CN117049707A - Integrated cultivation wastewater treatment reactor and application thereof in cultivation wastewater treatment - Google Patents
Integrated cultivation wastewater treatment reactor and application thereof in cultivation wastewater treatment Download PDFInfo
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- CN117049707A CN117049707A CN202311029409.1A CN202311029409A CN117049707A CN 117049707 A CN117049707 A CN 117049707A CN 202311029409 A CN202311029409 A CN 202311029409A CN 117049707 A CN117049707 A CN 117049707A
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- mbr membrane
- wastewater
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- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 17
- AHEWZZJEDQVLOP-UHFFFAOYSA-N monobromobimane Chemical compound BrCC1=C(C)C(=O)N2N1C(C)=C(C)C2=O AHEWZZJEDQVLOP-UHFFFAOYSA-N 0.000 claims abstract description 90
- 239000012528 membrane Substances 0.000 claims abstract description 79
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 73
- 230000003647 oxidation Effects 0.000 claims abstract description 65
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 65
- 239000002351 wastewater Substances 0.000 claims abstract description 46
- 238000006243 chemical reaction Methods 0.000 claims abstract description 41
- 238000004062 sedimentation Methods 0.000 claims abstract description 27
- 238000000926 separation method Methods 0.000 claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 claims abstract description 10
- 239000003344 environmental pollutant Substances 0.000 claims abstract description 9
- 231100000719 pollutant Toxicity 0.000 claims abstract description 9
- 238000012554 master batch record Methods 0.000 claims description 82
- 239000010802 sludge Substances 0.000 claims description 42
- 239000000945 filler Substances 0.000 claims description 41
- 238000005192 partition Methods 0.000 claims description 27
- 238000005273 aeration Methods 0.000 claims description 26
- 238000004891 communication Methods 0.000 claims description 18
- 239000012510 hollow fiber Substances 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 18
- 238000000151 deposition Methods 0.000 claims description 16
- 244000005700 microbiome Species 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 230000008021 deposition Effects 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 239000002957 persistent organic pollutant Substances 0.000 claims description 9
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 6
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 229910052698 phosphorus Inorganic materials 0.000 claims description 6
- 239000011574 phosphorus Substances 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- 238000009360 aquaculture Methods 0.000 claims description 4
- 244000144974 aquaculture Species 0.000 claims description 4
- 238000005842 biochemical reaction Methods 0.000 claims description 4
- 238000009348 integrated aquaculture Methods 0.000 claims description 4
- 239000000725 suspension Substances 0.000 claims description 4
- 230000007062 hydrolysis Effects 0.000 claims description 3
- 238000006460 hydrolysis reaction Methods 0.000 claims description 3
- 244000144972 livestock Species 0.000 claims description 3
- 230000020477 pH reduction Effects 0.000 claims description 3
- 238000009304 pastoral farming Methods 0.000 claims description 3
- 238000009374 poultry farming Methods 0.000 claims description 3
- 239000003621 irrigation water Substances 0.000 abstract description 2
- 230000014759 maintenance of location Effects 0.000 description 10
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000000969 carrier Substances 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 238000011010 flushing procedure Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 2
- 239000002033 PVDF binder Substances 0.000 description 2
- 229910052785 arsenic Inorganic materials 0.000 description 2
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 2
- 229910052793 cadmium Inorganic materials 0.000 description 2
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 229920001903 high density polyethylene Polymers 0.000 description 2
- 239000004700 high-density polyethylene Substances 0.000 description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 2
- 229910052753 mercury Inorganic materials 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 210000002700 urine Anatomy 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009395 breeding Methods 0.000 description 1
- 230000001488 breeding effect Effects 0.000 description 1
- 239000013530 defoamer Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- 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
- C02F2101/20—Heavy metals or heavy metal compounds
-
- 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
- C02F2101/20—Heavy metals or heavy metal compounds
- C02F2101/22—Chromium or chromium compounds, e.g. chromates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
-
- 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)
- Separation Using Semi-Permeable Membranes (AREA)
- Biological Treatment Of Waste Water (AREA)
Abstract
The invention relates to an integrated cultivation wastewater treatment reactor which comprises an inner circular plate and an outer circular plate, wherein the inner circular plate and the outer circular plate are concentric circular plates, a central sedimentation tank is arranged on the inner side of the inner circular plate, an annular gap chamber is formed between the inner circular plate and the outer circular plate, and an MBBR anoxic zone, an MBBR aerobic zone, a contact oxidation anoxic zone, a contact oxidation aerobic zone, an MBR membrane reaction zone and an MBR membrane water production zone are arranged in the annular gap chamber in a separated mode and are separated by a separation plate. The integrated cultivation wastewater reactor provided by the invention effectively utilizes the combined arrangement of MBBR, contact oxidation and MBR, effectively reduces pollutants (COD, BOD, SS) in cultivation wastewater, and ensures that the effluent reaches the irrigation water discharge standard.
Description
Technical Field
The invention relates to the field of wastewater treatment, in particular to an integrated cultivation wastewater treatment reactor and application thereof in cultivation wastewater treatment.
Background
The cultivation wastewater refers to excrement, urine and flushing sewage generated in the cultivation excrement. The cow breeding wastewater has the characteristics of poor biodegradability (high COD, low BOD), high suspended solids SS and the like, and is wastewater which is difficult to treat. The existing treatment method is to reuse farmlands after biological treatment such as oxidation ponds, MBBR, MBRs and the like, but the wastewater treated by the method still has the following problems: firstly, the pollutant concentration (COD, BOD, SS) is still higher, the pollutant can not meet the requirements of pollutant emission standards of livestock and poultry farming (GB 18596-2001), the pollutant can be directly recycled into the farmland, the soil volume weight is easily affected, the salinization and hardening of the soil are caused, secondly, the phenomena of sludge expansion and falling, more foam and unstable water quality of effluent are easily caused in the operation process, thirdly, the treatment process is complex, the occupied area of a treatment device is large, the reaction time is long, and the cost is higher. Therefore, researches on a method and a device for treating the aquaculture wastewater, which have higher degradation efficiency of wastewater pollutants, more stable system and simpler and more efficient treatment, are urgently needed in production.
Disclosure of Invention
The invention aims to provide an integrated cultivation wastewater treatment reactor which comprises an inner circular plate and an outer circular plate, wherein the inner circular plate and the outer circular plate are concentric circular plates, a central sedimentation tank is arranged on the inner side of the inner circular plate, an annular gap cavity is formed between the inner circular plate and the outer circular plate, an MBBR anoxic zone, an MBBR aerobic zone, a contact oxidation anoxic zone, a contact oxidation aerobic zone, an MBR membrane reaction zone and an MBR membrane water production zone are arranged in the annular gap cavity in a separated mode, and all stages of treatment zones are separated by separation plates;
the upper part of the MBBR anoxic zone is provided with a water inlet, the interior of the MBBR anoxic zone is provided with an MBBR biological suspension filler, and the side wall of the MBBR anoxic zone is provided with a submersible stirrer; the MBBR anoxic zone and the MBBR aerobic zone are separated by a first separation plate, and a first communication port is formed in the lower part of the first separation plate;
the MBBR biological suspended filler is arranged in the MBBR aerobic zone, the perforated aeration pipe is arranged at the bottom, the first water outlet pipeline is arranged at the upper part, and the central guide cylinder is communicated with the central sedimentation tank;
a central guide cylinder is arranged in the central sedimentation tank, a reflecting plate is arranged at the lower part of the central guide cylinder, a conical sludge settling hopper is arranged at the bottom of the central sedimentation tank, a triangular weir is arranged at the upper part of the central sedimentation tank, and a second water outlet pipeline is arranged on the triangular weir and communicated with the bottom of the contact oxidation anoxic zone;
biological rope filler is arranged in the contact oxidation anoxic zone, a submersible stirrer is arranged on the side wall of the contact oxidation anoxic zone, the contact oxidation anoxic zone and the contact oxidation aerobic zone are separated by a second partition plate, and a second communication port is formed in the upper part of the second partition plate;
biological rope filler is arranged in the contact oxidation aerobic zone, and a microporous aeration disc is arranged at the bottom of the contact oxidation aerobic zone; the contact oxidation aerobic zone and the MBR membrane reaction are separated by a third separation plate, and a third communication port is formed in the lower part of the third separation plate; the MBR membrane reaction zone is internally provided with a curtain type MBR hollow fiber membrane, the bottom of the MBR membrane reaction zone is provided with a microporous aeration device, and the upper part of the MBR membrane reaction zone is provided with a water suction pump and a third water outlet pipeline which are communicated with an MBR membrane water production zone;
and a water outlet is arranged in the MBR membrane water producing area.
In a preferred embodiment of the present invention, the MBBR bio-suspension filler is commercially available, preferably HDPE.
In a preferred embodiment of the present invention, the bio-rope filler is commercially available, preferably propylene fiber.
In a preferred technical scheme of the invention, the curtain type MBR hollow fiber membrane is commercially available, and is preferably an immersed type PVDF hollow fiber membrane.
Another object of the present invention is to provide a method for treating aquaculture wastewater by using the integrated aquaculture wastewater treatment reactor of the present invention, which specifically comprises the following steps:
(1) The wastewater enters an MBBR anoxic zone through a water inlet, an MBBR biological suspended filler is arranged in the MBBR anoxic zone and is used as a carrier to attach anaerobic microorganisms, a submersible stirrer is arranged on the side wall, a large amount of bottom sludge is prevented from depositing at the bottom through strong stirring, and effluent automatically flows into an MBBR aerobic zone through a first communication port at the lower part of a first partition plate;
(2) The MBBR biological suspended filler is arranged in the MBBR aerobic zone, and microorganisms attached to the filler further remove degradable organic pollutants in the wastewater; simultaneously, a perforated aeration pipe is arranged at the bottom, and the gas is uniformly distributed;
(3) The effluent of the MBBR aerobic zone enters a central guide cylinder in a central sedimentation tank through an upper pipeline, wastewater flows out from top to bottom in the central guide cylinder, flows upwards through a reflecting plate positioned at the lower part of the central guide cylinder, overflows along a water outlet triangular weir at the periphery of the upper part, and flows into a second pipeline to flow into the bottom of the contact oxidation anoxic zone;
(4) Biological rope filler is arranged in the contact oxidation anoxic zone and used for adsorbing sludge and microorganisms; the side wall of the contact oxidation anoxic zone is provided with a submersible stirrer, so that sludge deposition is avoided, and effluent overflows into the contact oxidation aerobic zone through an opening at the upper part of the second partition plate;
(5) Biological rope filler is arranged in the contact oxidation aerobic zone, and organic pollutants are degraded and purified through the combined action of a biological film and activated sludge; the bottom is provided with a micropore aeration disc, so that sufficient oxygen is provided for biochemical reaction, and activated sludge deposition is prevented; the effluent automatically flows into the MBR membrane reaction zone through a third communication port at the lower part of the third partition plate;
(6) The curtain type MBR hollow fiber membrane is arranged in the MBR membrane reaction zone, a microporous aeration device is arranged at the bottom of the MBR membrane reaction zone to avoid sludge deposition, and sludge-water separation is realized through the MBR hollow fiber membrane; and the effluent of the MBR membrane reaction zone is pumped into an MBR membrane water production zone by an upper water suction pump and is discharged through a water outlet.
In the preferred technical scheme of the invention, the wastewater is the culture wastewater after hydrolysis and acidification treatment, the COD of the wastewater is 10000-50000mg/L, the BOD is 5000-10000mg/L, the total nitrogen is 1000-5000mg/L, the ammonia nitrogen is 500-1000mg/L, and the total phosphorus is 100-500mg/L.
In the preferred technical scheme of the invention, the effluent quality meets the requirements of pollutant emission standards of livestock and poultry farming (GB 18596-2001), COD is less than 400mg/L, BOD is less than 100mg/L, total nitrogen is less than 100mg/L, ammonia nitrogen is less than 10mg/L, and total phosphorus is less than 10mg/L.
In the preferable technical scheme of the invention, the residence time of the MBBR aerobic zone is 30-40h, and the dissolved oxygen is 1-4mg/L.
In the preferable technical scheme of the invention, the residence time of the wastewater in the MBBR anoxic zone is 10-20h.
In the preferred technical scheme of the invention, the retention time of the central sedimentation tank is 1-10h.
In a preferred technical scheme of the invention, the residence time of the contact oxidation anoxic zone is 20-30h.
In the preferable technical scheme of the invention, the retention time of the contact oxidation aerobic zone is 40-50h, and the dissolved oxygen is 1-4mg/L
In the preferred technical scheme of the invention, the residence time of the MBR membrane reaction zone is 1-10h.
In the preferred technical scheme of the invention, the residence time of the MBR membrane water producing area is 1-10h.
In a preferred technical scheme of the invention, the MBBR anoxic zone: the effective volume ratio of the MBBR aerobic zone is 1:1-5.
In a preferred embodiment of the invention, the contact oxidation anoxic zone: the effective volume ratio of the contact oxidation aerobic zone is 1:1-5.
In a preferred technical scheme of the invention, the MBR membrane reaction zone: the effective volume ratio of the MBR membrane water producing area is 1:1-5.
Unless otherwise indicated, when the invention relates to a percentage between liquids, the percentages are volume/volume percentages; the invention relates to the percentage between liquid and solid, said percentage being volume/weight percentage; the invention relates to the percentage between solids and liquids, the percentage being weight/volume percentage; the balance being weight/weight percent.
Compared with the prior art, the invention has the following beneficial effects:
1. the integrated cultivation wastewater reactor provided by the invention effectively utilizes the combined arrangement of MBBR, contact oxidation and MBR, effectively reduces pollutants (COD, BOD, SS) in cultivation wastewater, and ensures that the effluent reaches the irrigation water discharge standard.
2. The invention solves the problem of sludge expansion in the traditional two-stage A/O, realizes the reduction of COD and BOD by sludge degradation under the facultative environment of low DO, realizes the reduction of ss by sludge adsorption, realizes sludge bubble pressing by spraying the sludge backflow through the spraying device, saves the use of defoamer, further realizes the degradation and adsorption of COD and ss by A/O and MBR, can effectively solve the problems of sludge expansion and blockage, does not need sludge backflow, and does not need back flushing water. On one hand, the sludge expansion can be solved through reflux water pressure soaking, on the other hand, the secondary sedimentation tank is replaced through an MBR membrane reaction zone, sludge interception is carried out by using an MBR, and occupied area is saved.
3. The whole process adopts an integrated lotus-type structure, realizes partition utilization, has compact layout, saves occupied area, is convenient for incremental capacity expansion, reduces investment running cost, is simple to operate, and achieves the aim of efficiently treating high-concentration organic wastewater.
4. The invention has simple operation, energy conservation and consumption reduction, effectively reduces the running cost of the system and ensures the treatment effect.
Drawings
FIG. 1 is a schematic top view of an integrated aquaculture wastewater treatment reactor of the present invention;
100. an integrated cultivation wastewater treatment reactor; 101. an inner circular plate; 102. an outer circular plate; 103. a central sedimentation tank; 104. an MBBR anoxic zone; 105. an MBBR aerobic zone; 106. contacting an oxidation anoxic zone; 107. contacting an oxidation aerobic zone; 108. an MBR membrane reaction zone; 109. an MBR membrane water producing area; 110. submersible agitators; 111. a first partition plate; 112. perforating the aeration pipe; 113. a second partition plate; 114. a microporous aeration disc; 115. curtain type MBR hollow fiber membrane; 116. a microporous aeration device; 117. a third divider plate, 118, a center guide shell; 119. a reflection plate; 120. triangular weir.
Detailed Description
The invention is further illustrated by the following examples.
The cultivation wastewater to be treated is: collecting cow dung, cow urine and flushing water produced in a cow farm, and carrying out solid-liquid separation to obtain wastewater and waste residues; the wastewater is the culture wastewater to be treated after hydrolysis and acidification treatment, wherein COD 33100mg/L, total suspended matters ss 6250mg/L, BOD 8110mg/L, total nitrogen 1230mg/L, ammonia nitrogen 876mg/L and total phosphorus 363mg/L. Heavy metal total mercury 10.5mg/L, total arsenic 22.2mg/L, total cadmium 1.35mg/L, total chromium 33.3mg/L, total nickel 49.7mg/L, total lead 19.0mg/L, total salt 2.52X10 4 mg/L, pH 7.1.
Example 1 an integrated aquaculture wastewater treatment reactor according to the invention
The integrated cultivation wastewater treatment reactor comprises an inner circular plate 101 and an outer circular plate 102, wherein the inner circular plate 101 and the outer circular plate 102 are concentric circular plates, a central sedimentation tank 103 is arranged on the inner side of the inner circular plate 101, an annular gap chamber is formed between the inner circular plate 101 and the outer circular plate 102, an MBBR anoxic zone 104, an MBBR aerobic zone 105, a contact oxidation anoxic zone 106, a contact oxidation aerobic zone 107, an MBR membrane reaction zone 108 and an MBR membrane water production zone 109 are arranged in the annular gap chamber in a separated mode, and all stages of treatment areas are separated by partition plates;
the upper part of the MBBR anoxic zone 104 is provided with a water inlet, the interior is provided with MBBR biological suspended filler, and the side wall is provided with a submersible stirrer 110; the MBBR anoxic zone 104 and the MBBR aerobic zone 105 are separated by a first partition plate 111, and a first communication port is formed in the lower part of the first partition plate 111;
the MBBR biological suspended filler is arranged in the MBBR aerobic zone 105, the perforated aeration pipe 112 is arranged at the bottom, the first water outlet pipeline is arranged at the upper part, and the first water outlet pipeline is communicated with the central guide cylinder of the central sedimentation tank 103;
the lower part of the center guide cylinder 118 is provided with a reflecting plate 119, the bottom of the center sedimentation tank is provided with a conical sludge sedimentation hopper, the upper part of the center sedimentation tank is provided with a triangular weir 120, and a second water outlet pipeline is arranged on the triangular weir and communicated with the bottom of the contact oxidation anoxic zone 106;
biological rope filler is arranged in the contact oxidation anoxic zone 106, a submersible stirrer 110 is arranged on the side wall of the contact oxidation anoxic zone 109 and the contact oxidation aerobic zone 107 are separated by a second partition plate 113, and a second communication port is formed in the upper part of the second partition plate 113;
biological rope filler is arranged in the contact oxidation aerobic zone 107, and a microporous aeration disc 114 is arranged at the bottom; the contact oxidation aerobic zone 107 and the MBR membrane reaction zone 108 are separated by a third partition plate 117, and a third communication port is formed in the lower part of the third partition plate; a curtain type MBR hollow fiber membrane 115 is arranged in the MBR membrane reaction zone 108, a microporous aeration device 116 is arranged at the bottom, and a water suction pump and a third water outlet pipeline are arranged at the upper part and are communicated with an MBR membrane water production zone 109;
a water outlet is arranged in the MBR membrane water producing area 109.
The MBBR biological suspension filler is HDPE.
The biological rope filler is propylene fiber.
The curtain type MBR hollow fiber is an MBR hollow fiber membrane made of membrane immersed PVDF.
Example 2 cultivation wastewater depth Process
The cultivation wastewater treatment process comprises the following steps:
(1) The culture wastewater to be treated enters an MBBR anoxic zone 104 through a water inlet, MBBR biological suspended filler (commercial available, the adding amount is 30 percent of the volume of the anoxic zone) is arranged in the MBBR anoxic zone 104, anaerobic microorganisms are attached as carriers, a submersible stirrer 110 is arranged on the side wall, a large amount of bottom sludge is prevented from depositing by strong stirring, and the effective volume of the MBBR anoxic zone 104 is 878.23m 3 The residence time is 17.6h, and the effluent enters the MBBR aerobic zone 105 through a first communication port at the lower part of the first partition plate 111;
(2) The MBBR biological suspended filler is arranged in the MBBR aerobic zone 105, and microorganisms attached to the filler further remove degradable organic pollutants in the wastewater; simultaneously, a perforated aeration pipe 112 is arranged at the bottom, and gas is uniformly distributed; the effective volume of the MBBR aerobic zone 105 is 1811.16m 3 The retention time is 36.2h, and the dissolved oxygen is 2mg/L;
(3) The effluent of the MBBR aerobic zone 105 enters a central guide cylinder 118 in the central sedimentation tank 103 through an upper pipeline, the wastewater flows out from top to bottom in the central guide cylinder 118, and the effective volume of the central sedimentation tank 103 is 442.26m 3 The residence time is 8.8 hours; the wastewater flows upwards through the reflecting plate 119 positioned at the lower part of the central guide cylinder 118, overflows along the triangular water outlet weirs 120 at the periphery of the upper part, flows into the bottom of the contact oxidation anoxic zone 106 through the second pipeline, and the sludge is settled and discharged into the conical sludge settling hopper at the bottom of the tank;
(4) Biological rope fillers are arranged in the contact oxidation anoxic zone 106 and are used for adsorbing sludge and microorganisms; the side wall of the contact oxidation anoxic zone 106 is provided with a submersible stirrer 110 to avoid sludge deposition, and the effective volume of the contact oxidation anoxic zone 106 is 1091.34m 3 Residence time 21.8h; the effluent overflows into the contact oxidation aerobic zone 107 through the upper opening of the second partition plate 113;
(5) Biological rope filler is arranged in the contact oxidation aerobic zone 107, and organic pollutants are degraded and purified through the combined action of a biological film and activated sludge; the bottom is provided with a microporous aeration disc 114, so that sufficient oxygen is provided for biochemical reaction to prevent activated sludge deposition; the effective volume of the contact oxidation aerobic zone 107 is 2476.80m 3 The retention time is 49.5 hours, and the dissolved oxygen is 2mg/L; the effluent automatically flows into the MBR membrane reaction zone through a third communication port at the lower part of the third partition plate 117;
(6) The curtain type MBR hollow fiber membrane 115 is arranged in the MBR membrane reaction zone 108, the microporous aeration device 116 is arranged at the bottom to avoid sludge deposition, mud-water separation is realized through the MBR hollow fiber membrane 116, and the effective volume of the MBR membrane reaction zone 108 is 313.47m 3 The residence time is 6.3h; the effluent of the MBR membrane reaction zone 108 is pumped into an MBR membrane water producing zone 109 by an upper water pump, and the effective volume of the MBR membrane water producing zone 109 is 400.50m 3 The retention time is 8.0h, and the waste water is discharged through a water outlet. Through detection, COD 322mg/L, BOD 5mg/L, SS not detected, total nitrogen 40mg/L, ammonia nitrogen 5.75mg/L, total phosphorus 9.33mg/L, heavy metals total mercury, total arsenic, total cadmium, total chromium, total nickel and total lead are not detected, and the pH value is 8.3.
Comparative example 1
(1) Feeding the culture wastewater to be treated into an MBBR anoxic zone through a water inlet, wherein an MBBR biological suspended filler (the adding amount is 30% of the volume of the anoxic zone) is arranged in the MBBR anoxic zone, anaerobic microorganisms are attached to the MBBR biological suspended filler as carriers, a submerged stirrer is arranged on the side wall of the MBBR anoxic zone, a large amount of sediment is prevented from being deposited at the bottom of the MBBR anoxic zone through strong stirring, and the effective volume of the MBBR anoxic zone is 878.23m 3 The residence time is 17.6 hours, and the effluent automatically flows into the MBBR aerobic zone through a first communication port at the lower part of the first partition plate;
(2) The MBBR biological suspended filler is arranged in the MBBR aerobic zone, and microorganisms attached to the filler further remove degradable organic pollutants in the wastewater; simultaneously, a perforated aeration pipe is arranged at the bottom, and the gas is uniformly distributed; the effective volume of the MBBR aerobic zone is 1811.16m 3 The retention time is 36.2h, and the dissolved oxygen is 2mg/L;
(3) The effluent of the MBBR aerobic zone enters a central guide cylinder in a central sedimentation tank through an upper pipeline, the wastewater flows out from top to bottom in the central guide cylinder, and the effective volume of the central sedimentation tank is 442.26m 3 The residence time is 8.8 hours; the wastewater flows upwards through the reflecting plate positioned at the lower part of the central guide cylinder, overflows along the triangular weir for water outlet at the periphery of the upper part, and the water outlet is obtained. Through detection, COD 1562mg/L, BOD 539mg/L and SS 895mg/L in the effluent.
Comparative example 2
(1) Feeding the culture wastewater to be treated into an MBBR anoxic zone through a water inlet, wherein an MBBR biological suspended filler (the adding amount is 30% of the volume of the anoxic zone) is arranged in the MBBR anoxic zone, anaerobic microorganisms are attached to the MBBR biological suspended filler as carriers, a submerged stirrer is arranged on the side wall of the MBBR anoxic zone, a large amount of sediment is prevented from being deposited at the bottom of the MBBR anoxic zone through strong stirring, and the effective volume of the MBBR anoxic zone is 878.23m 3 The residence time is 17.6 hours, and the effluent automatically flows into the MBBR aerobic zone through a first communication port at the lower part of the first partition plate;
(2) The MBBR biological suspended filler is arranged in the MBBR aerobic zone, and microorganisms attached to the filler further remove degradable organic pollutants in the wastewater; simultaneously, a perforated aeration pipe is arranged at the bottom, and the gas is uniformly distributed; the effective volume of the MBBR aerobic zone is 1811.16m 3 The retention time is 36.2h, and the dissolved oxygen is 2mg/L;
(3) The effluent of the MBBR aerobic zone enters a central guide cylinder in a central sedimentation tank through an upper pipeline, the wastewater flows out from top to bottom in the central guide cylinder, and the effective volume of the central sedimentation tank is 442.26m 3 The residence time is 8.8 hours; the wastewater flows upwards through a reflecting plate positioned at the lower part of the central guide cylinder, overflows along a triangular weir for water outlet at the periphery of the upper part, flows into a second pipeline and flows into an MBR membrane reaction area, and sludge is settled and discharged into a conical sludge settling hopper at the bottom of the tank;
(4) The curtain type MBR hollow fiber membrane is arranged in the MBR membrane reaction zone, a microporous aeration device is arranged at the bottom of the MBR membrane reaction zone to avoid sludge deposition, sludge-water separation is realized through the MBR hollow fiber membrane, and the effective volume of the MBR membrane reaction zone is 313.47m 3 The residence time is 6.3h; the effluent of the MBR membrane reaction zone is pumped into an MBR membrane water producing zone by an upper water suction pump, and the effective volume of the MBR membrane water producing zone is 400.50m 3 The retention time is 8.0h, and the water is discharged through the water outlet, thus obtaining the effluent. The COD 847mg/L and BOD 351mg/L in the water are detected and are not detected. MBR is easy to block and the effluent treatment effect is poor.
Comparative example 3
(1) Introducing the culture wastewater to be treated into a contact oxidation anoxic zone, wherein a biological rope filler is arranged in the contact oxidation anoxic zone and used for adsorbing sludge and microorganisms; the side wall of the contact oxidation anoxic zone is provided with a submersible stirrer to avoid sludge deposition, and the effective volume of the contact oxidation anoxic zone is 1091.34m 3 Residence time 21.8h; the effluent overflows into the contact oxidation aerobic zone through an opening at the upper part of the second partition plate;
(2) Biological rope filler is arranged in the contact oxidation aerobic zone, and organic pollutants are degraded and purified through the combined action of a biological film and activated sludge; the bottom is provided with a micropore aeration disc, so that sufficient oxygen is provided for biochemical reaction, and activated sludge deposition is prevented; the effective volume of the contact oxidation aerobic zone is 2476.80m 3 The retention time is 49.5 hours, and the dissolved oxygen is 2mg/L; the effluent automatically flows into the MBR membrane reaction zone through a third communication port at the lower part of the third partition plate;
(3) The curtain type MBR hollow fiber membrane is arranged in the MBR membrane reaction zone, a microporous aeration device is arranged at the bottom of the MBR membrane reaction zone to avoid sludge deposition, and the sludge is solidified through the MBR hollow fiber membraneThe effective volume of the MBR membrane reaction zone is 313.47m 3 The residence time is 6.3h; the effluent of the MBR membrane reaction zone is pumped into an MBR membrane water producing zone by an upper water suction pump, and the effective volume of the MBR membrane water producing zone is 400.50m 3 The retention time is 8.0h, and the water is discharged through the water outlet, thus obtaining the effluent. The COD 1273mg/L and BOD 560mg/L in the water are detected and are not detected.
The above description of the embodiments of the present invention is not intended to limit the present invention, and those skilled in the art can make various changes or modifications according to the present invention without departing from the spirit of the present invention, and shall fall within the scope of the claims of the present invention.
Claims (10)
1. The integrated cultivation wastewater treatment reactor comprises an inner circular plate and an outer circular plate, wherein the inner circular plate and the outer circular plate are concentric circular plates, a central sedimentation tank is arranged on the inner side of the inner circular plate, an annular gap cavity is formed between the inner circular plate and the outer circular plate, an MBBR anoxic zone, an MBBR aerobic zone, a contact oxidation anoxic zone, a contact oxidation aerobic zone, an MBR membrane reaction zone and an MBR membrane water production zone are arranged in the annular gap cavity in a separated manner, and all stages of treatment zones are separated by a separation plate;
the upper part of the MBBR anoxic zone is provided with a water inlet, the interior of the MBBR anoxic zone is provided with an MBBR biological suspension filler, and the side wall of the MBBR anoxic zone is provided with a submersible stirrer; the MBBR anoxic zone and the MBBR aerobic zone are separated by a first separation plate, and a first communication port is formed in the lower part of the first separation plate;
the MBBR biological suspended filler is arranged in the MBBR aerobic zone, the perforated aeration pipe is arranged at the bottom, the first water outlet pipeline is arranged at the upper part, and the central guide cylinder is communicated with the central sedimentation tank;
a central guide cylinder is arranged in the central sedimentation tank, a reflecting plate is arranged at the lower part of the central guide cylinder, a conical sludge settling hopper is arranged at the bottom of the central sedimentation tank, a triangular weir is arranged at the upper part of the central sedimentation tank, and a second water outlet pipeline is arranged on the triangular weir and communicated with the bottom of the contact oxidation anoxic zone;
biological rope filler is arranged in the contact oxidation anoxic zone, a submersible stirrer is arranged on the side wall of the contact oxidation anoxic zone, the contact oxidation anoxic zone and the contact oxidation aerobic zone are separated by a second partition plate, and a second communication port is formed in the upper part of the second partition plate;
biological rope filler is arranged in the contact oxidation aerobic zone, and a microporous aeration disc is arranged at the bottom of the contact oxidation aerobic zone; the contact oxidation aerobic zone and the MBR membrane reaction are separated by a third separation plate, and a third communication port is formed in the lower part of the third separation plate; the MBR membrane reaction zone is internally provided with a curtain type MBR hollow fiber membrane, the bottom of the MBR membrane reaction zone is provided with a microporous aeration device, and the upper part of the MBR membrane reaction zone is provided with a water suction pump and a third water outlet pipeline which are communicated with an MBR membrane water production zone;
and a water outlet is arranged in the MBR membrane water producing area.
2. A method for treating aquaculture wastewater using the integrated aquaculture wastewater treatment reactor of claim 1, comprising the steps of:
(1) The wastewater enters an MBBR anoxic zone through a water inlet, an MBBR biological suspended filler is arranged in the MBBR anoxic zone and is used as a carrier to attach anaerobic microorganisms, a submersible stirrer is arranged on the side wall, a large amount of bottom sludge is prevented from depositing at the bottom through strong stirring, and effluent automatically flows into an MBBR aerobic zone through a first communication port at the lower part of a first partition plate;
(2) The MBBR biological suspended filler is arranged in the MBBR aerobic zone, and microorganisms attached to the filler further remove degradable organic pollutants in the wastewater; simultaneously, a perforated aeration pipe is arranged at the bottom, and the gas is uniformly distributed;
(3) The effluent of the MBBR aerobic zone enters a central guide cylinder in a central sedimentation tank through an upper pipeline, wastewater flows out from top to bottom in the central guide cylinder, flows upwards through a reflecting plate positioned at the lower part of the central guide cylinder, overflows along a water outlet triangular weir at the periphery of the upper part, and flows into a second pipeline to flow into the bottom of the contact oxidation anoxic zone;
(4) Biological rope filler is arranged in the contact oxidation anoxic zone and used for adsorbing sludge and microorganisms; the side wall of the contact oxidation anoxic zone is provided with a submersible stirrer, so that sludge deposition is avoided, and effluent overflows into the contact oxidation aerobic zone through an opening at the upper part of the second partition plate;
(5) Biological rope filler is arranged in the contact oxidation aerobic zone, and organic pollutants are degraded and purified through the combined action of a biological film and activated sludge; the bottom is provided with a micropore aeration disc, so that sufficient oxygen is provided for biochemical reaction, and activated sludge deposition is prevented; the effluent automatically flows into the MBR membrane reaction zone through a third communication port at the lower part of the third partition plate;
(6) The curtain type MBR hollow fiber membrane is arranged in the MBR membrane reaction zone, a microporous aeration device is arranged at the bottom of the MBR membrane reaction zone to avoid sludge deposition, and sludge-water separation is realized through the MBR hollow fiber membrane; and the effluent of the MBR membrane reaction zone is pumped into an MBR membrane water production zone by an upper water suction pump and is discharged through a water outlet.
3. The method according to claim 2, wherein the wastewater is aquaculture wastewater after hydrolysis and acidification treatment, COD of the wastewater is 10000-50000mg/L, BOD is 5000-10000mg/L, total nitrogen is 1000-5000mg/L, ammonia nitrogen is 500-1000mg/L, and total phosphorus is 100-500mg/L.
4. A method according to any one of claims 2 to 3, wherein the effluent quality meets the requirements of the emission standards for pollutants for livestock and poultry farming (GB 18596-2001), COD is less than 400mg/L, BOD is less than 100mg/L, total nitrogen is less than 100mg/L, ammonia nitrogen is less than 10mg/L, and total phosphorus is less than 10mg/L.
5. The method according to any one of claims 2 to 4, wherein the MBBR aerobic zone has a residence time of 30 to 40 hours and a dissolved oxygen of 1 to 4mg/L.
6. The method of any one of claims 2-5, wherein the wastewater has a residence time in the MBBR anoxic zone of 10 to 20 hours.
7. The method of any one of claims 2-6, wherein the residence time of the central settling tank is 1-10 hours.
8. The method of any one of claims 2-7, wherein the residence time of the contact oxidation anoxic zone is from 20 to 30 hours.
9. The method of any one of claims 2 to 8, wherein the contact oxidation aerobic zone has a residence time of 40 to 50 hours and a dissolved oxygen of 1 to 4mg/L.
10. The method of any one of claims 2-9, wherein the residence time of the MBR membrane reaction zone is from 1 to 10 hours.
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