CN114835256A - Sewage treatment method and device - Google Patents
Sewage treatment method and device Download PDFInfo
- Publication number
- CN114835256A CN114835256A CN202210603619.6A CN202210603619A CN114835256A CN 114835256 A CN114835256 A CN 114835256A CN 202210603619 A CN202210603619 A CN 202210603619A CN 114835256 A CN114835256 A CN 114835256A
- Authority
- CN
- China
- Prior art keywords
- tank
- hollow fiber
- fiber membrane
- sewage treatment
- carbon source
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—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
- C02F3/02—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
- C02F3/28—Anaerobic digestion processes
- C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Microbiology (AREA)
- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a sewage treatment method and a sewage treatment device, and belongs to the technical field of sewage treatment. A sewage treatment device comprises an anaerobic tank, an anoxic tank and an aerobic tank which are connected in sequence; the anoxic tank comprises a waste hollow fiber membrane component. The waste hollow fiber membrane module introduced in the technical scheme effectively enriches hydrolytic zymophyte and denitrifying bacteria in the sewage treatment process, improves the denitrification efficiency and the process stability of the system, and reduces the consumption of carbon source required by sewage treatment, thereby successfully reutilizing the waste hollow fiber membrane which is difficult to treat, and relieving the reuse problem of the waste membrane module in the current urban sewage treatment plant; in addition, the technical scheme provided by the invention is suitable for sewage or wastewater with low carbon-nitrogen ratio such as urban domestic sewage, and can realize high-efficiency and stable removal of nitrogen in the sewage, so that the quality of the effluent is far lower than the national first-class A standard.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to a sewage treatment method and a sewage treatment device.
Background
The membrane separation technology plays a key role in the fields of water resources, energy, environment, chemical industry and the like in China. Under the great situation that the country strongly supports and the market demand is increased sharply, the film industry of China already enters a rapid growth period. Among them, Membrane Bioreactor (MBR) has become the most competitive technology in municipal sewage treatment industry as a new and efficient sewage treatment technology. By 2018, more than 200 MBR sewage/wastewater treatment projects with over ten thousand tons in scale are in operation in China, and the accumulated treatment capacity is less than 50 ten thousand m from 2007 3 (d) has proliferated to over 1400 km in 2018 3 /d。
The conventional MBR system mostly adopts a lining enhanced polyvinylidene fluoride (PVDF) hollow fiber composite membrane, and the average design service life is about 3 years. With the large scale operation of MBR systems, large amounts of waste membrane are produced each year. PVDF has extremely high stability, so that the PVDF is difficult to treat by adopting a conventional solid waste treatment method; and PVDF is F-containing polymer, so that serious environmental pollution problems can be caused by improper treatment. At present, the treatment and disposal of waste membrane materials are one of the important bottleneck problems in the water treatment industry in China.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a sewage treatment method and a sewage treatment device based on the in-situ utilization of a failure membrane material and overcoming the problem of treatment and disposal of waste membrane solid wastes.
In order to achieve the purpose, the invention adopts the technical scheme that: a sewage treatment device comprises an anaerobic tank 4, an anoxic tank 7 and an aerobic tank 16 which are connected in sequence; the anoxic tank 7 comprises a waste hollow fiber membrane component 8.
The waste hollow fiber membrane component 8 is introduced into the anoxic tank 7 in the sewage device, and can be used as a microbial filler to strengthen the denitrification performance of activated sludge in the sewage treatment process, so that the waste hollow fiber membrane difficult to treat is successfully reused, the ecological niche of a sludge system is enriched, and the utilization depth of microorganisms on organic matters difficult to degrade in sewage is enhanced; has obvious economic benefit and environmental benefit.
As a preferred embodiment of the device, the ratio of the surface area of the waste hollow fiber membrane module 8 to the volume of the anoxic tank 7 is 8-9m 2 /m 3 。
The surface area of the waste hollow fiber membrane 8 in the anoxic tank 7 can be adjusted according to the size and the water inflow of the tank body, and when the volume ratio of the surface area of the waste hollow fiber membrane 8 to the volume of the anoxic tank 7 is 8-9m 2 /m 3 When the method is used, a better sewage treatment effect can be obtained; if the ratio of the two is too small, the denitrifying bacteria cannot be enriched in sufficient quantity in the sewage treatment process, the sewage treatment effect and efficiency are reduced, and if the ratio of the two is too large, the introduced carbon source cannot be uniformly diffused, so that the efficiency is reduced and the cost is increased.
As a preferred embodiment of the device of the present invention, the waste hollow fiber membranes in the waste hollow fiber membrane module 8 include a lining reinforced polyvinylidene fluoride hollow fiber membrane, a polyether sulfone hollow fiber membrane, and a polysulfone hollow fiber membrane.
As a preferred embodiment of the device, the device further comprises a carbon source barrel 1, and the carbon source barrel 1 is connected with the anoxic tank 7 through a water suction pump 3.
The introduced carbon source barrel can provide enough energy for denitrifying bacteria, so that the activity of the denitrifying bacteria is improved, and the efficiency of sewage treatment is improved.
As a preferable embodiment of the device of the invention, a membrane module 12 and an aeration head 17 are arranged in the aerobic tank 16; the membrane module 12 is connected with a water outlet pump 15 through a connecting pipeline, and a vacuum pressure gauge 13 is arranged on the connecting pipeline; the aeration head 17 is positioned at the bottom of the aerobic tank 16 and is connected with the air pump 10 and the gas flowmeter 11 in sequence.
The provision of the vacuum pressure gauge 13 enables monitoring of contamination in the membrane module 12.
As a preferred embodiment of the device, the aerobic tank 16 is connected with the anoxic tank 7 and the anaerobic tank 4 through a reflux pump 14.
As a preferred embodiment of the device of the invention, the ratio of the surface area of the membrane module 12 to the volume of the aerobic tank 16 is 12.0-13.2m 2 /m 3 。
As a preferred embodiment of the apparatus of the present invention, the membranes in the membrane module 12 comprise lined reinforced polyvinylidene fluoride hollow fiber membranes.
As a preferred embodiment of the device, the anaerobic pool 4 comprises a stirrer 5 and an overflow pipe 6; the overflow pipe 6 is positioned above one side of the anaerobic tank 4 connected with the anoxic tank 7.
As a preferred embodiment of the device of the invention, the anoxic pond 7 comprises a stirrer 9 and an overflow pipe 6; the overflow pipe 6 is positioned above the side where the anoxic tank 7 is connected with the aerobic tank 16.
In addition, the invention also provides a sewage treatment method, which comprises the following steps: introducing sewage into an anaerobic tank 4 inoculated with activated sludge, then sequentially flowing into an anoxic tank 7 and an aerobic tank 16 through an overflow pipe 6, and then flowing into the anaerobic tank 4 and the anoxic tank 7 through a reflux pump 14; meanwhile, the water pump 3 pumps the carbon source in the carbon source barrel 1 into the waste hollow fiber membrane module 8 in the anoxic tank 7.
As a preferred embodiment of the process according to the invention, the carbon source is a mixture of glucose and glacial acetic acid.
As a preferred embodiment of the method of the present invention, the mass ratio of glucose and glacial acetic acid is 3: 1.
Preferably, when the mass ratio of the glucose to the glacial acetic acid in the mixture of the glucose and the glacial acetic acid is 3:1, on one hand, a carbon source which is favorable for the denitrifying bacteria to absorb and utilize can be provided, and on the other hand, the denitrifying bacteria can be stored for a long time at room temperature and outdoor conditions, so that the storage cost and difficulty of the carbon source are reduced.
As a preferred embodiment of the method of the present invention, the mass concentration of the carbon source is 42 to 60 mg/L.
The mass concentration of the carbon source can be adjusted according to the water quality of the sewage, and the sufficient energy source of the denitrifying bacteria can be ensured within the range of 42-60 mg/L.
As a preferred embodiment of the method, the carbon source is pumped into the waste hollow fiber membrane module 8 in the anoxic pond 7 through the water pump 3 and then is diffused through the membrane cavity for 1.5 to 2.5 hours every day.
When the diffusion time of the membrane cavity is 1.5-2.5 hours, the denitrifying bacteria can have enough energy sources, and compared with the conventional feeding mode, the feeding amount can be reduced by about 30 percent in the membrane cavity diffusion mode; in addition, the diffusion time of the membrane cavity is not higher and better, and when the diffusion time of the membrane cavity is too long, membrane pollution can occur inside the membrane cavity, so that the pressure of the pump is increased when a carbon source is introduced through the water suction pump 3, and even membrane explosion in the waste hollow fiber membrane module 8 can be caused.
As a preferred embodiment of the method of the invention, the concentration of the activated sludge is 4000-6000mg/L, the retention time is 18-22 days, and the hydraulic retention time is 10-13 hours.
In a preferred embodiment of the method of the present invention, the mass concentration of the dissolved oxygen in the aerobic tank 16 is 3-4 mg/L.
As a preferred embodiment of the method of the present invention, the reflux ratio of the reflux into the anaerobic tank 6 and the anoxic tank 7 through the reflux pump 14 is 100-300%.
In a preferred embodiment of the method of the present invention, the method further comprises that the treated sewage is filtered by the membrane module 12 and then discharged by the water discharge pump 15.
The invention has the beneficial effects that:
firstly, the method comprises the following steps: according to the technical scheme provided by the invention, the waste hollow fiber membrane component 8 is introduced and can be used as a microbial filler to enhance the denitrification performance of activated sludge in the sewage treatment process, so that the waste hollow fiber membrane which is difficult to treat is successfully reused, and the problem of recycling the waste membrane component in the current urban sewage treatment plant is solved;
secondly, the method comprises the following steps: according to the technical scheme provided by the invention, the waste hollow fiber membrane component 8 is introduced, so that hydrolytic fermentation bacteria and denitrifying bacteria are effectively enriched on the waste hollow fiber membrane, the denitrification efficiency and the process stability of the system are improved, and the consumption of a carbon source required by sewage treatment is reduced;
thirdly, the method comprises the following steps: the technical scheme provided by the invention is suitable for sewage or wastewater with low carbon-nitrogen ratio such as urban domestic sewage, can realize high-efficiency and stable removal of nitrogen in the sewage, and has the effluent COD lower than 20mg/L, the effluent ammonia nitrogen lower than 0.2mg/L, the effluent total nitrogen lower than 5.5mg/L, the effluent total phosphorus lower than 0.4mg/L and the effluent quality far lower than the national first-class A standard.
Drawings
FIG. 1 is a schematic view of a sewage apparatus according to the present invention;
1-a carbon source barrel, 2-a time relay water inlet pump, 3-a water suction pump, 4-an anaerobic tank, 5-a stirrer, 6-an overflow pipe, 7-an anoxic tank, 8-a waste hollow fiber membrane component, 9-a stirrer, 10-an air pump, 11-a gas flowmeter, 12-a membrane component, 13-a vacuum pressure pump, 14-a reflux pump, 15-a water outlet pump, 16-an aerobic tank and 17-an aeration head;
FIG. 2 is a real view of a pilot reactor of the sewage treatment plant;
FIG. 3 is a graph showing the operation results in the sewage treatment processes of example 1, comparative example 1 and comparative example 2.
Detailed Description
To better illustrate the objects, aspects and advantages of the present invention, the present invention will be further described with reference to specific examples.
Example 1
In the sewage treatment method of the embodiment, the used devices are the device schematic diagram shown in fig. 1 and the actual diagram shown in fig. 2, and include a carbon source barrel 1, an anaerobic tank 4, an anoxic tank 7 and an aerobic tank 16, wherein a waste hollow fiber membrane module 8 and a stirrer 9 are arranged in the anoxic tank 7, and a stirrer 5 is arranged in the anaerobic tank 4; the carbon source barrel 1 is connected with the anoxic tank 7 through a connecting pipeline, a water suction pump 3 is arranged on the connecting pipeline, the aerobic tank 16 is connected with the anaerobic tank 4 and the anoxic tank 7 through a reflux pump 14, the anaerobic tank 4 is further connected with a time relay water inlet pump 2, the aerobic tank 16 comprises a membrane component 12 and an aeration head 17, the aeration head 17 is positioned at the bottom of the aerobic tank 16 and is sequentially connected with an air pump 10 and a gas flowmeter 11, and the membrane component 12 is sequentially connected with a vacuum pressure pump 13 and a water outlet pump 15;
the effective volume of the device used in this example was 10m 3 Wherein the effective volume of the anaerobic tank 4 and the anoxic tank 7 is 2.5m 3 The effective volume of the aerobic tank 16 is 5m 3 The membrane in the waste hollow fiber membrane component 8 is a lining reinforced polyvinylidene fluoride (PVDF) hollow fiber composite membrane, the membrane pore agent is 0.1 mu m, and the surface area is 21.2m 2 The membrane in the membrane module 12 is lining enhanced polyvinylidene fluoride, and the surface area of the membrane is 63.6m 2 The carbon source in the carbon source barrel 1 is a mixture of glucose and glacial acetic acid, and the mass ratio of the glucose to the glacial acetic acid in the mixture is 3: 1.
The method for treating sewage by adopting the device of the invention specifically comprises the following steps:
takes actual domestic sewage as inlet water, COD of the sewage is 108.18mg/L, NH 4 + The N content is 10.26mg/L, the TN content is 15.61mg/L, and the TP content is 1.00 mg/L;
(1) start-up phase (1-90 days)
With A 2 Anaerobic tank sludge of a certain municipal sewage plant mainly adopting the/O process is used as inoculation sludge, effluent of a fine grid of the sewage plant is used as sewage inlet water, the sewage is introduced into an anaerobic tank 4 through a time relay water inlet pump 2, and sludge in the anaerobic tank 4 is mixedThe mixed liquid enters an anoxic tank 7 through an overflow pipe 6, the sludge mixed liquid in the anoxic tank 7 enters an aerobic tank 16 through the overflow pipe 6, and an aeration head 17 in the aerobic tank 16 is connected with an air pump 10 through a gas flowmeter 11 to control continuous aeration; the sludge in the aerobic tank 16 realizes the reflux of the sludge and the nitrifying liquid to the anaerobic tank 4 and the anoxic tank 7 through the reflux pump 14, the treated sewage is filtered by the membrane component 12 and then is discharged under the control of the water outlet pump 15, and a vacuum pressure gauge 13 is arranged for detecting the pollution condition of the membrane component 12; the carbon source barrel 1 is used for preparing a denitrification carbon source for the anoxic tank 7 by water, the mass concentration of the added carbon source is set to be 60mg/L, and the diffusion time through the die cavity is 2 hours every day; the sludge concentration is maintained at 4000-6000mg/L in the initial operation stage of the reactor, the sludge age of the system is set to be 20 days, the dissolved oxygen of the aerobic tank is maintained at 3-4mg/L, the sludge and the nitrifying liquid flow back to the anoxic tank 7 and the anaerobic tank 4 from the aerobic tank 16, the reflux ratio is 200 percent, and the membrane flux of the aerobic tank 16 is set to be 12L/m 2 H, corresponding to a hydraulic retention time of 13 hours. The effluent of the reactor is filtered by the membrane module and then discharged, thereby reaching the discharge standard.
(2) Carbon source reduction stage (91-200 days):
the addition of the external carbon source is reduced by 30 percent.
Comparative example 1
The apparatus of comparative example 1 is different from that of example 1 only in that no waste hollow fiber membrane module 8 is provided in the anoxic tank 7;
the only difference between the treatment method of comparative example 1 and the treatment method of example 1 is that the carbon source was added directly to the sludge mixture for 24 hours per day without diffusion through the membrane lumen and the initial carbon source dosage was maintained during the carbon source reduction phase.
Comparative example 2
The only difference between the treatment method of this comparative example and the treatment method of example 1 is that the amount of the external carbon source was diffused through the mold cavity for 4 hours per day.
Examples of effects
The present effect example examined the decarburizing and denitrogenating conditions of example 1, comparative example 1 and comparative example 2 after 200 days of continuous operation, as shown in fig. 3; as can be seen from fig. 3a, the effluent COD concentration of example 1 was stable and was not significantly different from that of comparative example 1(p ═ 0.794), indicating that carbon source reduction did not significantly affect the organic matter treatment performance of example 1. However, the effluent COD of comparative example 2 was significantly higher than that of example 1 (p-0.03078), indicating that luminal diffusion of the external carbon source affected the organic removal efficiency. On the whole, the COD concentration of the effluent of the three groups of reactors meets the discharge standard of the first class A. For the removal of total nitrogen, the effluent quality of the example 1, the comparative example 1 and the comparative example 2 is stable, the effluent quality meets the discharge standard of the first-class A, the total nitrogen of the effluent of the three groups of reactors has no significant difference (p is greater than 0.05), and the example 1 can still maintain excellent denitrification and denitrification performance after the carbon source is reduced.
Table 1: data and results table of carbon and nitrogen removal and phosphorus removal of examples and comparative examples
| Examples | TN | NH 4 + -N | P | COD |
| Water outlet (mg/L) | 6.96 | 0.67 | 0.07 | 21.42 |
| Removal Rate (%) | 55.4 | 93.5 | 93.2 | 80.2 |
| Comparative example 1 | TN | NH 4 + -N | P | COD |
| Water outlet (mg/L) | 9.28 | 0.71 | 0.06 | 21.92 |
| Removal Rate (%) | 40.5 | 93.1 | 93.8 | 80.0 |
| Comparative example 2 | TN | NH 4 + -N | P | COD |
| Water outlet (mg/L) | 9.13 | 1.33 | 0.07 | 30.00 |
| Removal Rate (%) | 41.5 | 87.0 | 93.1 | 72.3 |
As can be seen from Table 1, the quality of the effluent obtained by adopting the technical scheme of the invention is superior to the national first-class A emission standard.
Finally, it should be noted that the above embodiments are intended to illustrate the technical solutions of the present invention and not to limit the scope of the present invention, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications and equivalent substitutions can be made to the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention.
Claims (10)
1. A sewage treatment device is characterized by comprising an anaerobic tank (4), an anoxic tank (7) and an aerobic tank (16) which are connected in sequence;
the anoxic tank (7) comprises a waste hollow fiber membrane component (8).
2. The device according to claim 1, characterized in that the ratio of the surface area of the waste hollow fiber membrane module (8) to the volume of the anoxic tank (7) is 8-9m 2 /m 3 (ii) a The waste hollow fiber membrane in the waste hollow fiber membrane component (8) comprises an inner lining enhanced polyvinylidene fluoride hollow fiber membrane, a polyether sulfone hollow fiber membrane and a polysulfone hollow fiber membrane.
3. The device according to claim 1, characterized in that the device further comprises a carbon source barrel (1), and the carbon source barrel (1) is connected with the anoxic tank (7) through a water suction pump (3).
4. The apparatus according to claim 1, wherein a membrane module (12) and an aeration head (17) are arranged in the aerobic tank (16); the membrane module (12) is connected with a water outlet pump (15) through a connecting pipeline, and a vacuum pressure gauge (13) is arranged on the connecting pipeline; the aeration head (17) is positioned at the bottom of the aerobic tank (16) and is sequentially connected with the air pump (10) and the gas flowmeter (11).
5. The apparatus according to claim 1, characterized in that the aerobic tank (16) is connected to the anoxic tank (7) and the anaerobic tank (4) by means of a return pump (14).
6. The apparatus according to claim 4, wherein the ratio of the surface area of the membrane module (12) to the volume of the aerobic tank (16) is 12.0-13.2m 2 /m 3 (ii) a The membranes in the membrane modules (12) comprise lining reinforced polyvinylidene fluoride hollow fiber membranes.
7. A method of treating wastewater, the method comprising the steps of: introducing sewage into an anaerobic tank (4) inoculated with activated sludge, then sequentially flowing into an anoxic tank (7) and an aerobic tank (16) through an overflow pipe (6), and then flowing into the anaerobic tank (4) and the anoxic tank (7) through a reflux pump (14); meanwhile, the water pump (3) pumps the carbon source in the carbon source barrel (1) into the waste hollow fiber membrane component (8) in the anoxic pond (7).
8. The method of claim 7, wherein the carbon source is a mixture of glucose and glacial acetic acid; the mass concentration of the carbon source is 42-60 mg/L.
9. The method as claimed in claim 7, wherein the concentration of the activated sludge is 4000-6000mg/L, the retention time is 18-22 days, and the hydraulic retention time is 10-13 hours.
10. The method according to claim 7, wherein the mass concentration of dissolved oxygen in the aerobic tank (16) is 3-4 mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210603619.6A CN114835256B (en) | 2022-05-30 | 2022-05-30 | Sewage treatment method and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210603619.6A CN114835256B (en) | 2022-05-30 | 2022-05-30 | Sewage treatment method and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114835256A true CN114835256A (en) | 2022-08-02 |
| CN114835256B CN114835256B (en) | 2023-06-16 |
Family
ID=82572981
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210603619.6A Active CN114835256B (en) | 2022-05-30 | 2022-05-30 | Sewage treatment method and device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114835256B (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101580299A (en) * | 2009-06-26 | 2009-11-18 | 哈尔滨工业大学深圳研究生院 | Wastewater denitrification processing method and system |
| CN102502959A (en) * | 2011-12-20 | 2012-06-20 | 同济大学 | Process for enhancing denitrogenation of membrane bioreactor by anaerobic fermentation acid production |
| CN207483450U (en) * | 2017-09-21 | 2018-06-12 | 江苏大学 | Basalt biological nest orients supplementary carbon source sewage water denitrification device |
| CN108341481A (en) * | 2018-01-18 | 2018-07-31 | 同济大学 | It is a kind of using discarded hollow fiber ultrafiltration membrane or microfiltration membranes as the processing method of the biologic packing material of matrix |
| CN108439590A (en) * | 2018-06-25 | 2018-08-24 | 郑州大学 | A kind of water course in situ nitrate nitrogen cutting device |
| CN209098453U (en) * | 2018-10-22 | 2019-07-12 | 东莞博润环保科技有限公司 | Sanitary sewage disposal complexes |
| US20210101811A1 (en) * | 2014-03-11 | 2021-04-08 | University College Dublin, National University Of Ireland, Dublin | Aerated biofilm reactor hollow fibre membrane |
-
2022
- 2022-05-30 CN CN202210603619.6A patent/CN114835256B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101580299A (en) * | 2009-06-26 | 2009-11-18 | 哈尔滨工业大学深圳研究生院 | Wastewater denitrification processing method and system |
| CN102502959A (en) * | 2011-12-20 | 2012-06-20 | 同济大学 | Process for enhancing denitrogenation of membrane bioreactor by anaerobic fermentation acid production |
| US20210101811A1 (en) * | 2014-03-11 | 2021-04-08 | University College Dublin, National University Of Ireland, Dublin | Aerated biofilm reactor hollow fibre membrane |
| CN207483450U (en) * | 2017-09-21 | 2018-06-12 | 江苏大学 | Basalt biological nest orients supplementary carbon source sewage water denitrification device |
| CN108341481A (en) * | 2018-01-18 | 2018-07-31 | 同济大学 | It is a kind of using discarded hollow fiber ultrafiltration membrane or microfiltration membranes as the processing method of the biologic packing material of matrix |
| CN108439590A (en) * | 2018-06-25 | 2018-08-24 | 郑州大学 | A kind of water course in situ nitrate nitrogen cutting device |
| CN209098453U (en) * | 2018-10-22 | 2019-07-12 | 东莞博润环保科技有限公司 | Sanitary sewage disposal complexes |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114835256B (en) | 2023-06-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101671090B (en) | Combined processing technique of garbage percolates | |
| CN104058555B (en) | Based on low ratio of carbon to ammonium municipal effluent denitrification system and the treatment process of Anammox | |
| CN101708919A (en) | Method for treating leachate in refuse landfill site | |
| CN210122541U (en) | Intelligent sewage advanced treatment system based on micro-nano bubble technology | |
| CN101811803A (en) | Rubbish leachate biological nitrogen removal process and device | |
| CN102603128A (en) | Method for advanced treatment and recycling of landfill leachate | |
| CN111268796A (en) | System and method for treating low C/N ratio domestic sewage by anaerobic/anoxic filler and staged water inlet three-stage AO | |
| CN217809105U (en) | Integrated town sewage treatment device | |
| CN201665583U (en) | Garbage percolate biological denitrogenation device | |
| CN110980947A (en) | Denitrifying phosphorus removal sewage treatment device based on multistage anaerobism-MABR | |
| CN110759585A (en) | Device and method for removing total nitrogen in sewage | |
| CN213895523U (en) | Processing system is reformed transform to mark of carrying of town sewage factory | |
| CN106007267A (en) | Large integrated sewage treatment device and sewage treatment technology | |
| CN113213714A (en) | Raw material medicine wastewater treatment process | |
| CN111018101B (en) | Membrane biofilm culture domestication process and membrane biofilm reaction device for treating high-salinity wastewater | |
| CN202322548U (en) | Anerobic, anoxic, aerobic tanks and bio-membrane reactor combined device for floating boat aeration | |
| US20220073390A1 (en) | Fixed Biofilm Anaerobic-Aerobic Combined Reactor For Treating Wastewater | |
| CN114835256A (en) | Sewage treatment method and device | |
| CN110697991B (en) | Garbage leachate biological treatment process and system | |
| CN209367927U (en) | A kind of high concentration organic nitrogen waste water dis posal equipment | |
| CN111072234A (en) | ZONBER efficient energy-saving small-sized sewage treatment integrated device | |
| CN215906050U (en) | MBR sewage treatment plant of rearmounted oxygen deficiency | |
| CN113800639B (en) | Intensive biochemical pool with activated sludge circulation capacity | |
| CN212894103U (en) | Filler-reinforced three-stage AO (anaerobic-anoxic-oxic) domestic sewage treatment system with low C/N ratio | |
| CN114275969B (en) | Antibiotic sewage treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |