CN218435384U - High enriched pharmacy effluent disposal system - Google Patents
High enriched pharmacy effluent disposal system Download PDFInfo
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- CN218435384U CN218435384U CN202222446110.3U CN202222446110U CN218435384U CN 218435384 U CN218435384 U CN 218435384U CN 202222446110 U CN202222446110 U CN 202222446110U CN 218435384 U CN218435384 U CN 218435384U
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- electrolysis reaction
- pipe connection
- reaction tower
- treatment system
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- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 34
- 239000012528 membrane Substances 0.000 claims abstract description 20
- 238000004062 sedimentation Methods 0.000 claims abstract description 18
- 238000000034 method Methods 0.000 claims abstract description 9
- 239000010802 sludge Substances 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 11
- 238000004065 wastewater treatment Methods 0.000 claims description 10
- 239000002002 slurry Substances 0.000 claims description 7
- 238000005273 aeration Methods 0.000 claims description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- 238000000108 ultra-filtration Methods 0.000 claims description 6
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 claims description 5
- 238000005276 aerator Methods 0.000 claims description 3
- 239000012510 hollow fiber Substances 0.000 claims description 3
- 238000009434 installation Methods 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 230000003139 buffering effect Effects 0.000 abstract description 8
- 230000001590 oxidative effect Effects 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 238000012423 maintenance Methods 0.000 abstract description 2
- 239000007800 oxidant agent Substances 0.000 abstract description 2
- 239000002351 wastewater Substances 0.000 description 24
- 230000001105 regulatory effect Effects 0.000 description 12
- 238000007599 discharging Methods 0.000 description 8
- 239000000203 mixture Substances 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 4
- 230000000593 degrading effect Effects 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000007062 hydrolysis Effects 0.000 description 3
- 238000006460 hydrolysis reaction Methods 0.000 description 3
- 241001148470 aerobic bacillus Species 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 150000002894 organic compounds Chemical class 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 208000034699 Vitreous floaters Diseases 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003115 biocidal effect Effects 0.000 description 1
- 238000006065 biodegradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 239000000546 pharmaceutical excipient Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 1
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The utility model discloses a high enriched pharmacy effluent disposal system, include: the grid well, the grid well has equalizing basin and equalizing basin through pipe connection and has little electrolysis reaction tower, little electrolysis reaction tower passes through pipe connection IC anaerobism tower through pipeline buffering sedimentation tank and buffering sedimentation tank, IC anaerobism tower passes through pipe connection SBRThe reactor and SBR reactor are connected with the MBR tank through a pipeline. The utility model discloses a little electrolysis reaction tower carries out the preliminary treatment, can effectively reduce COD content, improves the biodegradability, has utilized the Fe of the production of electrolysis process simultaneously 2+ The use amount of the oxidant is reduced, the operation cost is reduced, the impact load resistance of the IC anaerobic tower and the SBR reactor is high, the cost is low, the nitrification and denitrification effects are good, the subsequent treatment load can be reduced, the MBR membrane pollution is reduced, the investment cost of the system is low, the structure is compact, the occupied area is small, the automation degree is high, and the management and the maintenance are convenient.
Description
Technical Field
The utility model relates to a waste water treatment system technical field, more specifically are a high enriched pharmacy effluent disposal system.
Background
The chemical synthesis type pharmaceutical wastewater is the wastewater which is difficult to treat in the pharmaceutical industry wastewater, and can be roughly divided into four types, namely mother liquor wastewater, flushing wastewater, residual liquid recovery, auxiliary process drainage, domestic sewage and the like. The chemical synthesis pharmaceutical wastewater has COD up to 30000mg/L, high salinity, high chroma, difficult direct biodegradation and great influence on the surrounding environment. In addition, the residual antibiotic components in the wastewater have inhibitory effect on microorganisms in the biological treatment system, the microorganisms are difficult to culture, and some raw materials or products have biological toxicity.
Chinese patent CN215480394U discloses a pharmaceutical wastewater treatment system, which comprises a treatment system of micro-electrolysis + Fenton pool + UASB + A/O/A/O + MBR + ozone treatment and the like, and the system has the advantages of long process route, large floor area and high investment cost. Chinese patent CN112979094A provides a technological method for treating production wastewater of pharmaceutic adjuvants, which adopts a process of a comprehensive adjusting tank + a hydrolysis acidification tank + SBR + MBR + discharge tank, and because the pretreatment water quality does not meet the MBR water inlet requirement, the effluent water quality cannot meet the discharge standard, and meanwhile, the MBR membrane is seriously polluted, so that the MBR membrane cleaning frequency is increased, and the MBR service life is shortened. Therefore, a new technical solution needs to be provided.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a high enriched pharmacy effluent disposal system has solved preliminary treatment quality of water and has reached MBR requirement of intaking, leads to out water quality of water and can not reach emission standard, and MBR membrane pollutes seriously simultaneously, increases MBR membrane cleaning frequency, shortens MBR life's problem.
In order to achieve the above object, the utility model provides a following technical scheme: a high-consistency pharmaceutical wastewater treatment system comprising: the grid well, the grid well has equalizing basin and equalizing basin through pipe connection and has little electrolysis reaction tower, little electrolysis reaction tower passes through pipe connection IC anaerobism tower through pipeline buffering sedimentation tank and buffering sedimentation tank, IC anaerobism tower passes through pipe connection SBR reactor and passes through the pipe connection MBR pond, little electrolysis reaction tower, buffering sedimentation tank, IC anaerobism tower, SBR reactor, MBR pond all link to each other and the mud pipe has sludge treatment equipment through pipe connection with the mud pipe through the pipeline, IC anaerobism tower has marsh gas collection device through pipe connection.
As a preferred embodiment of the utility model, the grid well is made of stainless steel materials, the grid gap is 1-50 mm, and the installation gradient is 30-80 degrees.
As a preferred embodiment of the utility model, a pre-aeration device and a liquid level control device are arranged in the regulating reservoir.
As a preferred embodiment of the utility model, little electrolysis reaction tower adopts the little electrolysis tower of iron carbon, be equipped with aeration head, supporting layer, packing layer and bottom in the little electrolysis reaction tower and be provided with the mud pipe.
As a preferred embodiment of the utility model, a three-phase separator, a gas-liquid separator and a slurry downcomer are arranged in the IC anaerobic tower.
As a preferred embodiment of the utility model, the bottom of the SBR reactor is provided with a sludge discharge port and an aerator and is provided with water outlets with different heights.
As a preferred embodiment of the present invention, an ultrafiltration membrane is disposed in the MBR tank, and the ultrafiltration membrane may be one of a hollow fiber membrane or a flat membrane.
Compared with the prior art, the beneficial effects of the utility model are as follows:
the utility model discloses a little electrolysis reaction tower carries out the preliminary treatment, can effectively reduce COD content, improves the biodegradability, has utilized the Fe of the production of electrolysis process simultaneously 2+ The use amount of the oxidant is reduced, the operation cost is reduced, the impact load resistance of the IC anaerobic tower and the SBR reactor is high, the cost is low, the nitrification and denitrification effects are good, the subsequent treatment load can be reduced, the MBR membrane pollution is reduced, the investment cost of the system is low, the structure is compact, the occupied area is small, the automation degree is high, and the management and the maintenance are convenient.
Drawings
Fig. 1 is the overall structure diagram of the present invention.
In the figure: 1. a grid well; 2. a regulating tank; 3. a micro-electrolysis reaction tower; 4. a buffer sedimentation tank; 5. an IC anaerobic tower; 6. an SBR reactor; 7. an MBR tank; 8. a biogas collection device; 9. a sludge treatment device.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Referring to fig. 1, the present invention provides a technical solution: a high-consistency pharmaceutical wastewater treatment system comprising: the device comprises a grid well 1, wherein the grid well 1 is connected with an adjusting tank 2 through a pipeline, the adjusting tank 2 is connected with a micro-electrolysis reaction tower 3 through a pipeline, the micro-electrolysis reaction tower 3 is connected with an IC anaerobic tower 5 through a pipeline buffering sedimentation tank 4 and a buffering sedimentation tank 4, the IC anaerobic tower 5 is connected with an SBR reactor 6 through a pipeline, the SBR reactor 6 is connected with an MBR tank 7 through a pipeline, the micro-electrolysis reaction tower 3, the buffering sedimentation tank 4, the IC anaerobic tower 5, the SBR reactor 6 and the MBR tank 7 are connected with a sludge discharge pipe through pipelines, the sludge discharge pipe is connected with a sludge treatment device 9 through a pipeline, the IC anaerobic tower 5 is connected with a methane collection device 8 through a pipeline, and waste water intercepts large suspended matters or floating matters through the grid well 1 and is lifted to the adjusting tank 2 through a lifting pump; homogenizing the water quality and quantity in the regulating tank 2, and regulating COD, temperature and pH; and (2) extracting the effluent from the regulating reservoir 2 to a micro-electrolysis reaction tower 3 through a lift pump, regulating the pH to 2-4 in the micro-electrolysis reaction tower 3, adding scrap iron and activated carbon according to the iron-carbon mass ratio of 4:5, electrolyzing for 2-6 hours, adding 30% hydrogen peroxide for oxidizing hydrolysis, regulating the pH to 8.5-9.0, and adding boric sludge and PAM for flocculation precipitation. The micro-electrolysis reaction tower 3 can hydrolyze macromolecular organic matters in the wastewater into micromolecular organic matters to improve the biochemical property of pharmaceutical wastewater, the pretreated wastewater enters a buffer sedimentation tank 4 for sedimentation, the pretreated wastewater enters a mixing zone at the bottom of an IC anaerobic tower 5 after water quality is adjusted, the mixture is fully mixed with an internal circulation slurry mixture from a slurry descending pipe and then enters a granular sludge expansion bed zone for COD biochemical degradation, most of inflow COD is degraded to generate a large amount of biogas, the biogas is collected by a primary three-phase separator, the mixture of the biogas and water rises along a pneumatic control lifting pipe to a gas-liquid separator at the top, the biogas is separated from the sludge and the water and then is output to a biogas collecting device 8 for recycling, the IC anaerobic tower 5 can remove most of organic compounds to reduce the organic chemical load at the SBR stage, the water yield automatically flows out to the SBR reactor 6, and the SBR reactor 6 consists of 5 processes of an inflow stage, a reaction stage, a sedimentation stage, a drainage stage and an idle stage to form a period; controlling the pH value in the SBR reactor 6 to be 5-8, the water temperature to be 20-30 ℃, the DO to be 1.0-5.0mg/L, and each period time to be 6-12h, fully degrading organic matters in the wastewater, realizing water-sludge separation by standing, discharging the wastewater into an MBR tank 7 by an SBR decanter, discharging residual sludge into a sludge treatment system, further degrading COD (chemical oxygen demand) in the wastewater by using aerobic bacteria in the MBR tank 7, performing solid-liquid separation on water and activated sludge by using an MBR membrane, discharging the separated residual sludge into the sludge treatment system, and directly discharging produced water to reach the first-grade A standard of the industry.
Further improved, as shown in fig. 1: the grid well 1 is made of stainless steel materials, the grid gap is 1-50 mm, and the installation inclination is 30-80 degrees.
Further improved, as shown in fig. 1: a pre-aeration device and a liquid level control device are arranged in the adjusting tank 2.
Further improved, as shown in fig. 1: the micro-electrolysis reaction tower 3 adopts an iron-carbon micro-electrolysis tower, an aeration head, a bearing layer and a packing layer are arranged in the micro-electrolysis reaction tower 3, and a sludge discharge pipe is arranged at the bottom of the micro-electrolysis reaction tower.
Further improved, as shown in fig. 1: and a three-phase separator, a gas-liquid separator and a slurry descending pipe are arranged in the IC anaerobic tower 5.
Further improved, as shown in fig. 1: and a sludge discharge port and an aerator are arranged at the bottom of the SBR reactor 6, and water discharge ports with different heights are arranged.
Further improved, as shown in fig. 1: an ultrafiltration membrane is arranged in the MBR tank 7, and the ultrafiltration membrane can be one of a hollow fiber membrane or a flat membrane.
The waste water of the utility model is intercepted by the grid well 1 with larger suspended matters or floaters and is lifted to the adjusting tank 2 by the lift pump; homogenizing the water quality and quantity in the regulating tank 2, and regulating COD, temperature and pH; and (2) extracting the effluent from the regulating reservoir 2 to a micro-electrolysis reaction tower 3 through a lift pump, regulating the pH to 2-4 in the micro-electrolysis reaction tower 3, adding scrap iron and activated carbon according to the iron-carbon mass ratio of 4:5, electrolyzing for 2-6 hours, adding 30% hydrogen peroxide for oxidizing hydrolysis, regulating the pH to 8.5-9.0, and adding boric sludge and PAM for flocculation precipitation. The micro-electrolysis reaction tower 3 can hydrolyze macromolecular organic matters in the wastewater into micromolecular organic matters to improve the biochemical property of the pharmaceutical wastewater, the pretreated wastewater enters a buffer sedimentation tank 4 for sedimentation, the wastewater enters a mixing zone at the bottom of an IC anaerobic tower 5 after water quality is adjusted, the mixture is fully mixed with an internal circulation slurry mixture from a slurry downcomer and then enters a granular sludge expanded bed zone for COD biochemical degradation, most of inflow COD is degraded to generate a large amount of biogas, the biogas is collected by a primary three-phase separator, the mixture of the biogas and water rises along a pneumatic control riser to a gas-liquid separator at the top, the biogas is separated from the sludge and water and then output to a biogas collecting device 8 for recycling, the IC anaerobic tower 5 can remove most of organic compounds to reduce the organic chemical load at an SBR stage, the water yield automatically flows out to an SBR reactor 6, and the SBR reactor 6 consists of 5 working procedures of an inflow stage, a reaction stage, a sedimentation stage, a drainage stage and an idle stage to form a period; controlling the pH value in the SBR reactor 6 to be 5-8, the water temperature to be 20-30 ℃, the DO to be 1.0-5.0mg/L, and each period time to be 6-12h, fully degrading organic matters in the wastewater, realizing water-sludge separation by standing, discharging the wastewater into an MBR tank 7 by an SBR decanter, discharging the residual sludge into a sludge treatment system, further degrading COD (chemical oxygen demand) in the wastewater by the MBR tank 7 by using aerobic bacteria, performing solid-liquid separation on water and activated sludge by an MBR membrane, discharging the separated residual sludge into the sludge treatment system, and directly discharging the produced water to reach the first-level A standard of the industry.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described in the foregoing embodiments, or equivalents may be substituted for elements thereof. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (7)
1. The utility model provides a high enriched pharmacy effluent disposal system which characterized in that: the method comprises the following steps: grid well (1), there are equalizing basin (2) and equalizing basin (2) through pipe connection in grid well (1) have little electrolysis reaction tower (3), little electrolysis reaction tower (3) are through pipe connection IC anaerobism tower (5) in pipeline buffer sedimentation tank (4) and buffer sedimentation tank (4), IC anaerobism tower (5) are through pipe connection SBR reactor (6) and SBR reactor (6) through pipe connection MBR pond (7), little electrolysis reaction tower (3), buffer sedimentation tank (4), IC anaerobism tower (5), SBR reactor (6), MBR pond (7) all link to each other and the mud pipe has sludge treatment device (9) through pipe connection with the mud pipe through the pipeline, IC anaerobism tower (5) have marsh gas collection device (8) through pipe connection.
2. The high-concentration pharmaceutical wastewater treatment system according to claim 1, wherein: the grid well (1) is made of stainless steel materials, the grid gap is 1-50 mm, and the installation inclination is 30-80 degrees.
3. The high-concentration pharmaceutical wastewater treatment system according to claim 1, wherein: a pre-aeration device and a liquid level control device are arranged in the adjusting tank (2).
4. The high-concentration pharmaceutical wastewater treatment system according to claim 1, wherein: the micro-electrolysis reaction tower (3) adopts an iron-carbon micro-electrolysis tower, an aeration head, a supporting layer and a packing layer are arranged in the micro-electrolysis reaction tower (3), and a sludge discharge pipe is arranged at the bottom of the micro-electrolysis reaction tower.
5. The high-concentration pharmaceutical wastewater treatment system according to claim 1, wherein: and a three-phase separator, a gas-liquid separator and a slurry descending pipe are arranged in the IC anaerobic tower (5).
6. The high-concentration pharmaceutical wastewater treatment system according to claim 1, wherein: and a sludge discharge port and an aerator are arranged at the bottom of the SBR reactor (6) and water discharge ports with different heights are arranged.
7. The high-concentration pharmaceutical wastewater treatment system according to claim 1, wherein: an ultrafiltration membrane is arranged in the MBR tank (7), and the ultrafiltration membrane can be one of a hollow fiber membrane or a flat membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222446110.3U CN218435384U (en) | 2022-09-13 | 2022-09-13 | High enriched pharmacy effluent disposal system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222446110.3U CN218435384U (en) | 2022-09-13 | 2022-09-13 | High enriched pharmacy effluent disposal system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218435384U true CN218435384U (en) | 2023-02-03 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202222446110.3U Active CN218435384U (en) | 2022-09-13 | 2022-09-13 | High enriched pharmacy effluent disposal system |
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| Country | Link |
|---|---|
| CN (1) | CN218435384U (en) |
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- 2022-09-13 CN CN202222446110.3U patent/CN218435384U/en active Active
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