CN108862848A - The treatment process and processing system of pharmacy waste water - Google Patents
The treatment process and processing system of pharmacy waste water Download PDFInfo
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- CN108862848A CN108862848A CN201810717778.2A CN201810717778A CN108862848A CN 108862848 A CN108862848 A CN 108862848A CN 201810717778 A CN201810717778 A CN 201810717778A CN 108862848 A CN108862848 A CN 108862848A
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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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
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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
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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
- C02F1/722—Oxidation by peroxides
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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
-
- 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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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a kind for the treatment of process of pharmacy waste water, Fenton reagent oxidation is first carried out using by pharmacy waste water to be processed, then it is settled through sedimentation basin, it sequentially enters UASB reactor, biological contact oxidation pond, the treatment process handled with MBR reaction tank again later, obtains the water outlet for meeting urban wastewater treatment firm pollutant emission standard.The pharmaceutical wastewater treatment process of acquisition, further combined with the use of processing system, completes to pharmacy waste water pollutant efficiently to administer, water outlet is made to meet urban wastewater treatment firm pollutant emission standard, it realizes the stabilization of pharmacy waste water, thoroughly administer, there is significant economical and environmentally friendly meaning.
Description
Technical field
The present invention relates to pharmacy wastewater treatment technical field more particularly to a kind for the treatment of process of pharmacy waste water, and should
The processing system that treatment process uses.
Background technique
Pharmacy waste water mainly includes antibiotic production wastewater, synthetic drug production waste water, Chinese patent medicine production wastewater and each
Four major class of washing water and flushing waste water of class formulation manufacturing processes.Wherein, chemical pharmacy waste water is from chemical synthesis purifying or medicine
With techniques such as plant separating-purifyings, have organic matter and inorganic salt content high, BOD5And fluctuation low with CODcr ratio is big, can give birth to
The features such as property changed is poor, intermittent discharge, water fluctuation；Wastewater in Biologic Pharmacy is mainly from the processes such as saccharification, fermentation, extraction, tool
Have that variation water quality range is big, intermittent discharge, CODCrThe features such as concentration is high, and water process difficulty is big；Therefore pharmacy waste water is a kind of high
Concentration, difficult to degrade, virose organic wastewater, and with the development of medical industry, the discharge amount of pharmacy waste water increases increasingly,
As one of pollution most serious, most intractable industrial wastewater.
The processing method of pharmacy waste water can be summarized as following several：Materializing strategy, chemical treatment, biochemical treatment and a variety of
The combined treatment etc. of method.Various processing methods all have respective advantage and insufficient, at present for pharmacy waste water apply compared at
Ripe treatment process is the biochemical treatment process using Anaerobic Treatment combination Aerobic Process for Treatment, but due to the methanogen pair of Anaerobic Treatment
Poisonous and harmful substances adaptability is poor, causes anaerobic bacteria survival rate low, causes water quality after processing unstable and be often unable to reach
Discharge standard.
Summary of the invention
To solve the shortcomings of the prior art, the present invention provides a kind for the treatment of process of pharmacy waste water, which is adopted
With the method for materializing strategy combination biochemical treatment, and it is breakthrough materializing strategy is set to biochemical treatment before, to realize
Stably reaching standard processing to high concentration, high salinity pharmacy waste water.
To achieve the above object, the treatment process of pharmacy waste water provided by the invention, using by pharmacy waste water to be processed
Fenton reagent oxidation is first carried out, then through sedimentation basin sedimentation, degassing pond aeration, sequentially enters UASB reactor, biology again later
Contact-oxidation pool, the treatment process handled with MBR reaction tank, obtain meeting urban wastewater treatment firm pollutant emission standard
Water outlet.
As the restriction to above-mentioned technical proposal, the treatment process of the pharmacy waste water includes the following steps：
A, Fenton reagent aoxidizes：Pharmacy waste water pH to be processed is adjusted to 2.5~3.5 with acid, Fenton reagent is then added
H2O2With FeSO4, stir rear 30~60min of oxidation processes；The Fenton reagent dosage：H2O2=2.5~3g/L,
H2O2With FeSO4Add ratio be H2O2：FeSO4=(1.5~2):1；
B, sedimentation, aeration：Through step a treated waste water adjusting PH with base to 7~8, flocculation aid is then added, is sufficiently stirred
Enter settling tank afterwards, after 15~30min of iron cement floc settlement, waste water is discharged into degassing pond from settling tank, passes through aeration
Remove H remaining in water removal2O2；
C, UASB reacts：Enter UASB reactor through water pump lifting by the waste water of degassing pond discharge, control wastewater pH 6.5~
7.8, between 30~40 DEG C of waste water temperature, complete the Anaerobic Treatment to waste water；
D, catalytic oxidation is handled：Waste water after UASB reactor for treatment enters biological contact oxidation pond, in activated sludge
It is aoxidized 4~6 hours under conditions of 3~4g/L of amount, aeration 3~4mg/L of dissolved oxygen amount, 15~35 DEG C of waste water temperature of control；
E, MBR reacts：Finally by waste water by MBR reaction tank, 8~10g/L of sludge concentration, dissolved oxygen concentration 2 in pond
Under the conditions of~2.5mg/L, the water outlet for meeting urban wastewater treatment firm pollutant emission standard is obtained.
Treatment process of the invention, for the large amount of organic and inorganic salts contained in bio-pharmaceuticals, chemical pharmacy waste water
The intractability of substance and poisonous and harmful property will by the way of first Fenton reagent being used to carry out Strong oxdiative processing to waste water
Arene substance difficult to degrade is oxidized to alkane or cycloalkane substance, to greatly reduce Pollutants in Wastewater to active dirty
The impact of mud improves the treatment effect of subsequent UASB reactor and biological contact oxidation pond.Then, it is set after Fenton oxidation processing
Sedimentation basin and degassing pond are set, on the one hand using the sedimentation of the iron ion floccule body foundry loam generated after Fenton oxidation, flocculation, only
Change some of the contaminants in waste water, is convenient for subsequent efficient processing；On the other hand, fill Fenton reagent in sedimentation basin
Resolution, then the Air Exposure in degassed pond is divided to remove remaining H2O2, to eliminate its oxygen poison to anaerobic bacteria in UASB reactor.
Waste water successively carries out UASB, aerobic and MBR processing again after Fenton oxidation, precipitating, degassing, raw by anaerobism and aerobic combination
Change processing, finally by the biological treatment combination membrane separation technique of MBR reaction tank, completion to pharmacy waste water pollutant is efficiently controlled
Reason makes water outlet meet urban wastewater treatment firm pollutant emission standard.
As the restriction to above-mentioned technical proposal, pre-treatment step is additionally provided with before step a, i.e., by system to be processed
Medicine waste water first carries out grid and intercepts filtering or the pretreatment of primary precipitation, then carries out Fenton reagent oxidation and subsequent processing steps.
Before Fenton oxidation, the pretreatment to waste water can be also added, simple lattice are carried out according to different waste water qualities
Grid filtering or primary precipitation, remove the bulky grain pollutant in waste water.
As the restriction to above-mentioned technical proposal, step a adjusts the sulfuric acid solution that the acid that wastewater pH uses is 25~30%.
As the restriction to above-mentioned technical proposal, it is NaOH solution or Ca (OH) that step b, which adjusts the alkali that wastewater pH uses,2It is outstanding
Turbid；The flocculation aid selects polyacrylamide, and flocculation aid additional amount is 2~5mg/L；Aeration gas-water ratio in the degassing pond
It is 3:1~5:1.
As the restriction to above-mentioned technical proposal, control waste water basicity is higher than 2000mg/ in UASB reactor described in step c
L controls waste water volatile organic acids within 200mg/L.
As the restriction to above-mentioned technical proposal, MBR membrane flux is controlled in 15~25L/ in MBR reaction tank described in step e
m2·h。
It further limits waste water treatment process different phase and adjusts the wastewater pH acid, the alkaloid substance that use, flocculation aid substance, and
Deaerate aeration condition, and the optimization such as control of waste water operating parameter, guarantees waste water stable operation in UASB reactor, MBR reaction tank
And processing, and it is conducive to intensive treatment effect.
Meanwhile the present invention also provides a kind of processing systems of pharmacy waste water, including what is be sequentially connected in series from upstream to downstream
PH conditioning tank, Fenton oxidation pond, neutralization reaction pond, sedimentation basin, bottom are equipped with the degassing pond of aerator, UASB reactor, life
Object contact-oxidation pool and MBR reaction tank.
As the restriction to above-mentioned technical proposal, pretreatment pool is additionally provided in pH conditioning tank upstream.
As the restriction to above-mentioned technical proposal, the processing system further includes following monitoring element：The pH conditioning tank,
Online pH meter is respectively set in neutralization reaction pond；Online thermometer and heating dress are set at the water inlet of the UASB reactor
It sets；Elastic solid filler or gimp filler are provided in the contact-oxidation pool；Flow is set at the water outlet of the MBR reaction tank
Meter.
For convenient for the stable operation of pharmacy waste water processing, the present invention also provides more applicable processing systems, and further
Detecting element and setting site that wastewater treatment process carries out monitoring water quality are limited, to obtain to the stabilization of pharmacy waste water, thoroughly
It administers, there is significant economical and environmentally friendly meaning.
In conclusion using technical solution of the present invention, the pharmaceutical wastewater treatment process of acquisition, using by Fenton oxidation
The method that materializing strategy is combined with anaerobism, aerobic treatment, and breakthrough Fenton oxidation is set at UASB anaerobism
It before reason, had both realized to the refractory organics of high concentration, high salinity pharmacy waste water and capturing for poisonous and harmful property, had gone out after making processing
Water energy stably reaching standard；Again using after Fenton oxidation sedimentation basin, degassing pond play double effects be solved perfectly anaerobism it
Preceding setting oxidation processes meeting bring limits the oxygen poison of anaerobic bacteria, finally by the biological treatment combination film point of MBR reaction tank
From technology, completes to pharmacy waste water pollutant efficiently to administer, water outlet is made to meet urban wastewater treatment firm pollutant emission standard,
It realizes the stabilization to pharmacy waste water, thoroughly administer, there is significant economical and environmentally friendly meaning.
Detailed description of the invention
Fig. 1 is the pharmacy wastewater treatment system and device schematic diagram that embodiment of the present invention is related to；
In figure：1, pretreatment pool；2, pH conditioning tank, 3, Fenton oxidation pond；4, neutralization reaction pond, 5, sedimentation basin；6, it deaerates
Pond；7, UASB reactor；8, aerobic tank；9, MBR reaction tank.
Specific embodiment
Below in conjunction with embodiment, technical solution of the present invention is clearly and completely described, it is clear that described
Embodiment is only a part of the embodiment of the present invention, instead of all the embodiments.Based on the embodiments of the present invention, this field
Those of ordinary skill's every other embodiment obtained without making creative work, belongs to protection of the present invention
Range.
Embodiment
The present embodiment is related to the treatment process to pharmacy waste water.
The treatment process can carry out in pharmacy wastewater treatment system as shown in Figure 1, and the processing system includes from upper
Swim the pH conditioning tank 2 being sequentially connected in series to downstream, Fenton oxidation pond 3, neutralization reaction pond 4, sedimentation basin 5, degassing pond 6, UASB reaction
Device 7, biological contact oxidation pond 8 and MBR reaction tank 9；It is described degassing pond 6 bottom be equipped with aerator, and deaerate pond 6 with
It is connected between UASB reactor 7 via water pump.
For the stable operation for guaranteeing processing system, also settable following monitoring element：In pH conditioning tank 2 and neutralization reaction pond
Online pH meter is respectively set in 4；Online thermometer and heating apparatus are set at the water inlet of UASB reactor 7；In contact oxygen
Change in pond 8 and is provided with elastic solid filler or gimp filler；Flowmeter is set at the water outlet of MBR reaction tank.
In 2 upstream of pH conditioning tank, it is connected with pretreatment pool 1 with the water inlet of pH conditioning tank 2, the pretreatment tank 1 is specific
It can be grid pond or primary sedimentation tank.
Embodiment 1
Waste water from chemical pharmaceutical production field, COD are 20000~25000mg/L, and SS is 1000~1500mg/
L, B/C < 0.1, pH 6.8 is handled the waste water using following technique；
Simple primary clarifier is carried out according to different waste water quality selections, removes the bulky grain pollutant in waste water
Afterwards, then successively process is carried out the following processing：
A, Fenton reagent aoxidizes：Pharmacy waste water pH to be processed is first adjusted to 2.5 using the sulfuric acid solution that concentration is 30%,
Then Fenton reagent H is added2O2With FeSO4, in stock agitating paddle oxidation processes 40min after mixing evenly；Wherein, Fenton reagent
Dosage is H2O2=3g/L, FeSO4=1.6g/L；
B, it settles：Through step a treated waste water with Ca (OH)2Suspension is adjusted to neutrality, adds flocculation aid
PAM2.5mg/L, after stirring enter settling tank, to iron cement floc settlement 15min, waste water from settling tank be discharged into
Enter the pond that deaerates, to be aerated gas-water ratio 3 in degassing pond:1 Air Exposure 20min removes H remaining in water removal2O2。
C, UASB reacts：Enter UASB reactor, initial breakdown high concentration through water pump lifting by the waste water of degassing pond discharge
Organic matter controls wastewater pH 6.5~7.8,30~40 DEG C of waste water temperature, completes the Anaerobic Treatment to waste water；Control UASB reaction
Waste water basicity is (with CaCO in device3Meter) it is higher than 2000mg/L, waste water volatile organic acids (VFA) is within 200mg/L, to increase
Interior circulation is to reduce influent concentration, so that UASB reactor be made to reach 80% or more to the removal efficiency of organic matter；
D, catalytic oxidation is handled：Waste water after UASB reactor for treatment enters biological contact oxidation pond, in activated sludge
It is aoxidized 6 hours under conditions of 3~4g/L of amount, aeration 3~4mg/L of dissolved oxygen amount, 15~35 DEG C of waste water temperature of control；
E, MBR reacts：Waste water is finally passed through into MBR reaction tank, sludge concentration is controlled in 8~10g/L in MBR reaction tank,
Under the conditions of dissolved oxygen concentration is 2mg/L, and MBR membrane flux is controlled in 15~25L/m2H, waste water water temperature is preferably at 15~35 DEG C
Between, effluent quality can be made to reach COD45mg/L, SS8mg/L, to meet urban wastewater treatment firm pollutant emission standard
Water outlet.
Embodiment 2
Waste water from bio-pharmaceuticals production field, COD 8400mg/L, SS 240mg/L, BOD 4300mg/L,
PH is 8.6, is handled using following technique the waste water；
Simple primary precipitation is carried out according to different waste water quality selections, after removing the bulky grain pollutant in waste water,
Process is successively carried out the following processing again：
A, Fenton reagent aoxidizes：Pharmacy waste water pH to be processed is first adjusted to 3 using the sulfuric acid solution that concentration is 25%, so
Fenton reagent H is added afterwards2O2With FeSO4, in stock agitating paddle oxidation processes 30min after mixing evenly, wherein Fenton reagent is thrown
Dosage is H2O2=2g/L, FeSO4=1.2g/L；
B, it settles：Through step a treated waste water NaOH solution, it is adjusted to neutrality, flocculation aid PAM2.5mg/L is added, fills
Divide and enter settling tank after mixing evenly, to iron cement floc settlement 25min, waste water is discharged into degassing pond from settling tank, de-
To be aerated gas-water ratio 4 in gas pond:1 Air Exposure about 20min removes H remaining in water removal2O2；
C, UASB reacts：Enter UASB reactor, initial breakdown high concentration through water pump lifting by the waste water of degassing pond discharge
Organic matter controls wastewater pH 6.5~7.8,30~40 DEG C of waste water temperature, completes the Anaerobic Treatment to waste water；Control UASB reaction
Waste water basicity is (with CaCO in device3Meter) it is higher than 2000mg/L, waste water volatile organic acids (VFA) is within 200mg/L, to increase
Interior circulation is to reduce influent concentration, so that UASB reactor be made to reach 80% or more to the removal efficiency of organic matter；
D, catalytic oxidation is handled：Waste water after UASB reactor for treatment enters biological contact oxidation pond, in activated sludge
It is aoxidized 4 hours under conditions of 3~4g/L of amount, aeration 3~4mg/L of dissolved oxygen amount, 15~35 DEG C of waste water temperature of control；
E, MBR reacts：Waste water is finally passed through into MBR reaction tank, sludge concentration is controlled in 8~10g/L in MBR reaction tank,
Under the conditions of dissolved oxygen concentration is 2mg/L, and MBR membrane flux is controlled in 15~25L/m2H, waste water water temperature is preferably at 15~35 DEG C
Between, effluent quality can be made to reach COD35mg/L, SS7mg/L, BOD7mg/L, to meet urban wastewater treatment firm pollutant
The water outlet of discharge standard.
Comparative example
Using routine techniques Pharmaceutical Wastewater Treatment, that is, use UASB+ catalytic oxidation+MBR+ Fenton oxidation (various processes
By first UASB again the last Fenton oxidation of the subsequent MBR of catalytic oxidation statement sequence carry out) treatment process, due to pharmacy waste water
COD concentration is high, is not suitable for directlying adopt UASB reactor, and UASB reactor load is excessively high, be easy to cause system crash.
Treatment process of the invention is preposition by Fenton oxidation, can not only reduce COD concentration, can also improve biochemical
Property, it is beneficial to subsequent bio degradation of organic substances.
In conclusion pharmaceutical wastewater treatment process of the invention, using by the materializing strategy of Fenton oxidation and anaerobism, aerobic
The method that biochemical treatment combines, and it is breakthrough Fenton oxidation is set to UASB Anaerobic Treatment before, both realized to height
Concentration, the refractory organics of high salinity pharmacy waste water and poisonous and harmful property are captured, and in turn avoid being arranged at oxidation before anaerobism
Comprehend the limitation of bring oxygen poison, goes out water energy stably reaching standard after making processing, thus realize the stabilization to pharmacy waste water, thoroughly administer,
With significantly economical and environmentally friendly meaning.
Claims (10)
1. a kind for the treatment of process of pharmacy waste water, it is characterised in that：Fenton reagent is first carried out using by pharmacy waste water to be processed
Oxidation, then through sedimentation basin sedimentation, degassing pond aeration, sequentially enter again later UASB reactor, biological contact oxidation pond, with
The treatment process that MBR reaction tank is handled obtains the water outlet for meeting urban wastewater treatment firm pollutant emission standard.
2. the treatment process of pharmacy waste water according to claim 1, it is characterised in that：Include the following steps：
A, Fenton reagent aoxidizes：Pharmacy waste water pH to be processed is adjusted to 2.5~3.5 with acid, Fenton reagent H is then added2O2With
FeSO4, stir rear 30~60min of oxidation processes；The Fenton reagent dosage：H2O2=2.5~3g/L, H2O2With
FeSO4Add ratio be H2O2：FeSO4=(1.5~2):1；
B, sedimentation, aeration：Through step a treated waste water adjusting PH with base to 7~8, flocculation aid is then added, is sufficiently stirred laggard
Enter settling tank, after 15~30min of iron cement floc settlement, waste water is discharged into degassing pond from settling tank, removes by aeration
Remaining H in water2O2；
C, UASB reacts：Enter UASB reactor through water pump lifting by the waste water of degassing pond discharge, control wastewater pH 6.5~7.8,
Between 30~40 DEG C of waste water temperature, the Anaerobic Treatment to waste water is completed；
D, catalytic oxidation is handled：Waste water after UASB reactor for treatment enters biological contact oxidation pond, active mud content 3~
It is aoxidized 4~6 hours under conditions of 4g/L, aeration 3~4mg/L of dissolved oxygen amount, 15~35 DEG C of waste water temperature of control；
E, MBR reacts：Finally by waste water by MBR reaction tank, in pond 8~10g/L of sludge concentration, dissolved oxygen concentration 2~
Under the conditions of 2.5mg/L, the water outlet for meeting urban wastewater treatment firm pollutant emission standard is obtained.
3. the treatment process of pharmacy waste water according to claim 2, it is characterised in that：It is additionally provided with before step a pre-
Pharmacy waste water to be processed is first carried out grid and intercepts filtering or the pretreatment of primary precipitation, then carries out Fenton by processing step
Reagent oxidation and subsequent processing steps.
4. the treatment process of pharmacy waste water according to claim 2, it is characterised in that：Step a adjusts what wastewater pH used
The sulfuric acid solution that acid is 25~30%.
5. the treatment process of pharmacy waste water according to claim 2, it is characterised in that：Step b adjusts what wastewater pH used
Alkali is NaOH solution or Ca (OH)2Suspension；The flocculation aid selects polyacrylamide, and flocculation aid additional amount is 2~5mg/L；
Aeration gas-water ratio in the degassing pond is 3:1~5:1.
6. the treatment process of pharmacy waste water according to claim 2, it is characterised in that：In UASB reactor described in step c
It controls waste water basicity and is higher than 2000mg/L, control waste water volatile organic acids within 200mg/L.
7. the treatment process of pharmacy waste water according to claim 2, it is characterised in that：In MBR reaction tank described in step e
MBR membrane flux is controlled in 15~25L/m2·h。
8. a kind of processing system of pharmacy waste water, it is characterised in that：Including pH conditioning tank, the sweet smell being sequentially connected in series from upstream to downstream
Oxidation pond, neutralization reaction pond, sedimentation basin, bottom are equipped with the degassing pond of aerator, UASB reactor, bio-contact oxidation
Pond and MBR reaction tank.
9. the processing system of pharmacy waste water according to claim 8, it is characterised in that：It is additionally provided in pH conditioning tank upstream
Pretreatment pool.
10. the processing system of pharmacy waste water according to claim 8, which is characterized in that the processing system further include with
Lower monitoring element：Online pH meter is respectively set in the pH conditioning tank, neutralization reaction pond；At the water inlet of the UASB reactor
Online thermometer and heating apparatus are set；Elastic solid filler or gimp filler are provided in the contact-oxidation pool；The MBR
Flowmeter is set at the water outlet of reaction tank.
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| CN201810717778.2A CN108862848A (en) | 2018-07-03 | 2018-07-03 | The treatment process and processing system of pharmacy waste water |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110563282A (en) * | 2019-10-10 | 2019-12-13 | 上海玉畔环保设备有限公司 | Treatment system and treatment method for amino resin production wastewater |
| CN110790460A (en) * | 2019-12-02 | 2020-02-14 | 中化(宁波)润沃膜科技有限公司 | Method for treating waste water in production of cephalosporin pharmaceutical intermediates |
| CN111995169A (en) * | 2020-07-10 | 2020-11-27 | 同济大学 | Novel treatment device and treatment method for pharmaceutical wastewater |
| WO2021243732A1 (en) * | 2020-06-05 | 2021-12-09 | 南京德壹环境科技发展有限公司 | Medical wastewater treatment system and treatment method |
| CN115259540A (en) * | 2022-05-17 | 2022-11-01 | 景德镇澳蓝亚特环境科技有限公司 | Treatment method of respiratory targeting drug wastewater |
-
2018
- 2018-07-03 CN CN201810717778.2A patent/CN108862848A/en not_active Withdrawn
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110563282A (en) * | 2019-10-10 | 2019-12-13 | 上海玉畔环保设备有限公司 | Treatment system and treatment method for amino resin production wastewater |
| CN110790460A (en) * | 2019-12-02 | 2020-02-14 | 中化(宁波)润沃膜科技有限公司 | Method for treating waste water in production of cephalosporin pharmaceutical intermediates |
| WO2021243732A1 (en) * | 2020-06-05 | 2021-12-09 | 南京德壹环境科技发展有限公司 | Medical wastewater treatment system and treatment method |
| CN111995169A (en) * | 2020-07-10 | 2020-11-27 | 同济大学 | Novel treatment device and treatment method for pharmaceutical wastewater |
| CN115259540A (en) * | 2022-05-17 | 2022-11-01 | 景德镇澳蓝亚特环境科技有限公司 | Treatment method of respiratory targeting drug wastewater |
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