autotrophic nitrogen removal related process mostly stays at the laboratory level; the AOB is aerobic bacteria, the AnAOB is anaerobic bacteria, too high dissolved oxygen can inhibit the AnAOB, too low dissolved oxygen can not ensure the conversion of ammonia nitrogen to nitrite, and the too low nitrite can cause the deficiency of the AnAOB matrix and inhibit the growth. In addition, the current one-stage autotrophic nitrogen removal process system mostly adopts a suspended state granular sludge form or an attached state biological membrane form, the autotrophic nitrogen removal granular sludge has low tolerance to dissolved oxygen (mostly below 1 mg/L), and slightly high dissolved oxygen is easy to inhibit the ANAOB, even the system is collapsed. In addition, the granular sludge process is difficult to realize the synergy between the nitrification performance of flocculent sludge and the activity of anaerobic ammonium oxidation bacteria of granular sludge, and meanwhile, the sludge floating upwards causes the falling of the anaerobic ammonium oxidation bacteria and the deterioration of the system performance. In addition, the AOB has strong occupation on ecological sites of attached carriers and poor adhesive force, and can be peeled off from the biological membrane by slightly high hydraulic shearing, which is also a reason that the total nitrogen removal load can not stably rise because the autotrophic nitrogen removal process mostly adopting the biological membrane method is finally limited by nitrosation effect after long-time operation. The MBBR combines the autotrophic nitrogen removal process system of activated sludge to divide AOB and AnAOB on activated sludge and MBBR filler, not only can reach higher total nitrogen removal load, but also has certain impact resistance.

The research reports of the related aspects of the prior art mainly include:

liuyang et al (Liuyang, Chengxiang, R.Lemaire. autotrophic denitrogenation ANITAMox MBBR and IFAS operation starting experience [ J)]China water supply and drainage, 2017(22): 38-42) develops an IFAS process combining suspended activated sludge and fixed biological membranes, and the concentration of dissolved oxygen required by the operation of the IFAS process is 0.2-0.5 mg/L. Actual operation data show that the TN of the modified polycarbonate resin can remove the surface load up to 2.2 kgN/(m)³D). However, the C/N of the inlet water of the process is only 0.17, and no data support is provided for the denitrification effect of the water quality with high C/N ratio, in addition, the process has no nitrate nitrogen removal facility, the nitrate nitrogen of the outlet water is directly discharged, and the feasibility of the engineering project with high requirement on the outlet water is poor.

Staring of integrated anaerobic ammonium oxidation process for treating high ammonia nitrogen sludge digestive liquid [ J]Chinese environmental science 2015, 35: (4) 1082-1087.) a novel fixed biological membrane-activated sludge reactor is adopted to treat actual sludge digestive juice, the ammonia nitrogen concentration of inlet water is gradually increased and the dissolved oxygen concentration is controlled to be 0.11-0.42 mg/L by inoculating shortcut nitrification sludge and anaerobic ammonium oxidation biological membrane filler, and the system realizes the starting of the shortcut nitrification-anaerobic ammonium oxidation reaction within 65 days. The COD and ammonia nitrogen concentration of the inlet water are 921 and 1120.8mg/L, and the removal rates of the COD, the ammonia nitrogen and the total nitrogen are 66.8%, 99.0% and 94.4% respectively. The method starts the reactor only by taking the concentration of the ammonia nitrogen in the effluent as a standard, the HRT of the reactor is longer, the reactor control is not carried out aiming at the removal load of TN, and the total nitrogen removal load is only 0.27 kgN/(m) after stable operation³D), and the digestive juice is gradually diluted by water distribution in the starting process of the device to be used as the water inlet of the reactor, so the process is complicated, and the feasibility of the practical engineering project is poor.

Wanggang et al (Wanggang. simultaneous nitrosation/anaerobic ammoxidation/denitrification (SNAD) technology-based sludge digestion liquid denitrification process research [ D)]University of continental managerial work, 2017.) the actual engineering sludge digestion liquid is treated by starting the serial nitrosation-anammox and then starting the SNAD, the nitrosation process is started by debugging the starting nitrosation process, stable effluent suitable for the anammox process is obtained, the anammox sludge and the biofilm formation MBBR filler pre-cultured by the other two pilot reactors (providing seed sludge and biofilm formation filler respectively) are inoculated into the anammox tank in batches, after the anammox tank is cultured to obtain more anammox sludge, the nitrosation tank sludge and the sludge and filler of the anammox tank are mixed, and the SNAD integrated process is started by the two tanks. The SNAD tank has the filling rate of 35 percent, 20kg of anaerobic ammonia oxidation sludge (dry weight) is inoculated to the anaerobic ammonia oxidation tank in the whole starting process, the calculated sludge concentration is 200mg/L, and the biofilm formation filler is 25m³The inoculation rate of the filler is calculated to be about 9%, the time from starting to obtaining stable series nitrosation-anaerobic ammoxidation exceeds 340d, the integral SNAD starting is completed within two months, the total starting time is about 400d, the total nitrogen removal rate is about 70%, and the DO of the SNAD pool is 0.3-0.8mg/L after the starting is successful. The starting method has a complex process, and two pilot reactors are required to continuously inoculate the seed sludge and the biofilm formation filler for engineering projectsLong time consumption, low total nitrogen removal rate, large demand for seed source biomass, and difficulty in realizing large-scale amplification of multiple projects for a long time.

Startup and operation of Li Huibo et al (Li Huibo, Wang Yinshuang, Dingjuan et al, ANITA Mox autotrophic Denitrification MBBR reactor [ J]China water supply and drainage, 2014,30(5): 1-5), and starting a CANON process by using an inoculation method to treat anaerobic sludge digestion liquid. 3% total area of seeded packing Start-Up 50m³The reactor (2) is operated for 120 days (without short-cut nitrification starting), and the total nitrogen removal volume load in the stabilization period is 0.7-1.1 kgN/(m)³D) calculated to have a TN removal surface load of 1.29 to 2.05 gN/(m)²D). The technology has low inoculation rate and quick start time, but NH removed by the system in a stable period₄ ⁺-N and NO formed₃ ^-The proportion of-N is 8-15%, and has a certain difference with chemical fixed ratio (11%), and generally, the system inlet water contains certain BOD₅This ratio is small due to the occurrence of denitrification, but is large due to the presence of Nitrite Oxidizing Bacteria (NOB) in the system, and it is noted that the presence of NOB competes with ANAOB for nitrite substrates, resulting in a system breakdown due to lack of suitable substrate ratio for ANAOB; in addition, the ammonia nitrogen concentration of the inlet water used by the technology is high, the water quantity is large, the total nitrogen removal load is not low, but the ammonia nitrogen concentration of the outlet water still reaches about 150mg/L and cannot approach to the higher treatment requirement.

CN108083581A discloses a low-energy-consumption autotrophic nitrogen removal municipal sewage treatment system and method, wherein a serial anaerobic decarburization-autotrophic nitrogen removal mode is adopted to inoculate excess sludge of a sewage treatment plant to start an anaerobic decarburization reactor, the start-up process of the anaerobic decarburization reactor needs 60-90d, then the start-up autotrophic nitrogen removal reactor needs to inoculate 3000mg/L anaerobic ammonia oxidation sludge in a whole tank to carry out early-stage anaerobic start, manual water distribution meets the requirement of anaerobic ammonia oxidation bacteria on a substrate, the start-up process of the reactor needs 90-120d, the start-up process of the whole process needs 150 d and 210d, the preposed anaerobic decarburization tank adopts a sludge system, sludge easily enters a post-stage treatment system after long-term operation, the whole process is influenced and easily expands, in addition, the method has overlarge demand on anaerobic ammonia oxidation bacteria, high inoculation difficulty and is difficult to realize large-scale expansion of a plurality of projects for a long time, the anaerobic ammonium oxidation strain which is successfully started by early-stage artificial water distribution has certain risk on the adaptation of actual waste water.

CN108585202A discloses a process for treating domestic sewage by realizing partial shortcut nitrification, sludge fermentation coupling denitrification and anaerobic ammonia oxidation in a sequencing batch reactor, and the method relates to the starting of autotrophic nitrogen removal: inoculating sponge filler with a film hung in a laboratory shortcut nitrification anaerobic ammonia oxidation integrated reactor, mixing the sponge filler with blank filler, and then fixedly adding the mixture into the reactor, wherein the filling ratio is 40%, and water is used for water distribution. The method also has overlarge requirement on the biomass of the provenance microorganism, cannot meet the starting of large-volume engineering projects, is operated by water distribution in the starting process, cannot predict whether the cultured autotrophic nitrogen removal functional microorganism can use the actual engineering water quality, and the sponge filler is easy to wear in the actual operation process, and when the biofilm forms a certain thickness, the blockage is easy to occur to influence mass transfer or the filler becomes heavy to block fluidization.

CN106630143 discloses an integrated reactor and denitrification method for pre-denitrification completely autotrophic denitrification, the reactor adopted is provided with an aerobic zone, an anoxic zone and an anaerobic zone to respectively culture nitrosobacteria, short-range denitrifying bacteria and anaerobic ammonium oxidation bacteria, the reflux of the experimental mixed liquid is performed through an air-lift device, the short-range denitrification adopted by the reactor controls the reflux of the nitrate nitrogen to be converted into a nitrite step, the requirement on water quality is high, the COD of the inlet water is too much or the retention time of the waterpower is too long, the whole-range denitrification can damage the balance of the reactor, the device is provided with the aerobic zone, the anoxic zone and the anaerobic zone in the same reactor, the actual control is complex, the proper conditions of each reaction zone are difficult to ensure, in addition, the reflux ratio cannot be controlled at will according to the water quality by adopting the air-lift device, and the practicability is poor.

Disclosure of Invention

In order to solve the technical defects in the prior art, the invention provides a high-efficiency autotrophic nitrogen removal system and an operation method for treating high-ammonia nitrogen wastewater, wherein the water outlet directions of four reaction tanks are controlled by a communication valve so as to realize the serial connection, parallel connection or independent operation of the reaction tanks, the quick start of an autotrophic nitrogen removal process is realized by means of inoculation, flow addition and the like, the sludge age of autotrophic microorganisms is prolonged by sludge backflow, more effective strain biomass in a reactor is maintained, and different process arrangement forms can be realized according to treatment standard requirements.

In order to achieve the above purpose, the technical problem to be overcome is as follows:

how to start the nitrosation and denitrification sludge membrane process at the same time by using a rapid sludge discharge method within a short period of time, reduce the inoculation proportion under the condition of limited seed sources, realize the rapid start of the autotrophic nitrogen removal system by controlling stirring, dissolved oxygen, aeration, different process arrangement forms and the like through a fed-batch method, achieve higher TN removal load and reduce the occupied area of a reaction device; how to control the opening of the communicating valve, the water inlet valve and the like and realize different process arrangement forms, thereby achieving different treatment standards and realizing the long-term stable operation of the system.

One of the tasks of the invention is to provide a high-efficiency autotrophic nitrogen removal system for treating high-ammonia nitrogen wastewater.

In order to solve the technical problems, the invention adopts the following technical scheme:

a high-efficiency autotrophic nitrogen removal system for treating high-ammonia-nitrogen wastewater comprises a central well, a reaction tank main body, a sludge reflux device, a mixed liquid reflux device, a communication device and an aeration device, wherein the reaction tank main body comprises two rows of four reaction tanks, namely a first reaction tank, a second reaction tank, a third reaction tank and a fourth reaction tank, wherein the first reaction tank and the fourth reaction tank are arranged in one row and positioned at the bottom;

the central well is positioned at the center of the diagonal connection line of the four reaction tanks and comprises a denitrification tank, a water distribution well, a water outlet well and a sedimentation tank, wherein the four reaction tanks are concentric tank bodies and are the denitrification tank, the water distribution well, the water outlet well and the sedimentation tank from inside to outside in sequence;

a water inlet of the denitrification tank is connected with a total water inlet pipeline, sewage to be treated enters the bottom of the denitrification tank through the total water inlet pipeline, and an interception screen is arranged at the upper part of the denitrification tank; sewage to be treated enters the distribution well through an interception screen on the upper part of the tank body of the denitrification tank, the distribution well is communicated with each reaction tank and is used for feeding water into each reaction tank, and a first sludge discharge port is formed in the bottom of the distribution well; the sedimentation tank is used for collecting effluent of the four reaction tanks and discharging the effluent into an effluent well through the upper part of the sedimentation tank, and a second sludge discharge port is arranged at the bottom of the sedimentation tank; a water outlet at the upper part of the water outlet well is connected with a main water outlet pipeline, and outlet water is discharged through the main water outlet pipeline; an intercepting screen is arranged at the water outlet of each reaction tank;

the first reaction tank and the second reaction tank, the second reaction tank and the third reaction tank, the third reaction tank and the fourth reaction tank, and the fourth reaction tank and the first reaction tank are respectively connected through a first connecting pipeline, a second connecting pipeline, a third connecting pipeline and a fourth connecting pipeline;

the communication device comprises a communication valve, and the communication valve comprises a first communication valve positioned on the first connecting pipeline, a second communication valve positioned on the second connecting pipeline, a third communication valve positioned on the third connecting pipeline and a fourth communication valve positioned on the fourth connecting pipeline; a first water inlet and a fourth water inlet are respectively arranged above the first reaction tank and the fourth reaction tank close to the central well, a second water inlet and a third water inlet are respectively arranged below the second reaction tank and the third reaction tank close to the central well, and water is respectively fed into the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank through the first water inlet, the second water inlet, the third water inlet and the fourth water inlet;

stirring devices are arranged in the denitrification tank and each reaction tank;

the bottom of the sedimentation tank is provided with a first sludge return pipe, a second sludge return pipe, a third sludge return pipe and a fourth sludge return pipe, and the other ends of the first sludge return pipe, the second sludge return pipe, the third sludge return pipe and the fourth sludge return pipe are respectively introduced into the bottoms of the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank; the sludge reflux device comprises a first sludge reflux pump, a second sludge reflux pump, a third sludge reflux pump, a fourth sludge reflux pump and a water distribution well reflux pump, wherein the first sludge reflux pump, the second sludge reflux pump, the third sludge reflux pump and the fourth sludge reflux pump are positioned at the bottom of the sedimentation tank and are respectively connected with the first sludge reflux pipe, the second sludge reflux pipe, the third sludge reflux pipe and the fourth sludge reflux pipe;

the mixed liquid reflux device comprises a mixed liquid reflux pump which is arranged on a reflux pipe connected with the upper part of the sedimentation tank, and the other end of the reflux pipe is introduced into the denitrification tank;

the aeration devices are distributed in each reaction tank, and suspension carriers are added into the denitrification tank and each reaction tank.

The beneficial technical effect that above-mentioned technical scheme brought is, realize the control to every reaction tank play water direction through above-mentioned intercommunication device. Three different control modes different from the prior art can be realized, namely: the reaction tanks are connected in series, parallel or independently operated by controlling the water outlet directions of the first reaction tank to the fourth reaction tank, and the three control modes are adopted, so that the system has the advantages of small occupied area, small inoculation proportion, quick start, high denitrification efficiency, good tolerance to water inlet organic matters and strong impact resistance. The specific beneficial technical effects are shown in the specific implementation mode of the specification.

As a preferred aspect of the present invention, the first water inlet, the second water inlet, the third water inlet and the fourth water inlet are respectively connected to the water distribution well through a first water inlet pipeline, a second water inlet pipeline, a third water inlet pipeline and a fourth water inlet pipeline, the first water inlet pipeline is provided with a first water inlet valve, the second water inlet pipeline is provided with a second water inlet valve, the third water inlet pipeline is provided with a third water inlet valve, and the fourth water inlet pipeline is provided with a fourth water inlet valve; the interception screen meshes positioned at the water outlet of each reaction tank comprise a first interception screen mesh positioned in the first reaction tank, a second interception screen mesh positioned in the second reaction tank, a third interception screen mesh positioned in the third reaction tank and a fourth interception screen mesh positioned in the fourth reaction tank.

As another preferable scheme of the invention, the aeration device in each reaction tank consists of a plurality of groups of perforated aeration pipes and microporous aeration pipes.

Furthermore, the water outlet ends of the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank are respectively connected with the sedimentation tank through a first water outlet pipeline, a second water outlet pipeline, a third water outlet pipeline and a fourth water outlet pipeline, and a first water outlet valve, a second water outlet valve, a third water outlet valve and a fourth water outlet valve are correspondingly arranged on the first water outlet pipeline, the second water outlet pipeline, the third water outlet pipeline and the fourth water outlet pipeline.

Furthermore, the first water outlet pipeline, the second water outlet pipeline, the third water outlet pipeline and the fourth water outlet pipeline are respectively connected with the sedimentation tank through a first muddy water buffer plate, a second muddy water buffer plate, a third muddy water buffer plate and a fourth muddy water buffer plate, and the first muddy water buffer plate, the second muddy water buffer plate, the third muddy water buffer plate and the fourth muddy water buffer plate are all located on the lower portion of the sedimentation tank.

The invention also aims to provide an operation method of the high-efficiency autotrophic nitrogen removal system for treating the high-ammonia-nitrogen wastewater, which comprises the following three control modes:

first, parallel operating mode:

the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank are in parallel relation, each reaction tank independently feeds water and independently discharges water, the discharged water is converged into the sedimentation tank by controlling a relevant valve, part of discharged water in the sedimentation tank flows back to the denitrification tank, the rest of discharged water is discharged from a main water outlet pipeline through a water outlet well, and the first sludge reflux pump, the second sludge reflux pump, the third sludge reflux pump and the fourth sludge reflux pump which are positioned in the sedimentation tank are started to reflux sludge to the reaction tanks;

second, dual series a mode of operation:

the sewage to be treated enters the denitrification tank through a water inlet of the denitrification tank, enters a water distribution well through an intercepting screen at the upper part of a tank body of the denitrification tank, continuously enters the first reaction tank and the fourth reaction tank through a first water inlet and a fourth water inlet respectively, water in the first reaction tank enters the second reaction tank through controlling a relevant valve, water in the fourth reaction tank enters the third reaction tank, the effluent of the second reaction tank and the effluent of the fourth reaction tank are finally collected into the sedimentation tank, part of effluent of the sedimentation tank flows back to the denitrification tank, the rest of effluent is discharged from a main water outlet pipeline through a water outlet well, and a first sludge reflux pump, a second sludge reflux pump and a fourth sludge reflux pump which are positioned in the sedimentation tank are started to flow back sludge to each reaction tank;

third, dual series B mode of operation:

the sewage treatment method comprises the following steps that a first reaction tank, a second reaction tank and a third reaction tank are in a group, sewage to be treated enters the denitrification tank through a water inlet of the denitrification tank, enters a water distribution well through an interception screen on the upper portion of a tank body of the denitrification tank, continuously enters the first reaction tank through a first water inlet, water in the first reaction tank respectively enters the second reaction tank and the fourth reaction tank through controlling related valves, water in the second reaction tank enters the third reaction tank, effluent of the third reaction tank and the fourth reaction tank is collected into a sedimentation tank, part of effluent of the sedimentation tank flows back to the denitrification tank, the rest of effluent is discharged from a main water outlet pipeline through a water outlet well, and a first sludge reflux pump, a second sludge reflux pump, a third sludge reflux pump and a fourth sludge reflux pump which are located in the sedimentation tank are started to reflux sludge to the reaction tanks.

Preferably, the parallel operation mode comprises the following specific steps: the sewage to be treated enters a denitrification tank through a water inlet of the denitrification tank, enters a water distribution well through an interception screen on the upper part of a tank body of the denitrification tank, then continuously enters each reaction tank through a first water inlet valve, a second water inlet valve, a third water inlet valve, a fourth water inlet valve, a first water inlet, a second water inlet, a third water inlet and a fourth water inlet respectively, the effluent water passes through the first interception screen, the second interception screen, the third interception screen and the fourth interception screen respectively, then is collected into a sedimentation tank through respective water outlet valves, partial effluent water in the sedimentation tank flows back to the denitrification tank, the rest effluent water is discharged from a main water outlet pipeline through a water outlet well, and first to fourth sludge reflux pumps positioned in the sedimentation tank are started to reflux sludge to each reaction tank so as to maintain the proper sludge concentration of each reaction tank.

Preferably, the double-series a operation mode comprises the following specific steps: the sewage to be treated enters a denitrification tank through a water inlet of the denitrification tank, enters a distribution well through an interception screen on the upper part of a tank body of the denitrification tank, then continuously enters a first reaction tank and a fourth reaction tank through a first water inlet valve, a fourth water inlet valve, a first water inlet and a fourth water inlet respectively, the effluent of the first reaction tank enters a second reaction tank through the first interception screen, a first communication valve and a second interception screen, is collected to a sedimentation tank through the second interception screen and a second water outlet valve, part of effluent of the sedimentation tank flows back to the denitrification tank, and the rest of effluent is discharged from a water outlet pipeline through a water outlet well; the effluent of the fourth reaction tank enters a third reaction tank through a fourth interception screen, a third communication valve and a third interception screen, the effluent of the third reaction tank is collected into a sedimentation tank after passing through the third interception screen and a third water outlet valve, part of effluent of the sedimentation tank flows back to a denitrification tank, the rest of effluent is discharged from a main water outlet pipeline through a water outlet well, and first to fourth sludge reflux pumps positioned in the sedimentation tank are started to reflux sludge to each reaction tank;

preferably, the above-mentioned double series B operation mode comprises the following specific steps: the sewage to be treated enters a denitrification tank through a water inlet of the denitrification tank, enters a water distribution well through an interception screen on the upper part of a tank body of the denitrification tank, then continuously enters a first reaction tank through a first water inlet valve and a first water inlet, the effluent of the first reaction tank enters a second reaction tank through a first interception screen, a first communicating valve and a second interception screen, the effluent of the first reaction tank simultaneously enters a fourth reaction tank through the first interception screen, a fourth communicating valve and a fourth interception screen, the effluent of the second reaction tank enters a third reaction tank through the second interception screen, a second communicating valve and a third interception screen, the effluent of the third reaction tank is collected to a sedimentation tank through a third interception screen and a third water outlet valve, partial effluent of the sedimentation tank flows back to the denitrification tank, the rest effluent is discharged from a main water outlet pipeline through a water outlet well, and the effluent of the fourth reaction tank is collected to the sedimentation tank through the fourth interception screen and a fourth water outlet valve, part of effluent of the sedimentation tank flows back to the denitrification tank, the rest of effluent is discharged from a main effluent pipeline through an effluent well, and first to fourth sludge reflux pumps positioned in the sedimentation tank are started to flow back sludge to each reaction tank.

Compared with the prior art, the invention has the following beneficial technical effects:

1) the starting time is short, and the starting can be successful only in 100 days at the fastest speed;

2) the autotrophic denitrification inoculation ratio is small, and the inoculation ratio is not more than 5 percent;

3) the starting scale is large, and the method is suitable for large-scale starting of large-volume engineering;

4) the operation is stable, and the engineering requirements are met;

5) the operation mode is flexible, and the water outlet directions of the four reaction tanks are controlled by the communicating valves according to the water outlet standard to realize the serial connection, parallel or independent operation among the reaction tanks to realize the stable operation;

6) the load is high, the occupied area is saved, the tank capacity can be saved by more than 40 percent compared with the pure membrane method for achieving the same TN removal volume load, and the TN removal volume load can reach 2.5 kgN/(m)³·d)；

7) The denitrification tank adopts a pure membrane form, and can prevent the fallen denitrification biomembrane from entering the autotrophic nitrogen removal reaction tank and bringing adverse effects to autotrophic nitrogen removal functional microorganisms by regularly discharging mud from the bottom of the water distribution well.

8) The operation control is simple, the MBBR technology and the activated sludge technology are combined in the autotrophic nitrogen removal reaction tank, the proper sludge concentration in the reaction tank is maintained through sludge backflow, two functional microorganisms AOB and AnAOB for autotrophic nitrogen removal are respectively arranged on the MBBR carrier and the sludge, the effective strain biomass is large, the treatment load is high, and the impact resistance is strong.

9) The addition of the preposed denitrification can reduce the adverse effect of the COD of the inlet water on the autotrophic nitrogen removal functional microorganisms, create a good environment for the autotrophic nitrogen removal reaction tank, improve the total nitrogen removal rate to a certain extent, and the denitrification tank can supplement a certain alkalinity to the autotrophic nitrogen removal reaction tank to enhance the nitrification effect.

Drawings

The invention is further described below with reference to the accompanying drawings:

FIG. 1 is a plan view of the high efficiency autotrophic nitrogen removal system for treating high ammonia nitrogen wastewater according to the present invention;

FIG. 2 is a left side view of the high efficiency autotrophic nitrogen removal system for treating high ammonia nitrogen wastewater according to the present invention;

in the figure, 1, a main water inlet pipeline; 2. a denitrification tank; 3. distributing a water well; 4. a water outlet well; 5. a sedimentation tank; 6. a main water outlet pipeline; 7. a reaction tank stirring device; 8. a denitrification tank stirring device; 9. an intercepting screen mesh at the upper part of the tank body of the denitrification tank; 10. a mud water buffer plate; C1-C4, a reaction tank (a first reaction tank-a fourth reaction tank); S1-S4, a reaction tank interception screen (a first interception screen-a fourth interception screen); I1-I4, a water inlet valve (first water inlet valve-fourth water inlet valve); E1-E4, outlet valve (first outlet valve-fourth outlet valve); h1, a water distribution well return pump; h2, a mixed liquid reflux pump of the sedimentation tank; M1-M4, a communication valve (first communication valve-fourth communication valve); B1-B4 and a sludge return pump (a first sludge return pump and a fourth sludge return pump) of the reaction tank.

Detailed Description

The invention provides a high-efficiency autotrophic nitrogen removal system for treating high-ammonia-nitrogen wastewater and an operation method thereof, and the invention is described in detail below by combining specific embodiments in order to make the advantages and technical scheme of the invention clearer and more clear.

First, the related art terms involved in the present invention are explained as follows:

1) the suspension carrier, the specific gravity is 0.93-0.97, the void ratio is more than 90%, and the suspension carrier is also called suspension filler, carrier and filler for short;

2) effective specific surface area: since the outer surfaces of the carriers rub against each other and it is difficult for microorganisms to attach to them, the effective specific surface area generally refers to the inner surface area, i.e., the effective surface area per unit volume of the carriers. Effective specific surface area ═ effective surface area ÷ volume, in m²/m³；

3) Specific gravity: the ratio of the density of the carrier to the density of water at normal temperature;

4) porosity: the ratio of the volume of the gaps between the carriers and the gaps among the carriers to the stacking volume of the carriers;

5) fluidization: under the action of aeration or stirring, the filler flows along with the water flow in the liquid and is in full contact with water pollutants, and the suspended carriers do not accumulate and can freely flow along with the water flow in the tank;

6) filling rate: the filling rate of the suspension carrier, namely the ratio of the volume of the suspension carrier to the pool capacity of the filling area, wherein the volume of the suspension carrier is the total volume under natural accumulation; e.g. 100m³Suspending vehicle, filled to 400m³The tank capacity is 25 percent;

7) surface loading: the amount of pollutants removed per day per unit specific surface area of the filler, gN/(m)²·d)；

8) Ammonia oxidation surface loading: the mass of the unit filler specific surface area oxidized ammonia nitrogen every day; gN/(m)²D); if the ammonia nitrogen of the inlet water is 400mg/L, the ammonia nitrogen of the outlet water is 200mg/L, and the inlet water flow is 5m³D, biofilm area 1000m²The ammonia oxidation surface load is 1.5 gN/(m) at (500-²·d)；

9) TN removal of surface load: the mass of total nitrogen per unit of effective specific surface area of the filler removed per day, gN/(m)²D); if the inlet water TN is 500mg/L, the outlet water TN is 100mg/L, and the inlet water flow is 10m³D, biofilm area 2000m²If the TN removal surface load is (500-100). times. 10/2000 ═ 2 gN/(m)²·d)；

10) Volumetric load of ammonia oxidation: the mass of ammonia nitrogen oxidized every day in a unit volume reaction tank is kgN/(m)³D); if the ammonia nitrogen of the inlet water is 400mg/L, the ammonia nitrogen of the outlet water is 200mg/L, and the inlet water flow is 50m³D, reaction tank volume 10m³The ammonia oxidation surface load is 1 kgN/(m) at (400-³·d)；

11) TN removal of volume load: total mass of nitrogen removed per day in unit volume reaction cell, kgN/(m)³D); if the inlet water TN500mg/L and the outlet water TN 100mg/L are adopted, the inlet water flow is 100m³D, reactionPool volume 20m³If the TN removal surface load is (500-100). times. 100/1000/20-2 kgN/(m)³·d)；

12) Autotrophic nitrogen removal: the process is a general name of nitrosation and anaerobic ammonia oxidation (ANAMMOX), so that the aim of denitrification is fulfilled; under aerobic conditions, Ammonia Oxidizing Bacteria (AOB) oxidize ammonia nitrogen part into nitrous acid, and the generated nitrous acid and part of the rest ammonia nitrogen are subjected to anaerobic ammonia oxidation (ANAMMOX) reaction under the action of anaerobic ammonia oxidizing bacteria (ANAOB) to generate nitrogen;

13) CANON process, i.e. autotrophic nitrogen removal in a single reactor; in CANON, AOB and AnAOB coexist in the same reactor; the AOB is positioned on the outer layer of the carrier, and oxygen is used as an electron acceptor to oxidize ammonia nitrogen into nitrite; the AnAOB is positioned in the inner layer of the carrier, and the nitrite is used as an electron acceptor to be converted into nitrogen together with the residual ammonia nitrogen;

14) CANON suspension vector: namely, the suspension carrier with CANON effect exists, AOB and AnAOB exist in a biomembrane mode in a layered mode;

15) nitrosation: microorganism will ammonia Nitrogen (NH)₄ ⁺) Oxidation to nitrite Nitrogen (NO)₂ ^-) Without further oxidation to nitrate Nitrogen (NO)₃ ^-) The process of (1), namely enriching Ammonia Oxidizing Bacteria (AOB) in the system and eliminating Nitrite Oxidizing Bacteria (NOB);

16) MBBR: moving Bed Biofilm reactor MBBR (moving Bed Biofilm reactor) the method increases the biomass and the biological species in the reactor by adding a certain amount of suspension carriers into the reactor, thereby increasing the treatment efficiency of the reactor;

17) aeration strength: aeration per unit area in m³/(m²H) including the sum of the two parts of micro-aeration and perforating aeration; for example, the aeration rate of the micropores is 10m³H, perforation aeration rate of 5m³H, the bottom area of the reactor is 5m²The aeration intensity is (10+ 5)/5-3 m³/(m²·h)；

18) Reflux ratio: the ratio of the water amount which flows back to the biological section for continuous treatment to the total water amount is percent;

19) total ammonia oxidation rate: the ratio of the total amount of ammonia nitrogen oxidized after the intake water passes through the multi-stage aerobic reaction tank to the total amount of ammonia nitrogen in the intake water is percent; if the ammonia nitrogen in the inlet water is 400mg/L, the ammonia nitrogen in the outlet water is 100mg/L after passing through the two-stage aerobic reaction tank, and the total ammonia oxidation rate is (400-100)/400-75%; for single stage reactors, it is generally referred to directly as the ammoxidation rate; for a multistage reactor, the ammonia oxidation rate refers to the ammonia nitrogen oxidation condition of each stage, and if the performance of the multistage whole is analyzed, the total ammonia oxidation rate is used;

20) TN removal rate: the total nitrogen removal amount accounts for the ratio of the total nitrogen of the inlet water;

21) common activated sludge: namely activated sludge in a biochemical pool of a sewage plant, and the inoculation of the sludge mainly comprises the primary acquisition of AOB strains and the accelerated biofilm formation;

22) C/N: i.e. the ratio of carbon to nitrogen in the feed water, refers to BOD in the feed water₅The ratio to Kjeldahl nitrogen (organic nitrogen + ammonia nitrogen);

23) pretreatment: if the C/N of the inlet water is too large and is not suitable for the treatment of the autotrophic nitrogen removal related process, the pretreatment is carried out to reduce the content of organic matters until the water quality requirement of autotrophic nitrogen removal is met;

24) stirrer power: i.e. the power per unit effective tank volume, W/m³(ii) a The activated sludge process is usually 3-5W/m³(ii) a In MBBR, the agitation power is correlated with the filling rate, and the higher the filling rate, the higher the agitation power.

The first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank are abbreviated as C1, C2, C3 and C4, a first water inlet valve, a second water inlet valve, a third water inlet valve and a fourth water inlet valve are abbreviated as I1, I2, I3 and I4, a first communication valve, a second communication valve, a third communication valve and a fourth communication valve are abbreviated as M1, M2, M3 and M4, a first water outlet valve, a second water outlet valve, a third water outlet valve and a fourth water outlet valve are abbreviated as E1, E2, E3 and E4, a first interception screen, a second interception screen, a third interception screen and a fourth interception screen are abbreviated as S1, S2, S3 and S4, and a first sludge reflux pump, a second sludge reflux pump, a third sludge reflux pump and a fourth sludge reflux pump are abbreviated as B1, B2, B3 and B4.

The invention relates to a high-efficiency autotrophic nitrogen removal system for treating high-ammonia nitrogen wastewater, which is combined with a graph 1 and a graph 2 and comprises a total water inlet pipeline 1, a denitrification tank 2, a distribution well 3, reaction tank bodies C1-C4, a water outlet well 4, a sedimentation tank 5, a total water outlet pipeline 6, a reaction tank stirring device 7, a denitrification tank stirring device 8, a communication device, a distribution well sludge reflux pump H1 and a sedimentation tank mixed liquid reflux pump H2, wherein the reaction tank bodies are two rows and two columns of four reaction tanks, namely a first reaction tank, a second reaction tank, a third reaction tank and a fourth reaction tank, wherein the first reaction tank and the fourth reaction tank are arranged in a row and positioned at the bottom, the first reaction tank and the second reaction tank are arranged in a row and are equivalent to the left lower side of the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank are respectively positioned in the clockwise direction, the process center is a concentric center well, the denitrification tank, the water distribution well, the water outlet well and the sedimentation tank are sequentially arranged from inside to outside.

A first water inlet and a fourth water inlet are respectively arranged above the sides (close to the water outlet well ends) of the first reaction tank and the fourth reaction tank, water enters the first reaction tank and the fourth reaction tank through I1 and I4, a second water inlet and a third water inlet are respectively arranged below the sides of the second reaction tank and the third reaction tank, water enters the second reaction tank and the third reaction tank through I2 and I3, a first interception screen mesh S1, a second interception screen mesh S2, a third interception screen mesh S3 and a fourth interception screen mesh S4 are respectively arranged at the first water outlet, the second water outlet, the third water outlet and the fourth water outlet, and the first interception screen mesh, the second interception screen mesh, the third interception screen mesh and the fourth interception screen mesh are obliquely arranged; the first water inlet, the second water inlet, the third water inlet and the fourth water inlet are respectively connected with the water distribution well through a first water inlet pipeline, a second water inlet pipeline, a third water inlet pipeline and a fourth water inlet pipeline, a first water inlet valve I1 is arranged on the first water inlet pipeline, a second water inlet valve I2 is arranged on the second water inlet pipeline, a third water inlet valve I3 is arranged on the third water inlet pipeline, and a fourth water inlet valve I4 is arranged on the fourth water inlet pipeline; the denitrification tank is provided with a total water inlet pipeline 1, a denitrification tank interception screen 9 and a denitrification tank stirring device 8, and water is fed from the total water inlet pipeline 1; the sewage to be treated enters the bottom of the denitrification tank through a main water inlet pipeline, and the effluent enters the distribution well 3 through an interception screen 9 at the upper part of the denitrification tank. The water outlet ends of the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank are respectively connected with the sedimentation tank 5 through a first water outlet pipeline, a second water outlet pipeline, a third water outlet pipeline and a fourth water outlet pipeline, and a first water outlet valve E1, a second water outlet valve E2, a third water outlet valve E3 and a fourth water outlet valve E4 are correspondingly arranged on the first water outlet pipeline, the second water outlet pipeline, the third water outlet pipeline and the fourth water outlet pipeline. The sedimentation tank is provided with four mud water buffer plates 10 which are respectively connected with a first water outlet pipeline, a second water outlet pipeline, a third water outlet pipeline and a fourth water outlet pipeline;

the distribution well is provided with pipelines connected with the four reaction tanks, and the pipelines are provided with water inlet valves I1, I2, I3 and I4; the sedimentation tank is provided with pipelines to connect four reaction tanks, the effluent of the four reaction tanks is collected through a water inlet pipeline and water outlet valves E1, E2, E3 and E4 and is discharged into an effluent well 4 through the upper part of the tank body, the effluent well collects the effluent of the sedimentation tank and is discharged through a main effluent pipeline 6 at the upper part of the tank body, the bottom of the distribution well is provided with a first sludge discharge port for discharging sludge, and the bottom of the sedimentation tank is provided with a second sludge discharge port for discharging sludge;

all set up a agitating unit in every reaction tank, agitating unit's concrete structure and operation mode borrow the prior art for reference and can realize, if the optional frequency conversion agitator of agitating unit.

The mixed liquid reflux pump of the sedimentation tank is characterized in that the reflux pump is arranged at the upper part of the sedimentation tank, and a reflux pipe is introduced into the denitrification tank;

the water outlet well sludge reflux pump is characterized in that a reflux pump is arranged at the bottom of a water outlet well, and a reflux pipe is introduced into a denitrification tank;

the communicating valves, namely the reactors are connected through the communicating valves and comprise a first communicating valve, a second communicating valve, a third communicating valve and a fourth communicating valve; the first communicating valve is positioned on a connecting pipeline between the first reaction tank and the second reaction tank, the second communicating valve is positioned on a connecting pipeline between the second reaction tank and the third reaction tank, the third communicating valve is positioned on a connecting pipeline between the third reaction tank and the fourth reaction tank, and the fourth communicating valve is positioned on a connecting pipeline between the first fourth reaction tank and the first reaction tank;

the sludge reflux pump of the reaction tank comprises a first sludge reflux pump B1, a second sludge reflux pump B2, a third sludge reflux pump B3 and a fourth sludge reflux pump B4 which are all arranged at the bottom of the sedimentation tank, and reflux pipes are respectively introduced into the bottoms of the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank;

the aeration devices are distributed in each reaction tank and consist of a plurality of groups of perforated aeration pipes and microporous aeration pipes, and suspension carriers are added into the denitrification tank and each reaction tank.

Secondly, the operation flow of the present invention is mainly described below with reference to the above system.

The operation flow comprises the following 3 control modes:

1) parallel operation mode: sewage to be treated passes through the denitrification tank 2, enters the distribution well 3 from the interception screen 9 at the upper part of the tank body of the denitrification tank, passes through the water inlet valve I1-I4 and the first to fourth interception screens S1-S4 by the distribution well, continuously enters each reaction tank C1-C4, and effluent water respectively passes through the interception screens S1-S4 and the water outlet valves E1-E4 to the sedimentation tank 5, enters the water outlet well 4 through the upper part of the sedimentation tank and is discharged from the main water outlet pipeline 6 at the upper part of the water outlet well; the four pools are connected in parallel and operate independently, effluent is finally gathered to a central sedimentation pool 5 and is discharged by a main effluent pipeline 6 at the upper part of an effluent well 4, and the process is controlled by a valve; the valves are not described as being in a closed state;

2) dual series a mode of operation: sewage to be treated passes through the denitrification tank 2, enters the distribution well 3 from the interception screen 9 at the upper part of the tank body of the denitrification tank, and continuously enters the reaction tanks C1 and C4 from the distribution well through water inlet valves I1 and I4 respectively; c1 effluent enters a reaction tank C2 through a first interception screen S1, a communication valve M1 and a second interception screen S2, C2 effluent passes through a second interception screen S2, a water outlet valve E2 and a sedimentation tank 5, passes through a water outlet well 4 and is discharged through a main water outlet pipeline 6 at the upper part of the water outlet well; c4 effluent enters a reaction tank C3 through a fourth interception screen S4, a communication valve M3 and a third interception screen S3, and C3 effluent passes through a third interception screen S3, a water outlet valve E3 and a sedimentation tank 5, passes through a water outlet well 4 and is discharged through a main water outlet pipeline 6 at the upper part of the water outlet well; the double series A mode is that two groups are connected in parallel, two grids of each group are respectively connected in series, namely C1-C2 and C4-C3, the effluent is finally gathered to a sedimentation tank 5 and an effluent well 4 in the center and is discharged by a main effluent pipeline 6 at the upper part of the effluent well;

3) dual series B mode of operation: sewage to be treated passes through a denitrification tank 2, enters a distribution well 3 from an interception screen 9 at the upper part of a tank body of the denitrification tank, and continuously enters a reaction tank C1 from the distribution well through a water inlet valve I1 and an interception screen S1 respectively; c1 effluent passes through a first interception screen mesh S1, a fourth interception screen mesh S4, a communication valve M1 and a communication valve M4 and enters reaction tanks C2 and C4; c2 effluent enters C3 through a second interception screen S2, a communication valve M2 and a third interception screen S3, C3 effluent passes through a third interception screen S3, a water outlet valve E3 and a sedimentation tank 5, passes through a water outlet well 4 and is discharged through a main water outlet pipeline 6 at the upper part of the water outlet well; c4 effluent passes through a fourth interception screen S4, an effluent valve E4 and a sedimentation tank 5, enters an effluent well 4 through the upper part of the sedimentation tank and is discharged through a main effluent pipeline 6 at the upper part of the effluent well; two series B modes, two sets in parallel: the three grids are connected in series, and the two grids are connected in series, namely C1-C2-C3 and C1-C4, and the effluent is finally gathered to a central sedimentation tank 5 and is discharged by a main water outlet pipeline 6 at the upper part of the water outlet well after passing through the water outlet well 4.

Different operation modes are set, and the functional requirements of different reactors and different operation stages are mainly considered to be met.

Thirdly, the starting method of the invention comprises the following steps:

1) starting preparation, namely adding a suspension carrier into each reaction tank and each denitrification tank, wherein the filling rate is 20-67%; common activated sludge is inoculated in both the reaction tank and the denitrification tank, and the sludge concentration after inoculation is 3-5 g/L;

2) nitrosation and denitrification are started, a parallel operation mode is adopted, and the specific operation mode is as follows: the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank are in parallel relation, each reaction tank independently feeds water and independently discharges water, the discharged water is collected in the sedimentation tank by controlling a relevant valve, part of discharged water in the sedimentation tank flows back to the denitrification tank, and the rest of discharged water is discharged from a main water outlet pipeline through a water outlet well; starting a sludge reflux pump of the distribution well to reflux the sludge to the denitrification tank, starting a second sludge discharge port at the bottom of the sedimentation tank and a first sludge discharge port at the bottom of the distribution well for a short time every day to discharge the sludge, so that the sludge is gradually lost, and the sludge concentration is reduced by not more than 10% every day until the sludge concentration in the denitrification tank is reduced to the maximum<0.5g/L, the sludge concentration in the reaction tank is about1.0 g/L; controlling DO in the reaction tank to be 1.5-3.0mg/L and aeration intensity>4m³/(m²H) run until denitrification pool BOD₅Removal rate>50% and the ammonia oxidation volume load of each reaction tank>1.0kgN/(m³D), go to the next step;

3) the autotrophic denitrification is started in advance, a double-series A operation mode is adopted, water is continuously fed, the effluent is converged into a sedimentation tank by controlling a relevant valve, part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from a main water outlet pipeline through a water outlet well; c4 and C3 control DO at 1.5-3mg/L, aeration intensity>4.0m³/(m²H), the total ammoxidation rate of C4 and C3 is more than 60 percent; stirring at 30-45r/min in C1 and C2, controlling DO at 1-1.5mg/L, and aerating at high intensity>3m³/(m²H); the operation is carried out until the total ammoxidation rate of C1 and C2 is more than 60 percent, and the ammoxidation volume load of the reaction tank C1 is>0.4kgN/(m³D), go to the next step;

4) starting autotrophic denitrification inoculation, adopting a double-series A operation mode, continuously feeding water, collecting effluent into a sedimentation tank by controlling a relevant valve, returning part of the effluent from the sedimentation tank to a denitrification tank, and discharging the rest of the effluent from a main effluent pipeline through an effluent well; inoculating a CANON suspension carrier into the first reaction tank, wherein the inoculation rate is 3-5%, and continuously feeding water; c4 and C3 control DO at 1.5-3.0mg/L, aeration intensity>5.0m³/(m²H), total ammoxidation rates of C4 and C3 > 60%; c1 controlling the rotation speed of the stirring device to be 15-30r/min, controlling DO to be 0.5-1.0mg/L and controlling the aeration intensity>2m³/(m²H); c2 controlling the rotation speed of the stirring device to be 15-30r/min, controlling DO to be 1.0-1.5mg/L and the aeration intensity>3m³/(m²H); the operation is carried out until the TN of the first reaction tank removes the volume load>1.0kgN/(m³D) go to the next step;

5) the autotrophic nitrogen removal fed-batch is started, and a double-series B operation mode is adopted to continuously feed water; the effluent is collected in a sedimentation tank by controlling a relevant valve, part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from an effluent pipeline through an effluent well; c1 controlling the rotation speed of the stirring device to be 15-30r/min, controlling DO to be 1.0-2.0mg/L and the aeration intensity>4.0m³/(m²H); c2, C4 stirring controlThe rotation speed of the device is 30-45r/min, DO is controlled to be 0.5-1.0mg/L, and the aeration intensity is controlled>2m³/(m²H); c3 controlling the rotation speed of the stirring device at 30-45r/min, DO at 1.0-2.0mg/L and the aeration intensity>3m³/(m²H), starting a reflux pump of each reaction tank to reflux the sludge in the sedimentation tank to each reaction tank; the operation is carried out until TN of C2 and C4 removes the volume load>1.5kgN/(m³D), go to the next step;

6) starting autotrophic denitrification, adopting a double-series A operation mode to replace 50% of suspended fillers in C4 and C3 and in C1 and C2 respectively, controlling the rotating speed of a stirring device in each reaction tank to be 15-30r/min, controlling the DO to be 1.0-2.0mg/L and controlling the aeration intensity to be more than 4m³/(m²H); the effluent is collected in a sedimentation tank by controlling a relevant valve, part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from a main effluent pipeline through an effluent well; running until the TN of each reaction tank removes the volume load>2.0kgN/(m³D), go to the next step;

7) the autotrophic nitrogen removal stably operates, and water continuously enters; when the TN removal rate is required<80%, adopting parallel operation mode, controlling the rotation speed of stirring device in each reaction tank at 30-45r/min, controlling DO at 2.0-4.0mg/L, and controlling aeration intensity>5m³/(m²H), collecting the effluent into a sedimentation tank by controlling a relevant valve, wherein part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from a main effluent pipeline through an effluent well; maintaining the sludge concentration of each reaction tank to be about 3.0 g/L; the ammonia nitrogen of the effluent of each reaction tank is 60-100mg/L, and the TN of each reaction tank removes the volume load>2.0kgN/(m³D) denitrification pool BOD₅The removal rate is more than 50 percent; when the TN removal rate is required to be more than or equal to 80 percent, a double-series A operation mode is adopted, the ammonia nitrogen of the effluent of C2 or C3 is 30-50mg/L, the rotating speed of the stirring device is controlled to be 30-45r/min by C1 and C4, the DO is controlled to be 2.0-4.0mg/L, and the aeration intensity is controlled to be 2.0-4.0mg/L>5m³/(m²H) removal rate of TN>50 percent, the rotating speed of the stirring device is controlled to be 15-30r/min for both the reaction tank C2 and the reaction tank C3, the DO is controlled to be 1.0-2.0mg/L, and the aeration intensity is controlled>3m³/(m²H), collecting the effluent into a sedimentation tank by controlling related valves, returning part of the effluent in the sedimentation tank to a denitrification tank, and allowing the rest of the effluent to pass through a water outlet wellThe main water outlet pipeline is used for discharging.

In the steps, when the C/N of the inlet water is less than 1, the reflux ratio of the outlet well is controlled to be 150-200%, when the C/N of the inlet water is more than or equal to 1 and less than 1.5, the reflux ratio of the outlet well is controlled to be 200-250%, and when the C/N of the inlet water is more than or equal to 1.5 and less than 2, the reflux ratio of the outlet well is controlled to be 300% of 250-; the stirring speed of the denitrification tank is controlled to be 30-50 r/min; and starting sludge reflux pumps B1-B4 of the reaction tanks in the processes of the steps 3) to 7) to reflux the sludge of the sedimentation tank to the reaction tanks, or starting a second sludge discharge port at the bottom of the sedimentation tank to discharge the sludge, and maintaining the concentration of the sludge in the reaction tanks to be about 1.50 g/L; controlling the sludge concentration of the denitrification tank to be less than 0.5g/L by opening a first sludge discharge port at the bottom of the distribution well; in the start process of the autotrophic denitrification fed-batch process, the water inlet flow ratio of the first reaction tank to the second reaction tank and the fourth reaction tank is controlled to be 2/3 and 1/3; the stirrer power of the stirring devices of the reaction tanks and the denitrification tank is 15-50W/m³And (4) selecting the type.

Fourth, supplementary explanation:

1) the method adopts the mode of combining MBBR with activated sludge to realize one-stage autotrophic nitrogen removal, mainly adopts a two-stage process, has complex control, needs to control the nitrosation water outlet ratio, and meets the process requirements of ANAMMOX; by adopting a granular sludge mode, the AnAOB is not easy to enrich, and the activated sludge method is easy to lose and difficult to start or granulate; the method adopts an MBBR pure membrane mode, the denitrification load is related to the transmission of matrixes in the biomembrane, such as density, thickness, temperature, matrix concentration and the like of the biomembrane, and in addition, the occupation and the adhesion capacity of AOB to the ecological niche of the MBBR filler are weaker than those of AnAOB, so the MBBR autotrophic denitrification in long-term operation can cause the limitation of the nitrosation effect of the system due to the loss of the AOB, and the total nitrogen removal effect is influenced finally. For autotrophic denitrification microorganisms, the attachment state and the suspension state show completely different property characteristics, the related methods of an activated sludge method cannot be directly applied to a biofilm method, and the characteristics of autotrophic denitrification, activated sludge and MBBR are required to be controlled in a targeted manner. In order to improve the matrix transmission rate, separate AOB and AnAOB and improve the denitrification efficiency, the process form of combining MBBR with activated sludge is adopted by combining the advantages of both MBBR and activated sludge methods;

2) DO control requirements at all stages are different, the DO is controlled to provide an aerobic or anaerobic environment for the autotrophic denitrification biomembrane, the survival environment of AOB and AnAOB is ensured, and the DO level is adjusted along with the thickness change and the maturation process of the biomembrane to meet the requirement of biomembrane layering; the more mature the biofilm, the relative increase in biofilm thickness, the stronger the tolerance to DO, the higher DO levels are required; meanwhile, the thickness of the biological membrane is relatively increased, and higher shearing force is also needed to control the thickness of the biological membrane and prevent the biological membrane from being too thick; therefore, two indexes of DO and aeration intensity are required to be controlled simultaneously; the MBBR autotrophic nitrogen removal process belongs to a complete biological membrane system, and has great difference with the traditional activated sludge method in control method and characteristics; for the activated sludge method, the DO of the autotrophic nitrogen removal process is not more than 1mg/L generally;

3) the operation modes of all stages are different, the inoculation mode and the operation mode are mainly considered, the biomembrane falls off, although the biomembrane falls off naturally in the aging process, more active strains still exist, the subsequent reactor can be inoculated, the starting process is accelerated, so that the inoculation is carried out step by step in multiple operation modes, and in the autotrophic denitrification inoculation starting process, the water inlet flow ratio of the first reaction tank to the second reaction tank and the fourth reaction tank is controlled to be 2/3 and 1/3;

4) the stirring speed of the autotrophic denitrification reaction tank is controlled in order to assist fluidization of the suspended carrier when aeration is insufficient and prevent the thickening of the biomembrane under the condition of over-low shearing force or the falling off of the biomembrane under the condition of over-high shearing force;

5) the invention is suitable for high-temperature wastewater with high ammonia nitrogen and C/N less than 2, and is particularly suitable for treating anaerobic sludge digestion supernatant, landfill leachate and the like;

6) different reflux ratios are required to be set for different inlet water C/N, and the main reason is that along with the increase of the inlet water C/N, the denitrification process can be enhanced by adjusting the reflux ratio upwards, the influence of COD (chemical oxygen demand) in the inlet water on an autotrophic nitrogen removal system is eliminated, and the nitrogen removal efficiency is improved.

As is well known to those skilled in the art, when the C/N of the inlet water is more than or equal to 2, the pretreatment is added to meet the requirement.

As is well known to those skilled in the art, a heat exchange system is added when the temperature of the inlet water is not between 25 and 35 ℃.

As is well known to those skilled in the art, the specific gravity of the suspension carrier before membrane formation is slightly smaller than that of water, usually 0.93-0.97, and the specific gravity after membrane formation is close to that of water, so as to achieve the suspension effect, and the suspension carrier is generally made of high-density polyethylene.

As is well known to those skilled in the art, short-flow prevention devices, such as partition plates, flow guide walls, etc., are installed between the connecting pipes collected in the individual reaction tanks to prevent uneven mixing of the influent water.

The present invention is further illustrated by the following specific examples.

Example 1:

high-concentration ammonia nitrogen wastewater generated in the production process of a certain bioengineering company is taken as system inlet water, and the water quantity is 3000m³(d), pH mean value 7.9, water temperature mean value 32 ℃, influent COD concentration mean value 2500mg/L, BOD₅The average concentration is 1500mg/L, the average concentration of ammonia nitrogen is 800mg/L, the average concentration of nitrite nitrogen is 2.0mg/L, and the average alkalinity is CaCO₃Calculated) 5000mg/L and the total effective volume of the reaction tank is 800m³Effective volume of denitrification tank is 800m³And the inlet water enters four reaction tanks C1-C4 through a denitrification tank.

Starting preparation, adding a suspension carrier into each reaction tank and each denitrification tank, wherein the effective specific surface area of the carrier is 800m²/m³The porosity is 90 percent, the industrial standard of high density polyethylene suspension carrier for water treatment (CJ/T461-2014) is met, and the filling rate is 50 percent; inoculating common activated sludge in the reaction tanks, wherein the concentration of the sludge in each reaction tank is 5 g/L;

nitrosation and denitrification are started, a parallel operation mode is adopted, each reaction tank independently feeds water and independently discharges water, the discharged water is collected into a sedimentation tank by controlling a relevant valve, part of discharged water in the sedimentation tank flows back to a denitrification tank, and the rest of discharged water is discharged from a main water outlet pipeline through a water outlet well; starting sludge return pumps (B1-B4) of the reaction tanks to return sludge of the sedimentation tanks to the reaction tanks; starting a distribution well sludge return pump (H1) to return sludge to the denitrification tank; controlling DO in the reaction tank to be 2.5mg/L and the aeration intensity to be 5m³/(m²H) the effluent is collected in a sedimentation tank by opening the effluent valves E1-E4, part of the effluent in the sedimentation tankAnd returning to the denitrification tank, discharging the rest of the discharged water through a water outlet well by a main water outlet pipeline, opening a first sludge discharge port at the bottom of the distribution well and a second sludge discharge port at the bottom of the sedimentation tank for sludge discharge in a short time every day after operation, gradually losing the sludge, reducing the sludge concentration by no more than 10% every day, and operating until the sludge concentration of the 11 th reaction tank is reduced to 1.0g/L and the sludge concentration of the denitrification tank is reduced to 0.5 g/L. And (5) running to the 17d system to obtain the effluent ammonia nitrogen concentration mean value of 392 mg/L. The ammoxidation rate of the system is 51 percent, and the ammoxidation volume load is 1.5 kgN/(m)³D) denitrification pool BOD₅The removal rate is 90%, and the next step is carried out.

Autotrophic nitrogen removal pre-starting, adopting a double-series A operation mode, continuously feeding water, controlling the stirring speed of 30r/min in the reaction tank C1 and the reaction tank C2, controlling the DO at 1.0mg/L and controlling the aeration intensity at 3.0m³/(m²H), the DO of the reaction tank C4 and the DO of the reaction tank C3 are controlled to be 3.0mg/L, and the aeration intensity is 4m³/(m²H), total ammoxidation rates of C4 and C3 > 70%; the effluent is collected into a sedimentation tank by opening effluent valves E2 and E3, part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from an effluent pipeline through an effluent well; after 10 days of operation, the total ammoxidation rate of C1 and C2 is 61 percent, and the ammoxidation surface load of C1 is 0.5 kgN/(m)³D) denitrification pool BOD₅The removal rate is 90 percent, and the next step is carried out;

starting autotrophic denitrification inoculation, adopting a double-series A operation mode, inoculating CANON suspension carriers into a reaction tank C1, wherein the inoculation rate is 4%, and continuously feeding water; the reaction tank C1 controls the rotating speed of the stirring device to be 30r/min, the DO to be 0.8mg/L and the aeration intensity to be 2m³/(m²H); the reaction tank C2 controls the rotating speed of the stirring device to be 30r/min, the DO to be 1.0mg/L and the aeration intensity to be 3m³/(m²H); the DO of the reaction tank C4 and the DO of the reaction tank C3 are controlled to be 3.0mg/L, and the aeration intensity is 4m³/(m²H), total ammoxidation rates of C4 and C3 > 77%; the effluent is collected in a sedimentation tank by controlling a relevant valve, part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from a main effluent pipeline through an effluent well; run 24d until TN of reaction cell C1 had removed the volume load by 1.5kgN/(m³D) denitrification pool BOD₅The removal rate is 90 percent, and the next step is carried out;

autotrophic weaningThe nitrogen feeding is started, a double-series B operation mode is adopted, the first reaction tank controls the rotating speed of the stirring device to be 30r/min, the DO to be 1.5mg/L and the aeration intensity to be 4m³/(m²H); the second reaction tank and the fourth reaction tank control the rotating speed of the stirring device to be 35r/min, DO to be 0.8mg/L and the aeration intensity to be 2m³/(m²H); the third reaction tank controls the rotating speed of the stirring device to be 45r/min, DO to be 1.2mg/L and the aeration intensity to be 4m³/(m²H), collecting the effluent into a sedimentation tank by controlling a relevant valve, wherein part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged through a main effluent pipeline of an effluent well; the operation is carried out for 19d, the TN of the second reaction tank and the fourth reaction tank is subjected to the removal of the volume load of 2.0 kgN/(m)³D) denitrification pool BOD₅The removal rate is 80 percent, and the next step is carried out;

starting the autotrophic denitrification in an expanding way, and continuously feeding water by adopting a double-series A operation mode; 50% of the suspended filler in the reaction tanks C4 and C3 and the reaction tanks C1 and C2 are replaced respectively, the rotating speed of a stirring device is controlled to be 30r/min, DO is controlled to be 1.0mg/L, and the aeration intensity is controlled to be 4m³/(m²H); the effluent is collected in a sedimentation tank by controlling a relevant valve, part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from a main effluent pipeline through an effluent well; run for 15d until TN of each reaction cell removed the surface loading of 2.3 kgN/(m)³D), go to the next step;

the autotrophic nitrogen removal system stably operates in a double-series A operation mode, the ammonia nitrogen in the effluent of C2 or C3 is 30-50mg/L, the rotating speed of the stirring device is controlled at 45r/min by C1 and C4, the DO is controlled at 2.0mg/L, and the aeration intensity is controlled>5m³/(m²H) removal rate of TN>50 percent, the rotating speed of the stirring device is controlled to be 30r/min for both the reaction tank C2 and the reaction tank C3, the DO is controlled to be 1.5mg/L, and the aeration intensity is controlled>4m³/(m²H), collecting the effluent into a sedimentation tank by controlling a relevant valve, wherein part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from a main effluent pipeline through an effluent well; each reaction tank TN removes the volume load 2.6 kgN/(m)³D) denitrification pool BOD₅The removal rate is more than 70 percent;

in the steps, the sludge reflux ratio of the sludge out of the sedimentation tank is always controlled at 300 percent, the stirring rotating speed of the denitrification tank is controlled at 45r/min, a sludge reflux pump B1-B4 of the reaction tank is started to reflux the sludge in the process from the autotrophic denitrification pre-starting to the stable operation of the autotrophic denitrification system, or a second sludge discharge port at the bottom of the sedimentation tank is started to discharge the sludge, the sludge concentration in the reaction tank is maintained to be about 1.50g/L, and the sludge concentration of the denitrification tank is controlled to be less than 0.5g/L by starting a first sludge discharge port at the bottom of a distribution well; the total nitrogen removal rate of the whole system in the final stable operation stage reaches 92%, wherein the total nitrogen removal rate contributed by the denitrification tank is 24%.

Example 2:

the sludge digestion liquid used for the test is a dehydrated filtrate obtained after sludge digestion in a certain sewage treatment plant, the sewage treatment plant adopts a mesophilic anaerobic digestion process to treat sludge, and the solid content of the sludge is 10%. The water quantity is 2000m³D, pH value of 7.8-7.9, water temperature mean value of 30 ℃, influent COD concentration mean value of 810mg/L and BOD₅The average concentration is 620mg/L, the average ammonia nitrogen concentration is 560mg/L, and the total effective volume of the reaction tank is 400m³The reaction tank is divided into four reaction tanks on average, and the effective volume of each reaction tank is 100m³Effective volume of denitrification tank is 100m³And the inlet water passes through the denitrification tank and then respectively enters four reaction tanks C1-C4.

Starting preparation, adding a suspension carrier into each reaction tank and each denitrification tank, wherein the effective specific surface area of the carrier is 800m²/m³The porosity is 90 percent, the industrial standard of high density polyethylene suspension carrier for water treatment (CJ/T461-2014) is met, and the filling rate is 50 percent; inoculating common activated sludge in the reaction tanks, wherein the concentration of the sludge in each reaction tank is 5.0 g/L;

nitrosation and denitrification are started, a parallel operation mode is adopted, each reaction tank independently feeds water and independently discharges water, the discharged water is collected into a sedimentation tank by controlling a relevant valve, part of discharged water in the sedimentation tank flows back to a denitrification tank, and the rest of discharged water is discharged from a main water outlet pipeline through a water outlet well; starting sludge return pumps (B1-B4) of the reaction tanks to return sludge of the sedimentation tanks to the reaction tanks; starting a distribution well sludge return pump (H1) to return sludge to the denitrification tank; controlling DO in the reaction tank to be 1.5mg/L and aeration intensity to be 4m³/(m²H) collecting the effluent in a sedimentation tank by opening an effluent valve E1-E4, and returning part of the effluent in the sedimentation tank to denitrificationAnd (4) discharging the rest effluent from the main water outlet pipeline through the water outlet well, opening a first sludge discharge port at the bottom of the distribution well and a second sludge discharge port at the bottom of the sedimentation tank for a short time every day after operation to discharge sludge, so that the sludge is gradually lost, the sludge concentration is reduced by no more than 10% every day, and the operation is carried out until the sludge concentration in the 10 th reaction tank is reduced to 1.0g/L and the sludge concentration in the denitrification tank is reduced to 0.5 g/L. And (5) running to the 19d system to obtain the effluent ammonia nitrogen concentration mean value of 260 mg/L. The ammoxidation rate of the system is 53 percent, and the ammoxidation volume load of each reaction tank is 1.87 kgN/(m)³D) denitrification pool BOD₅The removal rate is 90%, and the next step is carried out.

Autotrophic denitrification pre-starting, adopting a double-series A operation mode, continuously feeding water, controlling DO in a reaction tank C4 and a reaction tank C3 to be 2.5mg/L and controlling aeration intensity to be 4m³/(m²H); stirring speed of 30r/min, DO of 1mg/L and aeration intensity of 3m in reaction tanks C1 and C2³/(m²H), collecting the effluent into a sedimentation tank by opening effluent valves E2 and E3, wherein part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from an effluent pipeline through an effluent well; after running for 9 days, the total ammonia oxidation rate of C4 and C3 is more than 79 percent, the total ammonia oxidation rate of C1 and C2 is 61 percent, and the ammonia oxidation surface load of C1 is 0.45 kgN/(m)³D) denitrification pool BOD₅The removal rate is 90 percent, and the next step is carried out;

starting autotrophic denitrification inoculation, adopting a double-series A operation mode, inoculating a CANON suspension carrier into a reaction tank C1, wherein the inoculation rate is 5%, and continuously feeding water; the reaction tank C1 controls the rotating speed of the stirring device to be 30r/min, the DO to be 0.7mg/L and the aeration intensity to be 2m³/(m²H); the reaction tank C2 controls the rotating speed of the stirring device to be 30r/min, the DO to be 1.0mg/L and the aeration intensity to be 3m³/(m²H); the DO of the reaction tanks C4 and C3 is controlled at 2.5mg/L, and the aeration intensity is 4m³/(m²H); the effluent is collected in a sedimentation tank by controlling a relevant valve, part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from a main effluent pipeline through an effluent well; the operation is carried out for 24d until the total ammoxidation rate of C4 and C3 is more than 77 percent, and the TN removal volume load of the reaction tank C1 is 1.1 kgN/(m)³D) denitrification pool BOD₅The removal rate is 90 percent, and the next step is carried out;

autotrophic nitrogen removal fed-batch startAdopting a double-series B operation mode, C1 controlling the rotation speed of the stirring device to be 30r/min, DO to be 1.5mg/L and the aeration intensity to be 4m³/(m²H); c2 and C4 control the rotating speed of the stirring device to be 35r/min, DO to be 0.8mg/L and the aeration intensity to be 2m³/(m²H); the third reaction tank controls the rotating speed of the stirring device to be 45r/min, DO to be 1.2mg/L and the aeration intensity to be 4m³/(m²H), collecting the effluent into a sedimentation tank by controlling a relevant valve, wherein part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged through a main effluent pipeline of an effluent well; the operation is carried out for 20d until TN of the second reaction tank and the fourth reaction tank removes the volume load of 1.9 kgN/(m)³D) denitrification pool BOD₅The removal rate is 90 percent, and the next step is carried out;

starting the autotrophic denitrification in an expanding way, and continuously feeding water by adopting a double-series A operation mode; 50% of the suspended filler in the reaction tanks C4 and C3 and the reaction tanks C1 and C2 are replaced respectively, the rotating speed of a stirring device is controlled to be 30r/min, DO is controlled to be 1.0mg/L, and the aeration intensity is controlled to be 4m³/(m²H); the effluent is collected in a sedimentation tank by controlling a relevant valve, part of the effluent in the sedimentation tank flows back to a denitrification tank, and the rest of the effluent is discharged from a main effluent pipeline through an effluent well; run for 15d until TN of each reaction cell removed the surface loading of 2.0 kgN/(m)³D), go to the next step;

the autotrophic nitrogen removal system runs stably in a parallel running mode, the rotating speed of the stirring device is controlled by each reaction tank to be 45r/min, the DO is controlled to be 2.0mg/L, and the aeration intensity is controlled to be 5m³/(m²H), collecting effluent into a sedimentation tank by controlling a relevant valve, returning part of the effluent in the sedimentation tank to a denitrification tank, and discharging the rest of the effluent through a water outlet well by a main water outlet pipeline to maintain the sludge concentration in the denitrification tank to be less than 0.5 g/L; the ammonia nitrogen of the effluent of each reaction tank is 60-100mg/L, and the TN removal volume load of each reaction tank can reach 2.26 kgN/(m)³D), the removal rate of BOD5 in the denitrification tank is more than 75 percent;

in the steps, the sludge reflux ratio of the sedimentation tank is always controlled at 200%, the stirring rotating speed of the denitrification tank is controlled at 45r/min, a sludge reflux pump B1-B4 of the reaction tank is started to reflux the sludge in the process from the autotrophic denitrification pre-start to the stable operation of the autotrophic denitrification system, or a second sludge discharge port at the bottom of the sedimentation tank is started to discharge the sludge, the sludge concentration in the reaction tank is maintained to be about 1.50g/L, and the sludge concentration of the denitrification tank is controlled to be less than 0.5g/L by starting a first sludge discharge port at the bottom of a water distribution well; the total nitrogen removal rate of the whole system in the final stable operation stage reaches 85%, wherein the total nitrogen removal rate contributed by the denitrification tank is 18%.

The invention realizes the serial, parallel or independent operation of the reaction tanks by controlling the water outlet directions of the four reaction tanks through the communicating valves; the autotrophic nitrogen removal process is quickly started by means of inoculation, fed-batch and the like; different process arrangement forms are realized according to the processing standard requirements.

The parts which are not described in the invention can be realized by taking the prior art as reference.

It is intended that any equivalents, or obvious variations, which may be made by those skilled in the art in light of the teachings herein, be within the scope of the present invention.

Claims

1. The utility model provides a high-efficient autotrophic denitrogenation system for handling high ammonia-nitrogen concentration waste water, its includes well, reaction tank main part, mud reflux unit, mixed liquid reflux unit, intercommunication device and aeration equipment, its characterized in that:

the reaction tank main body is provided with two rows of four reaction tanks, namely a first reaction tank, a second reaction tank, a third reaction tank and a fourth reaction tank, wherein the first reaction tank and the fourth reaction tank are arranged in a row and positioned at the bottom, and the first reaction tank and the second reaction tank are arranged in a row;

2. The high-efficiency autotrophic nitrogen removal system for treating high ammonia-nitrogen wastewater according to claim 1, characterized in that: the first water inlet, the second water inlet, the third water inlet and the fourth water inlet are respectively connected with the water distribution well through a first water inlet pipeline, a second water inlet pipeline, a third water inlet pipeline and a fourth water inlet pipeline, a first water inlet valve is arranged on the first water inlet pipeline, a second water inlet valve is arranged on the second water inlet pipeline, a third water inlet valve is arranged on the third water inlet pipeline, and a fourth water inlet valve is arranged on the fourth water inlet pipeline; the interception screen meshes positioned at the water outlet of each reaction tank comprise a first interception screen mesh positioned in the first reaction tank, a second interception screen mesh positioned in the second reaction tank, a third interception screen mesh positioned in the third reaction tank and a fourth interception screen mesh positioned in the fourth reaction tank.

3. The high-efficiency autotrophic nitrogen removal system for treating high ammonia-nitrogen wastewater according to claim 1, characterized in that: the aeration device in each reaction tank consists of a plurality of groups of perforated aeration pipes and microporous aeration pipes.

4. The high-efficiency autotrophic nitrogen removal system for treating high ammonia-nitrogen wastewater according to claim 2, characterized in that: the water outlet ends of the first reaction tank, the second reaction tank, the third reaction tank and the fourth reaction tank are respectively connected with the sedimentation tank through a first water outlet pipeline, a second water outlet pipeline, a third water outlet pipeline and a fourth water outlet pipeline, and a first water outlet valve, a second water outlet valve, a third water outlet valve and a fourth water outlet valve are correspondingly arranged on the first water outlet pipeline, the second water outlet pipeline, the third water outlet pipeline and the fourth water outlet pipeline.

5. The high-efficiency autotrophic nitrogen removal system for treating high ammonia-nitrogen wastewater according to claim 4, characterized in that: the first water outlet pipeline, the second water outlet pipeline, the third water outlet pipeline and the fourth water outlet pipeline are respectively connected with the sedimentation tank through a first muddy water buffer plate, a second muddy water buffer plate, a third muddy water buffer plate and a fourth muddy water buffer plate, and the first muddy water buffer plate, the second muddy water buffer plate, the third muddy water buffer plate and the fourth muddy water buffer plate are all located on the lower portion of the sedimentation tank.

6. The method for operating a high efficiency autotrophic nitrogen removal system for treating high ammonia nitrogen wastewater according to claim 4, is characterized in that it comprises the following three control modes:

first, parallel operating mode:

second, dual series a mode of operation:

third, dual series B mode of operation:

7. The operating method of the high-efficiency autotrophic nitrogen removal system for treating high-ammonia-nitrogen wastewater according to claim 6, wherein the parallel operation mode comprises the following specific steps: the sewage to be treated enters a denitrification tank through a water inlet of the denitrification tank, enters a water distribution well through an interception screen on the upper part of a tank body of the denitrification tank, then continuously enters each reaction tank through a first water inlet valve, a second water inlet valve, a third water inlet valve, a fourth water inlet valve, a first water inlet, a second water inlet, a third water inlet and a fourth water inlet respectively, the effluent water passes through the first interception screen, the second interception screen, the third interception screen and the fourth interception screen respectively, then is collected into a sedimentation tank through respective water outlet valves, part of effluent water in the sedimentation tank flows back to the denitrification tank, the rest of effluent water is discharged from a main water outlet pipeline through a water outlet well, and a first sludge reflux pump, a second sludge reflux pump, a third sludge reflux pump and a fourth sludge reflux pump which are positioned in the sedimentation tank are started to flow back to.

8. The operating method of the high efficiency autotrophic nitrogen removal system for treating high ammonia nitrogen wastewater according to claim 6, wherein the double series A operating mode comprises the following specific steps: the sewage to be treated enters a denitrification tank through a water inlet of the denitrification tank, enters a distribution well through an interception screen on the upper part of a tank body of the denitrification tank, then continuously enters a first reaction tank and a fourth reaction tank through a first water inlet valve, a fourth water inlet valve, a first water inlet and a fourth water inlet respectively, the effluent of the first reaction tank enters a second reaction tank through the first interception screen, a first communication valve and a second interception screen, is collected to a sedimentation tank through the second interception screen and a second water outlet valve, part of effluent of the sedimentation tank flows back to the denitrification tank, and the rest of effluent is discharged from a water outlet pipeline through a water outlet well; and the effluent of the fourth reaction tank enters a third reaction tank through a fourth interception screen, a third communication valve and a third interception screen, the effluent of the third reaction tank is collected into a sedimentation tank after passing through a third interception screen and a third water outlet valve, part of effluent of the sedimentation tank flows back to the denitrification tank, the rest of effluent is discharged from a main water outlet pipeline through a water outlet well, and first to fourth sludge reflux pumps positioned in the sedimentation tank are started to reflux sludge to the reaction tanks.

9. The operating method of the high efficiency autotrophic nitrogen removal system for treating high ammonia nitrogen wastewater according to claim 6, wherein the double series B operating mode comprises the following specific steps: the sewage to be treated enters a denitrification tank through a water inlet of the denitrification tank, enters a water distribution well through an interception screen on the upper part of a tank body of the denitrification tank, then continuously enters a first reaction tank through a first water inlet valve and a first water inlet, the effluent of the first reaction tank enters a second reaction tank through a first interception screen, a first communicating valve and a second interception screen, the effluent of the first reaction tank simultaneously enters a fourth reaction tank through the first interception screen, a fourth communicating valve and a fourth interception screen, the effluent of the second reaction tank enters a third reaction tank through the second interception screen, a second communicating valve and a third interception screen, the effluent of the third reaction tank is collected to a sedimentation tank through a third interception screen and a third water outlet valve, partial effluent of the sedimentation tank flows back to the denitrification tank, the rest effluent is discharged from a main water outlet pipeline through a water outlet well, and the effluent of the fourth reaction tank is collected to the sedimentation tank through the fourth interception screen and a fourth water outlet valve, part of effluent of the sedimentation tank flows back to the denitrification tank, the rest of effluent is discharged from a main effluent pipeline through an effluent well, and first to fourth sludge reflux pumps positioned in the sedimentation tank are started to flow back sludge to each reaction tank.