CN114590887A - Low-consumption biological denitrification device and method for source separation urine sewage treatment - Google Patents
Low-consumption biological denitrification device and method for source separation urine sewage treatment Download PDFInfo
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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
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- 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
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/20—Activated sludge processes using diffusers
- C02F3/201—Perforated, resilient plastic diffusers, e.g. membranes, sheets, foils, tubes, hoses
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/20—Total organic carbon [TOC]
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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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- Water Supply & Treatment (AREA)
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- Separation Using Semi-Permeable Membranes (AREA)
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Abstract
A low-consumption biological denitrification device and method for source separation urine sewage treatment, through adopting the aeration membrane of hydrophobic micropore as the biomembrane growth substrate, on the one hand realize the anchorage growth of microorganism, has reduced the output of the mud; on the other hand, the separation of oxygen and organic matters is realized through a bottom gas supply mode, the competition of autotrophic nitrifying bacteria and heterotrophic bacteria is weakened, and the formation of different functional areas in a single reactor is facilitated; connecting a membrane aeration biomembrane reactor device with a gas path, immersing the membrane aeration biomembrane reactor device into a reaction tank, and then inoculating aerobic activated sludge; in the operation stage, sewage enters the reaction tank in a continuous or intermittent mode, the continuous operation of aeration is kept, the full mixing of water in the reaction tank is kept through a submersible pump, the stable operation of the reactor can be kept for a long time by the process method, the TOC removal rate can reach 93-98%, the total nitrogen removal rate can reach 56-85% during the operation period, and the turbidity of effluent is lower than 10 NTU.
Description
Technical Field
The invention relates to the field of sewage treatment, in particular to a urine sewage biological denitrification device and a method.
Background
The invention relates to a biological treatment method for urine sewage, which can efficiently realize organic matter degradation and biological denitrification under the condition of no external carbon source and is beneficial to realizing the shunt treatment of domestic sewage, thereby reducing the total cost of the whole process of the domestic sewage treatment.
With the social development, people's consciousness on protecting ecological environment is remarkably improved, so pollutants generated in industrial production and daily life need to be effectively treated in time. The main pollutants of the municipal sewage comprise organic matters, nitrogen, phosphorus and other inorganic nutritional ingredients. Since the last century, eutrophication of water body caused by excessive residual nutrient content has occurred many times worldwide, and the normal life of people in a large area is seriously affected in a period of time, so the current policy has strict requirements on the related indexes of nitrogen and phosphorus in the sewage treatment effluent. In the mainstream process route (AAO process), nitrogen is converted into nitrogen through a nitrification-denitrification process to achieve harmless treatment and is separated from a water body, wherein the denitrification process is mostly completed by heterotrophic microorganisms, and the nitrogen conversion process is accompanied with consumption of a carbon source. However, in reality, carbon-nitrogen ratio in municipal sewage in China is generally lower, and denitrification efficiency by means of carbon sources contained in the sewage is very low, so that in most cases, additional carbon sources (methanol, sodium acetate and the like) need to be added to promote a denitrification process so as to enable the effluent quality to reach the standard, and the operation cost is difficult to reduce. To solve this problem, one direction is to improve the current process and increase the utilization rate of carbon source. The other direction is to improve the whole process of domestic sewage treatment, and treat the sewage from different sources respectively according to the pollution degree, so as to avoid the whole cost rise caused by cross pollution. The starting points of the two directions are different, and the derived developing technologies can complement each other to form an optimal solution.
From the long-term perspective, the whole process of domestic sewage treatment is improved, and sewage is subjected to split-flow treatment according to sources, so that the method is more suitable for the development direction of the society. With the increase of population mobility, the population density of large cities will further increase in the future, and the large cities are limited by land use, energy consumption and the like, and the daily treatment capacity still has an upper limit by only improving the operating efficiency of the centralized sewage treatment facility, and may not cope with a large amount of actually generated sewage. And adopt the reposition of redundant personnel to handle then can reduce domestic sewage's denitrogenation load by a very big degree, its reason lies in: the inorganic nutrient substances in the domestic sewage mainly come from urine, the nitrogen content of the inorganic nutrient substances can reach 8000mg/L, more than 70% of nitrogen in the domestic sewage is contributed, and meanwhile, the volume of the inorganic nutrient substances only accounts for 1-2% of the total volume of the domestic sewage. The urine-containing domestic sewage can be treated in a shunting manner, so that the integral pollution degree of the sewage entering a sewage pipe network can be greatly reduced, the treatment capacity of a sewage treatment plant is improved, and the running cost of the sewage treatment plant is reduced.
The key to realize the split-flow treatment of the domestic sewage lies in the development of a denitrification technology suitable for treating urine sewage. There are many current techniques for treating urine wastewater, including but not limited to: physical methods such as ammonia stripping and adsorption; molecular sieve adsorption, adding magnesium salt to generate struvite precipitate, electrochemical method and other chemical methods; and a biological treatment method. When denitrification is taken as a target, additional materials (an adsorbent, a chemical reaction reagent and the like) are required to be continuously added for denitrification by a physical and chemical method, and the operation cost is far higher than that of a biological method. As mentioned earlier, the biological pathway that is less depleted in carbon source is the more desirable pathway. In recent years, some technologies have been developed to reduce the material consumption in the biological denitrification process, such as the short-cut nitrification process by using the short-cut nitrification process and the anaerobic ammonia oxidation process by using the autotrophic SHARON-Annamox, so that the carbon source consumption in the denitrification process is reduced. We believe that the membrane-aerated biofilm reactor (MABR) process is also a promising route and explores its ability to treat urine wastewater.
Disclosure of Invention
The purpose of the invention is as follows: the urine sewage is treated by utilizing the activated sludge obtained by gradually domesticating the inlet water concentration through gradient rise, and the biological denitrification is realized by combining the MABR process with less occupied space and low energy and material consumption, so that the flow-dividing treatment of the domestic sewage is facilitated, and the integral operation cost of a sewage treatment system is reduced.
The technical scheme of the invention is as follows:
1) the membrane-aerated biofilm reactor device shown in the attached figure 1 is manufactured, and the main components of the membrane-aerated biofilm reactor device comprise: the device comprises an air inlet, an air outlet, an air chamber for stabilizing air flow in and out, a sealing end for communicating an air supply membrane wire with the air chamber and ensuring air tightness, and a supporting rod for connecting the two air chambers to play a role of structural support, wherein the device is wholly immersed in a reaction tank during working, the membrane wire is a biomembrane attachment growth part, air or oxygen can be supplied from the air inlet by a gas pump, a gas cylinder and the like, and the internal pressure of the device is adjusted by controlling the opening degree of the air outlet; the air supply firstly enters the air chamber, and the air flow is redistributed to the air supply membrane wire after being stabilized. The air chamber shell is made of acrylic plastic, and the sealing end is sealed through hot melt adhesive. The air supply membrane wire is a hydrophobic hollow fiber ultrafiltration membrane, the material is polyvinylidene fluoride (PVDF) or Polytetrafluoroethylene (PTFE), and the bubble point air pressure is not lower than 20 kPa; the device has a specific surface area (ratio of the total surface area of the hollow membrane filaments to the volume of space occupied by the device) of 50-150m2/m3The spacing between the air supply membrane filaments should be kept 3-5mm to ensure the uniformity of spatial distribution and avoid hindering the growth of the biological membrane. The support rod is made of ABS plastic and used for supporting the stability of the device and is not corroded.
2) Connecting a membrane aeration biomembrane reactor device with a gas path, immersing the membrane aeration biomembrane reactor device into a reaction tank, and then inoculating activated sludge; acclimating sludge with diluted urine sewage by gradually reducing urine sewageAnd (5) completing the acclimatization process by dilution times. Diluting urine sewage to the total nitrogen concentration of 50-100mg/L as inlet water in the initial domestication stage, wherein the hydraulic retention time is about 2 days; after each 5-8 hydraulic retention time, the ammonia nitrogen concentration can be increased by 1.5-2 times, and the water inlet speed is properly adjusted, so that the total nitrogen load of inlet water is not more than 150mg L-1d-1(ii) a Finally, the undiluted urine sewage is directly used.
3) And in the operation stage, urine sewage is continuously conveyed into the reaction tank through the water pump. The urine sewage contains sanitary wastewater and urine, the sanitary wastewater is prepared from cleaning products and tap water, the cleaning products comprise toothpaste, hand cleanser, shower gel, shampoo, face cleanser and laundry detergent, and the total concentration of the cleaning products is about 0.65 g/L; urine volume fraction can reach 40%. Adjusting the water inlet rate to ensure that the total nitrogen load of the inlet water is 100-150mg L-1d-1And (3) a range.
4) Sewage enters the reaction tank in a continuous or intermittent mode, continuous work of aeration is kept, air enters the reaction tank in a mode of a submersible pump or an external circulating pump and keeps full mixing of water in the reaction tank, and a stable pH value in the tank is kept by adding alkaline substances. During operation, the TOC removal rate can reach 93-98%, the total nitrogen removal rate can reach 56-85%, and the effluent turbidity is lower than 10 NTU.
Compared with the prior art, the invention has the beneficial effects that: (1) the urine sewage containing high-concentration ammonia nitrogen is directly treated by a planned sludge acclimation process and an MABR process, the TOC removal rate can reach 93-98% and the total nitrogen removal rate can reach 56-85% during operation, and external carbon sources are not required to be added at all. (2) The treatment can be carried out in a single-stage reactor, and the process has low space requirement. (3) The microorganism fixation growth is realized through a biomembrane technology, the suspended solid concentration and the sludge yield are reduced, and the effluent turbidity is lower than 10NTU in the operation process; (4) the aeration membrane is utilized to realize bubble-free aeration, the oxygen conveying efficiency is improved, and the air input required by the aeration membrane per unit area is only about 1.5-3L/(min m & m)2) And a large amount of aeration energy consumption can be saved.
Drawings
FIG. 1 is a schematic view of a membrane-aeration biofilm reactor apparatus
1. An air inlet; 2, an air outlet; 3 is an air cavity; 4, sealing the end of the air chamber; 5 is an aeration membrane yarn; and 6 is a support rod.
FIG. 2 is a schematic view of a denitrification process for urine wastewater
Detailed Description
The MABR process adopts a hydrophobic microporous aeration membrane as a biological membrane growth substrate, promotes the fixation growth of microorganisms and realizes the separation of functional areas, namely the interior of the biological membrane is close to an air supply position to form an aerobic area; the dissolved oxygen outside the biological membrane is lower, and an anoxic zone is formed, so that the denitrification can be realized in a single reactor. Compared with the traditional process, the MABR process has the advantages that the aerobic zone is far away from external pollutants, the microenvironment is beneficial to the growth of autotrophic nitrifying bacteria, and the pollutants firstly contact the anoxic zone and are beneficial to the denitrifying bacteria to carry out the denitrifying process, so that the utilization rate of a carbon source is improved. The non-bubble aeration can be realized through the microporous aeration membrane, the utilization efficiency of the biological membrane to oxygen is improved, and the aeration energy consumption is reduced. Compared with the processes of short-cut nitrification-denitrification and SHARON-Annamox, the MABR process is characterized in that: (1) the processes of short-cut nitrification-denitrification and SHARON-Annamox at least need two independent reaction areas to respectively provide a high dissolved oxygen environment and a low dissolved oxygen environment, while the MABR process only needs one reaction area to realize function differentiation through an asymmetric biological membrane; (2) the MABR process utilizes a fixed substrate to realize the fixation growth of microorganisms, can reduce the sludge yield and further reduce the cost generated by sludge treatment. Therefore, the MABR process can be complementary with the prior art, and a larger process selection range is provided for different use scenes.
The following examples are given to illustrate the technical solution of the present invention.
Example 1
A membrane area of 0.94m was prepared2MABR device with volume of 10.8L is arranged in a reaction tank with effective volume of 22L. Urine sewage with the pH value of about 9.0, the TOC of about 280mg/L and the total nitrogen of about 450mg/L is prepared by real urine and a cleaning agent. The sewage continuously enters the reaction tank through a peristaltic pump, and the retention time is 3 days. An air inlet pump is adopted to provide air for the device, the air supply pressure is about 5.5kPa, and the air inlet quantity is aboutIs 1.5L/min. Monitoring data of a stable operation period of 28 days show that the pH value of effluent of the system is 6.0-8.0, the average value of TOC is about 20mg/L, the average value of ammonia nitrogen is about 95mg/L, the turbidity of effluent is lower than 10NTU, about 93 percent of TOC removal rate and about 62 percent of total nitrogen removal rate are realized, and a specific flow is shown in figure 2.
Example 2
A membrane area of 0.94m was prepared2MABR device with volume of 10.8L is arranged in a reaction tank with effective volume of 22L. Urine sewage with the pH value of about 9.0, the TOC of about 383mg/L and the total nitrogen of about 610mg/L is prepared by real urine and a cleaning agent. The sewage continuously enters the reaction tank through a peristaltic pump, and the retention time is 4 days. An air inlet pump is adopted to provide air for the device, the air supply pressure is about 5kPa, and the air inlet quantity is about 1.5L/min. Monitoring data of a stable operation period of 30 days show that the pH value of effluent of the system is 7.0-8.0, the average value of TOC is about 27mg/L, the average value of total nitrogen is about 267mg/L, the turbidity of the effluent is lower than 10NTU, and the TOC removal rate of about 93 percent and the total nitrogen removal rate of about 58 percent are realized.
Example 3
A membrane area of 0.94m was prepared2MABR device with volume of 10.8L is arranged in a reaction tank with effective volume of 22L. Urine wastewater with a pH value of about 9.0, a TOC of about 1416mg/L and a total nitrogen of about 2292mg/L is prepared by mixing real urine and a cleaning agent. The sewage continuously enters the reaction tank through a peristaltic pump, and the retention time is 15 days. An air inlet pump is adopted to provide air for the device, the air supply pressure is about 4kPa, and the air inlet quantity is about 2.5L/min. Monitoring data in a stable operation period of 30 days show that the pH value of effluent of the system is 7.0-8.0, the average value of TOC is about 33mg/L, the average value of total nitrogen is about 353mg/L, the turbidity of the effluent is lower than 10NTU, and about 98% of TOC removal rate and about 85% of total nitrogen removal rate are realized.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (8)
1. A membrane-aeration biofilm reactor device is characterized in that the main components comprise: the device comprises an air inlet (1), an air outlet (2), an air chamber (3) for stabilizing air flow in and out, a sealing end (4) for communicating an air supply membrane wire (5) with the air chamber (3) and ensuring air tightness, and a support rod (6) for connecting the air chambers at two sides to play a role of structural support, wherein the device is wholly immersed in a reaction tank during working, the membrane wire (5) is a biological membrane attachment growth part, air or oxygen can be supplied from the air inlet (1) through an air pump, an air bottle and the like, and the internal pressure of the device is adjusted by controlling the opening degree of the air outlet (2); air supply firstly enters the air chamber (3), and the air flow is redistributed to the air supply membrane filaments (5) after being stabilized.
2. A membrane-aerated biofilm reactor device according to claim 1, characterized in that the housing of the air chamber (3) is acrylic plastic and the end-caps (4) are sealed by hot melt adhesive.
3. A membrane-aerated biofilm reactor apparatus according to claim 1 or 2, wherein the gas feed membrane filaments (5) are hydrophobic hollow fibre ultrafiltration membranes made of polyvinylidene fluoride (PVDF) or Polytetrafluoroethylene (PTFE) and have a bubble point pressure of not less than 20 kPa; the uniformity of spatial distribution among the air supply membrane filaments (5) is ensured and the growth of the biological membrane is prevented from being blocked.
4. A membrane-aerated biofilm reactor device according to claim 1, characterized in that the support rods (6) are made of ABS plastic for stability of the support device and corrosion resistance.
5. A low-consumption biological denitrification method for source separation urine sewage treatment is characterized by comprising the following steps:
(1) preparing the membrane-aerated biofilm reactor device of claim 1;
(2) connecting a membrane aeration biomembrane reactor device with a gas path, immersing the membrane aeration biomembrane reactor device into a reaction tank, and then inoculating activated sludge; domesticating the sludge by using the diluted urine sewage, finishing the domestication process by gradually increasing the volume fraction of the urine sewage, and finally directly using the undiluted urine sewage;
(3) in the operation stage, urine sewage is continuously conveyed into the reaction tank through a water pump; the urine sewage contains sanitary wastewater and urine, the sanitary wastewater is prepared from cleaning products and tap water, and the cleaning products comprise toothpaste, hand cleanser, shower gel, shampoo, face cleanser and laundry detergent;
(4) sewage enters the reaction tank in a continuous or intermittent mode, continuous work of aeration is kept, air enters the reaction tank in a mode of a submersible pump or an external circulating pump and keeps full mixing of water in the reaction tank, and a stable pH value in the tank is kept by adding alkaline substances.
6. The efficient biological nitrification method for source separation of urine wastewater according to claim 5, wherein the reaction tank of the step 4 is adjusted by acid and alkali to maintain the pH value in the stable range during the operation period, and the added alkaline substance is sodium bicarbonate.
7. The efficient biological nitrification process for source separation of urine sewage of claim 5, wherein in step 4, air is pumped into the apparatus by an air intake pump submersible pump or an external circulation pump.
8. The efficient biological nitrification process for source separation of urine wastewater according to claim 5, wherein the inoculated sludge is secondary sedimentation tank return sludge.
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