CN105621798A - Pharmaceutical wastewater treatment system and technique - Google Patents
Pharmaceutical wastewater treatment system and technique Download PDFInfo
- Publication number
- CN105621798A CN105621798A CN201610017258.1A CN201610017258A CN105621798A CN 105621798 A CN105621798 A CN 105621798A CN 201610017258 A CN201610017258 A CN 201610017258A CN 105621798 A CN105621798 A CN 105621798A
- Authority
- CN
- China
- Prior art keywords
- pond
- tank
- pool
- grid
- waste water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
-
- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F1/722—Oxidation by peroxides
-
- 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
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
-
- 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
- C02F3/28—Anaerobic digestion processes
-
- 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
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
Abstract
The invention relates to a pharmaceutical wastewater treatment system and technique. The system is characterized by comprising a grid tank, a regulating tank, a coagulative precipitation tank, a hydrolysis acidification tank, a UASB (upflow anaerobic sludge blanket) reaction tank, an intermediate precipitation tank, an anoxic tank, an aerobic tank, a secondary precipitation tank, an intermediate water tank, a Fenton oxidation tank, a neutralizing and degassing tank and a final precipitation tank which are sequentially arranged along the wastewater flow direction. The technique comprises the following steps: 1) the wastewater is sent to a sewage treatment station and naturally flows into the grid tank, wherein the grid spacing of the grid tank is 5-8mm; and 2) the wastewater flowing out of the grid tank enters the regulating tank, wherein the regulating tank is previously provided with wastewater with the COD (chemical oxygen demand) of 3000-6000 mg/L. The system and technique have the advantages of high treatment efficiency and favorable effect.
Description
Technical field
The present invention relates to pharmaceutical technology field, specifically a kind of pharmacy wastewater treatment system and technique.
Background technology
At present, along with the fast development of pharmaceuticals industry, the pollution control problem of pharmacy waste water is more and more severeer. Pharmacy waste water belongs to one of intractable industrial wastewater, it is because medicament categories is different, production technology is different, it is big that it has component difference, complicated components, amount of pollutant is many, COD is high, hard-degraded substance is many, the features such as strong toxicity, and the waste water in pharmaceutical factory is generally intermittent discharge, the kind of product and number change are relatively big, cause that the kind of the water quality of waste water, the water yield and pollutant changes greatly, bringing great difficulty to improvement, generally traditional stain disease processes technique can not meet the society process requirement to pharmacy waste water.
Summary of the invention
The technical problem to be solved is: provide a kind for the treatment of effeciency height, effective pharmacy wastewater treatment system and technique.
The technical solution adopted in the present invention is: provide a kind of pharmacy wastewater treatment system and technique, described system include flowing to waste water set gradually grid pond, regulating reservoir, coagulative precipitation tank, hydrolysis acidification pool, UASB reaction tank, medium sediment pool, anoxic pond, Aerobic Pond, second pond, intermediate pool, Fenton oxidation pond, neutralize degassed pond and final deposition pool; The flow process of described technique is as follows:
1) waste water flows automatically after delivering to Sewage Disposal into grid pond, and the grid gap in grid pond is 5-8mm;
2) waste water that grid pond is flowed out enters regulating reservoir, the waste water that regulating reservoir has COD to be 3000 ~ 6000mg/L in advance;
3) using sewage pump to be evacuated in coagulative precipitation tank by regulating reservoir water outlet, add flocculant PAC and coagulant PAM, PAC concentration is 5% in coagulative precipitation tank, the waste water that dosage is 100t adds 20kg; PAM concentration is 0.1%, and the waste water that dosage is 100t adds 2kg;
4) coagulative precipitation tank supernatant is from flowing into hydrolysis acidification pool, adds the NaOH of 10%, pH regulator to 6.5-7, and adds carbamide and phosphate fertilizer, and the ratio of adding is COD:N:P=100:5:1;
5) use sewage pump to be evacuated in UASB reaction tank by hydrolysis acidification pool water outlet, before entering UASB reaction tank, SS is dropped to less than 100;
6) water outlet of UASB reaction tank is from flowing into medium sediment pool, and by mud-water separation in medium sediment pool, sludge reflux is to UASB reaction tank or the anoxic pond of step 7);
7) medium sediment pool water outlet is from flowing into anoxic pond, has activated sludge, dissolved oxygen to control to hang with biologic packing material in 0.2 ~ 0.5mg/L, anoxic pond in anoxic pond;
8) anoxic pond water outlet flow to Aerobic Pond, has activated sludge, dissolved oxygen to control to hang with biologic packing material in 2 ~ 4mg/L, Aerobic Pond in Aerobic Pond;
9) Aerobic Pond water outlet is from flowing in second pond, in second pond, mud and sewage is carried out precipitate and separate, and sludge reflux is to anoxic pond, and excess sludge is discharged to sludge concentration tank and carries out concentration;
10) secondary clarifier effluent is from flowing into intermediate pool, adds sulphuric acid in intermediate pool, and regulating pH value is 3;
11) use sewage pump that intermediate pool water is evacuated to Fenton oxidation pond, add H2O2Oxidant and Fe2+Catalyst, the water outlet of Fenton oxidation pond is from flowing in the degassed pond of neutralization;
12) in and degassed pond in add alkali liquor, PH is adjusted to 8, is subsequently adding the waste water that PAM, PAM dosage is 100t and adds 2kg;
13) neutralize waste water in degassed pond, from flowing in final deposition pool, to carry out precipitating the separation realizing sewage and mud.
Pharmacy wastewater treatment system of the present invention and technique have the advantage that
1, coagulating sedimentation, can remove difficult degradation COD in advance, remove substantial amounts of float simultaneously.
2, adopting UASB anaerobic biochemical treatment technology, anoxia, aerobic contact oxidation technique, Fenton advanced oxidation processes treatment technology, high treating effect, efficiency is high.
3, stable water outlet, automaticity is high.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of the pharmacy wastewater treatment system of the present invention.
The schematic diagram of the pharmaceutical wastewater treatment process that Fig. 2 is the present invention.
In figure, 1, grid pond, 2, regulating reservoir, 3, coagulative precipitation tank, 4, hydrolysis acidification pool, 5, UASB reaction tank, 6, medium sediment pool, 7, anoxic pond, 8, Aerobic Pond, 9, second pond, 10, intermediate pool, 11, Fenton oxidation pond, 12, neutralize degassed pond, 13, final deposition pool.
Detailed description of the invention
Below in conjunction with drawings and Examples, the present invention is described in detail.
As shown in Figure 1 and Figure 2, pharmacy wastewater treatment system of the present invention include flowing to waste water set gradually grid pond 1, regulating reservoir 2, coagulative precipitation tank 3, hydrolysis acidification pool 4, UASB reaction tank 5, medium sediment pool 6, anoxic pond 7, Aerobic Pond 8, second pond 9, intermediate pool 10, Fenton oxidation pond 11, neutralize degassed pond 12 and final deposition pool 13, each pond is by sewage pump or from the streamed connection realizing waste water.
The flow process of pharmaceutical wastewater treatment process of the present invention is as follows:
1) waste water flows automatically after delivering to Sewage Disposal into grid pond 1, and the grid gap in grid pond 1 is 5-8mm, intercepts thick float by grid;
2) waste water that grid pond 1 is flowed out enters regulating reservoir 2, the waste water that regulating reservoir 2 has COD to be 3000 ~ 6000mg/L in advance, ensure water stabilization, COD be water sample under certain condition, to aoxidize in 1 liter of water sample the amount of the oxidant that reducing substances consumes for index, be converted to every liter of water sample all oxidized after, it is necessary to the milligram number of oxygen;
3) using sewage pump to be evacuated in coagulative precipitation tank 3 by regulating reservoir 2 water outlet, add flocculant PAC and coagulant PAM, PAC concentration is 5% in coagulative precipitation tank 3, the waste water that dosage is 100t adds 20kg; PAM concentration is 0.1%, the waste water that dosage is 100t adds 2kg, PAC is aluminium polychlorid, this product has stronger bridge formation absorption property, in hydrolytic process, with condensing, the physical and chemical processes such as absorption and precipitation, PAM is domestic conventional non-ionic high polymer coagulant, polyacrylamide, has and forms the consequent huge surface adsorption effect of bigger flco between granule;
4) coagulative precipitation tank 3 supernatant is from flowing into hydrolysis acidification pool 4, adds the NaOH of 10%, pH regulator to 6.5-7, and adds carbamide and phosphate fertilizer, and the ratio of adding is COD:N:P=100:5:1, and the substance decomposition of difficult degradation becomes the organic substrates of easily degraded;
5) sewage pump is used to be evacuated in UASB reaction tank 5 by hydrolysis acidification pool 4 water outlet, before entering UASB reaction tank 5, SS dropping to less than 100, SS refers to float, refer to the solid matter being suspended in water, including the inorganic matter of water fast, Organic substance and silt particle, clay, microorganism etc. In water, suspension content is one of index weighing water pollution degree;
6) UASB reaction tank 5 water outlet is from flowing into medium sediment pool 6, by mud-water separation in medium sediment pool 6, sludge reflux is to UASB reaction tank or the anoxic pond 7 of step 7), UASB is made up of sludge reaction district, gas-liquid-solid three-phase separator (including settling zone) and air chamber three part, a large amount of anaerobic sludge is retained in sludge reaction district, sewage to be processed flows into from anaerobic mud bed bottom to carry out mixing with mud sludge blanket and contacts, the Organic substance in microbial decomposition sewage in mud, is converted into biogas it, biogas is constantly released with micro-bubble form, micro-bubble is in uphill process, constantly merge, gradually form bigger bubble, on Sludge Bed top, the mud stirring one sludge concentration of formation leaner due to biogas ascends into three phase separator together with water, biogas enters air chamber through water layer, concentrate on air chamber biogas, derive with conduit, solid-liquid mixed liquor enters the settling zone of three phase separator, mud in sewage flocculates, granule is gradually increased, and settle under gravity, the mud being precipitated on skew wall slides back in anaerobic reaction district along skew wall, make the substantial amounts of mud of accumulation in reaction zone, process water outlet after separating with mud is overflowed from downflow weir top, settling zone, it is then discharged out Sludge Bed,
7) medium sediment pool 6 water outlet is from flowing into anoxic pond 7, has activated sludge, dissolved oxygen to control to hang with biologic packing material in 0.2 ~ 0.5mg/L, anoxic pond in anoxic pond 7, and this step is to remove the ammonia nitrogen pollutant in water, reduces part COD simultaneously;
8) anoxic pond 7 water outlet flow to Aerobic Pond 8, has activated sludge, dissolved oxygen to control at 2 ~ 4mg/L in Aerobic Pond 8, hanging with biologic packing material in Aerobic Pond 8, biologic packing material is divided into combined stuffing, 3 D elastic filler, porous suspended ball filler, Active biological filler, properly functioning enter, filler is suspended in water, filler growth inside anaerobe, produce Denitrification can denitrogenation, external growth aerobic bacteria,, in whole processing procedure, there is nitrification and denitrification process in organics removal simultaneously;
9) Aerobic Pond 8 water outlet is from flowing in second pond 9, in second pond 9, mud and sewage is carried out precipitate and separate, and sludge reflux is to anoxic pond 7, and excess sludge is discharged to sludge concentration tank and carries out concentration;
10) second pond 9 water outlet is from flowing into intermediate pool 10, adds sulphuric acid in intermediate pool 10, and regulating pH value is 3;
11) use sewage pump that intermediate pool 10 water is evacuated to Fenton oxidation pond 11, add H2O2Oxidant and Fe2+Catalyst, both produce hydroxyl free radical at reaction, and the high oxidative capacity of hydroxyl free radical reacts with the Organic substance in waste water, decomposable asymmetric choice net oxidation of organic compounds, and then reducing the COD that useless organism in water difficulty is decomposed, Fenton oxidation pond 11 water outlet neutralizes in degassed pond 12 from inflow;
12) in and degassed pond 12 in add alkali liquor, PH is adjusted to 7, addition PAM, PAM dosage is that the waste water of 100t adds 2kg;
13) neutralizing waste water in degassed pond 12 and certainly flow in final deposition pool 13, this pond is designed as flat flow, due to Fe3+Inherently extraordinary coagulant, adds a small amount of PAM and is up to good sedimentation effect, in this process except by Fe (OH)3Separating outside removing, colourity, SS are had extraordinary removal function simultaneously, final deposition pool 13 standard water discharge is discharged.
Claims (1)
1. a pharmacy wastewater treatment system and technique, it is characterised in that: described system include with waste water flow to set gradually grid pond, regulating reservoir, coagulative precipitation tank, hydrolysis acidification pool, UASB reaction tank, medium sediment pool, anoxic pond, Aerobic Pond, second pond, intermediate pool, Fenton oxidation pond, neutralize degassed pond and final deposition pool; The flow process of described technique is as follows:
1) waste water flows automatically after delivering to Sewage Disposal into grid pond, and the grid gap in grid pond is 5-8mm;
2) waste water that grid pond is flowed out enters regulating reservoir, the waste water that regulating reservoir has COD to be 3000 ~ 6000mg/L in advance;
3) using sewage pump to be evacuated in coagulative precipitation tank by regulating reservoir water outlet, add flocculant PAC and coagulant PAM, PAC concentration is 5% in coagulative precipitation tank, the waste water that dosage is 100t adds 20kg; PAM concentration is 0.1%, and the waste water that dosage is 100t adds 2kg;
4) coagulative precipitation tank supernatant is from flowing into hydrolysis acidification pool, adds the NaOH of 10%, pH regulator to 6.5-7, and adds carbamide and phosphate fertilizer, and the ratio of adding is COD:N:P=100:5:1;
5) use sewage pump to be evacuated in UASB reaction tank by hydrolysis acidification pool water outlet, before entering UASB reaction tank, SS is dropped to less than 100;
6) water outlet of UASB reaction tank is from flowing into medium sediment pool, and by mud-water separation in medium sediment pool, sludge reflux is to UASB reaction tank or the anoxic pond of step 7);
7) medium sediment pool water outlet is from flowing into anoxic pond, has activated sludge, dissolved oxygen to control to hang with biologic packing material in 0.2 ~ 0.5mg/L, anoxic pond in anoxic pond;
8) anoxic pond water outlet flow to Aerobic Pond, has activated sludge, dissolved oxygen to control to hang with biologic packing material in 2 ~ 4mg/L, Aerobic Pond in Aerobic Pond;
9) Aerobic Pond water outlet is from flowing in second pond, in second pond, mud and sewage is carried out precipitate and separate, and sludge reflux is to anoxic pond, and excess sludge is discharged to sludge concentration tank and carries out concentration;
10) secondary clarifier effluent is from flowing into intermediate pool, adds sulphuric acid in intermediate pool, and regulating pH value is 3;
11) use sewage pump that intermediate pool water is evacuated to Fenton oxidation pond, add H2O2Oxidant and Fe2+Catalyst, the water outlet of Fenton oxidation pond is from flowing in the degassed pond of neutralization;
12) in and degassed pond in add alkali liquor, PH is adjusted to 8, is subsequently adding the waste water that PAM, PAM dosage is 100t and adds 2kg;
13) neutralize waste water in degassed pond, from flowing in final deposition pool, to carry out precipitating the separation realizing sewage and mud.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610017258.1A CN105621798A (en) | 2016-01-12 | 2016-01-12 | Pharmaceutical wastewater treatment system and technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610017258.1A CN105621798A (en) | 2016-01-12 | 2016-01-12 | Pharmaceutical wastewater treatment system and technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105621798A true CN105621798A (en) | 2016-06-01 |
Family
ID=56037205
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610017258.1A Pending CN105621798A (en) | 2016-01-12 | 2016-01-12 | Pharmaceutical wastewater treatment system and technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105621798A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106007221A (en) * | 2016-07-12 | 2016-10-12 | 浙江环耀环境建设有限公司 | Pharmaceutical wastewater treatment process |
| CN106698856A (en) * | 2017-02-25 | 2017-05-24 | 郑州碧水环保科技有限公司 | Comprehensive treatment system for fermented antibiotic pharmaceutical wastewater |
| CN107032493A (en) * | 2017-05-16 | 2017-08-11 | 杭州绿夏环境科技有限公司 | Pharmacy wastewater treatment method and processing system |
| CN108911369A (en) * | 2018-06-26 | 2018-11-30 | 浙江环耀环境建设有限公司 | Reservoir sewage disposal system and its treatment process |
| CN110078139A (en) * | 2019-04-02 | 2019-08-02 | 菏泽学院 | A kind of logical sequence is cut down for the ablation method of Buddhist nun's production of raw medicine waste liquid |
| CN110395841A (en) * | 2019-05-17 | 2019-11-01 | 高邮市宇航化工机械厂 | Wastewater treating technique in a kind of biopharmaceutical production processes |
| CN111153557A (en) * | 2020-01-20 | 2020-05-15 | 上海泓济环保科技股份有限公司 | Integrated treatment device and treatment process for pickling and phosphating production wastewater |
| CN112093972A (en) * | 2019-06-18 | 2020-12-18 | 上海睿易环境科技有限公司 | Biological industrial wastewater treatment system and method |
| CN116495923A (en) * | 2023-05-06 | 2023-07-28 | 康龙化成(绍兴)药业有限公司 | System and process for treating high ammonia nitrogen wastewater in pharmaceutical industry |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009135276A1 (en) * | 2008-05-07 | 2009-11-12 | Vlc Industria E Comercio Ltda. | Process for large amounts of wastewater desinfection and treatment, water recycling and utilization of organic and inorganic charges |
| CN203144244U (en) * | 2013-03-27 | 2013-08-21 | 重庆地质矿产研究院 | High-efficiency treatment system for industrial wastewater difficult to degrade |
| CN204588945U (en) * | 2015-04-14 | 2015-08-26 | 河北天友环保工程有限公司 | A kind of pharmaceutical industry wastewater treatment equipment |
-
2016
- 2016-01-12 CN CN201610017258.1A patent/CN105621798A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009135276A1 (en) * | 2008-05-07 | 2009-11-12 | Vlc Industria E Comercio Ltda. | Process for large amounts of wastewater desinfection and treatment, water recycling and utilization of organic and inorganic charges |
| CN203144244U (en) * | 2013-03-27 | 2013-08-21 | 重庆地质矿产研究院 | High-efficiency treatment system for industrial wastewater difficult to degrade |
| CN204588945U (en) * | 2015-04-14 | 2015-08-26 | 河北天友环保工程有限公司 | A kind of pharmaceutical industry wastewater treatment equipment |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106007221A (en) * | 2016-07-12 | 2016-10-12 | 浙江环耀环境建设有限公司 | Pharmaceutical wastewater treatment process |
| CN106007221B (en) * | 2016-07-12 | 2018-10-09 | 浙江环耀环境建设有限公司 | A kind of pharmaceutical wastewater treatment process |
| CN106698856A (en) * | 2017-02-25 | 2017-05-24 | 郑州碧水环保科技有限公司 | Comprehensive treatment system for fermented antibiotic pharmaceutical wastewater |
| CN107032493A (en) * | 2017-05-16 | 2017-08-11 | 杭州绿夏环境科技有限公司 | Pharmacy wastewater treatment method and processing system |
| CN108911369A (en) * | 2018-06-26 | 2018-11-30 | 浙江环耀环境建设有限公司 | Reservoir sewage disposal system and its treatment process |
| CN110078139A (en) * | 2019-04-02 | 2019-08-02 | 菏泽学院 | A kind of logical sequence is cut down for the ablation method of Buddhist nun's production of raw medicine waste liquid |
| CN110395841A (en) * | 2019-05-17 | 2019-11-01 | 高邮市宇航化工机械厂 | Wastewater treating technique in a kind of biopharmaceutical production processes |
| CN112093972A (en) * | 2019-06-18 | 2020-12-18 | 上海睿易环境科技有限公司 | Biological industrial wastewater treatment system and method |
| CN111153557A (en) * | 2020-01-20 | 2020-05-15 | 上海泓济环保科技股份有限公司 | Integrated treatment device and treatment process for pickling and phosphating production wastewater |
| CN116495923A (en) * | 2023-05-06 | 2023-07-28 | 康龙化成(绍兴)药业有限公司 | System and process for treating high ammonia nitrogen wastewater in pharmaceutical industry |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105621798A (en) | Pharmaceutical wastewater treatment system and technique | |
| CN108751625B (en) | Treatment system and process for fermentation antibiotic wastewater | |
| CN103435235B (en) | Kitchen waste filtrate treatment equipment and method | |
| CN106927628A (en) | Light electrolysis-Fenton-EGSB-A/O-BCO-BAF-coagulating treatment pharmacy waste water technique | |
| WO2009124426A1 (en) | A method for treating pharmaceutical mixed wastewater in chemical industry park | |
| CN102659281B (en) | Treatment method of liquor production wastewater | |
| CN111573991B (en) | Chemical plating comprehensive wastewater treatment method | |
| CN111138028A (en) | Automobile production wastewater treatment method and system | |
| CN212293218U (en) | Anaerobic ammonia oxidation landfill leachate treatment system | |
| CN103449661A (en) | Method for treating polyether wastewater | |
| CN109111019A (en) | High concentration, chemical synthesis pharmacy wastewater treatment method and system difficult to degrade | |
| CN102515435A (en) | Method for processing silicon carbide industrial wastewater | |
| CN110183066B (en) | Blue algae deep dehydration wastewater treatment system and process | |
| CN204474504U (en) | The treatment unit of brown coal low-temperature pyrolysis waste water | |
| CN116495923A (en) | System and process for treating high ammonia nitrogen wastewater in pharmaceutical industry | |
| CN106746223A (en) | Aerobic collaboration processing cutting liquid waste plant and the method for coagulation anaerobic hydrolysis | |
| CN216808506U (en) | Kitchen and kitchen garbage and wastewater treatment system | |
| CN216236438U (en) | Pretreatment system for garbage extrusion leachate | |
| CN207227213U (en) | A kind of chemical synthesis class pharmacy wastewater treatment device | |
| CN115367952A (en) | High-salinity sewage accident sewage and low-salinity high-concentration sewage comprehensive treatment system and method | |
| KR20020018572A (en) | Electro coagulation and Bio-wrinkled circulation nutrients removal system | |
| US11447408B2 (en) | Combination of captivator and fixed film bioreactor solutions | |
| CN210340626U (en) | Blue algae deep dehydration wastewater treatment system | |
| CN113185066A (en) | Sewage treatment method for high-polymer high-salt oil extraction wastewater | |
| CN112408707A (en) | Medical intermediate wastewater treatment process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160601 |
|
| RJ01 | Rejection of invention patent application after publication |