CN110981116A - Treatment process of lincomycin antibiotic production wastewater - Google Patents
Treatment process of lincomycin antibiotic production wastewater Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
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- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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- 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
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- 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
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- 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
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/343—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the pharmaceutical industry, e.g. containing antibiotics
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- 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
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Abstract
The invention relates to a treatment process of lincomycin antibiotic production wastewater, wherein acidic anaerobic bacteria decompose macromolecular organic matters which are difficult to degrade biologically in the wastewater into micromolecular organic matters which are easy to degrade biologically, and the B/C ratio of the wastewater is improved to 0.26-0.30; the aerobic bacteria oxidize and decompose the easily biodegradable micromolecular organic matters in the wastewater into CO2、H2Inorganic substances such as O and the like effectively remove COD; the ozone oxidation oxidizes and decomposes most of the residual organic matters in the water into inorganic matters; the active carbon filters and adsorbs to remove organic matters, heavy metals, ammonia nitrogen and other inorganic matters in the water, and ensures that the COD concentration of the outlet water is less than 100 mg/L. The process technology of the invention can effectively treat the waste in the production of lincomycin antibioticsThe treatment effect of the water is obvious, the effluent quality is stable, the COD concentration of the effluent is below 100mg/L, and the operation cost is reasonable.
Description
Technical Field
The invention relates to a treatment process of industrial wastewater, in particular to a treatment process of lincomycin antibiotic production wastewater.
Background
The lincomycin antibiotics production wastewater has the characteristics of high COD concentration, various toxic and harmful substances, poor biodegradability, higher SS concentration, higher salt concentration and the like, so that the lincomycin antibiotics production wastewater is one of the difficulties in the wastewater treatment of the pharmaceutical industry. Along with the stricter and more strict requirements on environmental protection and pollution prevention and treatment in China and the law control, the improvement of the wastewater treatment technology in the pharmaceutical industry is more and more urgent.
For many years, in order to obtain good treatment effect, the core technical mode of reasonable lincomycin production wastewater treatment is basically consistent with the combination of an anaerobic and aerobic biochemical method and physicochemical methods such as air flotation, precipitation, adsorption, membrane separation and the like, or the technologies such as an iron-carbon micro-electrolysis method, a Fenton reagent method, a wet oxidation method and the like are supplemented; whether the anaerobic and aerobic biochemical technology can be successfully applied or not directly determines the quality of the treatment effect and the high and low treatment cost of the lincomycin production wastewater.
In order to ensure the healthy development of the pharmaceutical industry in China, the research on the biochemical treatment technology of lincomycin production wastewater has not been stopped, and the Fenton reagent method, the electrolysis method, the wet oxidation method, the photocatalytic oxidation method, the ozone oxidation method and other advanced oxidation method technologies are gradually adopted. The technical breakthrough of the anaerobic and aerobic biochemical method for treating the lincomycin production wastewater lies in how to effectively improve COD and NH on the premise of reasonable operation cost3-N, etc. contaminant index removal rate; the technical breakthrough of the advanced oxidation method is more concerned about the feasibility of engineering implementation and the simplicity of operation management.
Disclosure of Invention
Aiming at the treatment of the lincomycin antibiotic production wastewater, the invention provides a treatment process combining an anaerobic and aerobic biochemical method and ozone and activated carbon, namely the treatment process of the lincomycin antibiotic production wastewater, which can effectively degrade organic and inorganic pollutants in the lincomycin antibiotic production wastewater, and the COD concentration of the treated effluent is below 100 mg/L.
The technical scheme of the invention is as follows:
a treatment process of lincomycin antibiotics production wastewater is characterized by comprising the following steps:
1) the lincomycin antibiotics production wastewater discharged from a production workshop automatically flows into a regulating reservoir buried underground;
2) the method comprises the following steps of (1) enabling waste water in an adjusting tank to enter a heating tank, heating by steam introduced into the heating tank, and controlling the temperature of the heated water to be 34-36 ℃;
3) the effluent of the heating tank flows into an anaerobic reaction sedimentation tank by gravity, a water inlet is positioned at the bottom of the tank, and the anaerobic reaction sedimentation tank is arranged on the ground;
adding a composite carbon source into the anaerobic reaction sedimentation tank, wherein the composite carbon source is a biodegradable organic matter, under the action of co-metabolism, the acidic anaerobic bacteria decompose a high molecular organic matter which is difficult to degrade biologically in the wastewater into a biodegradable small molecular organic matter, and the B/C ratio of effluent reaches 0.26-0.30;
anaerobic excess sludge generated by the anaerobic reaction sedimentation tank is discharged into a sludge collecting well by gravity;
4) the effluent of the anaerobic reaction sedimentation tank flows into an aerobic reaction sedimentation tank by gravity, a water inlet is positioned at the upper part of the tank, and the aerobic reaction sedimentation tank is arranged on the ground; along the water flow in the horizontal direction, an aerobic reaction zone and a sedimentation zone are sequentially arranged in the tank;
supplying compressed air to the aerobic reaction zone, keeping the concentration of dissolved oxygen in the tank between 4.0 and 6.0mg/L, and oxidizing and decomposing the biodegradable micromolecular organic matters in the wastewater into CO by aerobic bacteria2、H2O, effectively removing COD;
semi-soft elastic filler is suspended in the aerobic reaction zone and is used as a carrier of aerobic bacteria; the effluent of the aerobic reaction zone enters a subsequent sedimentation zone to complete the separation of mud and water, and the aerobic residual sludge in the aerobic reaction sedimentation tank is discharged into a regulating tank by gravity;
5) discharging effluent of the aerobic reaction sedimentation tank into an ozone contact tank by gravity flow, introducing ozone into the ozone contact tank, and oxidizing and decomposing most residual organic matters in the effluent of the contact tank into inorganic matters by the ozone;
6) the outlet water of the ozone contact tank is connected with a water distribution tank at the upper part of the activated carbon filter tank, so that organic matters, heavy metals and ammonia nitrogen inorganic matters in the inlet water can be effectively adsorbed and removed, the COD concentration of the outlet water is ensured to be less than 100mg/L, and the backwashing sludge discharge of the activated carbon filter tank is gravity-fed into a sludge collection well;
7) anaerobic excess sludge and backwash water which are accommodated in an underground sludge collecting well are deposited and discharged, and are pumped to a sludge concentration tank by a sludge lifting pump arranged at the bottom of the well, and the water content of the sludge is reduced to 97-98% from more than 99% through the gravity concentration effect;
the sludge discharged from the sludge concentration tank flows into a sludge homogenizing tank by gravity, and a composite conditioner is added to improve the dehydration performance of the sludge; pumping the sludge discharged from the sludge homogenizing tank to a sludge dewatering machine by a sludge feeding pump arranged outside the tank for further mechanical dewatering, wherein the water content of the separated sludge cake is below 60%;
8) supernatant of the sludge concentration tank and percolate of the sludge dewatering machine are discharged into an underground adjusting tank together.
Further, in the step 1), the adjusting tank has the functions of balancing water quality and adjusting water quantity, the hydraulic retention time is 4.0-6.0 h, and effluent is pumped to the heating tank by a sewage lifting pump arranged at the bottom of the tank.
Further, in the step 2), the heating pool is arranged in an overhead manner, and the hydraulic retention time is 15 min.
Further, in the step 3), the hydraulic retention time is 27.0 h; 3 water distribution zones, a suspended sludge reaction zone and a sedimentation zone are sequentially arranged in the tank along water flow in the height direction from the bottom of the tank upwards; the added composite carbon source comprises wheat bran and glucose in a weight ratio of 1.2:1, and the added amount is as follows: per m31.20kg of composite carbon source is added into water.
Further, in the step 4), the hydraulic retention time of the aerobic reaction sedimentation tank is 15.0 h.
Further, in the step 5), the effluent of the aerobic reaction sedimentation tank is accessed from the upper part of an ozone contact tank, the ozone contact tank is arranged on the ground, and the hydraulic retention time is 20 min; the dosage of the ozone used is as follows: per m3Adding 20.0-30.0 g of ozone into the water.
Further, in the step 6), the activated carbon filter is arranged in a semi-underground mode, and the hydraulic retention time is 40 min; the activated carbon filter is filled with granular activated carbon with the height of 1.50 m.
Further, the components of the compound conditioner added in the step 7) are ferrous sulfate and lime which are heavyThe dosage ratio is 0.6:1, and the dosage is as follows: per m30.25kg of composite conditioner is added into the sludge.
According to the composite carbon source added during the anaerobic reaction, under the effect of co-metabolism, the acidic anaerobic bacteria decompose macromolecular organic matters which are difficult to degrade in the wastewater into micromolecular organic matters which are easy to degrade, so that the B/C ratio of the wastewater is improved to 0.26-0.30; the aerobic bacteria oxidize and decompose the easily biodegradable micromolecular organic matters in the wastewater into CO2、H2Inorganic substances such as O and the like effectively remove COD; ozone oxidation, which oxidizes and decomposes most of residual organic matters in water into inorganic matters; filtering with activated carbon, adsorbing and removing organic matters, heavy metals, ammonia nitrogen and other inorganic matters in the water, and ensuring that the COD concentration of the effluent is less than 100 mg/L; wet sludge produced in the wastewater treatment process is subjected to gravity concentration to remove supernatant, a composite conditioner consisting of ferrous sulfate and lime is added to improve the dehydration performance of the concentrated sludge, and then a sludge dehydrator is used for mechanical dehydration, so that the water content of a dehydrated mud cake is below 60%.
Drawings
Fig. 1 is a schematic diagram of the operation of the present invention.
Detailed Description
As shown in figure 1, the method for treating the lincomycin antibiotics production wastewater comprises the following main steps:
1) and the lincomycin antibiotics production wastewater discharged from the production workshop automatically flows into the regulating tank. The adjusting tank has the functions of uniformly mixing water quality and adjusting water quantity, the hydraulic retention time is 4.0-6.0 h, and the effluent is pumped to the heating tank by a sewage lifting pump arranged at the bottom of the tank.
2) And the wastewater enters a heating pool. And heating by steam introduced into the heating tank, controlling the temperature of the heated water to be 34-36 ℃, and controlling the hydraulic retention time of the heating tank to be 15 min.
3) And the effluent of the heating tank flows into an anaerobic reaction sedimentation tank by gravity. The hydraulic retention time of the anaerobic reaction sedimentation tank is 27.0 h.
The composite carbon source added in the anaerobic reaction sedimentation tank comprises wheat bran and glucose, the weight ratio of the wheat bran to the glucose is 1.2:1, and the adding amount is as follows: per m3Water throwing1.20kg of composite carbon source was added.
The composite carbon source is a biodegradable organic matter, under the effect of co-metabolism, the acidic anaerobic bacteria decompose a high molecular organic matter which is difficult to biodegrade in the wastewater into a small molecular organic matter which is easy to biodegrade, and the B/C ratio of the effluent reaches 0.26-0.30.
Anaerobic excess sludge generated by the anaerobic reaction sedimentation tank is drained into a sludge collecting well by gravity.
4) And the effluent of the anaerobic reaction sedimentation tank automatically flows into the aerobic reaction sedimentation tank by gravity. The aerobic reaction sedimentation tank is divided into 2 areas of an aerobic reaction area and a sedimentation area, and the hydraulic retention time is 15.0h in total.
Supplying compressed air to the aerobic reaction zone, keeping the concentration of Dissolved Oxygen (DO) in the tank between 4.0-6.0 mg/L, and oxidizing and decomposing the biodegradable micromolecular organic matters in the wastewater into CO by aerobic bacteria2、H2Inorganic substances such as O and the like effectively remove COD; semi-soft elastic filler is suspended in the aerobic reaction zone and used as a carrier of aerobic bacteria.
And the effluent of the aerobic reaction zone enters a subsequent sedimentation zone to complete the separation of mud and water. And aerobic residual sludge in the aerobic reaction sedimentation tank is discharged into the regulating tank by gravity.
5) And the effluent of the aerobic reaction sedimentation tank is discharged into the ozone contact tank by gravity flow. The hydraulic retention time of the ozone contact tank is 20 min.
Ozone is introduced into the ozone contact tank, most of residual organic matters in the water from the contact tank are oxidized and decomposed into inorganic matters by the ozone, and the adding amount of the ozone is as follows: per m3Adding 20.0-30.0 g of ozone into the water.
6) And the effluent of the ozone contact tank automatically flows into the activated carbon filter tank by gravity. The hydraulic retention time of the activated carbon filter is 40 min. The activated carbon filter is filled with granular activated carbon with the height of 1.50m, can effectively adsorb and remove organic matters, heavy metals, ammonia nitrogen and other inorganic matters in the incoming water, and ensures that the COD concentration of the outgoing water is less than 100 mg/L. And the back-flushing sludge discharge gravity of the activated carbon filter tank automatically flows and is discharged into the sludge collecting well.
7) Anaerobic excess sludge and backwash water discharged into the sludge collecting well are deposited and discharged, the sludge is pumped into a sludge concentration tank by a sludge lifting pump arranged at the bottom of the well, and the water content of the sludge is reduced to 97-98% from more than 99% through the gravity concentration effect;
the sludge discharged from the sludge concentration tank flows into a sludge homogenizing tank by gravity, a composite conditioner is added to improve the dehydration performance of the sludge, the composite conditioner comprises ferrous sulfate and lime in a weight ratio of 0.6:1, and the adding amount is as follows: per m3Adding 0.25kg of composite conditioner into the sludge;
and pumping the sludge discharged from the sludge homogenizing tank to a sludge dewatering machine by a sludge feeding pump arranged outside the tank for further mechanical dewatering, wherein the water content of the separated sludge cake is below 60%.
8) Supernatant of the sludge concentration tank and percolate of the sludge dewatering machine are discharged into the regulating tank together.
The process technology of the invention can effectively treat the lincomycin antibiotics production wastewater, has obvious treatment effect, stable effluent quality, effluent COD concentration of less than 100mg/L and reasonable operation cost.
Claims (8)
1. A treatment process of lincomycin antibiotics production wastewater is characterized by comprising the following steps:
1) the lincomycin antibiotics production wastewater discharged from a production workshop automatically flows into a regulating reservoir buried underground;
2) the method comprises the following steps of (1) enabling waste water in an adjusting tank to enter a heating tank, heating by steam introduced into the heating tank, and controlling the temperature of the heated water to be 34-36 ℃;
3) the effluent of the heating tank flows into an anaerobic reaction sedimentation tank by gravity, a water inlet is positioned at the bottom of the tank, and the anaerobic reaction sedimentation tank is arranged on the ground;
adding a composite carbon source into the anaerobic reaction sedimentation tank, wherein the composite carbon source is a biodegradable organic matter, under the action of co-metabolism, the acidic anaerobic bacteria decompose a high molecular organic matter which is difficult to degrade biologically in the wastewater into a biodegradable small molecular organic matter, and the B/C ratio of effluent reaches 0.26-0.30;
anaerobic excess sludge generated by the anaerobic reaction sedimentation tank is discharged into a sludge collecting well by gravity;
4) the effluent of the anaerobic reaction sedimentation tank flows into an aerobic reaction sedimentation tank by gravity, a water inlet is positioned at the upper part of the tank, and the aerobic reaction sedimentation tank is arranged on the ground; along the water flow in the horizontal direction, an aerobic reaction zone and a sedimentation zone are sequentially arranged in the tank;
supplying compressed air to the aerobic reaction zone, keeping the concentration of dissolved oxygen in the tank between 4.0 and 6.0mg/L, and oxidizing and decomposing the biodegradable micromolecular organic matters in the wastewater into CO by aerobic bacteria2、H2O, effectively removing COD;
semi-soft elastic filler is suspended in the aerobic reaction zone and is used as a carrier of aerobic bacteria; the effluent of the aerobic reaction zone enters a subsequent sedimentation zone to complete the separation of mud and water, and the aerobic residual sludge in the aerobic reaction sedimentation tank is discharged into a regulating tank by gravity;
5) discharging effluent of the aerobic reaction sedimentation tank into an ozone contact tank by gravity flow, introducing ozone into the ozone contact tank, and oxidizing and decomposing most residual organic matters in the effluent of the contact tank into inorganic matters by the ozone;
6) the outlet water of the ozone contact tank is connected with a water distribution tank at the upper part of the activated carbon filter tank, so that organic matters, heavy metals and ammonia nitrogen inorganic matters in the inlet water can be effectively adsorbed and removed, and the backwashing sludge discharge gravity of the activated carbon filter tank automatically discharges the sludge into a sludge collection well;
7) anaerobic excess sludge and backwash water which are accommodated in an underground sludge collecting well are deposited and discharged, and are pumped to a sludge concentration tank by a sludge lifting pump arranged at the bottom of the well, and the water content of the sludge is reduced to 97-98% from more than 99% through the gravity concentration effect;
the sludge discharged from the sludge concentration tank flows into a sludge homogenizing tank by gravity, and a composite conditioner is added to improve the dehydration performance of the sludge; pumping the sludge discharged from the sludge homogenizing tank to a sludge dewatering machine by a sludge feeding pump arranged outside the tank for further mechanical dewatering, wherein the water content of the separated sludge cake is below 60%;
8) supernatant of the sludge concentration tank and percolate of the sludge dewatering machine are discharged into an underground adjusting tank together.
2. The process for treating lincomycin antibiotics production wastewater as claimed in claim 1, wherein in the step 1), the regulating tank has the functions of balancing water quality and regulating water quantity, the hydraulic retention time is 4.0-6.0 h, and effluent is pumped to the heating tank by a sewage lifting pump arranged at the bottom of the tank.
3. The process for treating lincomycin antibiotics production wastewater as claimed in claim 1, wherein in the step 2), the heating tank is arranged in an overhead manner, and the hydraulic retention time is 15 min.
4. The process for treating lincomycin antibiotics production wastewater as claimed in claim 1, wherein in the step 3), the hydraulic retention time is 27.0 h; 3 water distribution zones, a suspended sludge reaction zone and a sedimentation zone are sequentially arranged in the tank along water flow in the height direction from the bottom of the tank upwards; the added composite carbon source comprises wheat bran and glucose in a weight ratio of 1.2:1, and the added amount is as follows: per m31.20kg of composite carbon source is added into water.
5. The process for treating lincomycin antibiotics production wastewater as claimed in claim 1, wherein in the step 4), the hydraulic retention time of the aerobic reaction sedimentation tank is 15.0 h.
6. The process for treating lincomycin antibiotics wastewater as claimed in claim 1, wherein in the step 5), the effluent of the aerobic reaction sedimentation tank is connected with the upper part of an ozone contact tank, the ozone contact tank is arranged on the ground, and the hydraulic retention time is 20 min; the dosage of the ozone used is as follows: per m3Adding 20.0-30.0 g of ozone into the water.
7. The process for treating lincomycin antibiotics production wastewater as claimed in claim 1, wherein in the step 6), the activated carbon filter is arranged in a semi-underground manner, and the hydraulic retention time is 40 min; the activated carbon filter is filled with granular activated carbon with the height of 1.50 m.
8. The process for treating lincomycin antibiotics production wastewater as claimed in claim 1, wherein the compound conditioner added in step 7) comprises ferrous sulfate and lime in a weight ratio of 0.6:1, and the adding amount is as follows: per m30.25kg of composite conditioner is added into the sludge.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113526824A (en) * | 2021-07-06 | 2021-10-22 | 绍兴市上虞区供水有限公司 | Heat energy and solar energy linkage drying sludge treatment equipment and process |
| CN115093020A (en) * | 2022-07-12 | 2022-09-23 | 国环电池科技(苏州)有限公司 | Detoxification method of heavy metal sewage anaerobic biological section |
| CN118388092A (en) * | 2024-06-24 | 2024-07-26 | 河北旺效环保工程有限公司 | Cooperative treatment process for hospital sewage |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101565261A (en) * | 2009-06-03 | 2009-10-28 | 南京大学 | Treatment process for medical intermediate production waste water |
| CN103011517A (en) * | 2012-12-24 | 2013-04-03 | 北京城市排水集团有限责任公司 | Device and control method for safety guarantee of municipal sewage recycling |
| CN105984991A (en) * | 2015-02-02 | 2016-10-05 | 江苏中金环保科技有限公司 | Process for advanced treatment of sewage |
| CN106477824A (en) * | 2016-11-28 | 2017-03-08 | 清华大学深圳研究生院 | A kind of method and system for removing residual antibiotic in eliminating water |
| CN206736017U (en) * | 2017-03-20 | 2017-12-12 | 四川科伦药业股份有限公司 | Antibiotic waste water processing unit |
| KR101903043B1 (en) * | 2018-04-27 | 2018-10-01 | 주식회사 대성그린테크 | Advanced oxidation, adsoption system for control of micropollutants in wastewater |
| EP3481780A2 (en) * | 2016-07-11 | 2019-05-15 | Curozone Ireland Limited | Recirculating, purifying, disinfecting, cooling, decontaminating, feedback controlled water system for drinking water and other uses to improve health and well being of animals and humans |
-
2019
- 2019-12-27 CN CN201911375422.6A patent/CN110981116A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101565261A (en) * | 2009-06-03 | 2009-10-28 | 南京大学 | Treatment process for medical intermediate production waste water |
| CN103011517A (en) * | 2012-12-24 | 2013-04-03 | 北京城市排水集团有限责任公司 | Device and control method for safety guarantee of municipal sewage recycling |
| CN105984991A (en) * | 2015-02-02 | 2016-10-05 | 江苏中金环保科技有限公司 | Process for advanced treatment of sewage |
| EP3481780A2 (en) * | 2016-07-11 | 2019-05-15 | Curozone Ireland Limited | Recirculating, purifying, disinfecting, cooling, decontaminating, feedback controlled water system for drinking water and other uses to improve health and well being of animals and humans |
| CN106477824A (en) * | 2016-11-28 | 2017-03-08 | 清华大学深圳研究生院 | A kind of method and system for removing residual antibiotic in eliminating water |
| CN206736017U (en) * | 2017-03-20 | 2017-12-12 | 四川科伦药业股份有限公司 | Antibiotic waste water processing unit |
| KR101903043B1 (en) * | 2018-04-27 | 2018-10-01 | 주식회사 대성그린테크 | Advanced oxidation, adsoption system for control of micropollutants in wastewater |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113526824A (en) * | 2021-07-06 | 2021-10-22 | 绍兴市上虞区供水有限公司 | Heat energy and solar energy linkage drying sludge treatment equipment and process |
| CN115093020A (en) * | 2022-07-12 | 2022-09-23 | 国环电池科技(苏州)有限公司 | Detoxification method of heavy metal sewage anaerobic biological section |
| CN115093020B (en) * | 2022-07-12 | 2023-10-10 | 华辰环保能源(广州)有限责任公司 | Detoxification method of anaerobic biological section of heavy metal sewage |
| CN118388092A (en) * | 2024-06-24 | 2024-07-26 | 河北旺效环保工程有限公司 | Cooperative treatment process for hospital sewage |
| CN118388092B (en) * | 2024-06-24 | 2024-09-17 | 河北旺效环保工程有限公司 | Cooperative treatment process for hospital sewage |
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Application publication date: 20200410 |