CN113526668A - Device and method for simultaneously realizing urban sewage treatment and excess sludge reduction - Google Patents
Device and method for simultaneously realizing urban sewage treatment and excess sludge reduction Download PDFInfo
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- CN113526668A CN113526668A CN202110612429.6A CN202110612429A CN113526668A CN 113526668 A CN113526668 A CN 113526668A CN 202110612429 A CN202110612429 A CN 202110612429A CN 113526668 A CN113526668 A CN 113526668A
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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
- C02F3/302—Nitrification and denitrification treatment
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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
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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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
- C02F2303/00—Specific treatment goals
- C02F2303/06—Sludge reduction, e.g. by lysis
Abstract
The invention belongs to the technical field of biological sewage treatment, and relates to a device and a method for simultaneously realizing urban sewage treatment and excess sludge reduction.
Description
The technical field is as follows:
the invention belongs to the technical field of biological sewage treatment, and relates to a device and a method for simultaneously realizing urban sewage treatment and excess sludge reduction.
Background art:
along with the acceleration of the urbanization process and the increasing of urban population, the urban sewage discharge amount is increased year by year. According to statistics, the number of sewage treatment plants in China reaches more than 10000 by 1 month in 2020, and the sewage treatment capacity in 2019 is increased by 18000 million tons/day compared with 2018. During the operation of the sewage treatment process, a part of sludge generated by the process is returned as a reactant of biological reaction, and the rest sludge is discharged out of the system. The amount of these excess sludges is surprising, with high water content, large volume, putrescibility, odor and containing large amounts of toxic and harmful substances such as heavy metals, germs and the like. How to treat the sludge becomes a great problem to be solved urgently in China. Therefore, if the treatment is not carried out through a scientific system, the pollution to the surrounding water body or soil can be serious, and even the damage to the human health can be caused. The treatment modes of sludge in China are divided into modes of landfill, composting, natural drying, incineration and the like, and the four treatment methods are 65%, 15%, 6% and 3% respectively. It can be seen that the landfill mode is still dominant, and the mode directly causes secondary pollution, and poses serious threat to the ecological environment.
In addition, water eutrophication caused by N, P discharge is also a big reason for water deterioration, and China promulgates strict sewage discharge standards, wherein the first-level standard requires that TP is less than 0.1mg/L, total nitrogen is less than 15mg/L, and ammonia nitrogen is less than 5 mg/L. Therefore, a newly-built sewage treatment plant is required to be equipped with a nitrogen and phosphorus removal device.
In the traditional denitrification process, the ratio of COD to nitrogen is the key of the removal efficiency, the nitrification and denitrification process needs a sufficient carbon source, and the denitrification efficiency is high. The carbon source in the municipal sewage is far from enough, and the external carbon source is required to be added for deep denitrification, so that the treatment cost is greatly increased; and the excess sludge is a byproduct of the biological conversion process after the secondary clarification, which is a cheap carbon source, so that the investment cost is reduced on one hand, and the yield of the sludge is also reduced on the other hand. Anaerobic sludge fermentation releases inorganic or organic carbon sources through the decay and cell lysis of autotrophic or heterotrophic microorganisms, proteins and some carbohydrates are hydrolyzed and fermented to organic acids, providing electrons and energy for the denitrification process, and WAS addresses the problem of sludge disposal during decay. But the ammonia nitrogen produced is not removed by sludge fermentation alone.
The invention content is as follows:
the invention aims to overcome the defects in the prior art, and provides a device and a method for simultaneously realizing municipal sewage treatment and excess sludge reduction.
In order to achieve the purpose, the device for simultaneously realizing urban sewage treatment and excess sludge reduction comprises an urban sewage raw water tank, a whole-course nitrification SBR reactor, a first intermediate water tank, a sludge fermentation and short-course denitrification integrated SFPD reactor, a sludge storage tank, a second intermediate water tank, an anaerobic ammonia oxidation UASB reactor and a water outlet tank; the urban sewage raw water tank is connected with the full-course nitrification SBR reactor through a first water inlet pump; the air pump is connected with the full-process nitrification SBR reactor; the full-process nitrification SBR reactor is connected with a first intermediate water tank through a first electric drain valve; the first intermediate water tank is connected with the sludge fermentation and short-cut denitrification SFPD reactor through a second water inlet pump; the sludge storage tank is connected with the sludge fermentation synchronous short-cut denitrification SFPD reactor by a peristaltic pump; the sludge discharge box is connected with the sludge fermentation synchronous short-cut denitrification SFPD reactor through a sludge discharge valve; the sludge fermentation synchronous short-cut denitrification SFPD reactor is connected with a second intermediate water tank through a second electric drain valve, and the second intermediate water tank is connected with the bottom of the anaerobic ammonia oxidation UASB reactor through a third water inlet pump; the anaerobic ammonia oxidation UASB reactor is connected with the water outlet tank through a third electric drain valve.
A first stirring paddle is arranged in the whole-course nitrification SBR reactor, one end of the first stirring paddle, extending out of the whole-course nitrification SBR reactor, is connected with a stirrer, a gas flowmeter is arranged on a pipeline of an air pump, connected with the whole-course nitrification SBR reactor, a pH sensor and a DO sensor are arranged in the whole-course nitrification SBR reactor and are respectively connected with a pH/DO tester, and a first sampling port is formed in the side wall of the whole-course nitrification SBR reactor above a first electric drain valve.
The sludge fermentation synchronous short-cut denitrification SFPD reactor is internally provided with a second stirring paddle, one end of the second stirring paddle, which extends out of the sludge fermentation synchronous short-cut denitrification SFPD reactor, is connected with a stirrer, a heating rod, a pH sensor, a temperature sensor and an ORP sensor are arranged in the sludge fermentation synchronous short-cut denitrification SFPD reactor, the pH sensor and the temperature sensor are respectively connected with a pH/temperature tester, and the ORP sensor is connected with the ORP tester.
A resistance wire and temperature control equipment are arranged in the anaerobic ammonia oxidation UASB reactor, the top end of the anaerobic ammonia oxidation UASB reactor is communicated with a gas collecting bottle, four second sampling ports are formed in the side wall of the water outlet end of the anaerobic ammonia oxidation UASB reactor, and a third water inlet pump is connected with the top of the anaerobic ammonia oxidation UASB reactor through a peristaltic pump.
The treatment process of the municipal sewage in the device comprises the following steps: pumping the urban sewage into a full-process nitrification SBR reactor from an urban sewage raw water tank through a first water inlet pump, and reducing nitrate nitrogen generated in the last aerobic stage into nitrogen by denitrifying bacteria by using organic matters in the inlet water in an anoxic stirring stage; in the aerobic stirring stage, ammonia nitrogen in the inlet water is converted into nitrate nitrogen through nitration reaction, and the outlet water enters a sludge fermentation synchronous short-cut denitrification SFPD reactor; the residual sludge enters a sludge fermentation synchronous short-cut denitrification SFPD reactor through a peristaltic pump, a series of short-chain fatty acids are generated through hydrolytic acidification reaction in the sludge fermentation process, meanwhile, denitrifying bacteria perform short-cut denitrification reaction by using the short-chain fatty acids as carbon sources to convert nitrate nitrogen into nitrite nitrogen, and effluent is pumped into an anaerobic ammonia oxidation UASB reactor through a second intermediate water tank by a third water inlet pump; in an anaerobic ammonia oxidation UASB reactor, ammonia nitrogen and nitrite nitrogen generate nitrogen and a small amount of nitrate nitrogen through anaerobic ammonia oxidation reaction so as to realize autotrophic nitrogen removal of municipal sewage.
The specific process for simultaneously realizing the reduction of the urban sewage and the excess sludge comprises the following steps:
1) and (3) starting a system:
adding nitrified sludge with good nitrification performance into the whole-course nitrification SBR reactor, so that the concentration of suspended activated sludge in the inoculated whole-course nitrification SBR reactor reaches 4500-5500 mg/L; inoculating sludge with short-cut denitrification characteristics into a sludge fermentation synchronous short-cut denitrification SFPD reactor, so that the concentration of activated sludge in the reactor reaches 8000-12000 mg/L; adding floc sludge with anaerobic ammonia oxidation activity into an anaerobic ammonia oxidation UASB reactor, and enabling the concentration of activated sludge in the inoculated reactor to reach 3000-5000 mg/L;
2) the run-time adjustments are as follows:
adding urban sewage into an urban sewage raw water tank, starting a first water inlet pump to pump the urban sewage into a full-process nitrification SBR reactor, carrying out anoxic stirring for 80-120 min, then carrying out aerobic stirring for 120-150 min, stopping aeration when the ammonia nitrogen removal rate reaches the maximum, precipitating and draining water, wherein the drainage ratio is 0.4-0.6, and discharging the discharged water into a first intermediate water tank; the aerobic aeration stirring means that the DO concentration is 0.5-1.0 mg/L;
pumping effluent containing nitrate nitrogen in the first intermediate water tank into a sludge fermentation synchronous short-cut denitrification SFPD reactor through a second water inlet pump, starting a peristaltic pump to pump residual sludge in a sludge tank into the sludge fermentation synchronous short-cut denitrification SFPD reactor, carrying out anoxic stirring for 12-48 h, controlling the temperature in the reactor to be 30-40 ℃ by using a heating rod, maintaining the pH value to be 9-11 through NaOH solution, stopping stirring when the concentration of the nitrate nitrogen in the reaction is lower than 1.0mg/L and the concentration of ammonia nitrogen reaches the maximum, precipitating and draining, and discharging effluent into a second intermediate water tank; in addition, when the sludge concentration in the reactor is lower than 8000mg/L, closing a sludge discharge valve to avoid sludge discharge so as to ensure the amount of activated sludge in the reactor;
pumping the effluent containing ammonia nitrogen and nitrite nitrogen in the second intermediate water tank into an anaerobic ammonia oxidation UASB reactor through a third water inlet pump, heating the reactor through a resistance wire, controlling the temperature at 30-35 ℃, controlling the rotation speed of the third water inlet pump to ensure that the water in the reactor stays for 4-8 h, and discharging the effluent into an effluent water tank.
Compared with the prior art, the method combines the advantages of sludge fermentation, short-cut denitrification and anaerobic ammonia oxidation, removes organic matters generated in the fermentation process of the excess sludge while realizing autotrophic denitrification of the municipal sewage, does not need to add an external organic carbon source, utilizes the fermentation product as the carbon source and realizes the reduction of the excess sludge, and has the following advantages:
1) the sludge fermentation acid production technology and the short-cut denitrification anaerobic ammonia oxidation technology are jointly applied to the denitrification process of the municipal sewage, the fatty acid generated by fermentation is directly used as a carbon source, an additional organic carbon source is not needed, and the problems of low C/N ratio and insufficient carbon source in the denitrification process of the municipal sewage are solved; meanwhile, the denitrifying bacteria utilize fatty acid generated by fermentation as a carbon source, so that the driving force of mass transfer of the system is increased;
2) the influent water of the sludge fermentation synchronous denitrification SFPD reactor contains a large amount of nitrate nitrogen, and due to the existence of the electron acceptors, the strict anaerobic state in the system is destroyed, so that the oxidation-reduction potential ORP is increased, the growth of strict anaerobic methanogens is inhibited, the methanogenic reaction is avoided, and the consumption of the methanogens on short-chain fatty acids is reduced, so that the nitrate nitrogen can be fully utilized as a denitrification carbon source;
3) the denitrification reaction consumes a large amount of organic acid generated by fermentation, so that the alkalinity is supplemented for the system, and a better growth environment is created for the hydrolytic zymophyte;
4) the denitrifying bacteria utilize fatty acid generated by fermentation as a carbon source, so that the denitrification effect can be enhanced, and organic matters in a solid phase are transferred to a liquid phase, so that sludge reduction is realized, the effects of less sludge discharge, no sludge discharge and even sludge consumption are achieved, and the two problems of insufficient denitrification carbon source and large residual sludge yield of a sewage plant at the present stage are solved.
Description of the drawings:
FIG. 1 is a schematic structural diagram of an apparatus for simultaneously performing municipal sewage treatment and excess sludge reduction according to the present invention, wherein 1 is a raw municipal sewage tank; 2 is a full-process nitration SBR reactor; 3 is a first intermediate water tank; 4 is a sludge tank; 5 is a sludge fermentation synchronous short-cut denitrification SFPD reactor; 6 is a sludge storage tank; 7 is a second intermediate water tank; 8 is an anaerobic ammonia oxidation UASB reactor; 9 is a water outlet tank; 2.1 is a first water inlet pump; 2.2 is a first electric drain valve; 2.3 is a first sampling port; 2.4 is a stirrer; 2.5 is a first stirring paddle; 2.6 is an air pump; 2.7 is a gas flowmeter; 2.8 is a pH sensor; 2.9 is a DO sensor; 2.10 is a pH/DO meter; 5.1 is a peristaltic pump; 5.2 is a stirrer; 5.3 is a second stirring paddle; 5.4 is a second water inlet pump; 5.5 is a heating rod; 5.6 is a pH sensor; 5.7 is a temperature sensor; 5.8 is a pH/temperature measuring instrument; 5.9 is a mud valve; 5.10 is a sampling port; 5.11 is an ORP sensor; 5.12 is ORP measuring instrument, 5.13 is a second electric drain valve, and 8.1 is a third water inlet pump; 8.2 is a peristaltic pump; 8.3 is resistance wire; 8.4 is temperature control equipment; 8.5 is a second sampling port; 8.6 is a third electric drain valve; 8.7 is a gas collecting bottle; and 9 is a water outlet tank.
Detailed Description
The invention is further described below with reference to the accompanying drawings and examples.
Example (b):
the structure of the device for simultaneously realizing urban sewage treatment and excess sludge reduction in the embodiment is shown in fig. 1, and the process for synchronously carrying out short-cut denitrification and anaerobic ammonia oxidation treatment on urban sewage and realizing excess sludge reduction comprises an urban sewage raw water tank 1, a full-cut nitrification SBR reactor 2, a first intermediate water tank 3, a sludge tank 4, an SFPD reactor 5 integrating sludge fermentation and short-cut denitrification, a sludge storage tank 6, a second intermediate water tank 7, an anaerobic ammonia oxidation UASB reactor 8 and a water outlet tank 9; the urban sewage raw water tank 1 is connected with the whole-course nitrification SBR reactor 2 through a first water inlet pump 2.1; the air pump 2.6 is connected with the full-process nitrification SBR reactor 2; the full-process nitrification SBR reactor 2 is connected with a first intermediate water tank 3 through a first electric drain valve 2.2; the first intermediate water tank 3 is connected with a sludge fermentation and short-cut denitrification SFPD reactor 5 through a second water inlet pump 5.4; the sludge storage tank 6 is connected with the sludge fermentation synchronous short-cut denitrification SFPD reactor 5 by a peristaltic pump 5.1; the sludge discharge box 6 is connected with the sludge fermentation synchronous short-cut denitrification SFPD reactor 5 through a sludge discharge valve 5.9; the sludge fermentation synchronous short-cut denitrification SFPD reactor 5 is connected with a second intermediate water tank 7 through a second electric drain valve 5.13, and the second intermediate water tank 7 is connected with the bottom of an anaerobic ammonia oxidation UASB reactor 8 through a third water inlet pump 8.1; the anaerobic ammonia oxidation UASB reactor 8 is connected with a water outlet tank 9 through a third electric drain valve 8.6.
This embodiment whole journey nitrifies SBR reactor 2 and embeds first stirring rake 2.5, and first stirring rake 2.5 stretches out whole journey nitrifies the one end of SBR reactor 2 and is connected with agitator 2.4, and air pump 2.6 is equipped with gas flowmeter 2.7 on the pipeline of whole journey nitrifying SBR reactor 2 and being connected, and pH sensor 2.8 and DO sensor 2.9 set up in whole journey nitrifying the SBR reactor and link to each other with pH/DO apparatus 2.10 respectively, and it has first sample connection 2.3 to open on the whole journey nitrifying SBR reactor 2 lateral wall above first electric drainage valve 2.2.
In the embodiment, the sludge fermentation synchronous short-cut denitrification SFPD reactor 5 is internally provided with a second stirring paddle 5.3, one end of the second stirring paddle 5.3, which extends out of the sludge fermentation synchronous short-cut denitrification SFPD reactor 5, is connected with a stirrer 5.2, a heating rod 5.5, a pH sensor 5.6, a temperature sensor 5.7 and an ORP sensor 5.11 are arranged in the sludge fermentation synchronous short-cut denitrification SFPD reactor 5, the pH sensor 5.6 and the temperature sensor 5.7 are respectively connected with a pH/temperature tester 5.8, and the ORP sensor 5.11 is connected with an ORP tester 5.12.
This embodiment anaerobic ammonium oxidation UASB reactor 8 embeds resistance wire 8.3 and temperature control equipment 8.4, and the top and the gas collecting bottle 8.7 intercommunication of anaerobic ammonium oxidation UASB reactor 8 open on the water outlet end lateral wall of anaerobic ammonium oxidation UASB reactor 8 has four second sample connection 8.5, and third water-intake pump 8.1 is connected with anaerobic ammonium oxidation UASB reactor 8 top through peristaltic pump 8.2.
This embodiment adopts the device to test, and in the experimentation, the test water is taken from certain university's family district domestic sewage, and specific quality of water is as follows: COD concentration is 160-250 mg/L, NH4 +The concentration of-N is 40-60 mg/L, NO2 -Concentration of-N<0.5mg/L，NO3 -Concentration of-N<1mg/L, each reactor is made of organic glass materials, wherein the effective volume of the whole-course nitration SBR reactor 2 is 5L, the effective volume of the sludge fermentation synchronous short-range denitrification SFPD reactor 5 is 5L, and the anaerobic ammonia oxidation UASB reactor 7 is provided withThe effective volume is 3.5L, and the specific process is as follows:
1) and (3) starting a system:
adding nitrifying sludge with good nitrification performance into the whole-course nitrifying SBR reactor 2, so that the concentration of suspended activated sludge in the inoculated whole-course nitrifying SBR reactor 2 reaches 5000 mg/L; inoculating sludge with short-cut denitrification characteristics into a sludge fermentation synchronous short-cut denitrification SFPD reactor, and simultaneously adding residual sludge in a secondary sedimentation tank of a sewage plant to enable the concentration of activated sludge in the reactor to reach 11000 mg/L; adding floc sludge with anaerobic ammonia oxidation activity to anaerobic ammonia oxidation UASB (upflow anaerobic sludge blanket) to ensure that the concentration of activated sludge in the inoculated reactor reaches 4500 mg/L;
2) the run-time adjustments are as follows:
adding municipal sewage into a municipal sewage raw water tank 1, starting a first water inlet pump 2.1, pumping 2L of municipal sewage into a full-process nitrification SBR reactor 2, stirring for 100min under oxygen deficiency, stirring for 140min under aerobic condition, stopping aeration when the removal rate of ammonia nitrogen reaches the maximum, precipitating and draining water, wherein the drainage ratio is 0.4, and discharging the discharged water into a first intermediate water tank 3; the aerobic aeration stirring means that the DO concentration is 0.8 mg/L;
pumping 2L of effluent containing nitrate nitrogen in the first intermediate water tank 3 into a sludge fermentation synchronous short-cut denitrification SFPD reactor 5 through a second water inlet pump 5.4, starting a peristaltic pump 5.1 to pump 250mL of excess sludge in a sludge tank 4 into the sludge fermentation synchronous short-cut denitrification SFPD reactor 5, stirring for 24h under oxygen deficiency, stopping stirring when the concentration of the nitrate nitrogen is lower than 1.0mg/L and the concentration of ammonia nitrogen reaches the maximum in the reaction, precipitating and draining, and discharging the effluent into a second intermediate water tank 7; in addition, the temperature in the reactor is controlled to be 35 ℃ by using a heating rod 5.5, the pH value is maintained to be about 9 by using NaOH solution, and the SRT is maintained to be about 20d by adjusting the starting time of a mud valve 5.9;
and pumping the effluent containing ammonia nitrogen and nitrite nitrogen in the second intermediate water tank 7 into an anaerobic ammonia oxidation UASB reactor 8 through a third water inlet pump 8.1, heating the reactor through a resistance wire, controlling the temperature to be 34 ℃, controlling the hydraulic retention time of the reactor to be 5h by regulating and controlling the rotating speed of the third water inlet pump 8.1, and discharging the effluent into a water outlet tank 9.
Test knot of this exampleThe result shows that after the operation is stable, the sludge fermentation synchronous short-cut denitrification SFPD reactor 5 has the conversion rate from nitrate nitrogen to nitrite>80 percent of sludge is reduced by 40 to 60 percent; effluent TN concentration of anaerobic ammonia oxidation UASB reactor 8<15mg/L of, wherein NH4 +Concentration of-N<5mg/L，NO2 --N<1mg/L，NO3 --N<5mg/L, and the effluent can reach the first-grade A discharge standard.
Claims (5)
1. A device for simultaneously realizing urban sewage treatment and excess sludge reduction is characterized by comprising an urban sewage raw water tank, a whole-course nitrification SBR reactor, a first intermediate water tank, a sludge fermentation and short-course denitrification integrated SFPD reactor, a sludge storage tank, a second intermediate water tank, an anaerobic ammonia oxidation UASB reactor and a water outlet tank; the urban sewage raw water tank is connected with the full-course nitrification SBR reactor through a first water inlet pump; the air pump is connected with the full-process nitrification SBR reactor; the full-process nitrification SBR reactor is connected with a first intermediate water tank through a first electric drain valve; the first intermediate water tank is connected with the sludge fermentation and short-cut denitrification SFPD reactor through a second water inlet pump; the sludge storage tank is connected with the sludge fermentation synchronous short-cut denitrification SFPD reactor by a peristaltic pump; the sludge discharge box is connected with the sludge fermentation synchronous short-cut denitrification SFPD reactor through a sludge discharge valve; the sludge fermentation synchronous short-cut denitrification SFPD reactor is connected with a second intermediate water tank through a second electric drain valve, and the second intermediate water tank is connected with the bottom of the anaerobic ammonia oxidation UASB reactor through a third water inlet pump; the anaerobic ammonia oxidation UASB reactor is connected with the water outlet tank through a third electric drain valve.
2. The device for simultaneously realizing municipal sewage treatment and residual sludge reduction according to claim 1, wherein a first stirring paddle is arranged in the whole nitrification SBR reactor, one end of the first stirring paddle, which extends out of the whole nitrification SBR reactor, is connected with a stirrer, a gas flowmeter is arranged on a pipeline of the air pump, which is connected with the whole nitrification SBR reactor, a pH sensor and a DO sensor are arranged in the whole nitrification SBR reactor and are respectively connected with a pH/DO tester, and a first sampling port is arranged on the side wall of the whole nitrification SBR reactor above the first electric drain valve.
3. The device for simultaneously realizing municipal sewage treatment and excess sludge reduction according to claim 2, wherein a second stirring paddle is arranged in the sludge fermentation synchronous short-cut denitrification SFPD reactor, one end of the second stirring paddle, which extends out of the sludge fermentation synchronous short-cut denitrification SFPD reactor, is connected with the stirrer, the heating rod, the pH sensor, the temperature sensor and the ORP sensor are arranged in the sludge fermentation synchronous short-cut denitrification SFPD reactor, the pH sensor and the temperature sensor are respectively connected with the pH/temperature measuring instrument, and the ORP sensor is connected with the ORP measuring instrument.
4. The device for simultaneously realizing urban sewage treatment and excess sludge reduction according to claim 3, wherein a resistance wire and a temperature control device are arranged in the anaerobic ammonia oxidation UASB reactor, the top end of the anaerobic ammonia oxidation UASB reactor is communicated with a gas collecting bottle, four second sampling ports are arranged on the side wall of the water outlet end of the anaerobic ammonia oxidation UASB reactor, and a third water inlet pump is connected with the top of the anaerobic ammonia oxidation UASB reactor through a peristaltic pump.
5. A method for simultaneously realizing urban sewage and excess sludge reduction by adopting the device of claim 4 is characterized by comprising the following specific processes:
1) and (3) starting a system:
adding nitrified sludge with good nitrification performance into the whole-course nitrification SBR reactor, so that the concentration of suspended activated sludge in the inoculated whole-course nitrification SBR reactor reaches 4500-5500 mg/L; inoculating sludge with short-cut denitrification characteristics into a sludge fermentation synchronous short-cut denitrification SFPD reactor, so that the concentration of activated sludge in the reactor reaches 8000-12000 mg/L; adding floc sludge with anaerobic ammonia oxidation activity into an anaerobic ammonia oxidation UASB reactor, and enabling the concentration of activated sludge in the inoculated reactor to reach 3000-5000 mg/L;
2) the run-time adjustments are as follows:
adding urban sewage into an urban sewage raw water tank, starting a first water inlet pump to pump the urban sewage into a full-process nitrification SBR reactor, carrying out anoxic stirring for 80-120 min, then carrying out aerobic stirring for 120-150 min, stopping aeration when the ammonia nitrogen removal rate reaches the maximum, precipitating and draining water, wherein the drainage ratio is 0.4-0.6, and discharging the discharged water into a first intermediate water tank; the aerobic aeration stirring means that the DO concentration is 0.5-1.0 mg/L;
pumping effluent containing nitrate nitrogen in the first intermediate water tank into a sludge fermentation synchronous short-cut denitrification SFPD reactor through a second water inlet pump, starting a peristaltic pump to pump residual sludge in a sludge tank into the sludge fermentation synchronous short-cut denitrification SFPD reactor, carrying out anoxic stirring for 12-48 h, controlling the temperature in the reactor to be 30-40 ℃ by using a heating rod, maintaining the pH value to be 9-11 through NaOH solution, stopping stirring when the concentration of the nitrate nitrogen in the reaction is lower than 1.0mg/L and the concentration of ammonia nitrogen reaches the maximum, precipitating and draining, and discharging effluent into a second intermediate water tank; in addition, when the sludge concentration in the reactor is lower than 8000mg/L, closing a sludge discharge valve to avoid sludge discharge so as to ensure the amount of activated sludge in the reactor;
pumping the effluent containing ammonia nitrogen and nitrite nitrogen in the second intermediate water tank into an anaerobic ammonia oxidation UASB reactor through a third water inlet pump, heating the reactor through a resistance wire, controlling the temperature at 30-35 ℃, controlling the rotation speed of the third water inlet pump to ensure that the water in the reactor stays for 4-8 h, and discharging the effluent into an effluent water tank.
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| CN114349161A (en) * | 2022-01-17 | 2022-04-15 | 郑州轻工业大学 | Method for rapidly starting anaerobic ammonia oxidation by using waste sludge |
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