CN115072860A - Three-section type urban sewage anaerobic ammonia oxidation efficient denitrification system and method - Google Patents
Three-section type urban sewage anaerobic ammonia oxidation efficient denitrification system and method Download PDFInfo
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 238000000034 method Methods 0.000 title claims abstract description 64
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 64
- 230000003647 oxidation Effects 0.000 title claims abstract description 63
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 61
- 239000010865 sewage Substances 0.000 title claims abstract description 38
- 230000008569 process Effects 0.000 claims abstract description 45
- 102100029974 GTPase HRas Human genes 0.000 claims abstract description 40
- 101000584633 Homo sapiens GTPase HRas Proteins 0.000 claims abstract description 40
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 27
- 239000010802 sludge Substances 0.000 claims abstract description 21
- 238000010992 reflux Methods 0.000 claims abstract description 6
- 238000006396 nitration reaction Methods 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 126
- 230000014759 maintenance of location Effects 0.000 claims description 18
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 238000005070 sampling Methods 0.000 claims description 9
- 238000005086 pumping Methods 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000005273 aeration Methods 0.000 claims description 6
- 238000004062 sedimentation Methods 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 3
- 239000004743 Polypropylene Substances 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims description 2
- -1 polypropylene Polymers 0.000 claims description 2
- 229920001155 polypropylene Polymers 0.000 claims description 2
- 238000004886 process control Methods 0.000 claims description 2
- 230000002035 prolonged effect Effects 0.000 claims description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 24
- 239000010841 municipal wastewater Substances 0.000 abstract description 2
- 230000009467 reduction Effects 0.000 abstract description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000009825 accumulation Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000003203 everyday effect Effects 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000002354 daily effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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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
- C02F3/006—Regulation methods for biological 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
- 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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
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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
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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Abstract
A three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification system and a three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification method belong to the technical field of sewage biological treatment. The municipal sewage passes through the HRAS unit, the partial nitrification unit and the anaerobic ammonia oxidation unit in turn, and organic matters contained in the municipal sewage are converted into sludge and partial NH 4 + Oxidation of-N to NO 2 ‑ N and removing part of nitrogen in the short-distance nitration effluent. Containing excess NO 3 ‑ The effluent of the anaerobic ammonium oxidation unit of-N enters a short-range denitrification unit, and NO is separated by utilizing organic matters in the municipal sewage flowing in from the side 3 ‑ Reduction of-N to NO 2 ‑ N, NO produced by refluxing the anaerobic ammonia oxidation unit with the effluent thereof 2 ‑ N and NH in the side influent municipal wastewater 4 + -N is further removed. The invention solves the problem that the prior short-cut nitrification-anaerobic ammonia oxidation process treats the urban sewageLow denitrification efficiency, NO 3 ‑ The concentration of N is high, and the short-cut nitrification unit does not need a complex control process during operation and is easy to operate and manage.
Description
The technical field is as follows:
the invention relates to a three-section type urban sewage anaerobic ammonia oxidation efficient denitrification system and method, and belongs to the technical field of sewage biological treatment.
Background art:
the removal of nitrogen has already been carried outBecomes one of the key problems in the field of water treatment in China. In the traditional denitrification technology, sewage needs NH under the action of aerobic nitrification 4 + Conversion of-N to NO 3 - -N. Then denitrification is carried out under the anoxic condition to finally convert nitrogen in the wastewater into N 2 And (4) overflowing. Although the traditional biological denitrification technology has mature process and good denitrification effect, the method has the defects of long process flow, large occupied area, frequently added carbon source, high energy consumption, high cost and the like. Therefore, a new and efficient denitrification technology is urgently needed to be found.
In recent years, the technique of anammox, which is the process of converting NH under anoxic conditions, has been the focus of research on sewage treatment 4 + -N and NO 2 - Direct conversion of-N to N 2 The process of (1). Compared with the traditional denitrification technology, the method has the advantages of low energy consumption, small organic carbon source utilization amount, small sludge yield and the like, and can achieve the purposes of economy and high efficiency in the aspect of wastewater treatment. However, the main form of nitrogen in municipal sewage is NH 4 + N, which does not meet the demand for anammox. Currently, it is common to provide stable NO for anammox by short-cut nitrification techniques 2 - N, a partial nitrification-anaerobic ammonia oxidation (PN/A) process. However, when the shortcut nitrification-anaerobic ammonia oxidation process is applied to the mainstream wastewater treatment project, the shortcut nitrification process is difficult to control due to frequent change of environmental conditions and sewage quality, and the effluent often contains a large amount of NO 3 - -N generation. On the other hand, the anammox denitrification process also produces a certain amount of NO 3 - -N, 10% -12% of total nitrogen removed, which further increases effluent NO 3 - -the concentration of N. Therefore, the effluent of the current mainstream shortcut nitrification-process often needs to be further treated to meet the total nitrogen emission requirement of the effluent.
Short-range denitrification (PD) can remove NO in water 3 - Stable and efficient conversion of-N to NO 2 - -N. Thus, by following the short-cut nitrification-anammox process with short-cut denitrification, the NO produced thereby is 3 - Conversion of-N to NO 2 - And the N flows back to the anaerobic ammonia oxidation reactor for further removal, so that the high-efficiency denitrification of the anaerobic ammonia oxidation in the urban sewage treatment process can be enhanced, and the operation cost is greatly reduced.
The invention content is as follows:
the invention provides a three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification system and a three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification method, and particularly relates to a method for converting organic matters contained in urban sewage into partial NH in sludge by sequentially passing through a HRAS unit, a short-range denitrification unit and an anaerobic ammonia oxidation unit 4 + Oxidation of-N to NO 2 - N and removing part of nitrogen in the effluent of the short-cut nitrification reactor. Containing excess NO 3 - The effluent of the anaerobic ammoxidation reactor of-N enters a short-cut denitrification reactor, and NO is converted by organic matters in the municipal sewage flowing in from the side 3 - Reduction of-N to NO 2 - N, NO produced by refluxing the effluent of the anaerobic ammonia oxidation reactor 2 - N and NH in the side influent municipal wastewater 4 + And (4) further removing N, and realizing high-efficiency denitrification of anaerobic ammonia oxidation of the municipal sewage by optimizing the water inlet flow of the short-cut denitrification reactor.
The purpose of the invention is realized by the following technical scheme
The three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification system is characterized by comprising a raw water tank (1), an HRAS reactor (2), a short-cut nitrification reactor (3), a first intermediate water tank (4), an anaerobic ammonia oxidation reactor (5), a second intermediate water tank (6), a short-cut denitrification reactor (7) and a third intermediate water tank (8); the HRAS reactor (2) is provided with a first stirrer (2.1), a first aeration head (2.2) and a sedimentation tank (2.3); the short-cut nitrification reactor (3) is provided with an air pump (3.1), a second aeration head (3.2), a first water inlet (3.3), a first water outlet (3.4), a second water inlet pump (3.5), a second stirrer (3.6) and a first sampling port (3.7); the anaerobic ammonia oxidation reactor (5) is provided with a second water inlet (5.1), a first backflow port (5.2), a first backflow pump (5.3), a second water outlet (5.4), an exhaust port (5.5), a gas collection bag (5.6), a three-phase separator (5.7), a first vent pipe (5.8), a second sampling port (5.9), a third water inlet pump (5.10) and a fourth water inlet pump (5.11); the short-cut denitrification reactor (7) is provided with a third water inlet (7.1), a fourth water inlet (7.2), a third water outlet (7.3), a third stirrer (7.4), a third sampling port (7.5), a fifth water inlet pump (7.6), a sixth water inlet pump (7.7), a seventh water inlet pump (7.8) and an eighth water inlet pump (7.9)
The raw water tank (1) is connected with the HRAS reactor (2) through a first water inlet pump (1.1), a sedimentation tank (2.3) of the HRAS reactor (2) is connected with a first water inlet (3.3) of the shortcut nitrification reactor (3) through a second water inlet pump (3.5), a first intermediate water tank (4) is connected with a second water inlet (5.1) of the anaerobic ammonia oxidation reactor (5) through a third water inlet pump (5.10), a third intermediate water tank (8) is connected with the second water inlet (5.1) of the anaerobic ammonia oxidation reactor (5) through a fourth water inlet pump (5.11), a second intermediate water tank (6) is connected with a fourth water inlet (7.2) of the shortcut denitrification reactor (7) through an eighth water inlet pump (7.9), the raw water tank (1) is connected with a third water inlet (7.1) of the shortcut denitrification reactor (7) through a fifth water inlet pump (7.6), and the shortcut denitrification reactor (7.2) is connected with a sixth water inlet (7.1) of the shortcut denitrification reactor (7).
The method is characterized by comprising the following steps:
(1) introducing the municipal sewage into an HRAS reactor, controlling the dissolved oxygen concentration of 1.0-4.0mg/L, the sludge concentration MLSS of 1.5-4.0g/L, the hydraulic retention time of 20-60 minutes and the sludge retention time of 0.5-4 days in the operation process of the HRAS reactor;
(2) pumping effluent of the HRAS reactor into a short-cut nitrification reactor, and controlling the sludge concentration MLSS to be 1.0-4.0g/L, the biofilm carrier filling volume ratio to be 20-60% and the dissolved oxygen concentration to be 0.2-1.0mg/L in the running process of the short-cut nitrification reactor;
(3) pumping the effluent of the partial nitrification reactor into an anaerobic ammonia oxidation reactor, controlling the concentration MLSS of the granular sludge in the running process of the anaerobic ammonia oxidation reactor to be 5.0-20.0g/L, and controlling the NO of the effluent 2 - -N concentration less than 1.0 mg/L;
(4) pumping the effluent of the anaerobic ammoxidation reactor, the municipal sewage and the effluent of the HRAS reactor into a short-cut denitrification reactor together, and controlling the MLSS of the granular sludge concentration of the short-cut denitrification reactor to be 3.0-1 in the running process of the short-cut denitrification reactor0.0g/L, 3-10 days of sludge retention time, 5-20 minutes of hydraulic retention time, and COD and NO in the mixed inlet water of the short-cut denitrification reactor 3 - A mass concentration ratio of-N to NO of 2.5-5.0 3 - -N and NH 4 + The mass concentration ratio of-N is 1.2-2.0, and the NO in the effluent of the short-cut denitrification reactor 3 - -N concentration less than 2.0 mg/L;
(5) the effluent of the partial denitrification reactor flows back to the anaerobic ammonia oxidation reactor, the reflux ratio is controlled to be 100-300%, and the effluent NH of the anaerobic ammonia oxidation reactor 4 + -N concentration less than 3.0mg/L, NO 3 - -N concentration less than 8.0 mg/L.
When the concentration of the dissolved organic matters in the effluent of the HRAS reactor in the operation process of the step (1) is more than 50mg/L, the concentration of the dissolved oxygen in the HRAS reactor is increased within the range of 1.0-4.0mg/L or the hydraulic retention time of the HRAS reactor is prolonged within the range of 20-60 minutes until the concentration of the dissolved organic matters in the effluent of the HRAS reactor is less than or equal to 50 mg/L;
the biomembrane carrier in the step (2) is polypropylene hollow ring light filler, and NO is discharged from the short-cut nitrification reactor in the operation process 2 - -N and NH 4 + The mass concentration ratio of-N to N is 1.0-1.8, if NO is discharged from the short distance nitration reactor 2 - -N and NH 4 + If the mass concentration ratio of-N is less than 1.0, the content of dissolved oxygen in the short-cut nitrification reactor is increased within the range of 0.2-1.0mg/L until the ratio is more than or equal to 1.0. If the water outlet NO of the short-cut nitrification reactor is discharged 2 - -N and NH 4 + If the mass concentration ratio of-N is more than 1.8, the content of dissolved oxygen in the short-cut nitrification reactor is reduced within the range of 0.2-1.0mg/L until the ratio is less than or equal to 1.8.
The effluent NO of the anaerobic ammonia oxidation reactor in the operation process of the step (3) 2 - When the N concentration is more than or equal to 1.0mg/L, prolonging the hydraulic retention time until the effluent NO 2 - -N concentration less than 1.0 mg/L;
the step (4) of operating the process control short-cut denitrification NO 3 - -N to NO 2 - The conversion rate of-N is more than 50 percent, COD and NO are mixed in the influent water 3 - When the mass concentration ratio of-N is more than 5.0, introducing HRAS reactor effluent to adjust until COD and NO in the short-range denitrification reactor 3 - -the ratio of the mass concentration of N is 5.0 or less;
the water NO discharged from the short-cut denitrification reactor in the operation process of the step (4) 3 - The concentration of N is more than or equal to 2.0mg/L, and COD and NO are improved within the range of 2.5 to 5.0 3 - -a ratio of N mass concentrations;
the MLSS concentration of the mixed liquid of the effluent of the short-cut denitrification reactor in the operation process of the step (4) is controlled to be less than 100 mg/L;
the effluent NH of the anaerobic ammonia oxidation reactor in the operation process of the step (5) 4 + When the N concentration is more than or equal to 3.0mg/L, the NO content in the mixed feed water of the short-cut denitrification reactor is increased within the range of 1.2-2.0 3 - -N and NH 4 + Mass concentration ratio of-N to effluent NH of anaerobic ammoxidation reactor 4 + -N concentration less than 3.0 mg/L;
the effluent NO of the anaerobic ammonia oxidation reactor in the operation process of the step (5) 3 - When the concentration of N is more than or equal to 8.0mg/L, the reflux ratio of the effluent of the anaerobic ammonia oxidation reactor is increased within the range of 100-300 percent until the effluent NO of the anaerobic ammonia oxidation reactor is 3 - -N concentration less than 8.0 mg/L.
The invention provides a three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification system and a three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification method, which have the following advantages and characteristics:
1) combines the short-cut nitrification and short-cut denitrification processes to ensure that the anaerobic ammonia oxidation reaction substrate NO 2 - The N is stably and efficiently supplied, the denitrification effect is fully exerted, and the operating cost of the urban sewage treatment process is greatly reduced.
2) The process solves the problems of low denitrification efficiency and high total nitrogen content of the effluent in the traditional shortcut nitrification-anaerobic ammonia oxidation process, and the total nitrogen content of the effluent can meet more strict discharge standards through optimization, thereby promoting the multi-target recycling of the municipal sewage.
3) Process system for shortcut nitration of NO 2 - low-N accumulation rate requirement and no need of complexityProcess control of (3) to achieve NO 2 - And the efficient accumulation of N is realized, and when the water quality condition changes, the effective removal of nitrogen in the system can be ensured only by optimizing the flow distribution of the inlet water of the short-cut denitrification system.
4) Part of organic matters bypass the HRAS reactor without passing through the HRAS reactor and are directly used as a denitrification carbon source, the waste of the organic matters in the HRAS reactor is reduced, the organic matters in the municipal sewage are used for providing an electron donor in the short-cut denitrification process, the use of an external carbon source is reduced, and the operation cost is saved.
Description of the drawings:
FIG. 1 is a process flow diagram of a three-stage anaerobic ammonia oxidation high-efficiency denitrification system and method for municipal sewage.
FIG. 2 is a nitrogen conversion diagram of a three-stage anaerobic ammonia oxidation high-efficiency denitrification system and method for urban sewage in an operation process.
The specific implementation mode is as follows:
the invention is described in further detail below with reference to the attached drawing and the detailed description
As shown in fig. 1, a three-stage anaerobic ammonia oxidation high-efficiency denitrification system for municipal sewage is characterized by comprising a raw water tank (1), an HRAS reactor (2), a short-cut nitrification reactor (3), a first intermediate water tank (4), an anaerobic ammonia oxidation reactor (5), a second intermediate water tank (6), a short-cut denitrification reactor (7) and a third intermediate water tank (8); the HRAS reactor (2) is provided with a first stirrer (2.1), a first aeration head (2.2) and a sedimentation tank (2.3); the short-cut nitrification reactor (3) is provided with an air pump (3.1), a second aeration head (3.2), a first water inlet (3.3), a first water discharge port (3.4), a second water inlet pump (3.5), a second stirrer (3.6) and a first sampling port (3.7); the anaerobic ammonia oxidation reactor (5) is provided with a second water inlet (5.1), a first backflow port (5.2), a first backflow pump (5.3), a second water outlet (5.4), an exhaust port (5.5), a gas collection bag (5.6), a three-phase separator (5.7), a first vent pipe (5.8), a second sampling port (5.9), a third water inlet pump (5.10) and a fourth water inlet pump (5.11); the short-cut denitrification reactor (7) is provided with a third water inlet (7.1), a fourth water inlet (7.2), a third water outlet (7.3), a third stirrer (7.4), a third sampling port (7.5), a fifth water inlet pump (7.6), a sixth water inlet pump (7.7), a seventh water inlet pump (7.8) and an eighth water inlet pump (7.9)
The raw water tank (1) is connected with the HRAS reactor (2) through a first water inlet pump (1.1), a sedimentation tank (2.3) of the HRAS reactor (2) is connected with a first water inlet (3.3) of the shortcut nitrification reactor (3) through a second water inlet pump (3.5), a first intermediate water tank (4) is connected with a second water inlet (5.1) of the anaerobic ammonia oxidation reactor (5) through a third water inlet pump (5.10), a third intermediate water tank (8) is connected with the second water inlet (5.1) of the anaerobic ammonia oxidation reactor (5) through a fourth water inlet pump (5.11), a second intermediate water tank (6) is connected with a fourth water inlet (7.2) of the shortcut denitrification reactor (7) through an eighth water inlet pump (7.9), the raw water tank (1) is connected with a third water inlet (7.1) of the shortcut denitrification reactor (7) through a fifth water inlet pump (7.6), and the shortcut denitrification reactor (7.2) is connected with a sixth water inlet (7.1) of the shortcut denitrification reactor (7).
The experimental water in this experimental example is municipal sewage, NH thereof 4 + The average concentration of-N was 55.2mg/L, and the average COD concentration was 330.5 mg/L. In the experiment, the effective volume of the short-cut nitrification SBR reactor is 10L, 12 periods are carried out every day, 4L of water is discharged every period, and the effective volume of the anaerobic ammonia oxidation UASB reactor is 5L; the effective volume of the short-cut denitrification SBR reactor is 10L, 12 periods are carried out every day, and 4.4L of water is drained every period.
The specific operation process is as follows:
the daily water inflow of the HRAS reactor is 50L, the HRAS reactor discharges NH under the conditions that the sludge concentration MLSS is 3.0g/L, the dissolved oxygen concentration is 2.5mg/L, the hydraulic retention time is 40 minutes and the sludge retention time is 2 days 4 + The average value of-N was 50.1mg/L, and the average value of COD was 35.3 mg/L.
Pumping effluent (48L/d) of the HRAS reactor into a short-cut nitrification reactor, and under the conditions that sludge concentration MLSS of the short-cut nitrification reactor is 2.5g/L, filling volume ratio of biomembrane carrier is 40%, dissolved oxygen concentration is 0.6mg/L and hydraulic retention time is 3h, discharging NH from the short-cut nitrification reactor 4 + Average value of-N concentration 10.3mg/L, NO 3 - Average value of-N concentration of 25.2mg/L, NO 2 - The average value of the concentration of-N was 15.1 mg/L.
Pumping effluent of the partial nitrification reactor into an anaerobic ammonia oxidation reactor, operating under the conditions that the sludge concentration MLSS of the anaerobic ammonia oxidation reactor is 13.0g/L and the hydraulic retention time is 2.3h, and discharging NO 2 - The concentration of-N is always maintained below 0.5 mg/L.
The effluent (48L/d) of the anaerobic ammonia oxidation reactor, the municipal sewage (3L/d) and the effluent (2L/d) of the HRAS reactor flow into the short-cut denitrification reactor together, and NO in the effluent of the short-cut denitrification reactor is treated under the conditions that the sludge concentration MLSS is 6.0g/L, the sludge retention time is 7 days and the hydraulic retention time is 20 minutes 3 - Average concentration of-N of 1.1mg/L, NO 2 - The average concentration of-N was 5.2 mg/L.
The effluent of the partial denitrification reactor completely flows back to the anaerobic ammonia oxidation reactor, and the effluent NH 4 + -N、NO 3 - The average values of the mass concentrations of the N and the TN are respectively 0.3mg/L, 6.5mg/L and 8.1mg/L, and the average removal rate of total nitrogen of inlet water in the running process of the whole system is more than 85 percent.
The process technology for realizing the maximization of the anammox denitrification of the municipal sewage provided by the invention is introduced in detail, and the principle and the implementation method of the invention are explained by applying specific examples, and the description of the examples is only used for helping to understand the method and the core idea of the method; for those skilled in the art, there may be variations to the specific embodiments based on the concept of the present invention, and therefore, the present description should not be construed as limiting the invention.
Claims (2)
1. A three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification system is characterized by comprising a raw water tank (1), an HRAS reactor (2), a short-cut nitrification reactor (3), a first intermediate water tank (4), an anaerobic ammonia oxidation reactor (5), a second intermediate water tank (6), a short-cut denitrification reactor (7) and a third intermediate water tank (8); the HRAS reactor (2) is provided with a first stirrer (2.1), a first aeration head (2.2) and a sedimentation tank (2.3); the short-cut nitrification reactor (3) is provided with an air pump (3.1), a second aeration head (3.2), a first water inlet (3.3), a first water discharge port (3.4), a second water inlet pump (3.5), a second stirrer (3.6) and a first sampling port (3.7); the anaerobic ammonia oxidation reactor (5) is provided with a second water inlet (5.1), a first backflow port (5.2), a first backflow pump (5.3), a second water outlet (5.4), an exhaust port (5.5), a gas collection bag (5.6), a three-phase separator (5.7), a first vent pipe (5.8), a second sampling port (5.9), a third water inlet pump (5.10) and a fourth water inlet pump (5.11); the short-range denitrification reactor (7) is provided with a third water inlet (7.1), a fourth water inlet (7.2), a third water outlet (7.3), a third stirrer (7.4), a third sampling port (7.5), a fifth water inlet pump (7.6), a sixth water inlet pump (7.7), a seventh water inlet pump (7.8) and an eighth water inlet pump (7.9);
the raw water tank (1) is connected with the HRAS reactor (2) through a first water inlet pump (1.1), a sedimentation tank (2.3) of the HRAS reactor (2) is connected with a first water inlet (3.3) of the shortcut nitrification reactor (3) through a second water inlet pump (3.5), a first intermediate water tank (4) is connected with a second water inlet (5.1) of the anaerobic ammoxidation reactor (5) through a third water inlet pump (5.10), a third intermediate water tank (8) is connected with the second water inlet (5.1) of the anaerobic ammoxidation reactor (5) through a fourth water inlet pump (5.11), a second intermediate water tank (6) is connected with a fourth water inlet (7.2) of the shortcut denitrification reactor (7) through an eighth water inlet pump (7.9), the raw water tank (1) is connected with a third water inlet (7.1) of the shortcut denitrification reactor (7) through a fifth water inlet pump (7.6), and the HRAS reactor (2) is connected with a sixth water inlet (7.7) of the shortcut denitrification reactor (7.1) through a third water inlet pump (7.6).
2. The method for carrying out the three-stage anaerobic ammonia oxidation and high-efficiency denitrification on the municipal sewage by using the system of claim 1 is characterized by comprising the following steps of:
(1) introducing the municipal sewage into an HRAS reactor, controlling the dissolved oxygen concentration of 1.0-4.0mg/L, the sludge concentration MLSS of 1.5-4.0g/L, the hydraulic retention time of 20-60 minutes and the sludge retention time of 0.5-4 days in the running process of the HRAS reactor;
(2) pumping effluent of the HRAS reactor into a short-cut nitrification reactor, and controlling the sludge concentration MLSS to be 1.0-4.0g/L, the biofilm carrier filling volume ratio to be 20-60% and the dissolved oxygen concentration to be 0.2-1.0mg/L in the running process of the short-cut nitrification reactor;
(3) pumping the effluent of the partial nitrification reactor into an anaerobic ammonia oxidation reactor, controlling the concentration MLSS of the granular sludge in the running process of the anaerobic ammonia oxidation reactor to be 5.0-20.0g/L, and controlling the NO of the effluent 2 - -N concentration less than 1.0 mg/L;
(4) pumping the effluent of the anaerobic ammonia oxidation reactor, the urban sewage and the effluent of the HRAS reactor into a short-cut denitrification reactor, controlling the concentration MLSS of the granular sludge in the running process of the short-cut denitrification reactor to be 3.0-10.0g/L, the retention time of the sludge to be 3-10 days, the retention time of the water power to be 5-20 minutes, mixing COD and NO in the influent of the short-cut denitrification reactor 3 - A mass concentration ratio of-N of 2.5 to 5.0, NO 3 - -N and NH 4 + The mass concentration ratio of-N is 1.2-2.0, and the NO in the effluent of the short-cut denitrification reactor 3 - -N concentration less than 2.0 mg/L;
(5) the effluent of the partial denitrification reactor flows back to the anaerobic ammonia oxidation reactor, the reflux ratio is controlled to be 100-300%, and the effluent NH of the anaerobic ammonia oxidation reactor 4 + -N concentration less than 3.0mg/L, NO 3 - -N concentration less than 8.0 mg/L;
when the concentration of the dissolved organic matters in the effluent of the HRAS reactor in the operation process of the step (1) is more than 50mg/L, the concentration of the dissolved oxygen in the HRAS reactor is increased within the range of 1.0-4.0mg/L or the hydraulic retention time of the HRAS reactor is prolonged within the range of 20-60 minutes until the concentration of the dissolved organic matters in the effluent of the HRAS reactor is less than or equal to 50 mg/L;
the biomembrane carrier in the step (2) is a polypropylene hollow ring, and the NO discharged from the shortcut nitrification reactor in the operation process 2 - -N and NH 4 + The mass concentration ratio of-N to N is 1.0-1.8, if NO is discharged from the short distance nitration reactor 2 - -N and NH 4 + If the mass concentration ratio of N is less than 1.0, the content of dissolved oxygen in the short-cut nitrification reactor is increased within the range of 0.2-1.0mg/L until the ratio is more than or equal to 1.0; if the water outlet NO of the short-cut nitrification reactor is discharged 2 - -N and NH 4 + When the mass concentration ratio of-N is more than 1.8, the content of dissolved oxygen in the short-cut nitrification reactor is reduced within the range of 0.2-1.0mg/L until the ratio is less than or equal to1.8；
The effluent NO of the anaerobic ammonia oxidation reactor in the operation process of the step (3) 2 - When the N concentration is more than or equal to 1.0mg/L, prolonging the hydraulic retention time until the effluent NO 2 - -N concentration less than 1.0 mg/L;
the step (4) of operating the process control short-cut denitrification NO 3 - -N to NO 2 - The conversion rate of-N is more than 50 percent, COD and NO are mixed in the influent water 3 - When the mass concentration ratio of-N is more than 5.0, introducing HRAS reactor effluent to adjust until COD and NO in the short-range denitrification reactor 3 - -the ratio of the mass concentration of N is 5.0 or less;
the water NO discharged from the short-cut denitrification reactor in the operation process of the step (4) 3 - The concentration of N is more than or equal to 2.0mg/L, and COD and NO are improved within the range of 2.5 to 5.0 3 - -a ratio of N mass concentrations;
the MLSS concentration of the mixed liquid of the effluent of the short-cut denitrification reactor in the operation process of the step (4) is controlled to be less than 100 mg/L;
the effluent NH of the anaerobic ammonia oxidation reactor in the operation process of the step (5) 4 + When the N concentration is more than or equal to 3.0mg/L, the NO content in the mixed feed water of the short-cut denitrification reactor is increased within the range of 1.2-2.0 3 - -N and NH 4 + Mass concentration ratio of-N to effluent NH of anaerobic ammoxidation reactor 4 + -N concentration less than 3.0 mg/L;
the effluent NO of the anaerobic ammonia oxidation reactor in the operation process of the step (5) 3 - When the concentration of N is more than or equal to 8.0mg/L, the reflux ratio of the effluent of the anaerobic ammonia oxidation reactor is increased within the range of 100-300 percent until the effluent NO of the anaerobic ammonia oxidation reactor is 3 - -N concentration less than 8.0 mg/L.
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| CN110709357A (en) * | 2017-03-30 | 2020-01-17 | 昆士兰大学 | Sludge treatment method |
| CN113767073A (en) * | 2019-05-24 | 2021-12-07 | 昆士兰大学 | Method for treating waste water or sludge |
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| CN110709357A (en) * | 2017-03-30 | 2020-01-17 | 昆士兰大学 | Sludge treatment method |
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