CN108178304B - Device for rapidly realizing BAF integrated autotrophic denitrification of high ammonia nitrogen wastewater and operation method - Google Patents

Device for rapidly realizing BAF integrated autotrophic denitrification of high ammonia nitrogen wastewater and operation method Download PDF

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CN108178304B
CN108178304B CN201810102963.0A CN201810102963A CN108178304B CN 108178304 B CN108178304 B CN 108178304B CN 201810102963 A CN201810102963 A CN 201810102963A CN 108178304 B CN108178304 B CN 108178304B
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water
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ammonia nitrogen
tank
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CN108178304A (en
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杨庆
李海鑫
李健敏
刘秀红
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Beijing University of Technology
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/301—Aerobic and anaerobic treatment in the same reactor
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
    • C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/02—Temperature
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/04—Oxidation reduction potential [ORP]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/14—NH3-N
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/16—Total nitrogen (tkN-N)
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/22—O2
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C02F2301/046—Recirculation with an external loop
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/14—Maintenance of water treatment installations
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

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  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

A device and an operation method for quickly realizing BAF integrated autotrophic nitrogen removal of high ammonia nitrogen wastewater belong to the field of wastewater treatment methods. The device comprises a reaction device, a water inlet system, a water outlet system, a back flushing system, an aeration system and a temperature control system, wherein the upper part of the reaction device is in a cylindrical shape and the lower end of the reaction device is in a conical shape; the conical shape at the lower end of the reaction device with the combined cylindrical shape at the upper part and the conical shape at the lower end is used as a water inlet area, and the clear water area at the upper part of the cylindrical shape is connected with the water inlet area through a return pipe by a second peristaltic pump; the device adopts a bottom aeration mode to adjust aeration quantity in the starting stage, the normal operation stage and the back flushing stage, so as to control the concentration of dissolved oxygen in the reactor. The sewage denitrification efficiency is improved, and the denitrification cost is saved.

Description

Device for rapidly realizing BAF integrated autotrophic denitrification of high ammonia nitrogen wastewater and operation method
Technical Field
The invention relates to a sewage treatment technology, in particular to a device and an operation method for realizing integrated autotrophic nitrogen removal of high ammonia nitrogen wastewater, and especially relates to a device and an operation method for realizing integrated autotrophic nitrogen removal in a biological aerated filter, which are suitable for nitrogen removal treatment of high ammonia nitrogen wastewater, are beneficial to economically and effectively controlling nitrogen pollution of water, improve sewage nitrogen removal efficiency and save nitrogen removal cost, and belong to the field of sewage treatment methods.
Background
With the rapid development of industry and agriculture, the water consumption of industry and agriculture is increased, but the water resource is limited, so that the environmental problem is also receiving attention of people, and the eutrophication phenomenon of water environment is attracting great attention. The traditional nitrification and denitrification are commonly adopted sewage denitrification methods at present. Traditional nitration is carried out in two steps: firstly, converting ammonia nitrogen into nitrous acid nitrogen under the action of Ammonia Oxidizing Bacteria (AOB); subsequently, nitrogen nitrite is further converted to nitrogen nitrate by the action of Nitrite Oxidizing Bacteria (NOB). The denitrification is that under the condition of oxygen deficiency and existence of organic carbon source, nitric acid nitrogen and nitrous acid nitrogen are reduced into gaseous nitrogen (N) 2 ) Is a process of (2).
The integrated autotrophic denitrification process means that the shortcut nitrification and the anaerobic ammonia oxidation process are realized in the same reactor, and the aim of denitrification is finally realized. Under aerobic conditions, ammonia Oxidizing Bacteria (AOB) consume oxygen to oxidize ammonia nitrogen into nitrite nitrogen, a reaction matrix is provided for the ANAMMOX reaction, and the Anamox bacteria convert the residual ammonia nitrogen and the generated nitrite nitrogen into nitrogen under anaerobic conditions. Compared with the traditional biological denitrification process, the aeration amount can be saved by 63%, the carbon source can be saved by 100%, and the sludge yield can be reduced by 80%. Meanwhile, the method has the advantages of high load removal, less greenhouse gas generation and the like. The realization of integration has important significance for improving the denitrification efficiency and saving energy and carbon sources, so the process has wide development prospect and is a sustainable development process.
Since the 70 s of the last century, biofilm processes have become a research hotspot for a vast number of researchers and engineers. The biological filter is a traditional process for treating sewage by a biological membrane method, and is developed at the end of the 19 th century and is preceded by an activated sludge method. The aeration biological filter is a modified form of the common biological filter, gradually develops from a single process to a series of comprehensive processes, and has the function of removing SS, COD, BOD 5 The functions of nitrification and denitrification are characterized by integrating biological oxidation and suspended solid interception, saving a subsequent secondary sedimentation tank and simplifying the treatment process on the premise of ensuring the treatment effect. In addition, the aeration biological filter process has high organic matter volume load, large hydraulic load, short hydraulic retention time, small investment in required capital construction, low energy consumption and running cost, and good effluent quality. Therefore, the research on the rapid implementation method and the stability problem of the integrated autotrophic nitrogen removal of the aeration biological filter has important theoretical significance and application prospect.
Disclosure of Invention
The invention aims to provide a device and an operation method for rapidly realizing the integrated autotrophic nitrogen removal of a high ammonia nitrogen wastewater biological aerated filter, and the device and the operation method provide optimal environmental control parameters by applying various regulation and control methods which are favorable for realizing the integrated autotrophic nitrogen removal of the biological aerated filter, thereby achieving the effect of rapidly realizing the integrated autotrophic nitrogen removal of the biological aerated filter.
The technical scheme of the invention is as follows:
the device for quickly realizing the integration of the high ammonia nitrogen wastewater aeration biological filter is characterized by comprising a reaction device, a water inlet system, a water outlet system, a back flushing system, an aeration system and a temperature control system, wherein the reaction device is formed by combining an upper part cylinder and a lower end cone; the conical type of the lower end of the reaction device (22) with the combined upper part cylindrical shape and the lower end conical shape is used as a water inlet area, the cylindrical type of the upper part is sequentially provided with a supporting layer, a filter material layer, a clear water area and a water outlet tank from bottom to top, the water outlet tank (24) is provided with an air outlet (25), the bottom of the filter material layer is provided with a pressure gauge (26), the side surface of the filter material layer is provided with a plurality of sampling ports (23) like 8, the side surface of the filter material layer is also provided with a plurality of filter material taking ports (27), and an aeration disc (7) is arranged in the conical bottom; the water inlet system is communicated with the bottom of the conical water inlet area through a water inlet tank (1), a water inlet pipe (2), a first peristaltic pump (3) and a valve; the water outlet groove at the top of the cylinder is communicated with a water outlet tank/back flushing water inlet tank (8) through a water outlet pipe (17); the water outlet tank/back flush water inlet tank (8) is connected with the conical bottom through a back flush water pump (9), a rotameter (11) and a valve through a back flush water inlet pipe (10); the water outlet tank (24) is connected with a backflushing water tank (19) through a backflushing water outlet pipe (18); the cylindrical clear water area is connected with the water inlet area through a return pipe (15) by a second peristaltic pump (16);
the air pump (4) is communicated with the aeration disc through a first air inlet pipe (6) via a first glass rotameter (5) and a valve, and an aeration head is arranged on the aeration disc; the air compressor (12) is communicated with the aeration disc through a second air inlet pipe (14) via a second glass rotameter (13) and a valve; the temperature control device (20) adjusts the temperature of the reaction device through a heating belt (21) on the outer side of the cylinder.
The filter material of the filter material layer of the reactor is volcanic rock, the particle size of the filter material is 3-5mm, and the aeration quantity of the device is regulated in a bottom aeration mode in the starting stage, the normal operation stage and the back flushing stage, so that the concentration of dissolved oxygen in the reactor is controlled.
The operation method of the integrated autotrophic nitrogen removal device for the high ammonia nitrogen wastewater biological aerated filter is characterized by comprising the following steps of:
1) And a system starting stage: opening a water inlet valve to mix the activated sludge from the secondary sedimentation tank with common ammonia nitrogen wastewater (such as common domestic wastewater and ammoniaThe nitrogen concentration is generally 60 mg.L -1 Left-right) according to the volume ratio of 2:1 is pumped into the reactor from the conical section by a first peristaltic pump so that it completely submerges the filter layer; opening a temperature control device, and controlling the temperature to be 25-30 ℃; the air pump is started, so that the gas flows through the first glass rotameter and then enters the reactor through the aeration disc, the gas flow is controlled to be 1-1.5L/h.L (namely, the gas flow per hour of the reaction volume of the effective volume per L is 1-1.5L), and the reactor enters the stuffy and aerated stage; in the aeration stage, DO, pH and ORP are continuously monitored, when 'ammonia valley' appears in the pH or ORP suddenly rises, aeration is closed, one aeration period is ended, then water is drained, and general ammonia nitrogen wastewater fully submerges a filter material layer and enters the next aeration period; reciprocating for 7 days, and then adopting a continuous flow mode to feed water;
i.e., days 8-11, water was fed at a feed water flow rate of 0.09m/h (i.e., water level increased by 0.09m per hour); water is fed at a water feeding flow rate of 0.14m/h in 12 th to 15 th days; on days 16-19, water is fed at a water feed flow rate of 0.21 m/h; under the condition of the three continuous flow water inflow, the aeration mode of the lower aeration disc is still adopted, and the aeration quantity is 10Q m 3 H, Q is the water inflow; internal reflux is carried out from continuous water inflow, the internal reflux ratio is 1:1, and the ammonia nitrogen concentration of the water inflow is gradually increased from continuous water inflow until the ammonia nitrogen water inflow concentration is increased to the ammonia nitrogen concentration of the high ammonia nitrogen wastewater to be treated after 19 days, such as 350mg/L; so far, the shortcut nitrification is successfully started;
after the short-cut nitrification is successfully started, internal reflux is canceled, the effluent of the Anamox filter tank is taken as external reflux liquid to flow into the reactor through the bottom conical device, and the reflux ratio is 1:1 (namely, the ratio of the effluent of the Anamox filter tank to the high ammonia nitrogen wastewater with a volume ratio of 1:1 enters the reactor); after the Total Nitrogen (TN) removal rate is increased, the external reflux of the effluent of the Anamox filter tank is canceled, the internal reflux is changed into the internal reflux, the reflux ratio is 1:1, and the operation is carried out for 80 days to gradually form the BAF high ammonia nitrogen wastewater integrated autotrophic denitrification system; after 140 days, the normal and stable operation is carried out;
2) And (3) a normal operation stage: opening a water inlet valve, then opening a water inlet peristaltic pump, adjusting a rotameter, continuously feeding high ammonia nitrogen wastewater to be treated into a cylindrical aeration biological filter from the conical bottom, oxidizing part of ammonia nitrogen into nitrite nitrogen under the combined action of ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria through a filter material layer, jointly generating nitrogen by the residual ammonia nitrogen and the generated nitrite nitrogen, and discharging the nitrogen from a water outlet tank through a water outlet pipe into a water outlet tank; in the operation stage, an air compressor is turned on, so that gas passes through an air inlet pipe, flows through a glass rotameter, is aerated through an aeration disc and an aeration head, and the concentration of dissolved oxygen in the reactor is maintained to be 1.5-2.5mg/L by adjusting the glass rotameter; the reflux sewage enters the reactor again from the conical bottom after passing through the reflux pump by the reflux pipe, and the reflux ratio is 1:1, a step of;
3) And (3) back flushing operation stage: when the pressure difference of the filter material layer of the reactor, namely the pressure difference between the bottom and the top of the filter material layer of the reactor is more than 1m (the observation pressure represents a number>18 KPa), the water inlet valve, the first peristaltic pump and the second peristaltic pump are closed to perform back flushing, air flushing is performed through the air compressor, water flushing is performed through the back flushing water pump, air-water mixing flushing is performed simultaneously through the air compressor and the back flushing water pump, and air flushing is performed through the bottom aeration disc; the back flush mode is as follows: air-flushing for 4 min, its strength is 8L/(m) 2 S); the air and water are mixed and flushed for 5 minutes, and the air and water strength is 8L/(m) 2 S); the strength of the water flushing for 7 minutes is 8L/(m) 2 ·s)；
4) And (3) returning to the step (2) after the back flushing is finished, and continuing to perform the normal operation stage.
The implementation condition of the integrated autotrophic nitrogen removal process is essentially the optimization of nitrifying bacteria (mainly comprising two major types of bacteria of ammonia oxidizing bacteria and nitrous acid oxidizing bacteria) and anaerobic ammonia oxidizing bacteria structures, namely nitrous acid oxidizing bacteria in the system are eliminated as much as possible, and ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria are reserved.
The device and the operation method for quickly realizing the integrated autotrophic nitrogen removal of the high ammonia nitrogen wastewater biological aerated filter provided by the invention are used for improving the growth rate of AOB and Anamox and reducing the growth rate of nitrite oxidizing bacteria, namely the factors which are most beneficial to enriching the AOB and the Anamox and eliminating nitrite oxidizing bacteria are integrated together, and specifically comprise the following steps:
1) The normal operation temperature of the system is controlled to be about 25-30 ℃, the growth rate of ammonia oxidizing bacteria is larger than that of nitrite oxidizing bacteria, and the system operates at the temperature for a long time, so that enrichment of ammonia oxidizing bacteria is facilitated.
2) The normal operation of the system is controlled at a lower dissolved oxygen concentration of about 1.5-2.5mg/L, and according to the physiological characteristics of microorganisms, the growth rate of ammonia oxidizing bacteria is greater than that of nitrous acid oxidizing bacteria at a lower dissolved oxygen concentration because the affinity of ammonia oxidizing bacteria to oxygen is stronger than that of nitrous acid oxidizing bacteria. Long-term operation under the condition is beneficial to enriching ammonia oxidizing bacteria. Aerobic anoxic environments exist in the biological film with different thicknesses, and living environments are provided for Anamox.
3) The aeration biological filter is subjected to timely and moderate back flushing, and the back flushing period is about 18 days, so that the enrichment of ammonia oxidizing bacteria is facilitated. The generation time of ammonia oxidizing bacteria (i.e., the time for which bacteria multiply) is shorter than the generation time of nitrite oxidizing bacteria. Therefore, proper backwashing can lead nitrite oxidizing bacteria to be discharged out of the system without sufficient propagation, thereby ensuring that the proportion of ammonia oxidizing bacteria in the whole nitrifying bacteria group is continuously improved and further eliminating nitrite oxidizing bacteria.
4) The pH value is controlled within 7.5-8.5 during normal operation of the system, which is beneficial to enriching ammonia oxidizing bacteria. The optimum pH ranges for ammonia oxidizing bacteria and nitrite oxidizing bacteria differ from 7.0 to 8.5 and from 6.5 to 7.5, respectively. Thus, the operation is carried out under the condition for a long time, which is beneficial to enrichment of ammonia oxidizing bacteria.
5) Intermittent aeration is performed in the starting stage, which is beneficial to improving the competitiveness of ammonia oxidizing bacteria. According to the physiological characteristics of the two types of microorganisms, the ammonia oxidizing bacteria in the aerobic stage after each anoxic stage always recover activity earlier than the nitrite oxidizing bacteria, so that the growth rate of the ammonia oxidizing bacteria in the aerobic stage is higher than that of the nitrite oxidizing bacteria, and the growth opportunity of the nitrite oxidizing bacteria is reduced. The anoxic stage at the same time of intermittent aeration is also suitable for the growth of Anamox.
Compared with the existing treatment technology for treating the high ammonia nitrogen wastewater, the integrated autotrophic nitrogen removal device and the operation method of the high ammonia nitrogen wastewater biological aerated filter have the following advantages:
1) The energy saving and consumption reducing effects are good. Most of the cost of the sewage treatment plant is used for electricity consumption and medicine consumption, however, short-cut nitrification only needs to oxidize ammonia nitrogen into nitrous acid nitrogen, and the anaerobic ammonia oxidation process is performed anaerobically, so that 63% of aeration energy consumption is saved, namely, the electricity consumption is reduced, 100% of additional carbon source is saved, and the energy consumption of the sewage treatment plant is reduced.
2) The reliability is high. The aeration biological filter has strong impact load resistance, no sludge expansion problem, no operation for a period of time, no loss of microorganisms and recovery to the normal treatment level within a few days.
3) The capital cost and the running cost are low. The capital cost and the running cost of the aeration biological filter are greatly lower than those of the traditional conventional secondary treatment technology.
4) Simplifying the flow. The aeration biological filter tank integrates filtration, biological adsorption and biological oxidation, can play the roles of a common aeration tank, a secondary sedimentation tank and a sand filter tank at the same time, and completes physical interception and biological treatment in the same reactor.
5) Smaller pool volume and floor space. The occupied area of the aeration biological filter is only about 1/10-1/5 of that of the conventional secondary biological treatment, which has important significance for coastal cities or development areas with more expensive land and economically developed areas, and can find solutions for the situation of shortage of land in some factories.
Drawings
Fig. 1 is a schematic structural view of the present invention.
In the figure: 1, a water inlet tank; 2, a water inlet pipe; 3 a first peristaltic pump; 4, an air pump; 5 a first glass rotameter; 6, a first air inlet pipe; 7, an aeration disc; 8, water outlet tank/back flushing water inlet tank; 9 back flushing the water pump; 10 back flushing the water inlet pipe; 11 rotameter; 12 an air compressor; 13 a second glass rotameter; 14 a second air inlet pipe; 15 return pipes; a second peristaltic pump; 17 a water outlet pipe; 18 back flushing the water outlet pipe; 19 back flushing the water tank; 20 a temperature control device; 21 a heating belt; 22, a reaction device combining the upper part cylindrical shape with the lower end conical shape; 23 sampling ports; 24 water outlet grooves; 25 exhaust ports; 26 pressure gauge; 27, a filter material port is formed;
fig. 2 is a water inlet and outlet effect diagram of the embodiment.
Detailed description of the preferred embodiments
The present invention will be described with reference to the accompanying drawings and examples, but the present invention is not limited to the following examples.
Example 1:
referring to fig. 1, the device for rapidly realizing the integrated autotrophic biological denitrification of the high ammonia nitrogen wastewater aeration biological filter is as follows: the device is provided with a reaction device combining a cylindrical shape and a conical shape, a water inlet system, a water outlet system, a reflux system, a back flushing system, an aeration system and a temperature control system. The upper part of the reaction device 22 combining the cylindrical shape with the conical shape at the lower end is provided with a conical water inlet area, a cylindrical supporting layer, a filter material layer, a clear water area and a water outlet tank 24, an exhaust port 25 is arranged on the water outlet tank 24, the cylindrical reactor part is provided with the filter material layer, the bottom of the filter material layer is provided with a pressure gauge 26, the filter material layer part of the reactor is provided with 8 sampling ports 23 and 5 filter material taking ports 27, the lower part of the reactor is provided with the pressure gauge 26, and an aeration disc 7 is arranged in the conical reactor; the water inlet system is communicated with the conical water inlet area through a water inlet tank 1, a water inlet pipe 2, a first peristaltic pump 3 and a valve; the top of the cylindrical reactor is communicated with the water outlet tank/back flushing water inlet tank 8 through a water outlet tank 24 and a water outlet pipe 17; the water outlet tank/back flush inlet tank 8 is communicated with the conical reactor part through a back flush water pump 9, a rotameter 11, a back flush water inlet pipe 10 and a valve; the water outlet tank 24 is communicated with the backflushing water tank 19 through the backflushing water outlet pipe 18; the air pump 4 is communicated with the aeration disc 7 through the first glass rotameter 5, the first air inlet pipe 6 and the valve; the air compressor 12 is communicated with the aeration disc 7 through a second air inlet pipe 14, a second glass rotameter 13 and a valve; part of the effluent is connected with a conical area at the bottom of the reactor through a return pipe 15, a second peristaltic pump 16 and a valve; the temperature control device 20 adjusts the temperature of the reaction device by the heating belt 21. The filter material of the filter material layer of the reactor is volcanic rock, the particle size of the filter material is 3-5mm, and the aeration quantity is regulated in a bottom aeration mode in the starting stage, the normal operation stage and the back flushing stage of the device, so that the concentration of dissolved oxygen in the reactor is controlled.
Aeration of high ammonia nitrogen wastewaterThe operation method of the integrated autotrophic nitrogen removal device of the biological filter tank takes the autotrophic water as an experimental object: NH (NH) 4 The effective volume of the empty pool of the selected aeration biological filter is 19.2L, and the operation method is completed according to the following steps:
1) A starting stage: opening a water inlet valve to mix the activated sludge from the secondary sedimentation tank with common ammonia nitrogen wastewater (ammonia nitrogen concentration NH) 4 + -n=60 mg/L) at 2:1 is pumped into the reactor from the conical reactor part through a peristaltic pump so as to completely submerge the filter material layer; opening a temperature control device, and controlling the temperature to be about 30 ℃; the air compressor is turned on, so that the gas flows through the first glass rotameter and then enters the reactor through the aeration disc, the gas flow is controlled at 25L/h, and the gas enters the stuffy and aerated stage. In this stage, DO, pH and ORP are continuously monitored, when "ammonia valley" occurs in pH or ORP suddenly rises, aeration is turned off, one aeration cycle is ended, and sewage is exchanged into the next aeration cycle. This was repeated for 7 days, after which water was fed in a continuous flow. Water is fed at a flow rate of 0.04m/h for days 8-11, NH 4 The load of + -N is 0.22 kg/(m) 3 D) a step of; water is fed at a flow rate of 0.08m/h for 12-15 days, NH 4 The + -N load is 0.51 kg/(m) 3 D) a step of; on days 16-19, water is fed at a designed flow rate of 0.12m/h, NH 4 The load of + -N is 0.77 kg/(m) 3 D) is described. Under the condition of three continuous flow water inflow, the aeration mode of the lower aeration disc is adopted, and the aeration rate is 10Q m 3 /h (Q is water inflow), NH after stable treatment effect 4 + The N concentration gradually increases to 350 mg.L -1 The method comprises the steps of carrying out a first treatment on the surface of the The internal reflux ratio was 1:1. So far, the shortcut nitrification is successfully started. And taking the effluent of the Anamox filter as external reflux after the short-cut nitrification is successfully started. After the Total Nitrogen (TN) removal rate is increased, the external reflux of the effluent of the Anamox filter tank is canceled, the BAF internal reflux is adopted instead, and the BAF high ammonia nitrogen wastewater integrated autotrophic nitrogen removal system is gradually formed after the operation is carried out for 80 days, and the operation is normally and stably carried out after 140 days.
2) And (3) a normal operation stage: opening a water inlet valve, then opening a water inlet peristaltic pump, adjusting a rotameter, enabling the water inlet flow to be 1.85L/h, continuously feeding high ammonia nitrogen wastewater to be treated into an aeration biological filter from the conical bottom, oxidizing ammonia nitrogen into nitrite nitrogen under the combined action of ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria through a filter material layer, enabling the generated nitrite nitrogen and residual ammonia nitrogen to react to generate nitrogen, and enabling the nitrogen to flow through a water outlet pipe from a water outlet tank to be discharged into a water outlet tank; in the operation stage, an air pump is started to enable air to pass through an air inlet pipe, after the air passes through a glass rotameter, an aeration disc and an aeration head are used for aerating a clear water area, and the concentration of dissolved oxygen in a reactor is maintained to be 1.5-2.5mg/L by adjusting the glass rotameter; the reflux sewage is returned to the reactor from the conical bottom after passing through the reflux pump through the reflux pipe.
3) And (3) back flushing operation stage: when the pressure difference of the filter material layer of the reactor, namely the pressure difference of the bottom and the top of the filter material layer of the reactor is more than 1m (the reading of a pressure gauge is observed>18 KPa), the water inlet valve and the peristaltic pump are closed to perform back flushing, the air flushing is performed through the air compressor, the water flushing is performed through the back flushing water pump, the air-water mixing flushing is performed simultaneously through the air compressor and the back flushing water pump, and the air flushing is performed through the bottom aeration disc. The back flush mode is as follows: air-flushing for 4 min, its strength is 8L/(m) 2 S); the air and water are mixed and flushed for 5 minutes, and the air and water strength is 8L/(m) 2 S); the strength of the water flushing for 7 minutes is 8L/(m) 2 ·s)。
4) And (3) returning to the step (2) after the back flushing is finished, namely, the normal operation stage.
The water inlet and outlet effects of the process are shown in figure 2.

Claims (5)

1. The running method for denitrification treatment of ammonia nitrogen wastewater is characterized in that the adopted device is a device for quickly realizing integration of a high ammonia nitrogen wastewater biological aerated filter, and a reaction device, a water inlet system, a water outlet system, a back flushing system, an aeration system and a temperature control system are combined with each other in a cylindrical shape at the upper part and a conical shape at the lower end; the conical type of the lower end of the reaction device (22) with the combined upper part cylindrical shape and the lower end conical shape is used as a water inlet area, the cylindrical type of the upper part is sequentially provided with a supporting layer, a filter material layer, a clear water area and a water outlet tank from bottom to top, the water outlet tank (24) is provided with an air outlet (25), the bottom of the filter material layer is provided with a pressure gauge (26), the side surface of the filter material layer is provided with a plurality of sampling ports (23), the side surface of the filter material layer is also provided with a plurality of filter material taking ports (27), and the conical bottom is internally provided with an aeration disc (7); the water inlet system is communicated with the bottom of the conical water inlet area through a water inlet tank (1), a water inlet pipe (2), a first peristaltic pump (3) and a valve; the water outlet groove at the top of the cylinder is communicated with a water outlet tank/back flushing water inlet tank (8) through a water outlet pipe (17); the water outlet tank/back flush water inlet tank (8) is connected with the conical bottom through a back flush water pump (9), a rotameter (11) and a valve through a back flush water inlet pipe (10); the water outlet tank (24) is connected with a backflushing water tank (19) through a backflushing water outlet pipe (18); the cylindrical clear water area is connected with the water inlet area through a return pipe (15) by a second peristaltic pump (16);
the air pump (4) is communicated with the aeration disc through a first air inlet pipe (6) via a first glass rotameter (5) and a valve, and an aeration head is arranged on the aeration disc; the air compressor (12) is communicated with the aeration disc through a second air inlet pipe (14) via a second glass rotameter (13) and a valve; the temperature control device (20) adjusts the temperature of the reaction device through a heating belt (21) at the outer side of the cylinder; the filter material of the filter material layer of the reactor is volcanic rock, and the particle size is 3-5mm;
the operation method comprises the following steps:
1) And a system starting stage: opening a water inlet valve, and mixing the activated sludge from the secondary sedimentation tank with common ammonia nitrogen wastewater according to a volume ratio of 2:1 is pumped into the reactor from the conical section by a first peristaltic pump so that it completely submerges the filter layer; opening a temperature control device, and controlling the temperature to be 25-30 ℃; the air pump is started, so that the gas flows through the first glass rotameter and then enters the reactor through the aeration disc, the gas flow is controlled to be 1-1.5L/h.L, and the gas enters the stuffy and aerated stage; in the aeration stage, DO, pH and ORP are continuously monitored, when 'ammonia valley' appears in the pH or ORP suddenly rises, aeration is closed, one aeration period is ended, then water is drained, and general ammonia nitrogen wastewater is replaced to completely submerge a filter material layer into the next aeration period; reciprocating for 7 days, and then adopting a continuous flow mode to feed water;
i.e. days 8-11, water is fed at a water feed flow rate of 0.09 m/h; water is fed at a water feeding flow rate of 0.14m/h in 12 th to 15 th days; on days 16-19, the water is fed at a water feeding flow rate of 0.21m/hWater; under the condition of the three continuous flow water inflow, the aeration mode of the lower aeration disc is still adopted, and the aeration quantity is 10Q m 3 H, Q is the water inflow; internal reflux is carried out from continuous water inflow, the internal reflux ratio is 1:1, and the ammonia nitrogen concentration of the water inflow is gradually increased from continuous water inflow until the ammonia nitrogen water inflow concentration is increased to the ammonia nitrogen concentration of the high ammonia nitrogen wastewater to be treated after 19 days; so far, the shortcut nitrification is successfully started;
after the short-cut nitrification is successfully started, internal reflux is canceled, effluent of the Anamox filter tank is taken as external reflux liquid and flows into the reactor through the bottom cone device, and the reflux ratio is 1:1; after the Total Nitrogen (TN) removal rate is increased, the external reflux of the effluent of the Anamox filter tank is canceled, the internal reflux is changed into the internal reflux, the reflux ratio is 1:1, and the operation is carried out for 80 days to gradually form the BAF high ammonia nitrogen wastewater integrated autotrophic denitrification system; after 140 days, the normal and stable operation is carried out;
2) And (3) a normal operation stage: opening a water inlet valve, then opening a water inlet peristaltic pump, adjusting a rotameter, continuously feeding high ammonia nitrogen wastewater to be treated into a cylindrical aeration biological filter from the conical bottom, oxidizing part of ammonia nitrogen into nitrite nitrogen under the combined action of ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria through a filter material layer, jointly generating nitrogen by the residual ammonia nitrogen and the generated nitrite nitrogen, and discharging the nitrogen from a water outlet tank to a water outlet tank/backwash water inlet tank through a water outlet pipe; in the operation stage, an air compressor is turned on, so that gas passes through an air inlet pipe, flows through a glass rotameter, is aerated through an aeration disc and an aeration head, and the concentration of dissolved oxygen in the reactor is maintained to be 1.5-2.5mg/L by adjusting the glass rotameter; the reflux sewage enters the reactor again from the conical bottom after passing through the reflux pump by the reflux pipe, and the reflux ratio is 1:1, a step of;
3) And (3) back flushing operation stage: when the pressure difference of the filter material layer of the reactor, namely the pressure difference between the bottom and the top of the filter material layer of the reactor is more than 1m, closing a water inlet valve, a first peristaltic pump and a second peristaltic pump, and back flushing;
4) And (3) returning to the step (2) after the back flushing is finished, and continuing to perform the normal operation stage.
2. The method of claim 1, wherein the high ammonia nitrogen concentration is 350mg/L.
3. The method according to claim 1, wherein the back flushing in the step 3) is performed by an air compressor, the water flushing is performed by a back flushing water pump, the air-water mixing flushing is performed by the air compressor and the back flushing water pump simultaneously, and the air flushing is performed by a bottom aeration disc; the back flush mode is as follows: air-flushing for 4 min, its strength is 8L/(m) 2 S); the air and water are mixed and flushed for 5 minutes, and the air and water strength is 8L/(m) 2 S); the strength of the water flushing for 7 minutes is 8L/(m) 2 ·s)。
4. The method of claim 1, wherein the system is controlled to a normal operating temperature of 25 ℃ to 30 ℃.
5. The method according to claim 1, wherein the pH of the system in normal operation is controlled between 7.5 and 8.5.
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CN104355404A (en) * 2014-10-27 2015-02-18 北京工业大学 Method and device for rapidly realizing anaerobic ammonia oxidation of bacteria filter
CN105110462A (en) * 2015-09-14 2015-12-02 北京工业大学 Device and method for quickly achieving shortcut nitrification of high-ammonia-nitrogen waste water biological aerated filter
CN208166668U (en) * 2018-02-01 2018-11-30 北京工业大学 A kind of device fast implementing high ammonia-nitrogen wastewater BAF integration autotrophic denitrification

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CN102775027A (en) * 2012-08-15 2012-11-14 北京城市排水集团有限责任公司 Granular sludge integrated autotrophic nitrogen removal device and operating method thereof
CN104355404A (en) * 2014-10-27 2015-02-18 北京工业大学 Method and device for rapidly realizing anaerobic ammonia oxidation of bacteria filter
CN105110462A (en) * 2015-09-14 2015-12-02 北京工业大学 Device and method for quickly achieving shortcut nitrification of high-ammonia-nitrogen waste water biological aerated filter
CN208166668U (en) * 2018-02-01 2018-11-30 北京工业大学 A kind of device fast implementing high ammonia-nitrogen wastewater BAF integration autotrophic denitrification

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