CN111908727A - Advanced sewage treatment process for denitrification anaerobic ammonia oxidation of reflux part - Google Patents
Advanced sewage treatment process for denitrification anaerobic ammonia oxidation of reflux part Download PDFInfo
- Publication number
- CN111908727A CN111908727A CN202010840989.2A CN202010840989A CN111908727A CN 111908727 A CN111908727 A CN 111908727A CN 202010840989 A CN202010840989 A CN 202010840989A CN 111908727 A CN111908727 A CN 111908727A
- Authority
- CN
- China
- Prior art keywords
- water
- sewage
- mud
- ammonia oxidation
- purification
- 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.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F3/28—Anaerobic digestion processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
Abstract
The invention provides a sewage advanced treatment process for denitrification anaerobic ammonia oxidation of a backflow part, which comprises five steps of sewage preliminary purification, modulation treatment, material mixing, muddy water purification, adsorption purification and the like. The invention has simple operation process, effectively improves the working efficiency and quality of the purification operation, effectively shortens the flow of the purification operation on the one hand, and improves the controllability of the process flow of the purification operation and the control precision of the regulation operation on the other hand; on the other hand, the forming rate of the granular sludge is effectively improved, the inhibiting effect of raw water directly participating in the anaerobic ammonia oxidation reaction on anaerobic ammonia oxidation bacteria is effectively avoided, and the system impact resistance and the operation strength of the purification system of the sewage treatment operation of the process are greatly improved, so that the operation stability and reliability of the sewage purification system are effectively improved while the sewage purification operation efficiency and quality are improved.
Description
Technical Field
The invention relates to a sewage advanced treatment process for denitrification anaerobic ammonia oxidation of a reflux part, belonging to the technical field of wastewater treatment.
Background
In the sewage treatment at present, anaerobic ammonia oxidation purification operation is one of the currently important purification means, but in the actual purification operation, the traditional speech process has the defects of long purification power flow and numerous devices participating in the purification operation, so that the control capability of the purification operation flow is weak, and the regulation and control precision is relatively poor; meanwhile, the traditional purification process often has relatively poor sludge retention and low sludge particle forming rate, so that the work efficiency of the purification operation is seriously influenced, a large impact load is caused on a sewage purification system, the fault rate of the purification system is increased, and meanwhile, raw water in the traditional process is directly involved in the purification operation, so that the inhibition effect on anaerobic ammonium oxidation bacteria is large, and the work efficiency and the quality of the purification operation are seriously influenced.
Therefore, in order to meet the current situation, a brand-new anaerobic ammonia oxidation sewage purification process needs to be developed to meet the actual use requirement.
Disclosure of Invention
The invention aims to provide a sewage advanced treatment process for denitrifying anaerobic ammonium oxidation of a reflux part.
In order to achieve the purpose, the invention provides the following technical scheme:
a sewage advanced treatment process for denitrification anaerobic ammonia oxidation of a backflow part comprises the following steps:
s1, primarily purifying the sewage, namely firstly heating the returned part of the sewage to 25-40 ℃ and keeping the temperature, adding anaerobic bacteria strains into the heated sewage, and carrying out constant temperature cultivation for 1-6 hours for later use;
s2, performing modulation treatment, namely inoculating the nitrifying bacteria into sludge with the water content of not less than 70% and the sludge age of 10-50 days, then culturing for 1-3 days at the constant temperature of 25-40 ℃, and storing at the constant temperature for later use;
s3, mixing the materials, and adding the sludge prepared in the step S2 and the sewage prepared in the step S1 into a mixing reactionAdding the sludge and sewage into a mixing reaction kettle, ultrasonically and non-stirring and mixing the sludge and the sewage in the mixing reaction kettle to prepare a sludge-water mixture with the sludge concentration of 2000-3000 mg/L, adding the sludge-water mixture into an SBR reactor, mixing and stirring the sludge-water mixture in the SBR reactor for 3-10 hours, carrying out aeration stirring on the sludge-water mixture in the SBR reactor for 10-30 minutes every 2-3 hours, wherein the aeration stirring is not less than 5 times, the dissolved oxygen DO in the sludge-water mixture after the aeration stirring is 2-10 mg/L, then standing and precipitating to carry out drainage operation, wherein the drainage ratio of the SBR reactor is 50-80%, and the drained water is stored in a water storage tank, when the water NH drained from the SBR reactor is discharged4—N<2mg/L，NO2-N accumulation rate>After 80%, completing the operation of the SBR reactor, and discharging and caching the residual mud-water mixture in the SBR reactor in a mud-water tank;
s4, purifying the muddy water, adding the muddy water mixture cached in the muddy water tank into the UASB reactor, and oxidizing NH by nitrification anaerobic ammonia oxidation4N and NO2Conversion of N to N2 and NH in sludge-water mixtures in UASB reactors4N and NO2Finishing the treatment operation of the UASB reactor after the N content is not more than 1 mg/L, conveying the mud-water mixture in the UASB reactor to a belt filter for solid-liquid separation, conveying the separated water body to a water storage tank in the step S3, and mixing the water body in the water storage tank in the step S3;
s5, carrying out adsorption purification, continuously aerating the water in the water storage tank for 10-60 minutes, carrying out negative pressure filtration on the aerated water to realize solid-liquid separation on the water, and filtering the water after the solid-liquid separation through a porous ceramic particle layer and an activated carbon particle layer in sequence to obtain the treated and purified water.
Further, before adding anaerobic bacteria into the sewage of the backflow part in the S1, firstly, the pH value of the sewage of the backflow part is adjusted to 6.5-7.2, and the using amount of anaerobic bacteria is 300g/m3—800 g/m3。
Further, in the step S3, the muddy water mixture is stirred at a mixing speed of 10 to 100 revolutions per minute; when in aeration stirring, the direction of aeration airflow is from bottom to top, the diameter of aeration bubbles is not more than 1 mm, the pressure of the aeration airflow is 1.5 to 3 times of the standard atmospheric pressure, the oxygen content in the aeration airflow is not more than 20 percent, and the area of the contact surface of an aeration disc and a water body is 30 to 70 percent of the cross section area of the inner cavity of the SBR reactor.
Further, in the step S5, the air pressure at the inlet is at least 5 times of the air pressure at the outlet.
Furthermore, the thicknesses of the porous ceramic particle layer and the activated carbon particle layer are not less than 10 mm, wherein the particle size of the ceramic particles in the porous ceramic particle layer is not more than 5 mm, and the particle size of the activated carbon in the activated carbon particle layer is 1-3 mm.
The invention has simple operation process, effectively improves the working efficiency and quality of the purification operation, effectively shortens the flow of the purification operation on the one hand, and improves the controllability of the process flow of the purification operation and the control precision of the regulation operation on the other hand; on the other hand, the forming rate of the granular sludge is effectively improved, the inhibiting effect of raw water directly participating in the anaerobic ammonia oxidation reaction on anaerobic ammonia oxidation bacteria is effectively avoided, and the system impact resistance and the operation strength of the purification system of the sewage treatment operation of the process are greatly improved, so that the operation stability and reliability of the sewage purification system are effectively improved while the sewage purification operation efficiency and quality are improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic view of the process of the present invention.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
As shown in figure 1, the advanced treatment process of the sewage with denitrification anaerobic ammonia oxidation of a backflow part comprises the following steps:
s1, primarily purifying the sewage, namely firstly heating the backflow part of the sewage to 25 ℃, adding anaerobic bacteria strains into the heated sewage in a heat preservation state, and culturing for 1 hour at constant temperature for later use;
s2, performing modulation treatment, namely inoculating the nitrifying bacteria into sludge with the water content of 70% and the sludge age of 10 days, then culturing for 1-3 days in a constant-temperature environment at 25 ℃, and preserving at constant temperature for later use;
s3, mixing materials, adding the sludge prepared in the S2 step and the sewage prepared in the S1 step into a mixing reaction kettle, carrying out ultrasonic non-stirring mixing on the sludge and the sewage in the mixing reaction kettle to prepare a mud-water mixture with the sludge concentration of 2000mg/L, adding the mud-water mixture into the SBR reactor, mixing and stirring the mud-water mixture in the SBR reactor for 3 hours, carrying out aeration stirring on the mud-water mixture in the SBR reactor for 10 minutes every 2 hours, carrying out aeration stirring for 5 times, enabling dissolved oxygen DO in the aerated and stirred mud-water mixture to be 2mg/L, standing and precipitating to carry out drainage operation, wherein the drainage ratio of the SBR reactor is 50%, storing water discharged in a water storage tank, and when water NH is discharged from the SBR reactor4—N<2mg/L，NO2-N accumulation rate>After 80%, completing the operation of the SBR reactor, and discharging and caching the residual mud-water mixture in the SBR reactor in a mud-water tank;
s4, purifying the muddy water, adding the muddy water mixture cached in the muddy water tank into the UASB reactor, and oxidizing NH by nitrification anaerobic ammonia oxidation4N and NO2Conversion of N to N2 and NH in sludge-water mixtures in UASB reactors4N and NO2The treatment of the UASB reactor can be completed after the N content is not more than 1 mg/LConveying the mud-water mixture in the UASB reactor to a belt filter for solid-liquid separation, conveying the separated water body to a water storage tank in the step S3, and mixing the water body in the water storage tank in the step S3;
s5, carrying out adsorption purification, carrying out continuous aeration operation on the water body in the water storage tank for 10 minutes, carrying out negative pressure filtration on the aerated water body firstly to realize solid-liquid separation on the water body, and then filtering the water body after solid-liquid separation through a porous ceramic particle layer and an activated carbon particle layer in sequence to obtain the treated and purified water body.
Wherein, before anaerobic bacteria are added into the sewage of the backflow part in the S1, the pH value of the sewage of the backflow part is firstly adjusted to 6.5, and the using amount of anaerobic bacteria is 300g/m3。
In the step S3, the mixing speed is 10 rpm while the slurry-water mixture is being stirred; when in aeration stirring, the direction of aeration airflow is from bottom to top, the diameter of aeration bubbles is not more than 1 mm, the pressure of the aeration airflow is 1.5 times of the standard atmospheric pressure, the oxygen content in the aeration airflow is 20 percent, and the area of the contact surface of an aeration disc and water is 30 percent of the cross section area of the inner cavity of the SBR reactor.
Meanwhile, in the step S5, the air pressure at the inlet is 5 times of the air pressure at the outlet.
Furthermore, the thickness of the porous ceramic particle layer and the activated carbon particle layer is 10 mm, wherein the particle size of the ceramic particles in the porous ceramic particle layer is 5 mm, and the particle size of the activated carbon in the activated carbon particle layer is 1 mm.
Example 2
A sewage advanced treatment process for denitrification anaerobic ammonia oxidation of a backflow part comprises the following steps:
s1, primarily purifying the sewage, namely firstly heating the backflow part of the sewage to 40 ℃ and keeping the temperature, adding anaerobic bacteria strains into the heated sewage, and culturing for 6 hours at constant temperature for later use;
s2, performing modulation treatment, namely inoculating the nitrifying bacteria into sludge with the water content of 80% and the sludge age of 50 days, then culturing for 3 days in a constant-temperature environment at 40 ℃ and preserving at constant temperature for later use;
s3, mixing materials, adding the sludge prepared in the S2 step and the sewage prepared in the S1 step into a mixing reaction kettle, carrying out ultrasonic non-stirring mixing on the sludge and the sewage in the mixing reaction kettle to prepare a mud-water mixture with the sludge concentration of 3000mg/L, adding the mud-water mixture into the SBR reactor, mixing and stirring the mud-water mixture in the SBR reactor for 10 hours, carrying out aeration stirring on the mud-water mixture in the SBR reactor for 30 minutes every 3 hours, carrying out aeration stirring for 10 times, keeping dissolved oxygen DO in the aerated and stirred mud-water mixture at 10mg/L, standing and precipitating to perform drainage operation, wherein the drainage ratio of the SBR reactor is 80%, and the drained water is stored in a water storage tank, when the water discharged by the SBR reactor is NH (NH)4—N<2mg/L，NO2-N accumulation rate>After 80%, completing the operation of the SBR reactor, and discharging and caching the residual mud-water mixture in the SBR reactor in a mud-water tank;
s4, purifying the muddy water, adding the muddy water mixture cached in the muddy water tank into the UASB reactor, and oxidizing NH by nitrification anaerobic ammonia oxidation4N and NO2Conversion of N to N2 and NH in sludge-water mixtures in UASB reactors4N and NO2Finishing the treatment operation of the UASB reactor after the N content is not more than 1 mg/L, conveying the mud-water mixture in the UASB reactor to a belt filter for solid-liquid separation, conveying the separated water body to a water storage tank in the step S3, and mixing the water body in the water storage tank in the step S3;
s5, carrying out adsorption purification, carrying out continuous aeration operation on the water body in the water storage tank for 60 minutes, carrying out negative pressure filtration on the aerated water body firstly to realize solid-liquid separation on the water body, and then filtering the water body after solid-liquid separation through a porous ceramic particle layer and an activated carbon particle layer in sequence to obtain the treated and purified water body.
Wherein, before anaerobic bacteria are added into the sewage of the backflow part in the S1, the pH value of the sewage of the backflow part is firstly adjusted to 7.2, and the using amount of anaerobic bacteria is 300g/m3—800 g/m3。
Meanwhile, in the step S3, the slurry-water mixture is stirred at a mixing speed of 100 rpm; when in aeration stirring, the direction of aeration airflow is from bottom to top, the diameter of aeration bubbles is not more than 1 mm, the pressure of the aeration airflow is 3 times of the standard atmospheric pressure, the oxygen content in the aeration airflow is 15 percent, and the area of the contact surface of an aeration disc and a water body is 70 percent of the cross section area of the inner cavity of the SBR reactor.
In this embodiment, in the step S5, the air pressure at the inlet is 8 times of the air pressure at the outlet.
In this embodiment, the thicknesses of the porous ceramic particle layer and the activated carbon particle layer are 20 mm, wherein the particle size of the ceramic particles in the porous ceramic particle layer is 3 mm, and the particle size of the activated carbon in the activated carbon particle layer is 1 mm.
Example 3
A sewage advanced treatment process for denitrification anaerobic ammonia oxidation of a backflow part comprises the following steps:
s1, primarily purifying the sewage, namely firstly heating the backflow part of the sewage to 30 ℃, adjusting the pH value of the backflow part of the sewage to 7 under the heat preservation state, then adding anaerobic bacteria strains into the heated sewage, and culturing for 3 hours at constant temperature for later use, wherein the using amount of the anaerobic bacteria strains is 600 g/m3；
S2, performing modulation treatment, namely inoculating the nitrifying bacteria into sludge with the water content of 85% and the sludge age of 20 days, then culturing for 2 days in a constant-temperature environment at 30 ℃ and preserving at constant temperature for later use;
s3, mixing materials, adding the sludge prepared in the S2 step and the sewage prepared in the S1 step into a mixing reaction kettle, carrying out ultrasonic non-stirring mixing on the sludge and the sewage in the mixing reaction kettle to prepare a mud-water mixture with the sludge concentration of 2200mg/L, adding the mud-water mixture into the SBR reactor, mixing and stirring the mud-water mixture in the SBR reactor for 5 hours, carrying out aeration stirring on the mud-water mixture in the SBR reactor for 15 minutes every 2.5 hours, carrying out aeration stirring for 10 times, keeping dissolved oxygen DO in the mud-water mixture after the aeration stirring at 4mg/L, standing and precipitating to perform drainage operation, wherein the drainage ratio of the SBR reactor is 60%, storing discharged water in a water storage tank, and when the water NH is discharged from the SBR reactor4—N<2mg/L，NO2-N accumulation rate>After 80%, completing the operation of the SBR reactor, and discharging and caching the residual mud-water mixture in the SBR reactor in a mud-water tank;
s4, purifying the muddy water, adding the muddy water mixture cached in the muddy water tank into the UASB reactor, and oxidizing NH by nitrification anaerobic ammonia oxidation4N and NO2Conversion of N to N2 and NH in sludge-water mixtures in UASB reactors4N and NO2Finishing the treatment operation of the UASB reactor after the N content is not more than 1 mg/L, conveying the mud-water mixture in the UASB reactor to a belt filter for solid-liquid separation, conveying the separated water body to a water storage tank in the step S3, and mixing the water body in the water storage tank in the step S3;
s5, adsorbing and purifying, wherein the water in the water storage tank is continuously aerated for 40 minutes, then the aerated water is firstly subjected to negative pressure filtration to realize solid-liquid separation of the water, and then the water subjected to solid-liquid separation is filtered through a porous ceramic particle layer and an activated carbon particle layer in sequence to obtain the treated and purified water.
In the step S3, the mixing speed is 90 rpm while the slurry-water mixture is being stirred; when in aeration stirring, the direction of aeration airflow is from bottom to top, the diameter of aeration bubbles is not more than 1 mm, the pressure of the aeration airflow is 2 times of the standard atmospheric pressure, the oxygen content in the aeration airflow is 5 percent, and the area of the contact surface of an aeration disc and a water body is 60 percent of the cross section area of the inner cavity of the SBR reactor.
In addition, in the step S5, the air pressure at the inlet is 10 times of the air pressure at the outlet.
Meanwhile, the thicknesses of the porous ceramic particle layer and the activated carbon particle layer are both 30 mm, wherein the particle size of the ceramic particles in the porous ceramic particle layer is 4 mm, and the particle size of the activated carbon in the activated carbon particle layer is 2 mm.
The invention has simple operation process, effectively improves the working efficiency and quality of the purification operation, effectively shortens the flow of the purification operation on the one hand, and improves the controllability of the process flow of the purification operation and the control precision of the regulation operation on the other hand; on the other hand, the forming rate of the granular sludge is effectively improved, the inhibiting effect of raw water directly participating in the anaerobic ammonia oxidation reaction on anaerobic ammonia oxidation bacteria is effectively avoided, and the system impact resistance and the operation strength of the purification system of the sewage treatment operation of the process are greatly improved, so that the operation stability and reliability of the sewage purification system are effectively improved while the sewage purification operation efficiency and quality are improved.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention, and all the changes or substitutions should be covered within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (5)
1. A sewage advanced treatment process for denitrification anaerobic ammonia oxidation of a backflow part is characterized in that: the advanced sewage treatment process for denitrifying anaerobic ammonium oxidation of the reflux part comprises the following steps:
s1, primarily purifying the sewage, namely firstly heating the returned part of the sewage to 25-40 ℃ and keeping the temperature, adding anaerobic bacteria strains into the heated sewage, and carrying out constant temperature cultivation for 1-6 hours for later use;
s2, performing modulation treatment, namely inoculating the nitrifying bacteria into sludge with the water content of not less than 70% and the sludge age of 10-50 days, then culturing for 1-3 days at the constant temperature of 25-40 ℃, and storing at the constant temperature for later use;
s3, mixing materials, adding the sludge prepared in the S2 step and the sewage prepared in the S1 step into a mixing reaction kettle, mixing the sludge and the sewage in the mixing reaction kettle without ultrasonic agitation to prepare a mud-water mixture with the sludge concentration of 2000-3000 mg/L, adding the mixture into an SBR reactor, mixing and stirring the mud-water mixture in the SBR reactor for 3-10 hours, carrying out aeration stirring on the mud-water mixture in the SBR reactor for 10-30 minutes every 2-3 hours with aeration stirring not less than 5 times, and enabling dissolved oxygen DO in the mud-water mixture after aeration stirring to be 2-10 mg/L,then standing and settling to perform drainage operation, wherein the drainage ratio of the SBR reactor is 50% -80%, the drained water is stored in a water storage tank, and NH is drained from the SBR reactor when water is drained4—N<2mg/L，NO2-N accumulation rate>After 80%, completing the operation of the SBR reactor, and discharging and caching the residual mud-water mixture in the SBR reactor in a mud-water tank;
s4, purifying the muddy water, adding the muddy water mixture cached in the muddy water tank into the UASB reactor, and oxidizing NH by nitrification anaerobic ammonia oxidation4N and NO2Conversion of N to N2 and NH in sludge-water mixtures in UASB reactors4N and NO2Finishing the treatment operation of the UASB reactor after the N content is not more than 1 mg/L, conveying the mud-water mixture in the UASB reactor to a belt filter for solid-liquid separation, conveying the separated water body to a water storage tank in the step S3, and mixing the water body in the water storage tank in the step S3;
s5, carrying out adsorption purification, continuously aerating the water in the water storage tank for 10-60 minutes, carrying out negative pressure filtration on the aerated water to realize solid-liquid separation on the water, and filtering the water after the solid-liquid separation through a porous ceramic particle layer and an activated carbon particle layer in sequence to obtain the treated and purified water.
2. The advanced wastewater treatment process for denitrification anaerobic ammonia oxidation of a reflux part according to claim 1, which is characterized in that: before anaerobic bacteria are added into the returned part of the sewage in the S1, the pH value of the returned part of the sewage is adjusted to 6.5-7.2, and the using amount of anaerobic bacteria is 300g/m3—800 g/m3。
3. The advanced wastewater treatment process for denitrification anaerobic ammonia oxidation of a reflux part as claimed in claim 2, which is characterized in that: in the step S3, the mud-water mixture is stirred at a mixing speed of 10-100 r/min; when in aeration stirring, the direction of aeration airflow is from bottom to top, the diameter of aeration bubbles is not more than 1 mm, the pressure of the aeration airflow is 1.5 to 3 times of the standard atmospheric pressure, the oxygen content in the aeration airflow is not more than 20 percent, and the area of the contact surface of an aeration disc and a water body is 30 to 70 percent of the cross section area of the inner cavity of the SBR reactor.
4. The advanced wastewater treatment process for denitrification anaerobic ammonia oxidation of a reflux part according to claim 1, which is characterized in that: in the step S5, the air pressure at the inlet is at least 5 times of the air pressure at the outlet.
5. The advanced wastewater treatment process for denitrification anaerobic ammonia oxidation of a reflux part according to claim 1, which is characterized in that: the thicknesses of the porous ceramic particle layer and the activated carbon particle layer are not less than 10 millimeters, wherein the particle size of the ceramic particles in the porous ceramic particle layer is not more than 5 millimeters, and the particle size of the activated carbon in the activated carbon particle layer is 1-3 millimeters.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010840989.2A CN111908727A (en) | 2020-08-20 | 2020-08-20 | Advanced sewage treatment process for denitrification anaerobic ammonia oxidation of reflux part |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010840989.2A CN111908727A (en) | 2020-08-20 | 2020-08-20 | Advanced sewage treatment process for denitrification anaerobic ammonia oxidation of reflux part |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111908727A true CN111908727A (en) | 2020-11-10 |
Family
ID=73278445
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010840989.2A Pending CN111908727A (en) | 2020-08-20 | 2020-08-20 | Advanced sewage treatment process for denitrification anaerobic ammonia oxidation of reflux part |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111908727A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102583883A (en) * | 2012-02-16 | 2012-07-18 | 北京工业大学 | Technology and method for treating urban sewage by sectional parallel anaerobic ammonia oxidation |
| CN103833185A (en) * | 2014-03-10 | 2014-06-04 | 北京工业大学 | Energy recovery-based landfill leachate autotrophic nitrogen removal method |
| CN105152454A (en) * | 2015-07-07 | 2015-12-16 | 北京工业大学 | Experimental apparatus and method coupling SBR shortcut denitrification phosphorus removal and anaerobic ammonium oxidation |
| CN105461178A (en) * | 2016-01-09 | 2016-04-06 | 北京工业大学 | System and method for treating municipal sewage through short-cut denitrification-anaerobic ammonia oxidation after short-cut nitrification-anaerobic ammonia oxidation |
| 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 |
-
2020
- 2020-08-20 CN CN202010840989.2A patent/CN111908727A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102583883A (en) * | 2012-02-16 | 2012-07-18 | 北京工业大学 | Technology and method for treating urban sewage by sectional parallel anaerobic ammonia oxidation |
| CN103833185A (en) * | 2014-03-10 | 2014-06-04 | 北京工业大学 | Energy recovery-based landfill leachate autotrophic nitrogen removal method |
| CN105152454A (en) * | 2015-07-07 | 2015-12-16 | 北京工业大学 | Experimental apparatus and method coupling SBR shortcut denitrification phosphorus removal and anaerobic ammonium oxidation |
| CN105461178A (en) * | 2016-01-09 | 2016-04-06 | 北京工业大学 | System and method for treating municipal sewage through short-cut denitrification-anaerobic ammonia oxidation after short-cut nitrification-anaerobic ammonia oxidation |
| 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 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101607777B (en) | Lurgi furnace coal gasification wastewater treatment and reuse technology | |
| JP3821011B2 (en) | Wastewater treatment method and treatment apparatus | |
| JP4224951B2 (en) | Denitrification method | |
| WO2016117210A1 (en) | Denitrification method and denitrification apparatus for nitrogen-containing waste water | |
| CN108658377B (en) | Full-submerged sewage treatment method capable of simultaneously removing nitrogen and phosphorus | |
| WO1998033745A1 (en) | Process, using ammonia rich water for the selection and enrichment of nitrifying micro-organisms for nitrification of wastewater | |
| WO2014146439A1 (en) | Biochemical method for treating synthetic leather wastewater comprising dimethylformamide | |
| CN112573652B (en) | Sulfur autotrophic denitrification treatment process | |
| CN108585189A (en) | The apparatus and method of segmentation water outlet denitrification dephosphorization-short distance nitration biological film coupling Anammox processing city domestic sewage | |
| CN106986442B (en) | Method for treating ammonia nitrogen sewage by combining microorganism carrier and fluidized bed | |
| JP4915036B2 (en) | Denitrification method and denitrification apparatus | |
| KR100643775B1 (en) | Treatment hybrid process for remove nutrient using floating microorganism | |
| CN108545887A (en) | The method of sulfide type DEAMOX postposition anoxics filter tank denitrification and desulfurization hydrogen based on AAO-BAF Process for Effluent | |
| JP5055667B2 (en) | Biological denitrification method and biological denitrification apparatus | |
| CN111908727A (en) | Advanced sewage treatment process for denitrification anaerobic ammonia oxidation of reflux part | |
| CN114477652B (en) | Advanced treatment system and method for urban sewage | |
| CN115838210A (en) | Sewage treatment system combining pure biomembrane/A3 AO sludge membrane and dual modes and operation method thereof | |
| JP7200248B2 (en) | Organic wastewater treatment method and organic wastewater treatment apparatus | |
| CN110615525A (en) | Method for enriching anaerobic ammonium oxidation bacteria and application | |
| CN210457854U (en) | Mainstream autotrophic nitrogen removal system based on MBBR | |
| CN107487841A (en) | A kind of denitrification integrates coupling dephosphorization and the waste water treatment process of Anammox | |
| JPH05228493A (en) | Method for treating waste water using sulfur bacterium and apparatus therefor | |
| JPH04341397A (en) | Methane fermentation treatment apparatus and methane fermentation method | |
| Lia | Simultaneous nitritation, anammox, and denitrification (SNAD) process in a membrane bioreactor: start-up, optimization, and membrane fouling behavior | |
| JPS59162997A (en) | Organic filthy water disposal |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20201110 |
|
| RJ01 | Rejection of invention patent application after publication |