CN109761455A - A kind of processing method of synthesis and the class pharmaceuticals industry sewage that ferments - Google Patents
A kind of processing method of synthesis and the class pharmaceuticals industry sewage that ferments Download PDFInfo
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Abstract
The present invention relates to the technical fields of sewage treatment, more particularly to a kind of synthesis and the processing method of fermentation class pharmaceuticals industry sewage.Sanitary sewage pretreatment, production waste pre-process and in composite wastewater processing；It is sufficiently mixed after production waste and sanitary sewage are individually pre-processed, further ensures the continual and steady of biochemical system water inlet；Simultaneously in the water quality and quantity feature for synthesis and fermented pharmaceutical waste water, the toxicity of waste water is reduced by Fenton high-level oxidation technology, biodegradability improves and acts on removal wadding body by flocculation sedimentation, by the synchronous denitrogen dephosphorus technology of A2/O that wastewater treatment effluent quality is stable and total hrt shortens, the active sand filter of advanced treating section is a kind of integrate coagulation, clarification, the high-efficiency filtration systems of filtering and reduction energy consumption, economize on resources.
Description
Technical field
The present invention relates to the technical fields of sewage treatment, more particularly to a kind of synthesis and the class pharmaceuticals industry sewage that ferments
Processing method.
Background technique
China's pharmaceuticals industry at present accounts for the 1.7% of national total industrial output value, and quantity of wastewater effluent but accounts for national quantity of wastewater effluent
2%, pharmaceuticals industry is put into one of 12 key industrys of environment protection treating, and the waste water that pharmaceuticals industry generates is known as environmental monitoring and controls
The most important thing of reason.The major pollutants contained in waste water of pharmaceutical industry have suspended matter (SS), COD (CODcr), life
The poisonous and harmful substances such as change oxygen demand (BOD), ammonia nitrogen (NH3-N), cyanide and volatile phenol.Pharmacy waste water belongs to intractable work
One of industry waste water, because medicament categories are different, production technology is different, component difference is big, and complicated components, amount of pollutant is more, gives up
Water has the distinguishing features such as CODcr concentration is higher, biochemical is poor, bio-toxicity is strong, brings great difficulty to improvement.
Pharmaceuticals industry waste water be broadly divided into antibiotic production wastewater, synthetic drug production waste water, Chinese patent medicine production wastewater with
And four major class of washing water and flushing waste water of all kinds of formulation manufacturing processes.The processing method of pharmacy waste water can be summarized as following several
Kind: materializing strategy, chemical treatment, biochemical treatment and combined treatment of a variety of methods etc., various processing methods have respective
Advantage and deficiency.According to the water quality characteristics of pharmacy waste water, needed during reason using materializing strategy as biochemical treatment at which
Pretreatment or postprocessing working procedures.The materilization freatment method applied at present mainly includes coagulation, air bearing, absorption, ammonia aeration, electricity
Solution, ion exchange and membrane separation process etc., biochemical treatment includes oxidation ditch, SBR, CAST etc..
For the pharmaceuticals industry waste water of synthesis class and class of fermenting, majority uses " pretreatment+biochemical treatment+advanced treating
Technique ", such as: " air bearing+filter tank hydrolysis+SBR+ ", " filter tank light electrolysis+UASB+CASS+ " technique, but can not all obtain compared with
Good treatment effect, technique itself is more adaptable to the pharmacy sewage of antibiotics, and for the class pharmacy that synthesizes and ferment
There are some defects in the processing capacity of trade effluent, the problem of being primarily present is: the process means that 1. pretreatment section uses are single,
It is low to the cellulose in synthesis and fermented pharmaceutical waste water, the removal efficiency of lignin substance；2. pretreatment section is to sewage
The increase rate of biodegradability is little, and the distinguishing feature of pharmacy class waste water is that biodegradability is poor, by general treatment process or low
The treatment process of oxidability, is extremely difficult to improvement effect；3. for the class pharmaceuticals industry waste water that synthesizes and ferment, water quality and quantity
There is biggish variation with the difference of drug variety, raw materials for production and production technology, biochemical system there must be shock resistance energy
Power.
Summary of the invention
The present invention for synthesis and fermented pharmaceutical waste water water quality and quantity feature, the problems in background technique of solution,
A kind of synthesis and the class pharmaceuticals industry sewage water treatment method that ferments are provided, water quality and quantity fluctuation is reduced and sewage disposal system is rushed
Hitting property is reduced the toxicity of waste water by Fenton high-level oxidation technology, biodegradability improves and is spent by flocculation sedimentation
Except wadding body, by the way that the synchronous denitrogen dephosphorus technology of A2/O is by wastewater treatment effluent quality stabilization and total hrt shortens,
The active sand filter that filtration treatment uses is a kind of to integrate coagulation, clarification, the high efficiency filter processing unit of filtering and reduction
Energy consumption economizes on resources.In order to achieve the above object, the technical scheme adopted by the invention is as follows:
Synthesis and fermentation class pharmaceuticals industry sewage water treatment method, the method are based on synthesizing and fermenting class pharmaceuticals industry sewage treatment
System, system include garden sanitary sewage pipeline, garden production waste pipeline, homogeneous pond, Fenton oxidation pond, flocculation sedimentation tank,
Hydrolysis acidification pool, conditioning tank, A2The pond /O, secondary settling tank, coagulative precipitation tank, active sand filter and ultraviolet disinfection pond；The garden is raw
Plumbing drain living is equipped with Boosting pumping station and setting pot；Homogeneous pond, Fenton are sequentially connected in series on the garden production waste pipeline
Oxidation pond, flocculation sedimentation tank and hydrolysis acidification pool；The water outlet of the hydrolysis acidification pool and setting pot passes through pipeline connection respectively
The entrance of conditioning tank；Conditioning tank, A2The pond /O, secondary settling tank, coagulative precipitation tank, active sand filter and ultraviolet disinfection pond pass through pipeline
It is sequentially communicated；It is characterized in that sewage treatment operating procedure is as follows:
(1) sanitary sewage pre-processes
Sanitary sewage flows into Boosting pumping station by coarse rack, then flows into setting pot by fine fack；Wherein coarse rack and fine fack
By the floating material in sanitary sewage, suspended matter removal, the particulate matter in sanitary sewage is removed by the further precipitating of setting pot,
Residence time >=30s；SS removal rate >=40% in sanitary sewage；Obtain Pretreatment of Domestic Sewage；
(2) production waste pre-processes
2.1: homogenizing
Production waste, that is, pharmacy sewage flows into homogeneous pond, the first floating material and suspended matter in removal pharmacy sewage through fine fack；
Agitated machine stirring again, stirring intensity 8W/m3, mixing time 8h；Water quality and quantity homogeneous is mixed to get homogenizing production waste；
2.2: biochemistry pretreatment
Homogenizing production waste enters Fenton oxidation pond, and sulfuric acid is added in Fenton oxidation pond, and the pH value for adjusting homogenizing production waste is 4
~5；It adds Fenton reagent and carries out Fenton oxidation reaction, wherein H2O2/Fe2+Mass values be 15~25；Fenton oxidation is anti-
Stirring intensity >=the 20W/m answered3, reaction time 90min；It obtains ring molecule and long-chain molecule organic matter carries out chain rupture decomposition
At the biochemical production waste of small organic molecule；
Biochemical production waste enters flocculation sedimentation tank, and the strong base solution that concentration is 10% is added, and carries out acid-base neutralization reaction, reaction
Time is 10 ~ 30min, and the pH value for adjusting production waste is 7~9；Biochemical production waste flocculation sedimentation under alkaline condition, flocculation
Sedimentation time is 2~3h, surface loading >=2.0m3/m2H obtains precipitating production waste；
Precipitating production waste enters hydrolysis acidification pool, and hydrolysis acidification pool is flowed back using mud method, by adequately stirring that reflux is dirty
Mud and sewage mixed hydrolysis, stirring intensity are 6 ~ 12W/m3, mixing time 12h, by the toxicity and macromolecular substances in sewage
Further hydrolysis acidification, makes particulate matter be hydrolyzed to dissolved matter, obtains hydrolysis production waste；
(3) composite wastewater is handled
3.1: mixing
The hydrolysis production waste of step (1) Pretreatment of Domestic Sewage and step (2), which flows into conditioning tank, to be stirred, and it is mixed to carry out homogeneous
It closes, Pretreatment of Domestic Sewage and hydrolysis production waste ratio are 2:1 ~ 1:1, stirring intensity 8W/m3, time 4h, obtain
Matter composite wastewater；
3.2: biochemical
Homogeneous composite wastewater enters biochemistry pool i.e. A2The pond /O carries out the removal of denitrogenation dephosphorizing and organic matter, obtains biochemical synthesis dirt
Water；
The A2The pond /O is anaerobism, anoxic, three sections aerobic；Anaerobism section is equipped with submersible stirring pump, is thoroughly mixed sewage, reflux
Sludge, anaerobism section residence time 2.6h；Anoxic section is pumped equipped with diving propelling, sewage in pond is stirred with phegma, anoxic
Section residence time 7h；Aerobic section is equipped with more gallerys, is equipped with aerator in gallery, so that gas-water ratio is 15:1~20:1, shape in pond
At pulling flow type water distribution is thoroughly mixed, to meet biodegradable demand；
3.3: precipitating
Biochemical synthesis sewage enters in secondary settling tank, surface loading≤1.0m3/m2H, the sedimentation time is 4h, carries out solid-liquid point
From；The base sludge of secondary settling tank is sent to sludge pumping plant, and supernatant is discharged into coagulative precipitation tank, and it is 0.5%~1% that mass concentration, which is added,
Polyacrylamide and mass concentration be 1%~5% aluminium polychloride, polyacrylamide and aluminium polychloride be added the sum of volume with
The volume ratio of supernatant is 1:1000~1:100；Surface loading >=2.0m of coagulative precipitation tank3/m2H, coagulating sedimentation time is
2~3h further removes oil removal, obtains precipitating composite wastewater；
3.4: filtering
Precipitating composite wastewater is entered from bottom to top in active sand filter, and filtering velocity is 6~8m/s, filtration time >=8min, activity
Sand-bed height >=2.5m of sand filter；By coagulation, clarification, filtering a small amount of organic matter that further removal SS and SS is adsorbed, and
There is the removal amount of 5mg/L or more for TN, obtains filtering composite wastewater；
3.5: disinfection
Filtering composite wastewater enters ultraviolet disinfection pond, outlet after the coliform in ultraviolet lamp tube irradiation removal sewage；By
Ultraviolet disinfection coliform content≤103A/L obtains disinfection composite wastewater；
By the processing of above-mentioned processing step, in composite wastewater the removal rate of removal rate >=80%, NH3-N of CODcr reach >=
Removal rate >=70% of removal rate >=90%, TN of 65%, SS；
Sewage water treatment method of the invention is 11000m for production waste discharge amount3The synthesis of/d and the class pharmacy corporation that ferments
When sewage treatment, CODCrEvery year can be about 0.23 ten thousand tons of emission reduction, BOD5Annual 0.11 ten thousand tons of emission reduction, 0.11 ten thousand tons of the annual emission reduction of SS,
NH3- N every year can be 0.12 ten thousand tons of emission reduction.
Further, the production waste pipeline is equipped with accident pool, and the water inlet of accident pool is connected to by valve pipe
Produce the production waste import of pipeline；The outlet of accident pool is connected to homogeneous pond by Boosting pumping station pipeline.
Further, in step 2.1, production waste is entered in homogeneous pond by fine fack, when influent quality is exceeded, is passed through
Pharmacy sewage drains into accident regulating reservoir by valve transfer, then is promoted to homogeneous pond by the small flow of elevator pump of accident regulating reservoir
In；When the excessive influence subsequent processing of the water for flowing into production waste in homogeneous pond, extra water overflow to accident regulating reservoir
In, then by the small flow enhancement of elevator pump into homogeneous pond.
Further, it is the sodium hydroxide solution that concentration is 10% that strong base solution is added in step 2.2, in flocculation sedimentation tank.
Further, in step 3.3, the base sludge of secondary settling tank is sent to sludge pumping plant, and sludge pumping plant returns sludge a part
It flow to A2The anaerobism section in the pond /O, and returned sludge is back to anaerobism section by reflux ratio 100%~150%, a part is sent into sludge-tank, dirty
Sludge in mud sump send to after being dehydrated between sludge dewatering and transports outward.
Further, the flocculation sedimentation tank is equipped with ramp type precipitation plate.
Further, in step 3.2, the nitrate nitrogen and nitrite nitrogen that generate in aerobic section pass through 200% or more mixing
Liquid, which is back in anoxic section, occurs denitrification, generates nitrogen evolution, reaches denitrogenation purpose.
Beneficial effects of the present invention:
(1) present invention solves the problems, such as to synthesize and the processing of fermentation class pharmaceuticals industry waste water, the sanitary sewage and pharmacy to plant area are dirty
Water, which carries out individually pre-processing respectively, enters back into progress second homogenate (homogenizing time 4h or more) in conditioning tank, and two strands of sewage are abundant
Mixing, can reduce the pretreatment energy consumption of sewage, further ensure the continual and steady of biochemical system water inlet；Wherein pharmacy sewage is pre-
Independent homogeneous pond (homogenizing time 8h or more) is arranged in processing section, sewage is sufficiently mixed homogeneous, to guarantee sewage quality water
Stable and uniform in some segment again；Sanitary sewage pretreatment is removed floating material, the suspended matter in sewage by thick, fine fack
It removes, then the particulate matter in the further precipitating removal sewage for passing through setting pot, SS in sanitary sewage can be removed by pretreatment
40% or more.
(2) pretreatment (Fenton oxidation+flocculation sedimentation+hydrolysis acidification) of production waste, is greatly improved the biochemical of sewage
Property, B/C value can be risen to >=0.3 from≤0.15；Meanwhile by sewage Poisoning substance by Fenton reagent degradation toxicity, and
Sediment fraction heavy metal ion.
(3) processing of composite wastewater, wherein biochemistry pool uses the A of synchronous denitrification dephosphorizing2/ O technique, total residence time HRT=
The anaerobic zone 30.6h(HRT=2.6h, anoxic zone HRT=7h, aerobic zone HRT=21h), compared to other similar process residence times
Short and stable effluent quality can reach level-one A standard requirements, it may be assumed that CODcr, NH substantially3- N, TN, TP etc. obtain degradation and go
It removes, and standard discharge；
Sewage and exteenal reflux sludge initially enter anaerobic pond, and amphimicrobian zymogenous bacteria is by organic matter biodegradable in sewage
It is converted into VFA(volatile fat acids) this kind of low molecule fermentation intermediate product, and the poly- phosphorus that polyP bacteria can store in vivo it
Hydrochlorate decomposes, and the energy discharged survives under anaerobic environment for aerobic polyP bacteria, another part energy also for
VFA class low molecule organic matter in polyP bacteria active absorption environment, and with the poly- β hydroxybutyric acid of PHB() form stored in vivo at it
Get up, to prevent sewage from generating precipitating, sets underwater stirrer in this section；Subsequent sewage enters anoxic pond, and denitrifying bacterium utilizes
Nitrate that aerobic rank pond generates, being brought by mixed liquor reflux aoxidizes the organic matter in water inlet, together as final electron acceptor
Shi Zishen is reduced to nitrogen and escapes from water, reaches while reducing BOD5With the purpose of denitrogenation, this Duan Keshe underwater stirrer
Or a certain number of aerators；Then sewage enters the aerobic tank of aeration, polyP bacteria absorb, can biology using remnants in sewage
While degradation of organic substances, mainly released energy by the PHB stored in decomposer to maintain its growth and breeding, while excessive
The dissolution phosphorus in ambient enviroment is absorbed, and is stockpiled in vivo in the form of poly- phosphorus, reaches dissolution phosphorus concentration in water outlet most
It is low；And BOD5After anaerobic pond, anoxic pond are utilized by polyP bacteria and denitrifying bacterium respectively, the aerobic tank for being equipped with aerator is reached
When concentration decreased, and significantly degraded in aerobic tank by aerobic microbiological, BOD5The reduction of concentration is conducive to autotrophic type
The growth and breeding of nitrifier, and be nitrate by mineralized nitrogen by nitrification.In the excess sludge of discharge, due to containing big
Amount energy excess stockpiles the polyP bacteria of poly- phosphorus, and P content in sludge is up to 6%(dry weight) more than.
(4) composite wastewater is discharged after biochemistry enters secondary settling tank separation of solid and liquid, and major pollutants SS is removed to 20mg/L
Hereinafter, the sludge part of sedimentation in secondary sedimentation tank is as activity sludge reflux (100%~150% reflux ratio) to A simultaneously2The pond /O is to meet
The sludge concentration in the pond O reaches 3~4mg/L or more；Again by mixed precipitation, the further coagulation of partial suspended thing is removed, to subtract
The load of light subsequent treatment section.
(5) coagulative precipitation tank water outlet is entered from bottom to top in active sand filter, and filtering is using collection coagulation, clarification, filtering
The high efficiency filter processing being integrated is not required to backwashing water, low water damage, greatly reduces energy consumption；Meanwhile it further being gone by sand filtration
Except a small amount of organic matter that SS and SS is adsorbed, guarantee that the SS in water outlet reaches 10mg/L hereinafter, high casting bed has 3~5mg/L for TN
Above removal amount, it is up to standard to TN to provide safeguard.
Detailed description of the invention
Fig. 1 is system flow chart of the invention.
Specific embodiment
In order to make the objectives, technical solutions, and advantages of the present invention clearer, with reference to the accompanying drawings and embodiments, right
The present invention is further elaborated.It should be appreciated that the specific embodiments described herein are only used to explain the present invention,
It is not intended to limit the present invention.
A kind of synthesis of the invention and the class pharmaceuticals industry sewage water treatment method that ferments are based on synthesis and fermentation class pharmacy work
Industry sewage disposal system, system include garden sanitary sewage pipeline, garden production waste pipeline, conditioning tank, A2The pond /O, two sink
Pond, coagulative precipitation tank, active sand filter and ultraviolet disinfection pond；Garden sanitary sewer road is equipped with Boosting pumping station and setting pot；
Homogeneous pond, Fenton oxidation pond, flocculation sedimentation tank and hydrolysis acidification pool are sequentially communicated on garden production waste pipeline；The hydrolysis
The water outlet of acidification pool and setting pot pass through respectively pipeline connection the entrance of conditioning tank；Conditioning tank, A2The pond /O, is mixed secondary settling tank
Solidifying sedimentation basin, active sand filter and ultraviolet disinfection pond are sequentially communicated by pipeline；It is additionally provided on the garden production waste pipeline
The water inlet of accident pool, accident pool is connected to the production waste import that garden produces pipeline by valve pipe；Accident pool goes out
Mouth is connected to homogeneous pond by Boosting pumping station pipeline；
Treatment sewage is the sewage effluent of synthesis and fermentation class pharmaceuticals industry, wherein synthesis and fermentation class pharmacy sewage discharge amount
For 11000m3/ d, sanitary sewage discharge amount 14000m3/d；
Sewage treatment step is as follows:
(1) sanitary sewage pre-processes
Sanitary sewage flows into Boosting pumping station by coarse rack, then flows into setting pot by fine fack；Wherein coarse rack and fine fack
By the floating material in sanitary sewage, suspended matter removal, the particulate matter in sanitary sewage is removed by the further precipitating of setting pot,
Residence time >=30s；SS can be down to 150mg/L from 250mg/L hereinafter, removal rate reaches 40% or more by pretreatment.?
To Pretreatment of Domestic Sewage.
Sanitary sewage influent quality water such as table 1:
(2) production waste pre-processes
2.1: homogenizing
Production waste, that is, pharmacy sewage flows into homogeneous pond, the first floating material and suspended matter in removal pharmacy sewage through fine fack；
Agitated machine stirring again, stirring intensity 8W/m3, mixing time 8h；Water quality and quantity homogeneous is mixed to get homogenizing production waste；
Independent homogeneous pond is arranged in pharmaceuticals industry sewage disinfection treatment section, sewage is sufficiently mixed homogeneous, to guarantee sewage quality water
Amount stable and uniform in some segment；
When influent quality is exceeded, production waste, that is, pharmacy sewage is drained by accident regulating reservoir by valve transfer, then by accident
The small flow of the elevator pump of conditioning tank is promoted in homogeneous pond；When the excessive influence subsequent processing of the water of pharmacy sewage in homogeneous pond
When, extra water overflow is into accident regulating reservoir, then by the small flow enhancement of elevator pump into homogeneous pond.
2.2: biochemistry pretreatment
Homogenizing production waste enters Fenton oxidation pond, and it is 4~5 that sulfuric acid, which is added, and adjusts the pH value of homogenizing production waste；Add sweet smell
The reagent that pauses carries out Fenton oxidation reaction, wherein H2O2/Fe2+Mass values be 20；The stirring intensity of Fenton oxidation reaction >=
20W/m3, reaction time 90min；The ring molecule and long-chain molecule organic matter for obtaining homogenizing production waste carry out chain rupture decomposition
At the biochemical production waste of small organic molecule；
Biochemical production waste enters flocculation sedimentation tank, and the flocculation sedimentation tank is equipped with ramp type precipitation plate；Add in flocculation sedimentation tank
Enter the sodium hydroxide solution that concentration is 10%, carry out acid-base neutralization reaction, reaction time 20min adjusts the pH value of production waste
It is 7~9；Flocculation sedimentation, flocculation sedimentation time are 2.5h, surface loading >=2.0m to production waste under alkaline condition3/m2·h；
Obtain precipitating production waste；
Precipitating production waste enters hydrolysis acidification pool, and hydrolysis acidification pool is flowed back using mud method, by adequately stirring that reflux is dirty
Mud and sewage mixed hydrolysis, stirring intensity 8W/m3, mixing time 10h, by sewage toxicity and macromolecular substances into one
The hydrolysis acidification of step, makes particulate matter be hydrolyzed to dissolved matter；Obtain acidification production waste；
>=0.3 is risen to from≤0.15 through biochemical pretreated production waste B/C value, the biodegradability of production waste improves；
Sewage Poisoning substance is passed through into Fenton reagent degradation toxicity, and sediment fraction heavy metal ion simultaneously.
Production waste influent quality water such as table 2:
Sanitary sewage is individually pre-processed with production waste by step (1) and step (2), reduces the fluctuation pair of water quality and quantity
The impact of system influences, while can reduce the pretreatment energy consumption of sewage.
(3) processing of composite wastewater
3.1: mixing
Step (1) Pretreatment of Domestic Sewage and step (2) hydrolysis production waste are flowed into conditioning tank and are stirred, and it is mixed to carry out homogeneous
It closes, stirring intensity 8W/m3, time 4h, obtain homogeneous composite wastewater.
3.2: biochemical
Homogeneous composite wastewater enters biochemistry pool i.e. A2The pond /O carries out the removal of denitrogenation dephosphorizing and organic matter；Obtain biochemical synthesis dirt
Water；
The A2The pond /O is anaerobism, anoxic, three sections aerobic；Anaerobism section is equipped with submersible stirring pump, is thoroughly mixed sewage, reflux
Sludge, anaerobism section residence time 2.6h；Anoxic section is pumped equipped with diving propelling, sewage in pond is stirred with phegma, anoxic
Section residence time 7h；Aerobic section is equipped with more gallerys, is equipped with aerator in gallery, so that gas-water ratio is 17:1 in pond, is formed complete
Mix pulling flow type water distribution, aerobic section residence time 21h；The nitrate nitrogen and nitrite nitrogen generated in aerobic section by 200% with
On mixed liquor be back in anoxic section denitrification occur, generate nitrogen evolution, reach denitrogenation purpose.
This technique biological treatment part is made of anaerobic pond, anoxic pond, aerobic tank.Sewage and exteenal reflux sludge initially enter
Organic matter biodegradable in sewage is converted VFA(volatile fat acids by anaerobic pond, amphimicrobian zymogenous bacteria) this
Class low molecule fermentation intermediate product, and polyP bacteria can decompose the Quadrafos that it is stored in vivo, the energy discharged is for good
The polyP bacteria of oxygen is survived under anaerobic environment, and another part energy is also for the VFA class in polyP bacteria active absorption environment
Low molecule organic matter, and with the poly- β hydroxybutyric acid of PHB() form stored in vivo at it, to prevent sewage from generating precipitating, herein
Section sets underwater stirrer；Subsequent sewage enters anoxic pond, and denitrifying bacterium is using generating in aerobic rank pond, flowed back band by mixed liquor
The nitrate entered aoxidizes the organic matter in water inlet as final electron acceptor, while itself being reduced to nitrogen and escaping from water,
Reach while reducing BOD5With the purpose of denitrogenation, this Duan Keshe underwater stirrer or a certain number of aerators；Then sewage into
Enter the aerobic tank of aeration, polyP bacteria absorb, using remaining biodegradable organic in sewage while, mainly pass through decomposition
The PHB stored in vivo releases energy to maintain its growth and breeding, while the dissolution phosphorus in excessive intake ambient enviroment, and with poly-
The form of phosphorus stockpiles in vivo, and dissolution phosphorus concentration in water outlet is made to reach minimum；And BOD5Through anaerobic pond, anoxic pond respectively by
After polyP bacteria and denitrifying bacterium utilize, concentration has decreased when reaching the aerobic tank for being equipped with aerator, and in aerobic tank
It is significantly degraded by aerobic microbiological, BOD5The reduction of concentration is conducive to the growth and breeding of autotrophic type nitrifier, and is made by nitrification
It is nitrate with by mineralized nitrogen.In the excess sludge of discharge, due to stockpiling the polyP bacteria of poly- phosphorus, sludge containing largely energy excess
Phosphorus content is up to 6%(dry weight) more than.
3.3: precipitating
Biochemical synthesis sewage enters in secondary settling tank, surface loading≤1.0m3/m2H, the sedimentation time is 4h, carries out solid-liquid point
From；The base sludge of secondary settling tank is sent to sludge pumping plant, and supernatant is discharged into coagulative precipitation tank, be added mass concentration be 0.8% it is poly-
Acrylamide and mass concentration are 3% aluminium polychloride, and the sum of volume and supernatant is added in polyacrylamide and aluminium polychloride
Volume ratio is 1:200；Surface loading >=2.0m3/m2H, coagulating sedimentation time are 2.5h, SS are removed to 20mg/L hereinafter, obtaining
To precipitating composite wastewater；The base sludge of secondary settling tank is sent to sludge pumping plant, and sludge a part is back to A by sludge pumping plant2The pond /O
Anaerobism section, and returned sludge is back to anaerobism section by reflux ratio 120%, reaches 3.5mg/L or more to meet the sludge concentration in the pond O.
Again by mixed precipitation, the further coagulation of partial suspended thing is removed, to mitigate the load of subsequent treatment section；Sludge pumping plant will be another
A part is sent into sludge-tank, and the sludge in sludge-tank, which is sent to after being dehydrated between sludge dewatering, to be transported outward.
3.4: filtering
When precipitating composite wastewater enters active sand filter, treatment sewage enters filtering by the water distributor for being located at filter bottom
Device, water flow from bottom to top countercurrently by filter bed, assemble in filter top by filtered fluid after filtering, flows out, obtains through overflow port
To filtering composite wastewater；The contaminated filtrate of filter bottom is thus lifted to the washed-out sand of filter top by air lift
Device separates pollutant from active sand by action of turbulent flow, and impurity is discharged by cleaning water outs, and net sand utilizes self weight
Casting bed is returned to realize continuous filtering.Using single-stage filtrate, it is not necessarily to gradation, no waterpower is unevenly distributed and primary filtrate, is not required to
It shuts down backwash and is not required to external backwashing water, head loss is less than 1.2m, backwash water is about the 5%~8% of processing capacity, filter
Speed is 7m/s, filtration time >=8min, sand-bed height >=2.5m of active sand filter；
Further remove SS and SS absorption a small amount of organic matter, guarantee water outlet in SS reach 10mg/L hereinafter, high casting bed for
TN has the removal amount of 3~5mg/L or more, up to standard to TN to provide safeguard.
3.5: disinfection
Filtering composite wastewater enters ultraviolet disinfection pond, outlet after the coliform in ultraviolet lamp tube irradiation removal sewage；At peak
When value flow and UV transmittance are 65%, effective uv dosage achieved by lamp tube service life terminal is not less than 25mJ/cm2；?
To disinfection composite wastewater, coliform content≤10 of composite wastewater are sterilized3A/L.
By the processing of above-mentioned processing step, removal rate >=80%, NH3-N removal rate of the CODcr of composite wastewater reaches >=
65%, SS removal rate >=90%, TN removal rate >=70%, CODCrEvery year can be about 0.23 ten thousand tons of emission reduction, BOD5Annual emission reduction 0.11 ten thousand
Ton, 0.11 ten thousand tons of the annual emission reduction of SS, NH3- N every year can be 0.12 ten thousand tons of emission reduction.
Sewage discharge index such as table 3 after above-mentioned process:
As it will be easily appreciated by one skilled in the art that the foregoing is merely illustrative of the preferred embodiments of the present invention, not to limit
The present invention, any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in this
Within the protection scope of invention.
Claims (7)
1. a kind of synthesis and fermentation class pharmaceuticals industry sewage water treatment method, the method is based on synthesizing and fermentation class pharmaceuticals industry is dirty
Water treatment system, system include garden sanitary sewage pipeline, garden production waste pipeline, homogeneous pond, Fenton oxidation pond, flocculate and sink
Shallow lake pond, hydrolysis acidification pool, conditioning tank, A2The pond /O, secondary settling tank, coagulative precipitation tank, active sand filter and ultraviolet disinfection pond；The garden
Area sanitary sewer road is equipped with Boosting pumping station and setting pot；Be sequentially connected in series on the garden production waste pipeline homogeneous pond,
Fenton oxidation pond, flocculation sedimentation tank and hydrolysis acidification pool；The water outlet of the hydrolysis acidification pool and setting pot passes through pipeline respectively
It is connected to the entrance of conditioning tank；Conditioning tank, A2The pond /O, secondary settling tank, coagulative precipitation tank, active sand filter and ultraviolet disinfection pond pass through
Pipeline is sequentially communicated；It is characterized in that, sewage treatment operating procedure is as follows:
(1) sanitary sewage pre-processes
Sanitary sewage flows into Boosting pumping station by coarse rack, then flows into setting pot by fine fack；Wherein coarse rack and fine fack
By the floating material in sanitary sewage, suspended matter removal, the particulate matter in sanitary sewage is removed by the further precipitating of setting pot,
Residence time >=30s；SS removal rate >=40% in sanitary sewage；Obtain Pretreatment of Domestic Sewage；
(2) production waste pre-processes
2.1: homogenizing
Production waste, that is, pharmacy sewage flows into homogeneous pond, the first floating material and suspended matter in removal pharmacy sewage through fine fack；
Agitated machine stirring again, stirring intensity 8W/m3, mixing time 8h；Water quality and quantity homogeneous is mixed to get homogenizing production waste；
2.2: biochemistry pretreatment
Homogenizing production waste enters Fenton oxidation pond, and it is 4~5 that sulfuric acid, which is added, and adjusts the pH value of homogenizing production waste；Add sweet smell
The reagent that pauses carries out Fenton oxidation reaction, wherein H2O2/Fe2+Mass values be 15~25；The stirring intensity of Fenton oxidation reaction
≥20W/m3, reaction time 90min；Ring molecule and long-chain molecule organic matter is obtained to carry out chain rupture to resolve into small molecule organic
The biochemical production waste of object；
Biochemical production waste enters flocculation sedimentation tank, and the strong base solution that concentration is 10% is added, and carries out acid-base neutralization reaction, reaction
Time is 10 ~ 30min, adjust biochemical production waste into pH value be 7~9；Biochemical production waste flocculates heavy under alkaline condition
It forms sediment, the flocculation sedimentation time is 2~3h, surface loading >=2.0m3/m2H obtains precipitating production waste；
Precipitating production waste enters hydrolysis acidification pool, and hydrolysis acidification pool is flowed back using mud method, by adequately stirring that reflux is dirty
Mud and precipitating production waste mixed hydrolysis, stirring intensity are 6 ~ 12W/m3, mixing time 12h, will precipitating production waste in
Toxicity and the further hydrolysis acidification of macromolecular substances, make particulate matter be hydrolyzed to dissolved matter, obtain hydrolysis production waste；
(3) composite wastewater is handled
3.1: mixing
Pretreatment of Domestic Sewage and hydrolysis production waste are entered in conditioning tank and stirred, homogeneous mixing is carried out；Pretreatment life
Sewage and hydrolysis production waste ratio 2:1 ~ 1:1, stirring intensity 8W/m3, time 4h, obtain homogenizing composite wastewater；
3.2: biochemical
Homogenizing composite wastewater enters biochemistry pool i.e. A2The pond /O carries out the removal of denitrogenation dephosphorizing and organic matter, obtains biochemical synthesis dirt
Water；
The A2The pond /O is anaerobism, anoxic, three sections aerobic；Anaerobism section is equipped with submersible stirring pump, is thoroughly mixed sewage and flows back
Sludge, anaerobism section residence time 2.6h；Anoxic section is pumped equipped with diving propelling, sewage in pond is stirred with phegma, anoxic
Section residence time 7h；Aerobic section is equipped with more gallerys, is equipped with aerator in gallery, so that gas-water ratio is 15:1~20:1, shape in pond
At pulling flow type water distribution is thoroughly mixed, to meet biodegradable demand；
3.3: precipitating
Biochemical synthesis sewage enters in secondary settling tank, surface loading≤1.0m3/m2H, the sedimentation time is 4h, carries out solid-liquid point
From；The base sludge of secondary settling tank is sent to sludge pumping plant, and supernatant is discharged into coagulative precipitation tank, and it is 0.5%~1% that mass concentration, which is added,
Polyacrylamide and mass concentration be 1%~5% aluminium polychloride, the sum of polyacrylamide and the addition volume of aluminium polychloride
And the ratio of supernatant volume is 1:1000~1:100, coagulative precipitation tank surface loading >=2.0m3/m2H, coagulating sedimentation time is
2~3h, further coagulating sedimentation remove oil removal, obtain precipitating composite wastewater；
3.4: filtering
Precipitating composite wastewater is passed through active sand filter from bottom to top, and the filtering velocity of active sand filter is 6~8m/s, filtration time >=
8min, sand-bed height >=2.5m of active sand filter；By in coagulation, clarification, filtering further removal precipitating composite wastewater
A small amount of organic matter of SS and SS absorption, and have the removal amount of 5mg/L or more for TN, obtain filtering composite wastewater；
3.5: disinfection
Filtering composite wastewater enters ultraviolet disinfection pond, outlet after the coliform in ultraviolet lamp tube irradiation removal sewage；By
Ultraviolet disinfection coliform content≤103A/L obtains disinfection composite wastewater；
By the processing of above-mentioned processing step, sterilize the removal rate of removal rate >=80%, NH3-N of CODcr in composite wastewater >=
Removal rate >=70% of removal rate >=90%, TN of 65%, SS；
Sewage water treatment method of the invention is 11000m for production waste discharge amount3The synthesis of/d and the class pharmacy corporation that ferments
When sewage treatment, CODCrEvery year can be about 0.23 ten thousand tons of emission reduction, BOD5Annual 0.11 ten thousand tons of emission reduction, 0.11 ten thousand tons of the annual emission reduction of SS,
NH3- N every year can be 0.12 ten thousand tons of emission reduction.
2. a kind of synthesis and fermentation class pharmaceuticals industry sewage water treatment method according to claim 1, it is characterised in that: the life
Produce plumbing drain and be equipped with accident pool, the water inlet of accident pool be connected to by valve pipe produce the production waste of pipeline into
Mouthful；The outlet of accident pool is connected to homogeneous pond by Boosting pumping station pipeline.
3. a kind of synthesis and fermentation class pharmaceuticals industry sewage water treatment method according to claim 1, it is characterised in that: step
In 2.1, production waste is entered in homogeneous pond by fine fack, when influent quality is exceeded, by valve transfer by pharmacy sewage
It drains into accident regulating reservoir, then is promoted in homogeneous pond by the small flow of elevator pump of accident regulating reservoir；It is given birth to when being flowed into homogeneous pond
When producing the excessive influence subsequent processing of water of sewage, extra water overflow is into accident regulating reservoir, then by the small flow of elevator pump
It is promoted in homogeneous pond.
4. a kind of synthesis and fermentation class pharmaceuticals industry sewage water treatment method according to claim 1, it is characterised in that: step
It is the sodium hydroxide solution that concentration is 10% that strong base solution is added in 2.2, in flocculation sedimentation tank.
5. a kind of synthesis and fermentation class pharmaceuticals industry sewage water treatment method according to claim 1, it is characterised in that: step
In 3.3, the base sludge of secondary settling tank is sent to sludge pumping plant, and sludge a part is back to A by sludge pumping plant2The anaerobism section in the pond /O,
And returned sludge is back to anaerobism section by reflux ratio 100%~150%, a part is sent into sludge-tank, and the sludge in sludge-tank is sent to dirt
It is transported outward after being dehydrated between mud dehydration.
6. a kind of synthesis and fermentation class pharmaceuticals industry sewage water treatment method according to claim 3, it is characterised in that: the wadding
Solidifying sedimentation basin is equipped with ramp type precipitation plate.
7. a kind of synthesis and fermentation class pharmaceuticals industry sewage water treatment method according to claim 1, it is characterised in that: step
In 3.2, the nitrate nitrogen and nitrite nitrogen generated in aerobic section is back to anoxic Duan Zhongfa by 200% or more mixed liquor
Raw denitrification generates nitrogen evolution, reaches denitrogenation purpose.
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| CN110627277A (en) * | 2019-10-24 | 2019-12-31 | 常飞 | Pharmaceutical factory sewage treatment method |
| CN111875189A (en) * | 2020-08-15 | 2020-11-03 | 海南绿境高科环保有限公司 | Treatment device containing biological-resistant mixed pharmaceutical wastewater |
| CN112551817A (en) * | 2020-12-17 | 2021-03-26 | 安徽舜禹水务股份有限公司 | Mixed wastewater integrated sewage treatment system |
| CN112851045A (en) * | 2021-03-02 | 2021-05-28 | 重庆化工职业学院 | Sulfanilamide wastewater treatment system and method |
| CN113548773A (en) * | 2021-08-09 | 2021-10-26 | 东华工程科技股份有限公司 | Industrial park wastewater pretreatment method and system |
| CN115259540A (en) * | 2022-05-17 | 2022-11-01 | 景德镇澳蓝亚特环境科技有限公司 | A kind of treatment method of respiratory targeted drug wastewater |
| CN115367952A (en) * | 2022-07-19 | 2022-11-22 | 江苏绿境生态环境科技股份有限公司 | High-salinity sewage accident sewage and low-salinity high-concentration sewage comprehensive treatment system and method |
| CN115385529A (en) * | 2022-09-08 | 2022-11-25 | 江苏百英生物科技有限公司 | Antibody protein purification wastewater treatment method |
| CN115947480A (en) * | 2022-12-22 | 2023-04-11 | 新泰清源水务有限公司 | Industrial wastewater treatment process and system based on multistage precipitation |
| CN116462374A (en) * | 2023-05-25 | 2023-07-21 | 长江生态环保集团有限公司 | A pretreatment method for industrial wastewater in a composite sewage treatment plant |
| CN116553774A (en) * | 2023-05-25 | 2023-08-08 | 长江生态环保集团有限公司 | A hybrid wastewater treatment method that improves biodegradability and optimizes carbon source allocation |
| CN118026435A (en) * | 2024-02-01 | 2024-05-14 | 中联西北工程设计研究院有限公司 | Alcohol extraction type toxic pharmaceutical wastewater resource utilization process treatment system and treatment method |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110627277A (en) * | 2019-10-24 | 2019-12-31 | 常飞 | Pharmaceutical factory sewage treatment method |
| CN111875189A (en) * | 2020-08-15 | 2020-11-03 | 海南绿境高科环保有限公司 | Treatment device containing biological-resistant mixed pharmaceutical wastewater |
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| CN112551817A (en) * | 2020-12-17 | 2021-03-26 | 安徽舜禹水务股份有限公司 | Mixed wastewater integrated sewage treatment system |
| CN112851045A (en) * | 2021-03-02 | 2021-05-28 | 重庆化工职业学院 | Sulfanilamide wastewater treatment system and method |
| CN113548773A (en) * | 2021-08-09 | 2021-10-26 | 东华工程科技股份有限公司 | Industrial park wastewater pretreatment method and system |
| CN115259540A (en) * | 2022-05-17 | 2022-11-01 | 景德镇澳蓝亚特环境科技有限公司 | A kind of treatment method of respiratory targeted drug wastewater |
| CN115367952A (en) * | 2022-07-19 | 2022-11-22 | 江苏绿境生态环境科技股份有限公司 | High-salinity sewage accident sewage and low-salinity high-concentration sewage comprehensive treatment system and method |
| CN115385529A (en) * | 2022-09-08 | 2022-11-25 | 江苏百英生物科技有限公司 | Antibody protein purification wastewater treatment method |
| CN115947480A (en) * | 2022-12-22 | 2023-04-11 | 新泰清源水务有限公司 | Industrial wastewater treatment process and system based on multistage precipitation |
| CN116462374A (en) * | 2023-05-25 | 2023-07-21 | 长江生态环保集团有限公司 | A pretreatment method for industrial wastewater in a composite sewage treatment plant |
| CN116553774A (en) * | 2023-05-25 | 2023-08-08 | 长江生态环保集团有限公司 | A hybrid wastewater treatment method that improves biodegradability and optimizes carbon source allocation |
| CN118026435A (en) * | 2024-02-01 | 2024-05-14 | 中联西北工程设计研究院有限公司 | Alcohol extraction type toxic pharmaceutical wastewater resource utilization process treatment system and treatment method |
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Application publication date: 20190517 |