CN108217950B - Device and method for FNA (FNA) enhanced sludge fermentation and short-range nitrogen and phosphorus removal of sewage - Google Patents
Device and method for FNA (FNA) enhanced sludge fermentation and short-range nitrogen and phosphorus removal of sewage Download PDFInfo
- Publication number
- CN108217950B CN108217950B CN201810203310.1A CN201810203310A CN108217950B CN 108217950 B CN108217950 B CN 108217950B CN 201810203310 A CN201810203310 A CN 201810203310A CN 108217950 B CN108217950 B CN 108217950B
- Authority
- CN
- China
- Prior art keywords
- sludge
- reactor
- fna
- nitrite
- nitrogen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
-
- 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
- C02F3/308—Biological phosphorus removal
-
- 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
- C02F2101/105—Phosphorus compounds
-
- 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
Abstract
FNA strengthens sludge fermentation and realizes device and method of sewage short distance nitrogen and phosphorus removal, belongs to sewage sludge treatment field. The device includes: raw water tank, SBR reactor, intermediate water tank, UASB reactor, sludge treatment reactor, sludge fermentation tank. The method combines the short-cut nitrification of Free Nitrous Acid (FNA) inhibiting nitrite oxidizing bacteria and the promotion of hydrolytic acidification as a sludge fermentation pretreatment step, wherein one part of sludge discharged from a short-cut nitrification reactor is returned after being treated by the FNA, and the other part of sludge enters a sludge fermentation tank. The SBR reactor firstly removes redundant nitrite in the upper period by anoxic denitrification, then releases phosphorus by anaerobic treatment, absorbs phosphorus by aerobic treatment and generates partial shortcut nitrification, effluent and sludge fermentation liquor enter UASB together, partial ammonia nitrogen and nitrite are autotrophic denitrified by anaerobic ammonium oxidation bacteria, and residual nitrite and generated nitrate nitrogen are removed by denitrification of organic matters in the sludge fermentation liquor. The invention promotes the development of internal carbon source by FNA, realizes the nitrogen and phosphorus removal of urban sewage, reduces sludge and reduces the energy consumption of sewage treatment.
Description
Technical Field
The invention relates to a device and a method for FNA (FNA) enhanced sludge fermentation and short-range nitrogen and phosphorus removal of sewage, belonging to the technical field of biological sewage treatment. The invention innovatively combines the short-cut nitrification of Free Nitrous Acid (FNA) inhibiting nitrite oxidizing bacteria and the promotion of hydrolytic acidification as a sludge fermentation pretreatment step, strengthens the development of carbon sources in sludge while realizing the biological nitrogen and phosphorus removal by the short-cut nitrification, and provides a new idea for the treatment of the municipal domestic sewage sludge.
Background
At present, most of municipal sewage treatment plants in China adopt the traditional nitrification and denitrification biological denitrification process to realize the standard discharge of nitrogen in sewage. Ammonia Oxidizing Bacteria (AOB) in traditional biological denitrification process take oxygen as electricity(ii) a sub-acceptor, to convert NH4 +Oxidation to NO2 -Followed by Nitrite Oxidizing Bacteria (NOB) with oxygen as electron acceptor, NO2 -Oxidation to NO3 -Finally, the denitrifying bacteria take organic matters as electron donors and NO3 -Reduction to N2Finally, the purpose of removing nitrogen from the sewage is achieved. Discovery of anammox bacteria enables autotrophic denitrification of wastewater, and anammox bacteria utilize NO2 -Oxidation of NH as an electron acceptor4 +Generating N2In the process, inorganic carbon is used as a carbon source, and organic matters are not needed to be used as the carbon source, so that the aim of autotrophic biological nitrogen removal is fulfilled. The key of applying the anaerobic ammonia oxidation biotechnology to the denitrification treatment of urban sewage is that the substrate NO is2 -Stable acquisition of (1).
The short-cut nitrification technology is to oxidize NH by ammonia oxidizing bacteria4 +Oxidation to NO2 -Can provide substrate NO for anaerobic ammonia oxidation2 -. At present, the technology for stably realizing the short-cut nitrification of the municipal sewage is less, so the stable realization of the short-cut nitrification of the municipal sewage is the bottleneck for limiting the anaerobic ammonia oxidation autotrophic nitrogen removal of the municipal sewage. Recent research finds that the inhibition effect of Free Nitrous Acid (FNA) on NOB is larger than that of AOB under the anoxic condition, and the short-cut nitrification is favorably realized.
Biological denitrification process based on activated sludge process has been widely applied in the field of urban sewage treatment, but the transfer of a large amount of organic substances in sewage to sludge results in increased sludge yield, which increases the investment and operation burden of sewage treatment plants. In addition, the low carbon-nitrogen ratio of the municipal sewage leads to the necessity of adding an external carbon source in the biological denitrification process, which causes the operating cost of the sewage treatment plant to be greatly increased. Therefore, the realization of the reduction and the resource utilization of the excess sludge and the development of the carbon source in the sludge become the difficult point and the key point of the municipal sewage treatment. The sludge fermentation can realize the conversion of organic matters in the sludge into Volatile Fatty Acids (VFAs) which are then used as a dominant carbon source available for microorganisms in the biological denitrification process. However, sludge disintegration is generally considered to be the rate limiting step in the fermentation process of excess sludge. Sludge fermentation generally breaks microbial cell walls by means of pyrolysis, physical (ultrasound), electrical and chemical sludge pretreatment techniques. However, the above techniques have problems of large energy consumption (high temperature or high pressure), necessity of a large amount of chemicals (chlorine, ozone, alkalinity, etc.), environmental pollution, etc. Therefore, it is important to find a sludge pretreatment technology to improve biodegradability. The related literature adopts FNA to pretreat the excess sludge, and microorganisms in the excess sludge are inactivated to promote sludge disintegration and improve the fermentation characteristic of the excess sludge.
Disclosure of Invention
In order to solve the problems, the invention aims to combine the effect of inhibiting nitrite oxidizing bacteria by Free Nitrous Acid (FNA) to realize short-cut nitrification and the effect of promoting hydrolytic acidification as a sludge fermentation pretreatment step, and strengthen the development of a carbon source in sludge while realizing the biological nitrogen and phosphorus removal by short-cut nitrification. After the sludge discharged by the short-cut nitrification reactor is treated by FNA, one part of the sludge returns, and the other part of the sludge enters a sludge fermentation tank. The SBR reactor firstly carries out anoxic denitrification to remove redundant nitrite in the upper period, then carries out anaerobic phosphorus release, carries out aerobic phosphorus absorption and carries out partial short-cut nitrification, effluent and sludge fermentation liquor enter the UASB reactor together, partial ammonia nitrogen and nitrite are subjected to autotrophic denitrification by anaerobic ammonia oxidizing bacteria, and residual nitrite and generated nitrate nitrogen are removed by utilizing organic matter denitrification in the sludge fermentation liquor, so that deep denitrification and phosphorus removal of domestic sewage are realized.
In order to achieve the above object, the present invention provides a device for FNA enhanced sludge fermentation and short-cut nitrogen and phosphorus removal of sewage, comprising: a raw water tank (1), an SBR reactor (2), an intermediate water tank (3), a UASB reactor (4), a sludge treatment reactor (5) and a sludge fermentation tank (6); the raw water tank (1) supplies water to the SBR reactor (2) through a raw water inlet pump (1.1), the SBR reactor (2) is provided with a first temperature control device (2.1), a first stirring device (2.2), a first pH tester (2.6) and a DO tester (2.7), oxygenation is carried out through an aeration device provided with a gas flowmeter (2.3), an air valve (2.4), an air compressor (2.5) and an aeration head (2.9), effluent enters the middle water tank (3) through a drain valve (2.8), and residual sludge is discharged to the sludge treatment reactor (5) through a sludge discharge valve I (2.10) and a sludge discharge pump (2.11); the intermediate water tank (3) is connected with the UASB reactor (4) through a nitrifying liquid inlet pump (3.1) and a nitrifying liquid inlet valve (3.2); the UASB reactor (4) is provided with a gas collecting device (4.1), a water outlet pipe (4.2), a three-phase separator (4.3), a heating belt device (4.4), a water distribution device (4.5), an internal circulating pump (4.6) and an internal circulating valve (4.7); the sludge treatment reactor (5) is provided with a dosing pipe (5.1) and a second stirring device (5.2), is connected with the sludge fermentation tank (6) through a sludge discharge valve II (5.3) and a sludge discharge valve III (5.4), and returns the treated sludge to the SBR reactor (2) through a return sludge valve (5.5) and a return sludge pump (5.6); the sludge fermentation tank (6) is provided with a second temperature control device (6.1), a third stirring device (6.2) and a second pH tester (6.3), and fermented sludge is pumped into the UASB reactor (4) through a sludge inlet pump (6.4) and a sludge inlet valve (6.5).
The invention also provides a method for FNA (FNA) enhanced sludge fermentation and short-range nitrogen and phosphorus removal of sewage, which comprises the following steps:
the device start-up operation is as follows:
starting the SBR reactor: injecting whole-course nitrified sludge of an actual urban sewage treatment plant into an SBR reactor (2) by taking inoculated sludge, controlling the sludge concentration to be 2500-4000mg/L, controlling the hydraulic retention time to be 6-8h, controlling the drainage ratio to be 40-60% and controlling the dissolved oxygen to be 0.8-1.5 mg/L, controlling the sludge age to be 15-20 d by discharging excess sludge, enabling the excess sludge to enter a sludge treatment reactor (5), realizing short-range nitrification by utilizing that the inhibition of Free Nitrous Acid (FNA) on nitrite oxidizing bacteria is far greater than that on ammonia oxidizing bacteria, and realizing SBR short-range nitrification when the accumulation rate of effluent nitrite is greater than 95% and continuously maintained for more than 15 days. According to the pH change curve, stopping aeration before the ammonia nitrogen completely reacts, realizing partial short-cut nitrification, enabling the concentration ratio of the nitrite/ammonia nitrogen in the effluent to be 1.3-1.5, and stably realizing partial short-cut nitrification.
Starting a sludge fermentation tank: the sludge fermentation tank (6) is a semi-continuous reactor, sludge is inoculated to be discharged from a secondary sedimentation tank of an urban sewage treatment plant, the sludge retention time SRT is 10-20 days, the pH is controlled to be 9-10, the residual sludge pretreated by FNA in the sludge treatment reactor (5) is discharged into the sludge fermentation tank (6), and the fermented sludge is pumped into the UASB reactor (4) through a sludge inlet pump (6.4) and a sludge inlet valve (6.5) according to the SRT.
Start-up of UASB reactor: the inoculated sludge is a mixture of sludge of an urban sewage anaerobic ammonia oxidation reactor and sludge discharged from a secondary sedimentation tank, and the volume ratio is 5: 1-10: 1, so that the dominant position of anaerobic ammonia oxidizing bacteria is ensured. Hydraulic retention time is 3-5h, sludge retention time is 10-20d, and NH is adopted as inlet water4 +-N/NO2 --N concentration ratio of 1: 1.3, carrying out artificial water distribution, wherein the initial TN concentration is 20mg/L, the nitrogen load is gradually increased by a gradient of 20mg/L until the nitrogen load reaches 60mg/L, the time point of increasing the nitrogen load at each time is that the autotrophic denitrification rate exceeds 95 percent and the autotrophic denitrification rate is continuously maintained for more than 15 days, and finally completing the anaerobic ammonia oxidation domestication treatment; the inlet water adopts NH4 +-N/NO2 --N concentration ratio of 1: 1.3 and 60mg/L of TN, and simultaneously adding sodium acetate as a denitrification carbon source to ensure that the concentration of SCOD is 100-150mg/L, wherein when the TN removal rate is higher than 90 percent and the TN is continuously maintained for more than 15 days, the coupling of anaerobic ammonia oxidation and denitrification is successfully realized; the sludge fermentation mixture replaces sodium acetate as a denitrification carbon source to keep the concentration of SCOD at 100-150mg/L, and when the removal rate of TN is higher than 90% and the TN is continuously maintained for more than 15 days, the coupling of anaerobic ammonia oxidation and denitrification is realized.
The operation during the operation adjustment is as follows:
domestic sewage and FNA treated excess sludge enter an SBR reactor (2) together, the SBR reactor (2) is firstly subjected to anoxic stirring for 1-1.5 h, an air compressor (2.10) is started, an air valve (2.9) and a gas flowmeter (2.8) are adjusted to perform aeration, dissolved oxygen is controlled to be 0.8-1.5 mg/L, the SBR reactor (2) is subjected to partial short-cut nitrification reaction, partial ammonia nitrogen is converted into nitrite nitrogen, the aeration time is determined according to a real-time control pH change curve, the ammonia nitrogen in effluent is 8-12 mg/L, and the nitrite is 10-15 mg/L. The effluent of the SBR reactor enters an intermediate water tank (3), the discharged residual sludge enters a sludge treatment reactor (5), sodium nitrite is added into the sludge treatment reactor (5) to ensure that the concentration of the nitrite in the sludge treatment reactor is 300-1000 mg/L, acid or alkali is added to control the pH value to be 5.5-6.0, and the sludge treatment time is 12-24 hours. 30-40% of the treated sludge flows back to the SBR reactor (2), and 60-70% of the treated sludge enters a sludge fermentation tank (6). And (3) pumping the sludge fermentation mixture and the nitrified effluent from the bottom of the UASB reactor (4), controlling the temperature of the UASB reactor at 28-32 ℃, and performing hydraulic retention for 3-5 hours, wherein the treated effluent is discharged through a water outlet pipe.
The technical principle of the invention is as follows:
the invention innovatively combines the short-cut nitrification of Free Nitrous Acid (FNA) inhibiting nitrite oxidizing bacteria and the promotion of hydrolytic acidification as a sludge fermentation pretreatment step, and strengthens the development of carbon sources in sludge while realizing the biological nitrogen and phosphorus removal by the short-cut nitrification. After the sludge discharged by the short-cut nitrification reactor is treated by FNA, one part of the sludge returns, and the other part of the sludge enters a sludge fermentation tank. The SBR reactor firstly carries out anoxic denitrification to remove redundant nitrite in the upper period, then carries out anaerobic phosphorus release, carries out aerobic phosphorus absorption and carries out partial short-cut nitrification, effluent and sludge fermentation liquor enter the UASB reactor together, partial ammonia nitrogen and nitrite are subjected to autotrophic denitrification by anaerobic ammonia oxidizing bacteria, and residual nitrite and generated nitrate nitrogen are removed by utilizing organic matter denitrification in the sludge fermentation liquor, so that deep denitrification and phosphorus removal of domestic sewage are realized.
Compared with the prior art, the invention has the following advantages:
the excess sludge is treated by Free Nitrous Acid (FNA), so that not only is short-cut nitrification realized, but also the excess sludge is used as a sludge fermentation pretreatment step, and the development of an internal carbon source is promoted by sludge pyrolysis reinforcement.
The device can realize deep nitrogen and phosphorus removal of domestic sewage on the basis of not adding an external carbon source, nitrate nitrogen of an anaerobic ammonia oxidation product can be removed through denitrification, the two are matched with each other, and the device has a complex flora structure and strong impact resistance.
The invention takes the fermentation treatment of the excess sludge as the denitrification carbon source, reduces the sludge yield, reduces the sludge treatment cost of the sewage treatment plant and saves the operation cost.
Drawings
FIG. 1 is a block diagram of the apparatus of the present invention
The main symbols are as follows: 1-raw water tank; 2-SBR reactor; 3-an intermediate water tank; 4-UASB reactor; 5-a sludge treatment reactor; 6-sludge fermentation tank; 1.1-raw water intake pump; 2.1-a first temperature control device; 2.2-a first stirring device; 2.3-gas flow meter; 2.4-air valve; 2.5-air compressor; 2.6-first pH meter; 2.7-DO meter; 2.8-drain valve; 2.9-aeration head; 2.10-mud valve I; 2.11-sludge pump; 3.1-nitrifying liquid inlet pump; 3.2-nitrifying liquid inlet valve; 4.1-gas collection device; 4.2-water outlet pipe; 4.3-three-phase separator; 4.4-heating belt device; 4.5-water distribution device; 4.6-internal circulation pump; 4.7-internal circulation valve; 5.1-a medicine feeding pipe; 5.2-a second stirring device; 5.3-a mud valve II; 5.4-mud valve III; 5.5-return sludge valve; 5.6-reflux sludge pump; 6.1-a second temperature control device; 6.2-a third stirring device; 6.3-second pH meter; 6.4-mud pump; 6.5-mud inlet valve.
Detailed Description
The invention is further explained in detail with reference to the drawings and examples.
As shown in figure 1, the device for FNA to strengthen sludge fermentation and realize short-cut nitrogen and phosphorus removal of sewage comprises: a raw water tank (1), an SBR reactor (2), an intermediate water tank (3), a UASB reactor (4), a sludge treatment reactor (5) and a sludge fermentation tank (6); the raw water tank (1) supplies water to the SBR reactor (2) through a raw water inlet pump (1.1), the SBR reactor (2) is provided with a first temperature control device (2.1), a first stirring device (2.2), a first pH tester (2.6) and a DO tester (2.7), oxygenation is carried out through an aeration device provided with a gas flowmeter (2.3), an air valve (2.4), an air compressor (2.5) and an aeration head (2.9), effluent enters the middle water tank (3) through a drain valve (2.8), and residual sludge is discharged to the sludge treatment reactor (5) through a sludge discharge valve I (2.10) and a sludge discharge pump (2.11); the intermediate water tank (3) is connected with the UASB reactor (4) through a nitrifying liquid inlet pump (3.1) and a nitrifying liquid inlet valve (3.2); the UASB reactor (4) is provided with a gas collecting device (4.1), a water outlet pipe (4.2), a three-phase separator (4.3), a heating belt device (4.4), a water distribution device (4.5), an internal circulating pump (4.6) and an internal circulating valve (4.7); the sludge treatment reactor (5) is provided with a dosing pipe (5.1) and a second stirring device (5.2), is connected with the sludge fermentation tank (6) through a sludge discharge valve II (5.3) and a sludge discharge valve III (5.4), and returns the treated sludge to the SBR reactor (2) through a return sludge valve (5.5) and a return sludge pump (5.6); the sludge fermentation tank (6) is provided with a second temperature control device (6.1), a third stirring device (6.2) and a second pH tester (6.3), and fermented sludge is pumped into the UASB reactor (4) through a sludge inlet pump (6.4) and a sludge inlet valve (6.5).
The test water adopts domestic sewage discharged from the family district of Beijing university of industry, and the water quality is as follows: pH is 7.1-7.9, COD concentration is 130-4 +N concentration of 50-70mg/L, NO2 --N and NO3 -and-N is below the detection limit, and the ratio of COD to N is 2-3. The experimental inoculated sludge is respectively from whole-course nitrified sludge of an urban sewage treatment plant and a pilot anaerobic ammonia oxidation device of urban domestic sewage. The effective volume of the SBR reactor is 10L, the water discharge ratio is 0.5, the sludge retention time is 15d, the SBR reactor runs for 4 periods every day, and each period comprises water feeding (0.25h), stirring (0.5h), aeration (3.5h), sedimentation (1h), water discharge (0.25h) and idling (0.5 h); the effective volume of the UASB reactor is 5L, the hydraulic retention time is 4.5h, and the internal circulation reflux ratio is 100 percent. The specific operation process is as follows:
the device start-up operation is as follows:
starting the SBR reactor: injecting whole-course nitrified sludge of an actual urban sewage treatment plant into an SBR reactor (2) by taking inoculated sludge, controlling the sludge concentration to be 2500-4000mg/L, controlling the hydraulic retention time to be 6-8h, controlling the drainage ratio to be 40-60% and controlling the dissolved oxygen to be 0.8-1.5 mg/L, controlling the sludge age to be 15-20 d by discharging excess sludge, enabling the excess sludge to enter a sludge treatment reactor (5), realizing short-range nitrification by utilizing that the inhibition of Free Nitrous Acid (FNA) on nitrite oxidizing bacteria is far greater than that on ammonia oxidizing bacteria, and realizing SBR short-range nitrification when the accumulation rate of effluent nitrite is greater than 95% and continuously maintained for more than 15 days. According to the pH change curve, stopping aeration before the ammonia nitrogen completely reacts, realizing partial short-cut nitrification, enabling the concentration ratio of the nitrite/ammonia nitrogen in the effluent to be 1.3-1.5, and stably realizing partial short-cut nitrification.
Starting a sludge fermentation tank: the sludge fermentation tank (6) is a semi-continuous reactor, sludge is inoculated to be discharged from a secondary sedimentation tank of an urban sewage treatment plant, the sludge retention time SRT is 10-20 days, the pH is controlled to be 9-10, the residual sludge pretreated by FNA in the sludge treatment reactor (5) is discharged into the sludge fermentation tank (6), and the fermented sludge is pumped into the UASB reactor (4) through a sludge inlet pump (6.4) and a sludge inlet valve (6.5) according to the SRT.
Start-up of UASB reactor: the inoculated sludge is a mixture of sludge of an urban sewage anaerobic ammonia oxidation reactor and sludge discharged from a secondary sedimentation tank, and the volume ratio is 5: 1-10: 1, so that the dominant position of anaerobic ammonia oxidizing bacteria is ensured. Hydraulic retention time is 3-5h, sludge retention time is 10-20d, and NH is adopted as inlet water4 +-N/NO2 --N concentration ratio of 1: 1.3, carrying out artificial water distribution, wherein the initial TN concentration is 20mg/L, the nitrogen load is gradually increased by a gradient of 20mg/L until the nitrogen load reaches 60mg/L, the time point of increasing the nitrogen load at each time is that the autotrophic denitrification rate exceeds 95 percent and the autotrophic denitrification rate is continuously maintained for more than 15 days, and finally completing the anaerobic ammonia oxidation domestication treatment; the inlet water adopts NH4 +-N/NO2 --N concentration ratio of 1: 1.3 and 60mg/L of TN, and simultaneously adding sodium acetate as a denitrification carbon source to ensure that the concentration of SCOD is 100-150mg/L, wherein when the TN removal rate is higher than 90 percent and the TN is continuously maintained for more than 15 days, the coupling of anaerobic ammonia oxidation and denitrification is successfully realized; the sludge fermentation mixture replaces sodium acetate as a denitrification carbon source to keep the concentration of SCOD at 100-150mg/L, and when the removal rate of TN is higher than 90% and the TN is continuously maintained for more than 15 days, the coupling of anaerobic ammonia oxidation and denitrification is realized.
The operation during the operation adjustment is as follows:
domestic sewage and FNA treated excess sludge enter an SBR reactor (2) together, the SBR reactor (2) is firstly subjected to anoxic stirring for 1-1.5 h, an air compressor (2.10) is started, an air valve (2.9) and a gas flowmeter (2.8) are adjusted to perform aeration, dissolved oxygen is controlled to be 0.8-1.5 mg/L, the SBR reactor (2) is subjected to partial short-cut nitrification reaction, partial ammonia nitrogen is converted into nitrite nitrogen, the aeration time is determined according to a real-time control pH change curve, the ammonia nitrogen in effluent is 8-12 mg/L, and the nitrite is 10-15 mg/L. The effluent of the SBR reactor enters an intermediate water tank (3), the discharged residual sludge enters a sludge treatment reactor (5), sodium nitrite is added into the sludge treatment reactor (5) to ensure that the concentration of the nitrite in the sludge treatment reactor is 300-1000 mg/L, acid or alkali is added to control the pH value to be 5.5-6.0, and the sludge treatment time is 12-24 hours. 30-40% of the treated sludge flows back to the SBR reactor (2), and 60-70% of the treated sludge enters a sludge fermentation tank (6). And (3) pumping the sludge fermentation mixture and the nitrified effluent from the bottom of the UASB reactor (4), controlling the temperature of the UASB reactor at 28-32 ℃, and performing hydraulic retention for 3-5 hours, wherein the treated effluent is discharged through a water outlet pipe.
The test result shows that: after the operation is stable, under the condition of not adding external carbon source, the COD concentration of the effluent of the device is 40-60mg/L, and NH4 +A concentration of-N of<3mg/L，NO2 --N<1mg/L，NO3 --N<3mg/L，TN<10mg/L, and reaches the first class A standard of pollutant discharge Standard of municipal wastewater treatment plant (GB 18918-2002).
Claims (1)
- The FNA intensified sludge fermentation and short-distance denitrification and dephosphorization method for sewage, the device is provided with a raw water tank (1), an SBR reactor (2), an intermediate water tank (3), a UASB reactor (4), a sludge treatment reactor (5) and a sludge fermentation tank (6); the raw water tank (1) supplies water to the SBR reactor (2) through a raw water inlet pump (1.1), the SBR reactor (2) is provided with a first temperature control device (2.1), a first stirring device (2.2), a first pH tester (2.6) and a DO tester (2.7), oxygenation is carried out through an aeration device provided with a gas flowmeter (2.3), an air valve (2.4), an air compressor (2.5) and an aeration head (2.9), effluent enters the middle water tank (3) through a drain valve (2.8), and residual sludge is discharged to the sludge treatment reactor (5) through a sludge discharge valve I (2.10) and a sludge discharge pump (2.11); the intermediate water tank (3) is connected with the UASB reactor (4) through a nitrifying liquid inlet pump (3.1) and a nitrifying liquid inlet valve (3.2); the UASB reactor (4) is provided with a gas collecting device (4.1), a water outlet pipe (4.2), a three-phase separator (4.3), a heating belt device (4.4), a water distribution device (4.5), an internal circulating pump (4.6) and an internal circulating valve (4.7); the sludge treatment reactor (5) is provided with a dosing pipe (5.1) and a second stirring device (5.2), is connected with the sludge fermentation tank (6) through a sludge discharge valve II (5.3) and a sludge discharge valve III (5.4), and returns the treated sludge to the SBR reactor (2) through a return sludge valve (5.5) and a return sludge pump (5.6); the sludge fermentation tank (6) is provided with a second temperature control device (6.1), a third stirring device (6.2) and a second pH tester (6.3), and fermented sludge is pumped into the UASB reactor (4) through a sludge inlet pump (6.4) and a sludge inlet valve (6.5);the method is characterized by comprising the following steps:1) the device start-up operation is as follows:1.1) start-up of the SBR reactor: injecting whole-course nitrified sludge of an actual urban sewage treatment plant into an SBR reactor (2) by taking inoculated sludge, controlling the sludge concentration to be 2500-4000mg/L, controlling the hydraulic retention time to be 6-8h, controlling the drainage ratio to be 40-60 percent, controlling the dissolved oxygen to be 0.8-1.5 mg/L, controlling the sludge age to be 15-20 d by discharging excess sludge, enabling the excess sludge to enter a sludge treatment reactor (5), realizing short-range nitrification by utilizing that the inhibition of Free Nitrous Acid (FNA) on nitrite oxidizing bacteria is far greater than that on ammonia oxidizing bacteria, and realizing SBR short-range nitrification when the accumulation rate of effluent nitrite is greater than 95 percent and continuously maintained for more than 15 days; according to the pH change curve, stopping aeration before the ammonia nitrogen completely reacts, realizing partial short-cut nitrification, enabling the nitrite/ammonia nitrogen in the effluent to be between 1.3 and 1.5, and stably realizing partial short-cut nitrification;1.2) starting a sludge fermentation tank: the sludge fermentation tank (6) is a semi-continuous reactor, sludge is inoculated to be discharged from a secondary sedimentation tank of an urban sewage treatment plant, the sludge retention time SRT is 10-20 days, the pH is controlled to be 9-10, the residual sludge pretreated by FNA in the sludge treatment reactor (5) is discharged into the sludge fermentation tank (6), and the fermented sludge is pumped into the UASB reactor (4) through a sludge inlet pump (6.4) and a sludge inlet valve (6.5) according to the SRT;1.3) start-up of the UASB reactor: the inoculated sludge is a mixture of sludge of an urban sewage anaerobic ammonia oxidation reactor and sludge discharged from a secondary sedimentation tank, and the volume ratio is 5: 1-10: 1, so that the dominant position of anaerobic ammonia oxidizing bacteria is ensured; hydraulic retention time is 3-5h, sludge retention time is 10-20d, and NH is adopted as inlet water4 +-N/NO2 --N concentration ratio of 1: 1.3, carrying out artificial water distribution, wherein the initial TN concentration is 20mg/L, the nitrogen load is gradually increased by a gradient of 20mg/L until the nitrogen load reaches 60mg/L, the time point of increasing the nitrogen load at each time is that the autotrophic denitrification rate exceeds 95 percent and the autotrophic denitrification rate is continuously maintained for more than 15 days, and finally completing the anaerobic ammonia oxidation domestication treatment; the inlet water adopts NH4 +-N/NO2 --a mass concentration ratio of N of 1: 1.3 and 60mg/L of TN, and simultaneously adding sodium acetate as a denitrification carbon source to ensure that the concentration of SCOD is 100-150mg/L, and when the TN removal rate is higher than 90 percent and the TN is continuously maintained for more than 15 days, coupling anaerobic ammonia oxidation and denitrificationThe successful realization is carried out; replacing sodium acetate with the sludge fermentation mixture as a denitrification carbon source to continuously maintain the concentration of SCOD at 100-150mg/L, and realizing the coupling of anaerobic ammonia oxidation and denitrification when the removal rate of TN is higher than 90% and the TN is continuously maintained for more than 15 days;2) the operation during the operation adjustment is as follows: domestic sewage and FNA-treated excess sludge enter an SBR reactor (2) together, the SBR reactor (2) is subjected to anoxic stirring for 1-1.5 hours, an air compressor (2.10) is started, an air valve (2.9) and a gas flowmeter (2.8) are adjusted to perform aeration, dissolved oxygen is controlled to be 0.8-1.5 mg/L, the SBR reactor (2) is subjected to partial short-cut nitrification reaction, partial ammonia nitrogen is converted into nitrite nitrogen, aeration time is determined according to a real-time control pH change curve, and effluent ammonia nitrogen is 8-12 mg/L and nitrite is 10-15 mg/L; the water discharged from the SBR reactor enters an intermediate water tank (3), the discharged excess sludge enters a sludge treatment reactor (5), the concentration of nitrite in the sludge treatment reactor (5) is 300-1000 mg/L by adding sodium nitrite into the sludge treatment reactor, the pH is controlled to be 5.5-6.0 by adding acid or alkali, and the sludge treatment time is 12-24 hours; 30-40% of the treated sludge flows back to the SBR reactor (2), and 60-70% of the treated sludge enters a sludge fermentation tank (6); and (3) pumping the sludge fermentation mixture and the nitrified effluent from the bottom of the UASB reactor (4), controlling the temperature of the UASB reactor at 28-32 ℃, and performing hydraulic retention for 3-5 hours, wherein the treated effluent is discharged through a water outlet pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810203310.1A CN108217950B (en) | 2018-03-13 | 2018-03-13 | Device and method for FNA (FNA) enhanced sludge fermentation and short-range nitrogen and phosphorus removal of sewage |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810203310.1A CN108217950B (en) | 2018-03-13 | 2018-03-13 | Device and method for FNA (FNA) enhanced sludge fermentation and short-range nitrogen and phosphorus removal of sewage |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108217950A CN108217950A (en) | 2018-06-29 |
| CN108217950B true CN108217950B (en) | 2021-08-13 |
Family
ID=62659420
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810203310.1A Active CN108217950B (en) | 2018-03-13 | 2018-03-13 | Device and method for FNA (FNA) enhanced sludge fermentation and short-range nitrogen and phosphorus removal of sewage |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108217950B (en) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109912027A (en) * | 2019-02-02 | 2019-06-21 | 中国矿业大学 | A kind of (A/O)2- SBR intensified denitrification and dephosphorization method |
| CN110002592B (en) * | 2019-05-05 | 2021-09-14 | 北京工业大学 | Device and method for treating domestic sewage by coupling short-cut denitrification-sludge fermentation with anaerobic ammonia oxidation system |
| EP3924306A4 (en) * | 2019-05-24 | 2023-08-09 | The University of Queensland | Method for treating wastewater or sludge |
| CN110818217A (en) * | 2019-11-28 | 2020-02-21 | 湖南大学 | Method for strengthening anaerobic digestion of excess sludge by combined pretreatment of freezing and free nitrous acid |
| CN111333178B (en) * | 2020-02-29 | 2021-09-24 | 北京工业大学 | Device and method for enhancing autotrophic nitrogen removal and synchronous phosphorus recovery of nitrate wastewater through alkaline sludge fermentation |
| CN111924962B (en) * | 2020-08-24 | 2022-04-12 | 北京工业大学 | Method for rapidly realizing short-cut nitrification treatment of urban sewage based on FNA pretreatment biomembrane |
| CN112250180B (en) * | 2020-09-24 | 2022-03-15 | 北京工业大学 | Device and method for realizing deep denitrification of domestic sewage by coupling half-shortcut nitrification-anaerobic ammonia oxidation with sulfur autotrophic denitrification |
| CN112607863B (en) * | 2020-12-24 | 2022-09-09 | 北京工业大学 | Device and method for realizing deep nitrogen and phosphorus removal of low C/N ratio municipal sewage combined sludge fermentation product by utilizing PN/A process |
| CN113003716A (en) * | 2021-02-20 | 2021-06-22 | 北京工业大学 | Device and method for synchronously treating nitrite nitrogen wastewater and excess sludge |
| CN113429071A (en) * | 2021-07-01 | 2021-09-24 | 清华大学 | Municipal sewage treatment system |
| CN113620505B (en) * | 2021-07-07 | 2022-11-15 | 北京工业大学 | Device and method for realizing starting and maintaining of short-cut nitrification by alternative side treatment of hydroxylamine and free nitrite |
| CN113480004B (en) * | 2021-07-15 | 2023-04-07 | 北京工业大学 | Method for deeply denitrifying urban sewage after carbon and phosphorus capture and realizing phosphorus recovery through PDA (personal digital Assistant) |
| CN114671522A (en) * | 2022-04-24 | 2022-06-28 | 广州一博环保科技有限公司 | High-efficient low energy consumption sewage treatment system |
| CN115403234A (en) * | 2022-08-29 | 2022-11-29 | 广州市香港科大霍英东研究院 | Method for realizing carbon source supplement and sludge reduction based on free nitrite and sulfate |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103663879A (en) * | 2013-12-24 | 2014-03-26 | 北京工业大学 | Device and method for synchronously treating high-ammonia-nitrogen wastewater through sludge fermentation |
| CN104528933A (en) * | 2014-11-29 | 2015-04-22 | 北京工业大学 | Method for realizing continuous-flow city sewage autotrophic nitrogen removal based on FNA treatment of sludge |
| CN105923770A (en) * | 2016-06-15 | 2016-09-07 | 北京工业大学 | Method and device for sewage denitrification by coupling of shortcut nitrification, anaerobic ammonia oxidation and shortcut denitrification |
| EP3255016A1 (en) * | 2016-06-10 | 2017-12-13 | FCC Aqualia, S.A. | Method for starting up and controlling a biological process for ammonium removal at low ammonium concentrations and low temperature through the use of a two stage autotrophic nitrogen removal process |
-
2018
- 2018-03-13 CN CN201810203310.1A patent/CN108217950B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103663879A (en) * | 2013-12-24 | 2014-03-26 | 北京工业大学 | Device and method for synchronously treating high-ammonia-nitrogen wastewater through sludge fermentation |
| CN104528933A (en) * | 2014-11-29 | 2015-04-22 | 北京工业大学 | Method for realizing continuous-flow city sewage autotrophic nitrogen removal based on FNA treatment of sludge |
| EP3255016A1 (en) * | 2016-06-10 | 2017-12-13 | FCC Aqualia, S.A. | Method for starting up and controlling a biological process for ammonium removal at low ammonium concentrations and low temperature through the use of a two stage autotrophic nitrogen removal process |
| CN105923770A (en) * | 2016-06-15 | 2016-09-07 | 北京工业大学 | Method and device for sewage denitrification by coupling of shortcut nitrification, anaerobic ammonia oxidation and shortcut denitrification |
Non-Patent Citations (1)
| Title |
|---|
| 游离亚硝酸预处理强化剩余污泥发酵同步反硝化性能;委燕等;《中国环境科学》;20151231;第35卷(第3期);第742-747页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108217950A (en) | 2018-06-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108217950B (en) | Device and method for FNA (FNA) enhanced sludge fermentation and short-range nitrogen and phosphorus removal of sewage | |
| CN108439595B (en) | Method for realizing partial shortcut nitrification-Anammox/denitrification of sewage by utilizing sludge fermentation product | |
| CN108545830B (en) | Process for enhancing partial shortcut nitrification anaerobic ammonia oxidation of continuous flow municipal sewage by utilizing sludge fermentation | |
| CN110143725B (en) | Device and method for treating urban sewage by using mixed sludge fermentation liquor as carbon source through continuous flow short-cut denitrification coupling anaerobic ammonia oxidation process | |
| CN108585202B (en) | Process for realizing partial short-cut nitrification, sludge fermentation coupling denitrification and anaerobic ammonia oxidation treatment of domestic sewage in sequencing batch reactor | |
| CN110054291B (en) | Device and method for connecting short-cut denitrification/anaerobic ammonia oxidation process after short-cut nitrification/anaerobic ammonia oxidation of low-C/N-ratio domestic sewage | |
| CN107381815B (en) | Device and method for realizing deep denitrification of domestic sewage by mainstream endogenous short-range denitrification/anaerobic ammonia oxidation process | |
| CN112250175B (en) | Device and method for realizing deep denitrification of municipal sewage by virtue of integrated shortcut nitrification-anaerobic ammonia oxidation coupling with endogenous shortcut denitrification | |
| CN105461178A (en) | System and method for treating municipal sewage through short-cut denitrification-anaerobic ammonia oxidation after short-cut nitrification-anaerobic ammonia oxidation | |
| CN108409033B (en) | Device and method for advanced nitrogen and phosphorus removal of segmented water inlet UCT by FNA (nitrogen rich aeration) enhanced short-cut nitrification | |
| CN110002587B (en) | Device and method for coupling segmented drainage type shortcut nitrification, parallel anaerobic ammonia oxidation, denitrification and phosphorus removal with endogenous denitrification | |
| CN113697951B (en) | Method for realizing granular sludge shortcut nitrification-anaerobic ammonia oxidation coupled endogenous denitrification nitrogen removal at low temperature | |
| CN113800636B (en) | Method and device for treating sludge digestive juice by coupling short-cut nitrification/anaerobic ammonia oxidation-fermentation and short-cut denitrification/anaerobic ammonia oxidation | |
| CN108128897B (en) | Device and method for realizing synchronous shortcut nitrification and denitrification dephosphorization treatment of municipal sewage based on hydroxylamine | |
| CN112250183B (en) | Device and method for treating urban sewage by combining whole-course nitrification with sludge fermentation and coupling short-range denitrification anaerobic ammonia oxidation | |
| CN112250176A (en) | Device and method for realizing advanced nitrogen and phosphorus removal of municipal sewage by integrated shortcut nitrification coupled with anaerobic ammonia oxidation denitrification phosphorus removal | |
| CN113200600B (en) | Device and method for treating high-ammonia-nitrogen organic matter wastewater by semi-shortcut nitrification anaerobic ammonia oxidation and serial shortcut denitrification anaerobic ammonia oxidation | |
| CN103723821A (en) | Method for rapid mutagenesis of autotrophic nitrosation sludge from complete nitrifying sludge | |
| CN113402021A (en) | Device and method for realizing sewage denitrification and sludge reduction by integrating in-situ sludge hydrolysis acidification and short-cut denitrification anaerobic ammonia oxidation | |
| CN113233592B (en) | Treatment device and method for realizing synchronous deep denitrification and decarbonization of advanced landfill leachate and domestic sewage | |
| US20230100166A1 (en) | Device and method for treating urban domestic sewage based on two-stage combined process of partial denitrification-anammox | |
| CN103910431A (en) | Device and method for enhancing reduction of denitrified coupling sludge in urban sewage by using intra-sludge carbon sources by two stages of sequencing batch reactors (SBR) | |
| CN113415882A (en) | Single-stage SBR (sequencing batch reactor) post-anoxic and endogenous denitrification enhanced synchronous nitrification and denitrification process for deeply denitrifying and dephosphorizing low-C/N-ratio sewage | |
| CN202688093U (en) | Improved A/O (anoxic/oxic) four-point section-water supply high-efficiency synchronous nitrogen and phosphorus removal device | |
| CN113415899B (en) | Device and method for deep denitrification based on adsorption hydrolysis coupling short-range denitrification serial anaerobic ammonia oxidation of slow degradation organic matters |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |