CN110606631A - Aerobic biological fluidized bed sewage treatment device and process - Google Patents
Aerobic biological fluidized bed sewage treatment device and process Download PDFInfo
- Publication number
- CN110606631A CN110606631A CN201911016982.2A CN201911016982A CN110606631A CN 110606631 A CN110606631 A CN 110606631A CN 201911016982 A CN201911016982 A CN 201911016982A CN 110606631 A CN110606631 A CN 110606631A
- Authority
- CN
- China
- Prior art keywords
- reactor
- wall
- phase separation
- gas
- sewage
- 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.)
- Pending
Links
- 239000010865 sewage Substances 0.000 title claims abstract description 119
- 238000000034 method Methods 0.000 title claims abstract description 21
- 230000008569 process Effects 0.000 title claims abstract description 17
- 238000005191 phase separation Methods 0.000 claims abstract description 78
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 75
- 238000005273 aeration Methods 0.000 claims abstract description 58
- 244000005700 microbiome Species 0.000 claims abstract description 54
- 239000000969 carrier Substances 0.000 claims abstract description 30
- 238000004062 sedimentation Methods 0.000 claims abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 238000007789 sealing Methods 0.000 claims abstract description 17
- 239000001301 oxygen Substances 0.000 claims description 97
- 229910052760 oxygen Inorganic materials 0.000 claims description 97
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 93
- 239000007789 gas Substances 0.000 claims description 60
- 238000005276 aerator Methods 0.000 claims description 45
- 239000010802 sludge Substances 0.000 claims description 36
- 238000005243 fluidization Methods 0.000 claims description 18
- 238000009826 distribution Methods 0.000 claims description 15
- 238000011049 filling Methods 0.000 claims description 15
- 238000007599 discharging Methods 0.000 claims description 8
- 238000012544 monitoring process Methods 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 8
- 230000005484 gravity Effects 0.000 claims description 7
- 230000001174 ascending effect Effects 0.000 claims description 6
- 239000004372 Polyvinyl alcohol Substances 0.000 claims description 3
- 239000000017 hydrogel Substances 0.000 claims description 3
- 238000011068 loading method Methods 0.000 claims description 3
- 229920002451 polyvinyl alcohol Polymers 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 239000012798 spherical particle Substances 0.000 claims description 2
- 238000004065 wastewater treatment Methods 0.000 claims 1
- 238000000926 separation method Methods 0.000 abstract description 13
- 238000005265 energy consumption Methods 0.000 abstract description 9
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 14
- 230000000694 effects Effects 0.000 description 12
- 239000012528 membrane Substances 0.000 description 11
- 230000014759 maintenance of location Effects 0.000 description 10
- 230000001276 controlling effect Effects 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 5
- 230000001737 promoting effect Effects 0.000 description 5
- 235000017166 Bambusa arundinacea Nutrition 0.000 description 4
- 235000017491 Bambusa tulda Nutrition 0.000 description 4
- 241001330002 Bambuseae Species 0.000 description 4
- 235000015334 Phyllostachys viridis Nutrition 0.000 description 4
- 239000011425 bamboo Substances 0.000 description 4
- 239000000725 suspension Substances 0.000 description 4
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 241000108664 Nitrobacteria Species 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 239000007900 aqueous suspension Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- -1 oxygen free radical Chemical class 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000035755 proliferation Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000003466 welding Methods 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
- C02F3/02—Aerobic processes
- C02F3/08—Aerobic processes using moving contact bodies
- C02F3/085—Fluidized beds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- 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
-
- 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)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Biological Treatment Of Waste Water (AREA)
Abstract
The invention discloses an aerobic biological fluidized bed sewage treatment device, which comprises a sealed reactor, wherein an aeration unit, a central cylinder and a three-phase separation unit are respectively arranged on the reactor from bottom to top; the central cylinder is provided with a water inlet pipe, and the water inlet pipe penetrates through the reactor and the central cylinder and enters the interior of the central cylinder; the aeration of the aeration unit faces between the outer wall of the central cylinder and the inner wall of the reactor; the three-phase separation unit, the inner wall of the reactor and the sealing top surface enclose a water outlet sedimentation area; the three-phase separation unit, the inner wall and the bottom surface of the reactor enclose a reaction zone, and immobilized microorganism carriers are contained in the reaction zone; the reactor at the upper part of the effluent settling zone is connected with an effluent unit; and the sealed top surface of the three-phase separation unit, which is in contact with the reactor, is connected with an exhaust unit. The device has the advantages of simple structure, low energy consumption, high sewage treatment efficiency and high carrier separation efficiency. Meanwhile, a corresponding treatment process is provided, and the high efficiency and effective operation of sewage treatment can be fully guaranteed.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to an aerobic biological fluidized bed sewage treatment device and process.
Background
The biological fluidized bed technology is a high-efficiency biological treatment technology which is researched and applied in the 70 s and used for sewage treatment, and is a biological membrane method treatment technology which fluidizes carriers with microorganisms growing on the surfaces by means of fluid (liquid and gas) and degrades organic pollutants. The aerobic biological fluidized bed technology is characterized in that microorganisms are attached to carriers and circulate in the reactor along with the carriers, so that the problem of microorganism loss is avoided, the concentration of the microorganisms in the reactor is high, the volume load of the device is improved, meanwhile, the retention time of microorganisms (such as nitrobacteria) with low proliferation speed and special microorganisms in the reactor can be prolonged, and the improvement of the system nitrification efficiency and the treatment efficiency of difficultly degraded substances is facilitated.
But the defects of the prior aerobic biological fluidized bed technology are obvious, and the main reasons are that the immobilized microorganism carrier is ceramsite and the specific gravity of rubber is 1.3-1.5 g/cm higher, so as to keep the carrier fully fluidized, the aeration quantity is more, and the energy consumption is higher3And the addition of the carrier is large, 15-30%, accumulation is easy to occur, and the treatment effect is difficult to meet the requirement, in addition, a labyrinth carrier separator is usually adopted in the aerobic biological fluidized bed, for example, Chinese patent document CN03123800.9, the structure of the aerobic biological fluidized bed is formed by three layers of triangular reflecting cones which are staggered with each other, the reflecting cones adopt an isosceles right-angle triangular structure, the sliding slope surface of the reflecting cones is smaller, the carrier is not favorably slid, meanwhile, the comprehensive factors of large processing errors caused by corrosion and roughness of the surfaces of the reflecting cones, complex structure and the like influence the carrier separation effect, and the carrier loss and the like are caused.
Chinese patent document CN201458905U provides a reactor in which a biological filter is coupled to an aerobic fluidized bed, the biological filter is disposed above the aerobic fluidized bed, the biological filter utilizes the tail gas of the aerobic fluidized bed as an oxygen source, so that aeration is fully utilized, and the problem of carrier loss is avoided.
Chinese patent document CN203668099U discloses an internal circulation aerobic biological fluidized bed, which adopts 4 rectangular partition plates which are vertical and have cross sections and are arranged in a cylinder body, the middle part of the cylinder body is uniformly divided into two upstream areas which are distributed diagonally and another two downstream areas which are distributed diagonally, a carrier separator is formed by combining a plurality of triangular reflecting cones in a staggered way into a laminar body, the carrier is ceramic and TiO2The porous sintering is finished, and the production of nascent oxygen free radicals can be excited in the operation process. The carrier separator adopted by the method also has the problems of complex structure, low separation efficiency and incapability of avoiding carrier loss, and the carriers are ceramics and TiO2The porous sintered material has high density, difficult fluidization, and oxygen free radical as powerful oxidant and bactericidal effect on microbes.
Therefore, the technical personnel in the field need to provide an aerobic biological fluidized bed sewage treatment device and a process which are convenient to operate, low in energy consumption, high in sewage treatment efficiency and high in carrier separation efficiency.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides an aerobic biological fluidized bed sewage treatment device and process which are simple and convenient to operate, low in energy consumption, high in sewage treatment efficiency and high in carrier separation efficiency.
In order to realize the purpose, the invention provides an aerobic biological fluidized bed sewage treatment device, which adopts the following technical scheme:
an aerobic biological fluidized bed sewage treatment device comprises a sealed reactor, wherein an aeration unit, a central cylinder and a three-phase separation unit are respectively arranged on the reactor from bottom to top; the central cylinder is provided with a water inlet pipe, and the water inlet pipe penetrates through the reactor and the central cylinder and enters the interior of the central cylinder; the aeration of the aeration unit faces between the outer wall of the central cylinder and the inner wall of the reactor;
the three-phase separation unit, the inner wall of the reactor and the sealing top surface enclose a water outlet sedimentation area; the three-phase separation unit, the inner wall and the bottom surface of the reactor enclose a reaction zone, and immobilized microorganism carriers are contained in the reaction zone;
the reactor at the upper part of the effluent settling zone is connected with an effluent unit;
and the sealed top surface of the three-phase separation unit, which is in contact with the reactor, is connected with an exhaust unit.
Preferably, the three-phase separation unit comprises a three-phase separation cover and a screen which is arranged on the three-phase separation cover and communicated with the three-phase separation cover;
the bottom of the three-phase separation cover is fixed on the inner wall of the reactor, the top of the three-phase separation cover is fixed on the sealing top surface of the reactor, and the sealing top surface is provided with an exhaust port used for being connected with an exhaust unit and used for discharging tail gas in sewage; the region between the outer wall of the three-phase separation cover and the inner wall and the sealing top surface of the reactor is a water outlet sedimentation region, and the upper part of the water outlet sedimentation region is provided with a water collecting port connected with a water outlet unit; and the bottom of the effluent settling zone is provided with a sludge discharge port connected with a sludge discharge unit, and the sludge discharge port is used for discharging settled sludge out of the system at regular intervals.
Further, the three-phase separation cover is in a circular truncated cone shape with a small top diameter and a large bottom diameter;
the reactor is cylindrical;
the bottom diameter of the three-phase separation cover is matched with the inner diameter of the reactor, so that the three-phase separation cover is fixedly connected with the inner wall of the reactor in a sealing manner.
Further, the screen and the three-phase separation cover are connected through a flange.
Further, the screen is a wedge-shaped wire screen, and the wire gap is 2-3 mm.
Furthermore, the screen cloth is evenly distributed on the inner side surface of the three-phase separation cover along the circumferential direction.
Furthermore, an included angle alpha between the three-phase separation cover and the inner wall of the reactor is 120-155 degrees.
Preferably, the immobilized microorganism carrier is polyvinyl alcohol hydrogel spherical particles.
Preferably, the particle size of the immobilized microorganism carrier is 3-10 mm.
Preferably, the immobilized microorganism carrier has a specific gravity of 1.0-1.1 g/cm3。
Preferably, the interior of the immobilized microorganism carrier is a porous medium, the aperture is 10-50 μm, and the porosity is 95-98%.
Preferably, the loading amount of the immobilized microorganism carrier is 8-15% of the effective volume of the reaction zone.
Preferably, the central cylinder is positioned at the central shaft of the reactor, and the outer wall of the central cylinder is fixedly connected with the inner wall of the reactor through ribs;
the outlet of the water inlet pipe faces downwards along the center of the central cylinder.
Preferably, the aeration unit comprises an air aerator;
the air aerator comprises an air inlet pipe, a gas distribution pipe communicated with the air inlet pipe and an air aeration disc arranged on the gas distribution pipe; and the air aeration discs are arranged between the outer wall of the central cylinder and the inner wall of the reactor and are uniformly distributed in an annular shape.
Furthermore, the aeration unit also comprises an oxygen aerator which is positioned above the air aerator and is arranged coaxially;
the oxygen aerator comprises an oxygen inlet pipe, a gas distribution pipe connected with the oxygen inlet pipe and an oxygen aeration disc arranged on the gas distribution pipe; and the oxygen aeration discs are arranged between the outer wall of the central cylinder and the inner wall of the reactor and are uniformly distributed in an annular shape.
Preferably, the reactor is also provided with a manhole for convenient observation.
Preferably, the reactor is also provided with a dissolved oxygen meter for monitoring the dissolved oxygen amount in the reactor.
Preferably, the reactor is also provided with a pH meter for monitoring the pH in the reactor.
The invention also aims to provide an aerobic biological fluidized bed sewage treatment process, which utilizes the sewage treatment device to carry out the following steps:
s1, the sewage sent by the water inlet pipe enters the center cylinder, then the outlet of the center cylinder faces downwards, and the sewage is uniformly discharged from the bottom of the center cylinder to the periphery under the driving of water flow and enters the space between the outer wall of the center cylinder and the inner wall of the reactor; air sent by a fan enters a space between the outer wall of the central cylinder and the inner wall of the reactor through an air aerator, and the air-water ratio (4-8): 1 is adjusted according to the filling amount of the immobilized microorganism carrier, so that the fluidization of the immobilized microorganism carrier in the sewage is promoted;
s2, aerating the sewage between the outer wall of the central cylinder and the inner wall of the reactor to reduce the density of water flow, and driving the sewage to flow upwards along with the immobilized microorganism carriers under the driving of ascending gas to reach a three-phase separation cover to guide the sewage and the immobilized microorganism carriers to gather inwards; after reaching the top of the three-phase separation cover: gas is discharged from a gas outlet at the sealed top of the reactor; the density of the sewage after gas discharge is increased, so that immobilized microorganism carriers are carried downwards to enter a central cylinder for backflow, then the sewage flows upwards again along with aeration after coming out from an outlet at the bottom of the central cylinder, so that internal circulation flow is formed, meanwhile, the sewage and a dropped biological film enter an effluent sedimentation area after passing through a screen, the dropped biological film falls into the bottom after natural sedimentation to form sludge, and the sludge is discharged through a sludge discharge unit; and discharging the settled water on the upper layer through a water outlet unit.
Preferably, in step S1, oxygen is introduced between the outer wall of the central cylinder and the inner wall of the reactor through an oxygen aerator on the upper side of the air aerator to provide additional oxygen required for the reaction for the aerobic organisms in the immobilized microorganism carriers;
and monitoring the concentration of dissolved oxygen in the reactor by a dissolved oxygen meter, and regulating the flow of oxygen to control the residual dissolved oxygen to be 2-5 mg/l.
Preferably, for the treatment of organic matter sewage: in step S1, the hydraulic retention time is 2-4 hr; the volume load of the reactor is 2-6 kgCOD/(m)3D); and (3) nitrification treatment of ammonia nitrogen sewage: in step S1, the hydraulic retention time is 12-24 hr; the volume load of the reactor is 0.15-0.35 kgNH3-N/(m3.d)。
The invention has the beneficial effects that:
1) the aeration unit, the central cylinder and the three-phase separation unit in the reactor are sequentially arranged from top to bottom, so that sewage firstly falls under the action of gravity after entering the central cylinder from the water inlet pipe and overflows from the outer wall of the central cylinder and the inner wall of the reactor, and immobilized microorganism carriers are driven to contact gas exposed upwards by the aeration unit to fully degrade the sewage. Under the drive of the ascending gas of the aeration unit, the sewage carries the immobilized microorganism carrier to flow upwards and reach a three-phase separation unit; after reaching the top of the three-phase separation cover, the gas is discharged from an exhaust unit connected with the sealed top surface of the reactor, the density of the sewage after the gas is discharged is increased, the immobilized microorganism carriers are further clamped to downwards enter the central cylinder for backflow, and then the sewage flows upwards again along with aeration after coming out from the outlet at the bottom of the central cylinder, so that internal circulation flow is formed; meanwhile, sewage and the fallen biological membrane enter the effluent sedimentation zone through the three-phase separation unit, the fallen biological membrane naturally settles and then falls into the bottom of the effluent sedimentation zone to form sludge, the sludge is periodically discharged, and the settled water on the upper layer is discharged through the water outlet unit. Therefore, the device disclosed by the invention is simple in structural design, and skillfully realizes high-efficiency treatment and separation of sewage through a three-phase separation structure, so that the stability and reliability of the sewage treatment process are ensured. Correspondingly, the treatment process is simple, the energy consumption is low, the carrier separation efficiency is high, and the high efficiency and the effective operation of sewage treatment are fully guaranteed.
2) The invention adopts the circular truncated cone-shaped three-phase separation cover, can effectively guide water to gather to the middle part of the reactor, and increases the internal circulation effect, thereby reducing the needed fluidizing gas, reducing the energy consumption and improving the treatment efficiency of the organic sewage.
3) The aeration in the reactor of the invention is used for providing power and oxygen supply required by fluidization, the air aerator provides power required by fluidization and bears part of oxygen supply through the air aerator and the oxygen aerator, the main oxygen supply is provided by the oxygen aerator, the volume load of the reactor is greatly improved due to the high oxygen transfer rate of pure oxygen and the high oxygen utilization rate, and the air aerator only needs to provide necessary air quantity required by fluidization compared with air, thereby avoiding the problems of carrier breakage, loss and the like caused by overhigh aeration intensity.
4) The wedge-shaped wire screen arranged on the three-phase separation cover can effectively retain the carrier in the reactor and allow sludge and sewage to pass through, and the three-phase separation cover is high in separation efficiency, not easy to block and simple in structure.
5) The invention further precipitates the suspended sludge in the sewage after the sewage subjected to solid-liquid separation of the carrier enters the sludge precipitation zone, and the effluent does not need to be precipitated.
Drawings
FIG. 1 is a schematic structural view of an aerobic biological fluidized bed sewage treatment plant according to the present invention.
Fig. 2 is an enlarged view of the air aeration pipe and the oxygen aeration pipe in fig. 1.
The notations in the figures have the following meanings:
1-a reactor, 10-a manhole, 11-a dissolved oxygen meter and 12-a PH meter;
2-aeration unit, 20-air aerator, 200-air inlet pipe, 201-first gas distribution pipe, 202-air aeration disc, 21-oxygen aerator, 210-oxygen inlet pipe, 211-second gas distribution pipe, 212-oxygen aeration disc;
3-central cylinder, 30-water inlet pipe;
4-three-phase separation unit, 40-three-phase separation cover, 41-screen;
5-a water outlet settling zone; 50-a reaction zone;
6-a water outlet unit; 7-a sludge discharge unit; 8-an exhaust unit.
Detailed Description
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following description will be made with reference to the accompanying drawings. It is obvious that the drawings in the following description are only some examples of the invention, and that for a person skilled in the art, other drawings and embodiments can be derived from them without inventive effort.
For the sake of simplicity, the drawings only schematically show the parts relevant to the present invention, and they do not represent the actual structure as a product.
As shown in fig. 1, the aerobic biological fluidized bed sewage treatment device comprises a sealed reactor 1, wherein an aeration unit 2, a central cylinder 3 and a three-phase separation unit 4 are respectively arranged on the reactor 1 from bottom to top; the central cylinder 3 is provided with a water inlet pipe 30, and the water inlet pipe 30 passes through the reactor and the central cylinder and enters the interior of the central cylinder; the aeration of the aeration unit faces between the outer wall of the central cylinder 3 and the inner wall of the reactor 1;
the three-phase separation unit 4, the inner wall of the reactor 1 and the sealing top surface enclose a water outlet sedimentation area 5; the three-phase separation unit 4 and the inner wall and the bottom surface of the reactor 1 enclose a reaction zone 50, and immobilized microorganism carriers are contained in the reaction zone 50;
the reactor 1 at the upper part of the effluent settling zone 5 is connected with an effluent unit 6, and the reactor at the bottom is connected with a sludge discharge unit 7;
the three-phase separation unit 4 is connected with an exhaust unit 8 on the sealing top surface contacted with the reactor 1.
In the embodiment, the aeration unit 2, the central cylinder 3 and the three-phase separation unit 4 in the reactor 1 are sequentially arranged from top to bottom, so that sewage firstly falls under the action of gravity after entering the central cylinder 3 from the water inlet pipe 30 and overflows to a position between the outer wall of the central cylinder 3 and the inner wall of the reactor 1, and then the immobilized microorganism carriers are driven to contact gas exposed upwards by the aeration unit 2, and aerobic organisms are utilized to fully degrade the sewage; and under the drive of the ascending gas of the aeration unit 2, the sewage carries the immobilized microorganism carrier to flow upwards and reaches the top of the three-phase separation unit 4: gas is discharged from an exhaust unit 8 connected with the sealed top surface of the reactor 1; the density of the sewage after the gas is discharged is increased, so that the sewage carries the immobilized microorganism carriers to downwards enter the central cylinder 3 for backflow, then the sewage flows upwards again along with aeration after coming out from an outlet at the bottom of the central cylinder 3, so that internal circulation flow is formed, meanwhile, the sewage and the fallen biological membranes enter the effluent sedimentation zone 5 through the three-phase separation unit 4, the fallen biological membranes fall into the bottom of the effluent sedimentation zone after natural sedimentation to form sludge, and the sludge is periodically discharged through the sludge discharge unit; the settled water in the upper layer is discharged through the water outlet unit. In practical applications, the water outlet unit 6 is a water outlet pipe with a water outlet valve, the sludge discharge unit 7 is a sludge discharge pipe with a sludge discharge valve 70 and a reflux valve 71, and the exhaust unit 8 is an exhaust pipe with an exhaust valve. By the aforesaid, this embodiment is not only structural design simple, and the energy consumption is low moreover, carrier separation efficiency is high, can realize the high efficiency treatment separation to sewage, guarantees sewage treatment process's reliable and stable nature.
As a preferred embodiment, the three-phase separation unit 4 comprises a three-phase separation cover 40, a screen 41 arranged on the three-phase separation cover 40 and communicated with the three-phase separation cover;
the bottom of the three-phase separation cover 40 is fixed on the inner wall of the reactor 1, the top of the three-phase separation cover is fixed on the sealing top surface of the reactor 1, and the sealing top surface is provided with an exhaust port for connecting with the exhaust unit 7 and discharging tail gas in sewage; the area between the outer wall of the three-phase separation cover 40 and the inner wall and the sealing top surface of the reactor 1 is a water outlet sedimentation area 5, and the upper part of the water outlet sedimentation area 5 is provided with a water collecting opening connected with a water outlet unit 6; and the bottom of the effluent settling zone 5 is provided with a sludge discharge port connected with a sludge discharge unit 7 for discharging settled sludge out of the system at regular intervals. In this embodiment, the mesh 41 is matched with the three-phase separation cover 40, so that when the treated sewage enters the three-phase separation cover 40, the immobilized microorganism carriers can be intercepted, and only the sewage and the fallen biological membrane are allowed to pass through and enter the effluent settling zone 5. Preferably, the screen 41 is connected with the three-phase separation cover 40 through a flange; can be conveniently disassembled, cleaned and replaced. Preferably, the screen 41 is a wedge-shaped wire screen, and the wire gap is 2-3 mm; thereby allowing the sewage and the detached biofilm to pass through and entrap the carriers and microorganisms in the reactor 1. Preferably, the three-phase separation cover 40 is in a circular truncated cone shape with a small top diameter and a large bottom diameter; the reactor is cylindrical; the bottom diameter of the three-phase separation cover is matched with the inner diameter of the reactor, so that the three-phase separation cover is fixedly connected with the inner wall of the reactor in a sealing manner. This embodiment adopts round platform shape three-phase separation cover, can effectual guide rivers gather together to the reactor middle part, increases the inner loop effect, reduces required fluidizing gas, reduces the energy consumption and improves organic sewage's treatment effeciency.
Preferably, the mesh screens 41 are uniformly distributed on the inner side surface of the three-phase separation hood 40 along the circumferential direction. More preferably, in a specific application, an included angle α between the three-phase separation hood 40 and the inner wall of the reactor 1 is 120-155 °. More preferably, the screens 41 are set to 4 to 12 groups.
In another preferred embodiment, the immobilized microorganism carrier is spherical hydrogel particles made of polyvinyl alcohol; the particle size of the carrier particles is 3-10 mm; the optimal particle size is 4-5 mm, the flow resistance is increased due to too large particles, the fluidization effect is poor, and the particles are too small and are easy to run off; the specific gravity of the carrier is 1.0-1.1 g/cm3(ii) a Preferably 1.02g/cm3Too large or too small a specific gravity does not make the fluidization uniform; the carrier is internally provided with a porous medium, the aperture is 10-50 mu m, and the porosity is 95-98%; microorganisms can be attached to the surface and the interior of the carrier, and the enrichment degree of the microorganisms is high; the loading amount of the immobilized microorganism carrier is 8-15% of the effective volume of the reaction zone 50. It should be noted that the reaction zone refers to a region formed in the reactor except for the effluent settling zone, and the effective volume of the reaction zone refers to the volume of a region surrounded by the three-phase separation unit, the inner wall and the bottom surface of the reactor.
As another preferred embodiment, the central cylinder 3 is located at the central axis of the reactor 1, and the outer wall of the central cylinder 3 is fixedly connected with the inner wall of the reactor 1 through ribs (not shown in the figure), and in practical application, the central cylinder can be fixed by welding; the outlet of the water inlet pipe 30 faces downward along the center of the central cartridge 3. The setting of this orientation is the same with the rivers direction in the central section of thick bamboo 3 in this embodiment, has strengthened the decurrent effect of rivers in the central section of thick bamboo 3, and raw materials sewage gets into central section of thick bamboo 3 after simultaneously, and even discharge from central section of thick bamboo 3 bottom to all around under rivers drive reaches the effect of raw materials sewage uniform water distribution, makes raw materials sewage mix in the reactor evenly, has strengthened the effect of mass transfer reaction.
As another preferred embodiment, as shown in fig. 1 and 2, the aeration unit 2 comprises an air aerator 20; the air aerator 20 comprises an air inlet pipe 200, a first gas distribution pipe 201 communicated with the air inlet pipe 200 and an air aeration disc 202 arranged on the first gas distribution pipe 201; and the air aeration discs 202 are arranged between the outer wall of the central cylinder 3 and the inner wall of the reactor 1 and are uniformly distributed in a ring shape. Preferably, the aeration unit 2 further comprises an oxygen aerator 21 positioned above and coaxially with the air aerator 20; the oxygen aerator 21 comprises an oxygen inlet pipe 210, a second gas distribution pipe 211 connected with the oxygen inlet pipe 210 and an oxygen aeration disc 212 arranged on the second gas distribution pipe 211; and the oxygen aeration discs 212 are arranged between the outer wall of the central cylinder 3 and the inner wall of the reactor 1 and are uniformly distributed in a ring shape. In the embodiment, the air aerator 20 provides power required by fluidization and bears part of oxygen supply, the main oxygen supply is provided by the oxygen aerator 21, the oxygen transmission rate of pure oxygen is high, the oxygen utilization rate is high, the volume load of the reactor is greatly improved, and the oxygen aeration amount is less than that of air, so that the air aerator 20 only needs to provide necessary gas amount required by fluidization, and the problems of carrier breakage, carrier loss and the like caused by overhigh aeration intensity are avoided.
As another preferred embodiment, as shown in fig. 1, the reactor 1 is further provided with a manhole 10 for easy observation.
As another preferred embodiment, as shown in fig. 2, a dissolved oxygen meter 11 for monitoring the dissolved oxygen amount in the reactor is further provided on the reactor 1. As another preferred embodiment, as shown in FIG. 2, a pH meter 12 for monitoring the pH in the reactor is further provided in the reactor 1. It should be noted that the dissolved oxygen meter 11 and the PH meter are conventional equipment instruments commercially available in the art, and therefore, will not be described herein in any greater detail.
Example 2
As shown in FIGS. 1 and 2, the aerobic biological fluidized bed sewage treatment process utilizes the sewage treatment device in example 1 to perform the following steps:
s1, the sewage sent by the water inlet pipe 30 enters the center cylinder 3, then the outlet is downward, and the sewage is uniformly discharged from the bottom of the center cylinder 3 to the periphery under the driving of water flow and enters between the outer wall of the center cylinder 3 and the inner wall of the reactor 1; air sent by a fan enters between the outer wall of the central cylinder 3 and the inner wall of the reactor 1 through an air aerator 20, and the air-water ratio (4-8): 1 is adjusted according to the filling amount of the carrier to promote the fluidization of the carrier in the sewage;
s2, aerating the sewage between the outer wall of the central cylinder 3 and the inner wall of the reactor 1, reducing the density of water flow, and leading the sewage to flow upwards along with the immobilized microorganism carriers under the drive of ascending gas and reach the three-phase separation cover 40 to guide the sewage and the immobilized microorganism carriers to gather inwards; after reaching the top of the three-phase separation hood 40: gas is discharged from an exhaust unit 8 connected with the sealed top of the reactor; the density of the sewage after the gas is discharged is increased, so that the sewage carries the immobilized microorganism carriers to downwards enter the central cylinder 3 for backflow, then the sewage flows upwards again along with aeration after coming out from the outlet at the bottom of the central cylinder 3, so that internal circulation flow is formed, meanwhile, the sewage and the fallen biological membranes enter the effluent sedimentation zone 5 after passing through the screen 41, the fallen biological membranes naturally settle and then fall to the bottom to form sludge, and the sludge is discharged through the sludge discharge unit 7; the settled water in the upper layer is discharged through the water outlet unit 6.
The sewage treatment method of the embodiment has the advantages of simple flow, low energy consumption, high carrier separation efficiency and difficult retention and accumulation, thereby ensuring the continuous stability of the sewage treatment effect, improving the volume load, further realizing the high-efficiency treatment and separation of sewage and ensuring the stability and reliability of the sewage treatment process.
As a preferred example, in step S1, oxygen is introduced between the outer wall of the central tube 3 and the inner wall of the reactor 1 through the oxygen aerator 21 on the upper side of the air aerator 20 to provide additional oxygen required for the reaction for the aerobic organisms in the immobilized microorganism carriers; the concentration of dissolved oxygen in the reactor is monitored by a dissolved oxygen meter 11, and the flow of the residual dissolved oxygen is controlled to be 2-5 mg/l by adjusting the oxygen flow.
In the embodiment, the oxygen aerator is additionally arranged on the air aerator, so that the process steps of oxygen aeration are increased, the air aerator provides power required by fluidization and bears part of oxygen supply, and main oxygen supply is provided by the oxygen aerator.
Further, when the present embodiment is applied to the treatment of organic matter sewage: in step S1, controlling the hydraulic retention time to be 2-4 hr; the volume load of the reactor is 2-6 kgCOD/(m)3D); when the embodiment is applied to the nitrification treatment of ammonia nitrogen sewage: in step S1, controlling the hydraulic retention time to be 12-24 hr; the volume load of the reactor is 0.15-0.35 kgNH3-N/(m3D). Therefore, the application of the embodiment can achieve the continuous, stable and excellent sewage treatment effect.
Application example 1
Aiming at petrochemical comprehensive sewage, CODcr is 513mg/l, and the following treatment steps are adopted:
s1, volume of reactor 1m3Filling immobilized microorganism carrier accounting for 8% of the volume of the reactor, and hydraulic retention time is 3 hr; the sewage fed by the water inlet pipe 30 enters the interior of the central cylinder 3, then the outlet of the sewage is downward, and the sewage is uniformly discharged from the bottom of the central cylinder 3 to the periphery under the driving of water flow and enters between the outer wall of the central cylinder 3 and the inner wall of the reactor 1; air sent by the fan enters between the outer wall of the central cylinder 3 and the inner wall of the reactor 1 through the air aerator 20; controlling the volume ratio of air to water to be 4:1 according to the filling amount of the carrier, and promoting the fluidization of the carrier in the sewage; the oxygen flow is adjusted by an oxygen aerator 21, and the residual dissolved oxygen is controlled to be 2mg/l by a dissolved oxygen instrument 11;
s2, aerating the sewage between the outer wall of the central cylinder 3 and the inner wall of the reactor 1, reducing the density of water flow, and leading the sewage to flow upwards along with the immobilized microorganism carriers under the drive of ascending gas and reach the three-phase separation cover 40 to guide the sewage and the immobilized microorganism carriers to gather inwards; after reaching the top of the three-phase separation hood 40: gas is discharged from an exhaust unit 8 connected with the sealed top of the reactor; the density of the sewage after the gas is discharged is increased, so that the sewage carries the immobilized microorganism carriers to downwards enter the central cylinder 3 for backflow, then the sewage flows upwards again along with aeration after coming out from the outlet at the bottom of the central cylinder 3, so that internal circulation flow is formed, meanwhile, the sewage and the fallen biological membranes enter the effluent sedimentation zone 5 after passing through the screen 41, the fallen biological membranes naturally settle and then fall to the bottom to form sludge, and the sludge is discharged through the sludge discharge unit 7; the settled water in the upper layer is discharged through the water outlet unit 6.
Finally, the CODcr of the effluent was found to be 104mg/l, and the CODcr volume load was found to be 3.3 kgCOD/(m)3D), CODcr treatment efficiency of 79.7%, effluent suspension 10 mg/l.
Application example 2
For petrochemical comprehensive sewage, CODcr is 605mg/l, and the adopted treatment steps are basically the same as the application example 1, except that:
in step S1, filling a carrier accounting for 10% of the volume of the reactor; controlling the volume ratio of air to water to be 5:1 according to the filling amount of the carrier, and promoting the fluidization of the carrier in the sewage; the oxygen flow rate was adjusted by an oxygen aerator 21, and the remaining dissolved oxygen was controlled to 3mg/l by a dissolved oxygen meter 11.
Finally, the CODcr of the effluent was found to be 112mg/l, and the CODcr volume load was found to be 3.9 kgCOD/(m)3D), CODcr treatment efficiency of 81.5%, yielding water suspension 15 mg/l.
Application example 3
For petrochemical comprehensive sewage, CODcr is 605mg/l, and the adopted treatment steps are basically the same as the application example 1, except that:
in step S1, filling carrier accounting for 10% of reactor volume, and hydraulic retention time 2 hr; controlling the volume ratio of air to water to be 5:1 according to the filling amount of the carrier, and promoting the fluidization of the carrier in the sewage; the oxygen flow rate was adjusted by an oxygen aerator 21, and the remaining dissolved oxygen was controlled to 2mg/l by a dissolved oxygen meter 11.
Finally, the CODcr of the effluent was found to be 115mg/l, and the CODcr volume load was found to be 5.9 kgCOD/(m)3D), CODcr treatment efficiency of 80.5%, effluent suspension 11 mg/l.
Application example 4
Aiming at the waste water of the waste acid recovery device of the acrylonitrile device, the ammonia nitrogen is 220mg/l, the adopted treatment steps are basically the same as the application example 1, and the difference is that:
in step S1, filling carrier accounting for 15% of reactor volume, and hydraulic retention time is 18 hr; controlling the air-water volume ratio of air to inlet water to be 8:1 according to the filling amount of the carrier; promoting fluidization of the carrier in the sewage; the oxygen flow rate was adjusted by an oxygen aerator 21, and the remaining dissolved oxygen was controlled to 5mg/l by a dissolved oxygen meter 11.
Finally, the ammonia nitrogen content of the effluent is measured to be 5mg/l, and the ammonia nitrogen volume load is measured to be 0.29kgNH3-N/(m3D), the ammonia nitrogen treatment efficiency is 98%.
Application example 5
Aiming at the waste water of the waste acid recovery device of the acrylonitrile device, the ammonia nitrogen is 220mg/l, the adopted treatment steps are basically the same as the application example 1, and the difference is that:
in step S1, filling carrier accounting for 15% of the reactor volume, and hydraulic retention time is 14.5 hr; controlling the air-water volume ratio of air to inlet water to be 8:1 according to the filling amount of the carrier; promoting fluidization of the carrier in the sewage; the oxygen flow rate was adjusted by an oxygen aerator 21, and the remaining dissolved oxygen was controlled to 5mg/l by a dissolved oxygen meter 11.
Finally, the ammonia nitrogen content of the effluent is measured to be 11mg/l, and the ammonia nitrogen volume load is measured to be 0.35kgNH3-N/(m3And d), the ammonia nitrogen treatment efficiency is 95%.
Comparative example 1
For petrochemical complex sewage, CODcr is 513mg/l, and the example is basically the same as the application example 1, except that:
in step S1, controlling the air-water volume ratio of air to inlet water to be 3:1 according to the filling amount of the carrier;
finally, the CODcr of the effluent was found to be 215mg/l, and the CODcr volume load was found to be 2.4 kgCOD/(m)3D), CODcr treatment efficiency of 58.1%, effluent suspension of 12 mg/l.
Analysis results show that the fluidization effect on the carrier is weakened due to the small air inflow, and the biodegradation efficiency is influenced.
Comparative example 2
Aiming at the waste water of the waste acid recovery device of the acrylonitrile device, the ammonia nitrogen is 220mg/l, and the embodiment is basically the same as the application example 4, and the difference is only that:
in step S1, the air-water volume ratio of air to inlet water is controlled to 9:1 according to the carrier filling amount.
Finally, the ammonia nitrogen content of the effluent is measured to be 8mg/l, and the ammonia nitrogen volume load is measured to be 0.28kg/(m3And d), the ammonia nitrogen treatment efficiency is 96%. However, the air aeration amount is too large, so that the microorganisms are detached from the carriers, and the treatment effect is lowered.
Comparative example 3
For petrochemical complex sewage, CODcr is 513mg/l, and the example is basically the same as the application example 1, except that: no oxygen aerator is arranged, and correspondingly, no oxygen aeration process is arranged in the treatment step.
Finally, the CODcr of the effluent was found to be 165mg/l, and the volume load of the CODcr was found to be 2.8 kgCOD/(m)3D), CODcr treatment efficiency of 67.8%, effluent suspension 26 mg/l. Analysis results show that due to lack of an oxygen aeration process, the oxygen transfer rate is slow, the oxygen utilization rate is low, and the immobilized microbial membrane falls off and runs off from the carrier due to the requirement of overhigh aeration strength, so that the degradation efficiency is further influenced.
It should be noted that the above embodiments can be freely combined as necessary. 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 (10)
1. The utility model provides an aerobe fluidized bed sewage treatment plant which characterized in that:
the device comprises a sealed reactor, wherein an aeration unit, a central cylinder and a three-phase separation unit are respectively arranged on the reactor from bottom to top; the central cylinder is provided with a water inlet pipe, and the water inlet pipe penetrates through the reactor and the central cylinder and enters the interior of the central cylinder; the aeration of the aeration unit faces between the outer wall of the central cylinder and the inner wall of the reactor;
the three-phase separation unit, the inner wall of the reactor and the sealing top surface enclose a water outlet sedimentation area; the three-phase separation unit, the inner wall and the bottom surface of the reactor enclose a reaction zone, and immobilized microorganism carriers are contained in the reaction zone;
the reactor at the upper part of the effluent settling zone is connected with an effluent unit;
and the sealed top surface of the three-phase separation unit, which is in contact with the reactor, is connected with an exhaust unit.
2. The sewage treatment apparatus of claim 1, wherein:
the three-phase separation unit comprises a three-phase separation cover and a screen which is arranged on the three-phase separation cover and communicated with the three-phase separation cover;
the bottom of the three-phase separation cover is fixed on the inner wall of the reactor, the top of the three-phase separation cover is fixed on the sealing top surface of the reactor, and the sealing top surface is provided with an exhaust port used for being connected with an exhaust unit and used for discharging tail gas in sewage; the region between the outer wall of the three-phase separation cover and the inner wall and the sealing top surface of the reactor is a water outlet sedimentation region, and the upper part of the water outlet sedimentation region is provided with a water collecting port connected with a water outlet unit; and the bottom of the effluent settling zone is provided with a sludge discharge port connected with a sludge discharge unit, and the sludge discharge port is used for discharging settled sludge out of the system at regular intervals.
3. The sewage treatment apparatus according to claim 2, wherein:
the three-phase separation cover is in a circular truncated cone shape with a small top diameter and a large bottom diameter;
the reactor is cylindrical;
the bottom diameter of the three-phase separation cover is matched with the inner diameter of the reactor, so that the three-phase separation cover is fixedly connected with the inner wall of the reactor in a sealing manner.
4. The sewage treatment apparatus according to claim 2, wherein:
the screen is connected with the three-phase separation cover through a flange; and/or the presence of a gas in the gas,
the screen is a wedge-shaped silk screen, and the silk gap is 2-3 mm.
5. The sewage treatment apparatus of claim 1, wherein:
the immobilized microorganism carrier is polyvinyl alcohol hydrogel spherical particles; and/or the presence of a gas in the gas,
the particle size of the immobilized microorganism carrier is 3-10 mm; and/or the presence of a gas in the gas,
the specific gravity of the immobilized microorganism carrier is 1.0-1.1 g/cm3(ii) a And/or the presence of a gas in the gas,
the inside of the immobilized microorganism carrier is a porous medium, the aperture is 10-50 mu m, and the porosity is 95-98%; and/or the presence of a gas in the gas,
the loading amount of the immobilized microorganism carrier is 8-15% of the effective volume of the reaction zone.
6. The sewage treatment apparatus of claim 1, wherein:
the central cylinder is positioned at the central shaft of the reactor, and the outer wall of the central cylinder is fixedly connected with the inner wall of the reactor through ribs; and/or the presence of a gas in the gas,
the outlet of the water inlet pipe faces downwards along the center of the central cylinder.
7. The sewage treatment apparatus of claim 1, wherein:
the aeration unit comprises an air aerator;
the air aerator comprises an air inlet pipe, a gas distribution pipe communicated with the air inlet pipe and an air aeration disc arranged on the gas distribution pipe; the air aeration discs are arranged between the outer wall of the central cylinder and the inner wall of the reactor and are uniformly distributed in an annular shape;
the aeration unit also comprises an oxygen aerator which is positioned above the air aerator and is arranged coaxially;
the oxygen aerator comprises an oxygen inlet pipe, a gas distribution pipe connected with the oxygen inlet pipe and an oxygen aeration disc arranged on the gas distribution pipe; and the oxygen aeration discs are arranged between the outer wall of the central cylinder and the inner wall of the reactor and are uniformly distributed in an annular shape.
8. The sewage treatment apparatus of claim 1, wherein:
a manhole convenient for observation is also arranged on the reactor; and/or the presence of a gas in the gas,
the reactor is also provided with a dissolved oxygen meter for monitoring the dissolved oxygen in the reactor; and/or the presence of a gas in the gas,
and a PH meter for monitoring the PH in the reactor is also arranged on the reactor.
9. An aerobic biological fluidized bed sewage treatment process, which utilizes the sewage treatment device of any one of claims 2 to 8, and is characterized by comprising the following steps:
s1, the sewage sent by the water inlet pipe enters the center cylinder, then the outlet of the center cylinder faces downwards, and the sewage is uniformly discharged from the bottom of the center cylinder to the periphery under the driving of water flow and enters the space between the outer wall of the center cylinder and the inner wall of the reactor; air sent by a fan enters a space between the outer wall of the central cylinder and the inner wall of the reactor through an air aerator, and the air-water ratio (4-8): 1 is adjusted according to the filling amount of the immobilized microorganism carrier, so that the fluidization of the immobilized microorganism carrier in the sewage is promoted;
s2, aerating the sewage between the outer wall of the central cylinder and the inner wall of the reactor to reduce the density of water flow, and driving the sewage to flow upwards along with the immobilized microorganism carriers under the driving of ascending gas to reach a three-phase separation cover to guide the sewage and the immobilized microorganism carriers to gather inwards; after reaching the top of the three-phase separation cover: gas is discharged from a gas outlet at the sealed top of the reactor; the density of the sewage after gas discharge is increased, so that immobilized microorganism carriers are carried downwards to enter a central cylinder for backflow, then the sewage flows upwards again along with aeration after coming out from an outlet at the bottom of the central cylinder, so that internal circulation flow is formed, meanwhile, the sewage and a dropped biological film enter an effluent sedimentation area after passing through a screen, the dropped biological film falls into the bottom after natural sedimentation to form sludge, and the sludge is discharged through a sludge discharge unit; and discharging the settled water on the upper layer through a water outlet unit.
10. The wastewater treatment process according to claim 9, characterized in that:
in step S1, oxygen enters between the outer wall of the central cylinder and the inner wall of the reactor through an oxygen aerator on the upper side of the air aerator to provide additional oxygen required by the reaction for aerobic organisms in the immobilized microorganism carriers;
and monitoring the concentration of dissolved oxygen in the reactor by a dissolved oxygen meter, and regulating the flow of oxygen to control the residual dissolved oxygen to be 2-5 mg/l.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911016982.2A CN110606631A (en) | 2019-10-24 | 2019-10-24 | Aerobic biological fluidized bed sewage treatment device and process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911016982.2A CN110606631A (en) | 2019-10-24 | 2019-10-24 | Aerobic biological fluidized bed sewage treatment device and process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110606631A true CN110606631A (en) | 2019-12-24 |
Family
ID=68895200
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911016982.2A Pending CN110606631A (en) | 2019-10-24 | 2019-10-24 | Aerobic biological fluidized bed sewage treatment device and process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110606631A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111777177A (en) * | 2020-05-21 | 2020-10-16 | 河南国威市政工程有限公司 | Integrated micro-power sewage treatment device based on UASB reactor |
| CN112939228A (en) * | 2021-04-01 | 2021-06-11 | 上海蓝科石化环保科技股份有限公司 | Immobilized microorganism sewage treatment device and method |
| CN113248017A (en) * | 2021-05-31 | 2021-08-13 | 江苏大学 | Rotary carrier sewage treatment device |
| CN116216921A (en) * | 2023-02-28 | 2023-06-06 | 华南理工大学 | Biological reaction device and method for fluidized wastewater treatment capable of recycling aeration surplus power |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1057984A (en) * | 1996-08-13 | 1998-03-03 | Kurita Water Ind Ltd | Biological treating device |
| JP2005007262A (en) * | 2003-06-18 | 2005-01-13 | Sumitomo Chem Co Ltd | Nitrification method of ammonia nitrogen in wastewater |
| CN103755017A (en) * | 2014-01-22 | 2014-04-30 | 东南大学 | Aerobic biological fluidized bed device combining enriched oxygen aeration and oxygen filling method thereof |
| CN208617482U (en) * | 2018-07-04 | 2019-03-19 | 湖北鼎誉环保科技有限公司 | A kind of waste water moved bed biochemistry and it is separated by solid-liquid separation purifying integration device |
| CN208964630U (en) * | 2018-10-17 | 2019-06-11 | 嘉兴港区工业污水处理有限公司 | A kind of three phase separator for sewage treatment |
| CN211111588U (en) * | 2019-10-24 | 2020-07-28 | 上海蓝科石化环保科技股份有限公司 | Aerobic biological fluidized bed sewage treatment plant |
-
2019
- 2019-10-24 CN CN201911016982.2A patent/CN110606631A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1057984A (en) * | 1996-08-13 | 1998-03-03 | Kurita Water Ind Ltd | Biological treating device |
| JP2005007262A (en) * | 2003-06-18 | 2005-01-13 | Sumitomo Chem Co Ltd | Nitrification method of ammonia nitrogen in wastewater |
| CN103755017A (en) * | 2014-01-22 | 2014-04-30 | 东南大学 | Aerobic biological fluidized bed device combining enriched oxygen aeration and oxygen filling method thereof |
| CN208617482U (en) * | 2018-07-04 | 2019-03-19 | 湖北鼎誉环保科技有限公司 | A kind of waste water moved bed biochemistry and it is separated by solid-liquid separation purifying integration device |
| CN208964630U (en) * | 2018-10-17 | 2019-06-11 | 嘉兴港区工业污水处理有限公司 | A kind of three phase separator for sewage treatment |
| CN211111588U (en) * | 2019-10-24 | 2020-07-28 | 上海蓝科石化环保科技股份有限公司 | Aerobic biological fluidized bed sewage treatment plant |
Non-Patent Citations (2)
| Title |
|---|
| 丁启圣等: "《污水生物处理新技术 修订版》", 31 July 2011, 哈尔滨工业大学出版社, pages: 528 - 529 * |
| 梁世中: "《生物工程设备》", 31 January 2002, 中国轻工业出版社, pages: 44 - 45 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111777177A (en) * | 2020-05-21 | 2020-10-16 | 河南国威市政工程有限公司 | Integrated micro-power sewage treatment device based on UASB reactor |
| CN112939228A (en) * | 2021-04-01 | 2021-06-11 | 上海蓝科石化环保科技股份有限公司 | Immobilized microorganism sewage treatment device and method |
| CN112939228B (en) * | 2021-04-01 | 2023-09-15 | 上海蓝科石化环保科技股份有限公司 | Immobilized microorganism sewage treatment device and method |
| CN113248017A (en) * | 2021-05-31 | 2021-08-13 | 江苏大学 | Rotary carrier sewage treatment device |
| CN116216921A (en) * | 2023-02-28 | 2023-06-06 | 华南理工大学 | Biological reaction device and method for fluidized wastewater treatment capable of recycling aeration surplus power |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110606631A (en) | Aerobic biological fluidized bed sewage treatment device and process | |
| CN1164507C (en) | Stuffing-throwing fluidized bed membrane bioreactor and water treating method | |
| EP0213691B1 (en) | A bioconversion reactor | |
| CN211111588U (en) | Aerobic biological fluidized bed sewage treatment plant | |
| CN209522643U (en) | A kind of jet stream floating stuffing membrane bioreactor | |
| CN208933189U (en) | A kind of water treatment facilities based on basalt fibre | |
| CN204369736U (en) | Samll cities and towns' integration Water feeding treatment device | |
| CN110526394A (en) | A kind of the anaerobic reaction method and reactor of primary flux gas supply circulation stirring | |
| CN106673257A (en) | Micropolluted raw water treatment integrated plant | |
| CN203048657U (en) | Suspended-bed biological aerated filter reactor | |
| CN204281406U (en) | A kind of membrane bioreactor based on fouling membrane in-situ control | |
| CN205061690U (en) | Anaerobism - good oxygen integrative sewage treatment device | |
| CN114314828B (en) | Anaerobic fluidized bed membrane bioreactor | |
| FI88514C (en) | Vertebrate bed reactor for cultivation of immobilized biocatalysts and method for operating it | |
| CN2791030Y (en) | Microbial reactor for water treatment | |
| CN113816565B (en) | Integrated assembly type water treatment equipment | |
| CN109734243A (en) | A kind of waste water treatment process and method of the more technology couplings of MBBR- sustained release carbon pond-BAF | |
| CN212356727U (en) | Take mud-water separator's MBBR equipment | |
| JPS63248499A (en) | Treatment of waste water | |
| CN210261288U (en) | Micro-heavy bed biochemical treatment device | |
| CN210261287U (en) | Mixed bed biochemical treatment device | |
| CN109626557B (en) | Membrane bioreactor capable of automatically adjusting MLSS concentration | |
| CN209583901U (en) | Biochemistry pool MBBR technique coupling denitrification deep-bed filter denitrification dephosphorization system | |
| CN207537208U (en) | A kind of aeration biochemical filter tank | |
| CN111573836A (en) | MBBR (moving bed biofilm reactor) equipment with sludge-water separator and sewage treatment method thereof |
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 |