CN115072860B - 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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- CN115072860B CN115072860B CN202210720933.2A CN202210720933A CN115072860B CN 115072860 B CN115072860 B CN 115072860B CN 202210720933 A CN202210720933 A CN 202210720933A CN 115072860 B CN115072860 B CN 115072860B
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 114
- 238000000034 method Methods 0.000 title claims abstract description 63
- 230000003647 oxidation Effects 0.000 title claims abstract description 59
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 59
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 57
- 239000010865 sewage Substances 0.000 title claims abstract description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 140
- 102100029974 GTPase HRas Human genes 0.000 claims abstract description 43
- 101000584633 Homo sapiens GTPase HRas Proteins 0.000 claims abstract description 43
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 24
- 239000010802 sludge Substances 0.000 claims abstract description 21
- 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
- 238000010992 reflux Methods 0.000 claims description 12
- 238000005070 sampling Methods 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000005086 pumping Methods 0.000 claims description 8
- 238000005273 aeration Methods 0.000 claims description 6
- 238000004062 sedimentation Methods 0.000 claims description 6
- 230000002035 prolonged effect Effects 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 3
- 239000004743 Polypropylene Substances 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims description 2
- 239000011259 mixed solution Substances 0.000 claims description 2
- -1 polypropylene Polymers 0.000 claims description 2
- 229920001155 polypropylene Polymers 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 24
- 238000005516 engineering process Methods 0.000 description 7
- 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
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000006396 nitration reaction Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000004886 process control 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
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
- C02F3/006—Regulation methods for 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
- C02F3/302—Nitrification and denitrification 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
- C02F3/302—Nitrification and denitrification treatment
- C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- 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
-
- 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
Abstract
A three-section urban sewage anaerobic ammonia oxidation high-efficiency denitrification system and method belong to sewageThe technical field of water biological treatment. The urban sewage sequentially passes through an HRAS unit, a short-cut nitrification unit and an anaerobic ammonia oxidation unit, and organic matters contained in the urban sewage are converted into sludge and partial NH 4 + Oxidation of N to NO 2 ‑ N and removing part of the nitrogen in the short-cut nitrified effluent. Containing excessive NO 3 ‑ The effluent of the anaerobic ammonia oxidation unit of-N enters a short-range denitrification unit, and NO is generated by utilizing organic matters in the urban sewage flowing in from the side 3 ‑ Reduction of N to NO 2 ‑ -N, the effluent of which flows back to the anaerobic ammonia oxidation unit to produce NO 2 ‑ N and NH in side-flowing municipal sewage 4 + -N is further removed. The invention solves the problems of low denitrification efficiency and NO when urban sewage is treated by the current short-cut nitrification-anaerobic ammonia oxidation process 3 ‑ The problem of high N concentration is solved, a short-cut nitrification unit does not need a complex control process in the operation process, and the operation and the management are easy.
Description
Technical field:
the invention relates to a three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification system and method, belonging to the technical field of sewage biological treatment.
The background technology is as follows:
the removal of nitrogen has become one of the key problems in the water treatment field of China. In the traditional denitrification technology, sewage is required to be subjected to NH under the action of aerobic nitrification 4 + Conversion of N to NO 3 - -N. Then denitrification is carried out under the anoxic condition, and nitrogen in the wastewater is finally converted into N 2 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, additional carbon source, high energy consumption, high cost and the like. There is therefore an urgent need to find new and efficient denitrification techniques.
In recent years, anaerobic ammonia oxidation technology has become a research hot spot for sewage treatment, wherein anaerobic ammonia oxidation refers to NH under anoxic conditions 4 + -N and NO 2 - Direct conversion of N to N 2 Is a process of (2). Compared with the traditional denitrification technology, the method has the advantages of low energy consumption, low organic carbon source utilization amount, low sludge yield and the like, and can achieve the purposes of economy and high efficiency in the aspect of wastewater treatment. But the main form of nitrogen in urban domestic sewage is NH 4 + N, which does not meet the requirements of anaerobic ammoxidation. At present, stable NO is provided for anaerobic ammonia oxidation by short-cut nitrification technology 2 - -N, short-cut nitrification-anaerobic ammoxidation (partial nitrification anammox, PN/a) process. However, when the short-cut nitrification-anaerobic ammoxidation process is applied to the mainstream wastewater treatment engineering, the short-cut nitrification process is difficult to control due to frequent changes of environmental conditions and sewage quality, and the effluent often contains a large amount of NO 3 - -N generation. On the other hand, anaerobic ammonia oxidation denitrification process also produces a certain amount of NO 3 - N, 10% -12% of the total nitrogen removed, which further increases the effluent NO 3 - -concentration of N. Therefore, the current main stream short-cut nitrification-process effluent often needs further treatment to meet the total nitrogen emission requirement of the effluent.
Short-cut denitrification (Partial denitrification, PD) can remove NO from water 3 - Stable and efficient conversion of N to NO 2 - -N. Thus, by following the short-cut nitrification-anaerobic ammonia oxidation process with short-cut denitrification, NO is produced therefrom 3 - Conversion of N to NO 2 - And N is returned 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 running cost is greatly reduced.
The invention comprises the following steps:
the invention provides a three-stage urban sewage anaerobic ammonia oxidation high-efficiency denitrification system and method, in particular to a method that urban sewage sequentially passes through an HRAS unit, a short-range denitrification unit and an anaerobic ammonia oxidation unit to convert organic matters contained in the urban sewage into sludge and partial NH 4 + Oxidation of N to NO 2 - N and removing part of the nitrogen in the effluent of the short-cut nitrification reactor. Containing excessive NO 3 - The effluent of the anaerobic ammonia oxidation reactor of-N enters a short-range denitrification reactor, and NO is generated by utilizing organic matters in the urban sewage flowing in from the side 3 - Reduction of N to NO 2 - -N, the effluent of which flows back to the anaerobic ammoxidation reactor to produce NO 2 - N and side-stream municipal sewageNH of (C) 4 + And (3) further removing N, and optimizing the water inflow of the short-cut denitrification reactor to realize the high-efficiency denitrification of the anaerobic ammoxidation of the urban sewage.
The aim of the invention is achieved by the following technical proposal
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 ammoxidation reactor (5) is provided with a second water inlet (5.1), a first reflux port (5.2), a first reflux pump (5.3), a second water outlet (5.4), an exhaust port (5.5), a gas collecting bag (5.6), a three-phase separator (5.7), a first blow-down 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 primary 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 short-range denitrification reactor (3) through a second water inlet pump (3.5), a first middle 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 middle water tank (8) is connected with a second water inlet (5.1) of the anaerobic ammonia oxidation reactor (5) through a fourth water inlet pump (5.11), a second middle water tank (6) is connected with a fourth water inlet (7.2) of the short-range denitrification reactor (7) through an eighth water inlet pump (7.9), the primary water tank (1) is connected with a third water inlet (7.1) of the short-range denitrification reactor (7) through a fifth water inlet pump (7.6), and the HRAS reactor (2) is connected with the third water inlet (7.1) of the short-range denitrification reactor (7) through a sixth water inlet pump (7.7).
The method is characterized by comprising the following steps of:
(1) Introducing urban sewage into an HRAS reactor, controlling the dissolved oxygen concentration in the operation process of the HRAS reactor to be 1.0-4.0mg/L, the sludge concentration MLSS to be 1.5-4.0g/L, the hydraulic retention time to be 20-60 minutes, and the sludge retention time to be 0.5-4 days;
(2) Pumping the HRAS reactor effluent into a short-cut nitrification reactor, controlling the sludge concentration MLSS in the operation process of the short-cut nitrification reactor 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;
(3) Pumping water from the short-cut nitrification reactor into an anaerobic ammonia oxidation reactor, controlling the granular sludge concentration MLSS in the running process of the anaerobic ammonia oxidation reactor to be 5.0-20.0g/L, and discharging water NO 2 - -N concentration less than 1.0mg/L;
(4) Pumping the effluent of the anaerobic ammoxidation reactor and the urban sewage as well as the effluent of the HRAS reactor into a short-cut denitrification reactor, controlling the granular sludge concentration MLSS in the operation process of the short-cut denitrification reactor to be 3.0-10.0g/L, the sludge retention time to be 3-10 days, the hydraulic retention time to be 5-20 minutes, and mixing COD and NO in the inflow water of the short-cut denitrification reactor 3 - -N mass concentration ratio of 2.5-5.0, NO 3 - -N and NH 4 + The ratio of the mass concentration of the-N is 1.2-2.0, and the effluent NO of the short-cut denitrification reactor 3 - -N concentration less than 2.0mg/L;
(5) Reflux of effluent from the short-cut denitrification reactor to the anaerobic ammonia oxidation reactor, and control of reflux ratio to 100% -300% and NH of effluent from the anaerobic ammonia oxidation reactor 4 + -N concentration less than 3.0mg/L, NO 3 - The N concentration is less than 8.0mg/L.
When the concentration of the dissolved organic matters in the water discharged from the HRAS reactor in the operation process of the step (1) is more than 50mg/L, the dissolved oxygen concentration of 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 water discharged from the HRAS reactor is less than or equal to 50mg/L;
the step (2) of biological filmThe carrier is polypropylene hollow ring light filler, and the effluent NO of the short-cut nitration reactor in the operation process 2 - -N and NH 4 + The mass concentration ratio of the N is 1.0 to 1.8, if the effluent NO of the short-cut nitrification reactor 2 - -N and NH 4 + And (3) increasing the dissolved oxygen content in the short-cut nitrification reactor within the range of 0.2-1.0mg/L until the ratio is more than or equal to 1.0 when the mass concentration ratio of N is less than 1.0. If the short-cut nitrification reactor is discharged with NO 2 - -N and NH 4 + And (3) reducing the dissolved oxygen content in the short-cut nitrification reactor within the range of 0.2-1.0mg/L until the ratio is less than or equal to 1.8 when the mass concentration ratio of N is more than 1.8.
The anaerobic ammonia oxidation reactor effluent NO in the operation process of the step (3) 2 - When the concentration of N is more than or equal to 1.0mg/L, the hydraulic retention time is prolonged until the water NO is discharged 2 - -N concentration less than 1.0mg/L;
the operation process of the step (4) controls short-range denitrification NO 3 - -N to NO 2 - The conversion rate of the-N is above 50%, and COD and NO in the mixed water are mixed 3 - When the mass concentration ratio of the-N is more than 5.0, introducing the water discharged from the HRAS reactor to adjust until the COD and the NO in the short-range denitrification reactor 3 - -the ratio of the mass concentration of N is less than or equal to 5.0;
the short-cut denitrification reactor effluent NO in the operation process of the step (4) 3 - The concentration of the-N is more than or equal to 2.0mg/L, and the COD and the NO are improved within the range of 2.5-5.0 3 - -ratio of N mass concentration;
the suspended solid concentration MLSS of the effluent mixed solution of the short-cut denitrification reactor in the operation process of the step (4) is controlled to be less than 100mg/L;
the anaerobic ammonia oxidation reactor effluent NH in the operation process of the step (5) 4 + When the concentration of N is more than or equal to 3.0mg/L, the concentration of NO in the mixed water of the short-cut denitrification reactor is improved within the range of 1.2-2.0 3 - -N and NH 4 + -N mass concentration ratio up to NH of the effluent of the anaerobic ammoxidation reactor 4 + -N concentration less than 3.0mg/L;
said step (5)Anaerobic ammoxidation reactor effluent NO during operation 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 3 - The N concentration is less than 8.0mg/L.
The invention provides a three-section type urban sewage anaerobic ammonia oxidation high-efficiency denitrification system and a method, which have the following advantages and characteristics:
1) Combining short-cut nitrification and short-cut denitrification to make the substrate NO of anaerobic ammoxidation reaction 2 - The N is stably and efficiently supplied, the denitrification effect of the N is fully exerted, and the running 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 of the traditional short-cut nitrification-anaerobic ammonia oxidation process, and the total nitrogen concentration of the effluent can meet stricter emission standards through optimization, thereby promoting the multi-target recycling of urban sewage.
3) Short-cut nitrification of NO by a process system 2 - Low N accumulation rate requirement, NO realization without complex process control 2 - The efficient accumulation of N and 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 when the water quality condition changes.
4) Part of organic matters do not need to pass through the HRAS reactor, bypass the HRAS reactor and are directly used as denitrification carbon sources, so that the waste of the organic matters in the HRAS reactor is reduced, the organic matters in the municipal sewage are utilized in the short-cut denitrification process to provide electron donors, the use of external carbon sources is reduced, and the operation cost is saved.
Description of the drawings:
FIG. 1 is a process flow diagram of a three-stage urban sewage anaerobic ammonia oxidation high-efficiency denitrification system and method.
FIG. 2 is a nitrogen conversion diagram of the operation process of the three-stage urban sewage anaerobic ammonia oxidation high-efficiency denitrification system and method.
The specific embodiment is as follows:
the invention will be described in further detail with reference to the drawings and the detailed description
As shown in fig. 1, the three-stage urban sewage anaerobic ammonia oxidation high-efficiency denitrification system is characterized by comprising a raw water tank (1), an HRAS reactor (2), a short range nitration reactor (3), a first intermediate water tank (4), an anaerobic ammonia oxidation reactor (5), a second intermediate water tank (6), a short range 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 ammoxidation reactor (5) is provided with a second water inlet (5.1), a first reflux port (5.2), a first reflux pump (5.3), a second water outlet (5.4), an exhaust port (5.5), a gas collecting bag (5.6), a three-phase separator (5.7), a first blow-down 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 primary 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 short-range denitrification reactor (3) through a second water inlet pump (3.5), a first middle 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 middle water tank (8) is connected with a second water inlet (5.1) of the anaerobic ammonia oxidation reactor (5) through a fourth water inlet pump (5.11), a second middle water tank (6) is connected with a fourth water inlet (7.2) of the short-range denitrification reactor (7) through an eighth water inlet pump (7.9), the primary water tank (1) is connected with a third water inlet (7.1) of the short-range denitrification reactor (7) through a fifth water inlet pump (7.6), and the HRAS reactor (2) is connected with the third water inlet (7.1) of the short-range denitrification reactor (7) through a sixth water inlet pump (7.7).
The experimental water in the experimental example is urban sewage, and NH thereof 4 + The average concentration of N was 55.2mg/L and the average COD concentration was 330.5mg/L. Short-cut nitrification in experimentThe effective volume of the SBR reactor is 10L, 12 cycles are carried out per day, 4L of water is discharged per cycle, and the effective volume of the anaerobic ammonia oxidation UASB reactor is 5L; the effective volume of the short-range denitrification SBR reactor is 10L, 12 cycles per day, and 4.4L of water is discharged per cycle.
The specific operation process is as follows:
the daily water inflow of the HRAS reactor is 50L, the dissolved oxygen concentration of the HRAS reactor is 2.5mg/L under the condition that the sludge concentration MLSS is 3.0g/L, the hydraulic retention time is 40 minutes and the sludge retention time is 2 days, the water NH is discharged from the HRAS reactor 4 + The average value of N is 50.1mg/L, and the average value of COD is 35.3mg/L.
Pumping the HRAS reactor effluent (48L/d) into a short-cut nitrification reactor, and under the condition that the sludge concentration MLSS of the short-cut nitrification reactor is 2.5g/L, the biofilm carrier filling volume ratio is 40%, the dissolved oxygen concentration is 0.6mg/L and the hydraulic retention time is 3h, performing NH in the short-cut nitrification reactor effluent 4 + The average value of the N concentration is 10.3mg/L, NO 3 - The average value of the N concentration is 25.2mg/L, NO 2 - The average value of the N concentration is 15.1mg/L.
Pumping the effluent water of the short-cut nitrification reactor into an anaerobic ammonia oxidation reactor, and operating under the condition that the sludge concentration MLSS of the anaerobic ammonia oxidation reactor is 13.0g/L and the hydraulic retention time is 2.3h, wherein the effluent water NO 2 - The N concentration is always kept below 0.5mg/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 a short-cut denitrification reactor together, and 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, the effluent NO of the short-cut denitrification reactor 3 - The average value of the N concentration is 1.1mg/L, NO 2 - The mean value of the N concentration is 5.2mg/L.
The effluent of the short-cut denitrification reactor is totally refluxed into the anaerobic ammonia oxidation reactor, and effluent NH 4 + -N、NO 3 - The average value of the mass concentration of the N and TN is 0.3mg/L, 6.5mg/L and 8.1mg/L respectively, and the average removal rate of the total nitrogen of the inflow water in the operation process of the whole system is more than 85 percent.
The process technology for realizing the maximum anaerobic ammonia oxidation denitrification of the urban sewage is described in detail, and specific examples are applied to illustrate the principle and the implementation method of the invention, and the description of the above embodiments is only used for helping to understand the method and the core idea of the invention; variations in the detailed description will be to one skilled in the art that fairly fall within the scope of the invention, and therefore, this description is not to be taken as limiting.
Claims (1)
1. The three-section urban sewage anaerobic ammonia oxidation high-efficiency denitrification method is characterized in that a system used by the method comprises a raw water tank (1), an HRAS reactor (2), a short-range nitrification reactor (3), a first intermediate water tank (4), an anaerobic ammonia oxidation reactor (5), a second intermediate water tank (6), a short-range 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), and 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 ammoxidation reactor (5) is provided with a second water inlet (5.1), a first reflux port (5.2), a first reflux pump (5.3), a second water outlet (5.4), an exhaust port (5.5), a gas collecting bag (5.6), a three-phase separator (5.7), a first blow-down 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 primary 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 short-range denitrification reactor (3) through a second water inlet pump (3.5), a first middle 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 middle water tank (8) is connected with a second water inlet (5.1) of the anaerobic ammonia oxidation reactor (5) through a fourth water inlet pump (5.11), a second middle water tank (6) is connected with a fourth water inlet (7.2) of the short-range denitrification reactor (7) through an eighth water inlet pump (7.9), the primary water tank (1) is connected with a third water inlet (7.1) of the short-range denitrification reactor (7) through a fifth water inlet pump (7.6), and the HRAS reactor (2) is connected with the third water inlet (7.1) of the short-range denitrification reactor (7) through a sixth water inlet pump (7.7);
the method comprises the following steps:
(1) Introducing urban sewage into an HRAS reactor, controlling the dissolved oxygen concentration in the operation process of the HRAS reactor to be 1.0-4.0mg/L, the sludge concentration MLSS to be 1.5-4.0g/L, the hydraulic retention time to be 20-60 minutes and the sludge retention time to be 0.5-4 days;
(2) Pumping the HRAS reactor effluent into a short-cut nitrification reactor, controlling the sludge concentration MLSS in the operation process of the short-cut nitrification reactor 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;
(3) Pumping water from the short-cut nitrification reactor into an anaerobic ammonia oxidation reactor, controlling the granular sludge concentration MLSS in the running process of the anaerobic ammonia oxidation reactor to be 5.0-20.0g/L, and discharging water NO 2 - -N concentration less than 1.0mg/L;
(4) Pumping the effluent of the anaerobic ammoxidation reactor and the urban sewage as well as the effluent of the HRAS reactor into a short-cut denitrification reactor, controlling the granular sludge concentration MLSS to be 3.0-10.0g/L, the sludge retention time to be 3-10 days, the hydraulic retention time to be 5-20 minutes, and mixing COD and NO in the inflow water of the short-cut denitrification reactor 3 - -N mass concentration ratio of 2.5-5.0, NO 3 - -N and NH 4 + The ratio of the mass concentration of the-N is 1.2-2.0, and the effluent NO of the short-cut denitrification reactor 3 - -N concentration less than 2.0mg/L;
（5）reflux of effluent from the short-cut denitrification reactor to the anaerobic ammonia oxidation reactor, and control of reflux ratio to 100% -300% and NH of effluent from 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 water discharged from the HRAS reactor in the operation process of the step (1) is more than 50mg/L, the dissolved oxygen concentration of 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 water discharged from the HRAS reactor is less than or equal to 50mg/L;
the biomembrane carrier in the step (2) is a polypropylene hollow ring, and the effluent NO of the short-cut nitrification reactor is in the operation process 2 - -N and NH 4 + The mass concentration ratio of the N is 1.0 to 1.8, if the effluent NO of the short-cut nitrification reactor 2 - -N and NH 4 + The mass concentration ratio of N is less than 1.0, and 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 short-cut nitrification reactor is discharged with NO 2 - -N and NH 4 + -the ratio of the mass concentration of N is greater than 1.8, the dissolved oxygen content in the short-cut nitrification reactor is reduced in the range of 0.2-1.0mg/L until the ratio is less than or equal to 1.8;
the anaerobic ammonia oxidation reactor effluent NO in the operation process of the step (3) 2 - When the concentration of N is more than or equal to 1.0mg/L, the hydraulic retention time is prolonged until the water NO is discharged 2 - -N concentration less than 1.0mg/L;
the operation process of the step (4) controls short-range denitrification NO 3 - -N to NO 2 - The conversion rate of the-N is above 50%, and COD and NO in the mixed water are mixed 3 - When the mass concentration ratio of the-N is more than 5.0, introducing the water discharged from the HRAS reactor to adjust until the COD and the NO in the short-range denitrification reactor 3 - -the ratio of the mass concentration of N is less than or equal to 5.0;
the short-cut denitrification reactor effluent NO in the operation process of the step (4) 3 - The concentration of N is more than or equal to 2.0mg/L, and the COD and the NO are improved within the range of 2.5-5.0 3 - -ratio of N mass concentration;
the suspended solid concentration MLSS of the effluent mixed solution of the short-cut denitrification reactor in the operation process of the step (4) is controlled to be less than 100mg/L;
the anaerobic ammonia oxidation reactor effluent NH in the operation process of the step (5) 4 + When the concentration of N is more than or equal to 3.0mg/L, the concentration of NO in the mixed water of the short-cut denitrification reactor is improved within the range of 1.2-2.0 3 - -N and NH 4 + -N mass concentration ratio up to NH of the effluent of the anaerobic ammoxidation reactor 4 + -N concentration less than 3.0mg/L;
the anaerobic ammonia oxidation reactor effluent NO 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 3 - The N concentration is less than 8.0mg/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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