CN209872706U - Circulation bioreactor - Google Patents
Circulation bioreactor Download PDFInfo
- Publication number
- CN209872706U CN209872706U CN201920639370.8U CN201920639370U CN209872706U CN 209872706 U CN209872706 U CN 209872706U CN 201920639370 U CN201920639370 U CN 201920639370U CN 209872706 U CN209872706 U CN 209872706U
- Authority
- CN
- China
- Prior art keywords
- reactor
- guide cylinder
- bottom end
- outer guide
- water
- 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.)
- Active
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 55
- 238000005273 aeration Methods 0.000 claims abstract description 27
- 230000001174 ascending effect Effects 0.000 claims abstract description 19
- 239000010802 sludge Substances 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 abstract description 28
- 239000007789 gas Substances 0.000 abstract description 8
- 239000010865 sewage Substances 0.000 abstract description 8
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 2
- 239000011574 phosphorus Substances 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract 2
- 229910052757 nitrogen Inorganic materials 0.000 abstract 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 10
- 229910052760 oxygen Inorganic materials 0.000 description 10
- 239000001301 oxygen Substances 0.000 description 10
- 238000000034 method Methods 0.000 description 9
- 238000004062 sedimentation Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 238000006213 oxygenation reaction Methods 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000007654 immersion Methods 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000006228 supernatant Substances 0.000 description 3
- 238000011161 development Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000006396 nitration reaction Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Landscapes
- Aeration Devices For Treatment Of Activated Polluted Sludge (AREA)
Abstract
The utility model discloses a circulation bioreactor, which comprises a reactor; the side wall of the reactor close to the top of the reactor is provided with a water outlet; an inner guide cylinder and an outer guide cylinder with openings at the top end and the bottom end are arranged in the reactor, and the inner guide cylinder is positioned in the outer guide cylinder; gaps are reserved between the top end and the bottom end of the inner guide cylinder and the top end and the bottom end of the reactor, the top end of the outer guide cylinder is connected with the top of the reactor, and a sludge backflow seam is arranged between the bottom end of the outer guide cylinder and the bottom of the reactor; a plurality of water permeable openings which are distributed annularly are arranged on the side wall of the outer guide cylinder close to the bottom of the reactor; the top of the reactor is provided with an air inlet pipe, and the bottom end of the air inlet pipe is positioned at the upper part of the inner ring ascending area and is connected with an aeration head; the circulating flow generated by the gas stripping action is utilized to complete the automatic backflow of the mixed liquid and the sludge, can effectively remove nitrogen and phosphorus, and is suitable for the decentralized treatment of rural domestic sewage.
Description
Technical Field
The utility model relates to an environmental protection equipment field, concretely relates to circulation bioreactor.
Background
Rural domestic sewage is one of the important factors of rural environmental pollution, but for a long time rural environmental protection consciousness is weak, infrastructure such as sewage collection and treatment is seriously lacked, the phenomenon of random pollutant discharge is very common, the pollution to surrounding surface water and underground water is serious, the living environment and body health of vast farmers are directly threatened, and the healthy development of rural economy is restricted.
The rural areas in China have fewer relatively living population, wide and dispersed distribution, large fluctuation of domestic sewage water quantity and quality, and unsound drainage pipe networks; the economic strength of villages and towns is weak; lack of professional personnel for sewage treatment. Aiming at the characteristics of the current situation, the treatment process of the rural domestic sewage needs to meet the requirements of strong impact load resistance, easy independent treatment, low construction cost, low operation cost, simple operation and management and the like.
SUMMERY OF THE UTILITY MODEL
In order to overcome the problems, the utility model provides a circulation bioreactor based on development of shallow aeration principle, this reactor collect biochemical reaction, mud-water separation in an organic whole, adopt shallow aeration, utilize the circulating flow that the air stripping effect produced to accomplish the automatic backward flow of mixed liquid and mud, can denitrogenate dephosphorization effectively, are suitable for rural domestic sewage's decentralized processing.
The utility model provides a technical scheme that its technical problem adopted is: a loop bioreactor comprising a reactor; the side wall of the reactor close to the top of the reactor is provided with a water outlet; an inner guide cylinder and an outer guide cylinder with openings at the top end and the bottom end are arranged in the reactor, and the inner guide cylinder is positioned in the outer guide cylinder; gaps are reserved between the top end and the bottom end of the inner guide cylinder and the top end and the bottom end of the reactor, the top end of the outer guide cylinder is connected with the top of the reactor, and a sludge backflow seam is arranged between the bottom end of the outer guide cylinder and the bottom of the reactor; a plurality of water permeable openings which are distributed annularly are arranged on the side wall of the outer guide cylinder close to the bottom of the reactor; an inner ring ascending area is arranged in the inner guide cylinder, an outer ring descending area is arranged between the inner guide cylinder and the outer guide cylinder, and a settling area is arranged between the outer guide cylinder and the side wall of the reactor; the top of the reactor is provided with an air inlet pipe, and the bottom end of the air inlet pipe is positioned at the upper part of the inner ring ascending area and is connected with an aeration head; the top of the reactor is provided with a water inlet pipe, and a water inlet at the bottom end of the water inlet pipe is positioned at the lower part of the outer ring descending area.
The reactor is of a square structure, a cylindrical structure or an inverted frustum structure.
The aeration head is a liftable aeration head, and the horizontal position of the aeration head can be adjusted.
After the air is introduced into the reactor from the aeration head, the air flows upwards; because the lifting action of air, muddy water mixed liquid has formed the upper and lower space circulation continuous annular flow state by interior draft tube to outer draft tube in the reactor: the muddy water mixed liquid flows upwards along the inner guide cylinder, turns around and flows downwards into the outer ring descending area after reaching the liquid level; wherein, a part of the mud-water mixed liquid enters the sedimentation area through the water permeable port, after sedimentation, supernatant liquid flows out of the reactor from a water outlet at the upper part of the sedimentation area, and the sedimentated sludge and the other part of the mixed liquid enter the inner ring ascending area through the sludge backflow seam.
In the descending process of the sludge-water mixed liquid, dissolved oxygen is continuously consumed and reaches the bottom of the reactor, the dissolved oxygen is less than 0.5mg/L, an anoxic zone can be formed at the lower parts of the outer ring descending zone and the inner ring ascending zone, and raw water firstly enters the anoxic zone to generate denitrification reaction; and because the dissolved oxygen concentration is higher at the upper parts of the inner ring ascending area and the outer ring descending area, an aerobic area can be formed to generate nitration reaction.
The mud-water mixed liquid completes the processes of organic matter degradation, biological denitrification and excessive phosphorus uptake in the process of up-down circular flow. The anoxic zone is not contacted with the atmosphere at the bottom layer, the anoxic environment is formed quickly, and the anoxic state can be well maintained. Raw water directly enters the anoxic zone to provide a carbon source for denitrification, and nitrification and denitrification can be realized in the same reactor.
The utility model has the advantages that:
(1) through reasonable integrated design, the structure is simple, the cost is low, the reactor is divided into 3 annular areas of an inner ring ascending area, an outer ring descending area and a settling area by adopting two built-in guide cylinders, and sewage orderly flows in the 3 areas to complete the processes of biological oxidation, nitrification, denitrification and sludge-water separation of organic matters;
(2) the conventional anoxic/aerobic reaction tank needs aeration equipment, mixed liquid backflow equipment and sludge backflow equipment, and the reactor can complete aeration, mixed liquid backflow and sludge backflow only by one set of aeration equipment, so that the operation is convenient;
(3) the reactor is not provided with conventional mixed liquid and sludge reflux equipment, fixedly installed aeration heads and transmission devices, the aeration heads are connected by hoses and suspended at a certain distance under water of the inner draft tube, and the power efficiency is high; when cleaning and maintenance are needed, the aeration head can be lifted upwards out of the reactor without emptying the reactor, special lifting equipment or entering the reactor, and even if the aeration head fails, the maintenance and the replacement can be quickly carried out;
(4) because the mixed liquid can form regular circular flow between the inner ring and the outer ring, the diffusion and mass transfer between materials are improved; the raw water is mixed with the circulating mixed liquid after entering the reactor, thereby reducing the impact of high-concentration wastewater or toxic wastewater on a system, improving the impact resistance of the reactor, simplifying the process flow, and not needing to arrange a regulating tank to regulate the water quantity and balance the water quality.
Drawings
The present invention will be further explained with reference to the drawings and examples.
Fig. 1 is a schematic structural diagram of the present invention.
FIG. 2 is a schematic flow diagram of the slurry-water mixture in the reactor.
FIG. 3 is a schematic flow diagram of sludge in the reactor.
FIG. 4 is a schematic flow diagram of the supernatant in the reactor.
The figure shows that 1, a reactor, 2, a water outlet, 3, an inner guide cylinder, 4, an outer guide cylinder, 5, a sludge backflow seam, 6, a water permeable opening, 7, an inner ring ascending area, 8, an outer ring descending area, 9, a settling area, 10, an air inlet pipe, 11, an aeration head, 12, a water inlet pipe and 13, and the liquid level.
Detailed Description
Referring to fig. 1, a loop bioreactor comprises a reactor 1; the side wall of the reactor 1 close to the top thereof is provided with a water outlet 2; an inner guide cylinder 3 and an outer guide cylinder 4 with openings at the top end and the bottom end are arranged in the reactor 1, the inner guide cylinder 3, the outer guide cylinder 4 and the reactor 1 are coaxially arranged, the inner guide cylinder 3 is positioned in the outer guide cylinder 4, and the inner guide cylinder 3 and the outer guide cylinder can be connected through a connecting rod to realize position fixation; gaps are reserved between the top end and the bottom end of the inner guide cylinder 3 and the top end and the bottom end of the reactor 1, the top end of the outer guide cylinder 4 is connected with the top end of the reactor 1, and a sludge backflow seam 5 is arranged between the bottom end of the outer guide cylinder 4 and the bottom end of the reactor 1; a plurality of water permeable openings 6 which are distributed annularly are arranged on the side wall of the outer guide cylinder 4 close to the bottom of the reactor 1; an inner ring ascending area 7 is arranged in the inner guide cylinder 3, an outer ring descending area 8 is arranged between the inner guide cylinder 3 and the outer guide cylinder 4, and a settling area 9 is arranged between the outer guide cylinder 4 and the side wall of the reactor 1; an air inlet pipe 10 is arranged in the center of the top of the reactor 1, the bottom end of the air inlet pipe 10 is positioned at the upper part of the inner ring ascending area 7 and is connected with a liftable aeration head 11 in a hanging manner, and the aeration head is positioned 0.8m below a water surface 13; the top of the reactor 1 is provided with a water inlet pipe 12, and a water inlet at the bottom end of the water inlet pipe 12 is positioned at the lower part of the outer ring descending area 8.
The reactor 1 is of an inverted frustum structure, and the inverted frustum structure enables the precipitation area of the precipitation zone 9 to be gradually increased in the water flow direction, so that mud-water separation is facilitated, and the precipitation effect is better; and the settled sludge can directly enter the bottom of the outer ring descending area 8 through the sludge return slit 5.
Referring to fig. 2-4, after air is introduced into the reactor 1 through the aeration head 11, the air flows upwards; due to the lifting action of the air, the muddy water mixed liquid forms an upper and lower space circulating continuous annular flow state from the inner guide cylinder 3 to the outer guide cylinder 4 in the reactor 1: the muddy water mixed liquid flows upwards along the inner draft tube 3, turns around and flows downwards into the outer ring descending area 8 after reaching the liquid level 13; wherein, a part of the mud-water mixed liquor enters the sedimentation zone 9 through the water permeable port 6, after sedimentation, supernatant fluid flows out of the reactor 1 from the water outlet 2 at the upper part of the sedimentation zone 9, and the sedimentary sludge and the other part of the mixed liquor enter the inner ring ascending zone 7 through the sludge backflow seam 5.
In the descending process of the mud-water mixed liquid, dissolved oxygen is continuously consumed and reaches the bottom of the reactor 1, an anoxic zone is formed at the lower part of the outer ring descending zone 8 and the inner ring ascending zone 7, and raw water firstly enters the anoxic zone to generate denitrification reaction; on the other hand, at the upper parts of the inner ring ascending region 7 and the outer ring descending region 8, an aerobic region can be formed due to the higher concentration of dissolved oxygen, and a nitration reaction can occur.
The shallow aeration principle of the utility model is as follows: in the air diffusion system, air blown into water forms bubbles firstly, then is broken and combined continuously in the rising process, and finally is broken and dissipated at the liquid level. Air is transferred from gas phase to liquid phase by contact at the gas-liquid interface. It is described that the oxygen transfer rate is highest at the moment when bubbles are just formed; the transfer rate decreased to 1/10 at the start after half a second of bubble escape, to 1/15 after one second, and then remained substantially constant during the rise of the bubbles, and increased slightly to the instant of bubble collapse at the liquid surface.
The oxygenation efficiency is related to the setting depth of the gas distribution system. When the aerator is close to the water surface, a large amount of bubbles are generated by the blown air, the blown air is disturbed strongly on the water surface and escapes, and the disturbance on the deep part under the water is very little, so the oxygenation efficiency of the whole pool is very low. As the immersion depth increases, the disturbance range is enlarged to reach a certain depth, and the oxygenation efficiency reaches a maximum value. When the total oxygen content is increased by increasing the immersion depth, the power consumption is increased sharply, so that the dynamic efficiency of oxygen charging is reduced. The test data show that: when the gas distributor is arranged under water for 70-90 cm, the oxygen charging amount of unit power consumption is the largest.
According to the principle, the shallow aeration is that an aeration head generally arranged at the bottom of the tank is increased to 70-90 cm below the water surface, and compared with the traditional aeration tank, the immersion depth of an air distributor is reduced by 2/3-3/4. Under the same power, the wind pressure is reduced, and the wind quantity is correspondingly increased. The increased air volume creates more bubbles sufficient to compensate for oxygen transfer losses by shortening the bubble rise path. Thus, although the gas distribution system is shallow and delivers gas at a low pressure, a high oxygenation efficiency can be obtained.
The gas action principle in the utility model is as follows: the gas stripping is a method for improving the liquid by utilizing the density difference of the liquid. When air is mixed with the mixed liquid at the upper part of the inner ring ascending area 7 through the aeration head 11, the density of the formed air-water mixed liquid is lower than that of the mixed liquid at the lower part, and pressure difference occurs. As a result, the mixed liquor in the inner ring ascending region 7 ascends, and the mixed liquor in the outer ring descending region 8 is continuously supplemented to the inner ring ascending region 7, so that the mixed liquor forms regular circular flow between the inner ring ascending region 7 and the outer ring descending region 8.
Claims (3)
1. A loop bioreactor comprising a reactor (1); it is characterized in that a water outlet (2) is arranged on the side wall of the reactor (1) close to the top of the reactor; an inner guide cylinder (3) and an outer guide cylinder (4) with openings at the top end and the bottom end are arranged in the reactor (1), and the inner guide cylinder (3) is positioned in the outer guide cylinder (4); gaps are reserved between the top end and the bottom end of the inner guide cylinder (3) and the top end and the bottom end of the reactor (1), the top end of the outer guide cylinder (4) is connected with the top of the reactor (1), and a sludge backflow seam (5) is arranged between the bottom end of the outer guide cylinder (4) and the bottom of the reactor (1); a plurality of water permeable openings (6) which are distributed annularly are arranged on the side wall of the outer guide cylinder (4) close to the bottom of the reactor (1); an inner ring ascending area (7) is arranged in the inner guide cylinder (3), an outer ring descending area (8) is arranged between the inner guide cylinder (3) and the outer guide cylinder (4), and a settling area (9) is arranged between the outer guide cylinder (4) and the side wall of the reactor (1); the top of the reactor (1) is provided with an air inlet pipe (10), and the bottom end of the air inlet pipe (10) is positioned at the upper part of the inner ring ascending area (7) and is connected with an aeration head (11); the top of the reactor (1) is provided with a water inlet pipe (12), and a water inlet at the bottom end of the water inlet pipe (12) is positioned at the lower part of the outer ring descending area (8).
2. The loop bioreactor as claimed in claim 1, characterized in that the reactor (1) is of square, cylindrical or inverted truncated configuration.
3. Loop bioreactor according to claim 1, characterized in that the aeration head (11) is a liftable aeration head.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920639370.8U CN209872706U (en) | 2019-05-07 | 2019-05-07 | Circulation bioreactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920639370.8U CN209872706U (en) | 2019-05-07 | 2019-05-07 | Circulation bioreactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209872706U true CN209872706U (en) | 2019-12-31 |
Family
ID=68964084
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920639370.8U Active CN209872706U (en) | 2019-05-07 | 2019-05-07 | Circulation bioreactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN209872706U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112920942A (en) * | 2021-01-27 | 2021-06-08 | 华东交通大学 | Water supply pipe network biofilm growth simulation device with multiple variable working conditions |
| CN112920945A (en) * | 2021-01-27 | 2021-06-08 | 华东交通大学 | Intelligent simulation device for microbial growth of domestic water pipeline in research room |
-
2019
- 2019-05-07 CN CN201920639370.8U patent/CN209872706U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112920942A (en) * | 2021-01-27 | 2021-06-08 | 华东交通大学 | Water supply pipe network biofilm growth simulation device with multiple variable working conditions |
| CN112920945A (en) * | 2021-01-27 | 2021-06-08 | 华东交通大学 | Intelligent simulation device for microbial growth of domestic water pipeline in research room |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN207313239U (en) | Efficient circulation biology recombination reaction sewage disposal system | |
| CN107311309B (en) | Upflow internal circulation microaerobic bioreactor and its aeration method and application method for enhancing mass transfer | |
| CN201517048U (en) | A wastewater treatment reactor integrating anaerobic hydrolysis-aerobic-sedimentation separation | |
| CN202400904U (en) | Denitrification-dephosphorization water purifier | |
| CN204097179U (en) | Biological fluidized bed | |
| CN209872706U (en) | Circulation bioreactor | |
| CN110734200A (en) | double-membrane three-phase internal circulation aeration biological fluidized bed and method for treating wastewater | |
| CN202785899U (en) | Sewage treatment device | |
| CN104150589A (en) | Integrated non-gradient activated sludge sewage treatment device | |
| CN107698025B (en) | Integrated sewage denitrification and dephosphorization device | |
| CN101012093A (en) | Integral synchronous denitrification dephosphorizing bioreactor | |
| CN211644768U (en) | Tank type integrated sewage treatment equipment | |
| CN105439279A (en) | Biological fluidized bed | |
| CN115010258B (en) | Integrated aeration sewage treatment tank for enriching microorganisms in intensive self-circulation manner and construction method thereof | |
| CN217265052U (en) | Biochemical tower with high-efficiency cyclone aerator and settling tank | |
| CN107651753B (en) | Sewage denitrification and dephosphorization device | |
| CN216639051U (en) | Short-range coupling anaerobic ammonia oxidation denitrification reactor and integrated equipment | |
| CN214299767U (en) | Integrated sedimentation built-in deepwater aeration bioreactor | |
| CN209759234U (en) | Integrated sewage treatment device | |
| CN209468196U (en) | One kind being based on A2The vertical integrated sewage disposal device of/O technique | |
| CN201850177U (en) | Vortex flow, laminar flow and pulse flow type anaerobic bioreactor | |
| CN112777741A (en) | Tank type integrated sewage treatment equipment | |
| CN112978923A (en) | Mixed fluidized bed reactor and application thereof | |
| CN106219745A (en) | A kind of energy-saving quick startup aerobic granular sludge reactor | |
| CN107651752B (en) | Biological nitrogen and phosphorus removal device for sewage |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20211108 Address after: 250000 room 902, block B, Jiaheng building, No. 1825, Hualong Road, Licheng District, Jinan City, Shandong Province Patentee after: SHANDONG WENQING ENVIRONMENTAL TECHNOLOGY Co.,Ltd. Patentee after: Wang Shuguang Address before: 266000 Guizhou Road, Shinan District, Qingdao, Shandong Patentee before: Wang Shuguang |
|
| TR01 | Transfer of patent right |