CN102198997B - Treatment process method for wastewater from abscisic acid production - Google Patents

Treatment process method for wastewater from abscisic acid production Download PDF

Info

Publication number
CN102198997B
CN102198997B CN201110095687A CN201110095687A CN102198997B CN 102198997 B CN102198997 B CN 102198997B CN 201110095687 A CN201110095687 A CN 201110095687A CN 201110095687 A CN201110095687 A CN 201110095687A CN 102198997 B CN102198997 B CN 102198997B
Authority
CN
China
Prior art keywords
waste water
water
pond
mud
wastewater
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.)
Active
Application number
CN201110095687A
Other languages
Chinese (zh)
Other versions
CN102198997A (en
Inventor
田庆华
刘敏
邵家华
王涛
刘学峰
杨斌中
岳峻
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Longmang Fusheng Science &. Technology Co., Ltd., Sichuan Prov.
Sichuan Environmental Protection Science and Technology Engineering Co., Ltd.
Original Assignee
SICHUAN ENVIRONMENTAL PROTECTION SCIENCE AND TECHNOLOGY ENGINEERING Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by SICHUAN ENVIRONMENTAL PROTECTION SCIENCE AND TECHNOLOGY ENGINEERING Co Ltd filed Critical SICHUAN ENVIRONMENTAL PROTECTION SCIENCE AND TECHNOLOGY ENGINEERING Co Ltd
Priority to CN201110095687A priority Critical patent/CN102198997B/en
Publication of CN102198997A publication Critical patent/CN102198997A/en
Application granted granted Critical
Publication of CN102198997B publication Critical patent/CN102198997B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Abstract

The invention relates to a treatment process method for wastewater from abscisic acid production. In the method provided by the invention, a high-concentration acidic extraction wastewater toxicity removing method and a multistage counter flow load control biological method are combined, a UASB (upflow anaerobic sludge blanket) anaerobic treatment section and a concentration gradient water distribution section are added, and three-grade sludge return three-stage clean water (treated water) is adopted to recycle and treat mixed wastewater which is generated during abscisic acid production, has high concentration (CODcr>100,000 mg/L) and high impact load, and contains refractory large molecules according to the pollution concentration change (pollutant load gradient and change). The treatment process method is high in impact load resisting capability and can be used for solving the difficulty in the treatment of ultrahigh-concentration wastewater from biological fermentation in China; and the wastewater effluent can reach the first-class standard of GB8978-1996.

Description

Dormin production wastewater treatment process method
Technical field
The present invention relates to process for treating industrial waste water, is the waste water treatment technology that is produced in dormin (S-abscisic acid) production process specifically, is applicable to that handling the composite waste that produces in the biotechnology fermentation enterprise production process handles; Processing especially for ultrahigh concentration (CODcr >=100,000 mg/L) organic waste water.
Background technology
[S-abscisic acid]: formal name used at school dormin, English name Abscisic Acid (being called for short ABA).The S-abscisic acid is the Chinese popular name through the name of national pesticide standard Technical Committee.CA registration number: 21293-29-8.
International (ISO) common name: (+)-cis, trans-Abscisic acid.
Chemical name (IUPAC): 5-(1 '-hydroxyl-2 ', 6 ', 6 '-trimethylammonium-4 '-oxo-2 '-tetrahydrobenzene-1 '-yl)-3-methyl-2-is suitable-and 4-is anti--pentadienoic acid.
[empirical formula]: C 15H 20O 4Relative molecular mass: 264.32.
Dormin is the sesquiterpenoid of one 15 carbon.Naturally occurring dormin is an enantiomorph, particularly dextrorotatory compound (S)-ABA.(R)-physiologically active of ABA is identical with (S)-ABA as a rule.Its physiologically active depends on following condition: 1. free carboxyl group is arranged, 2. on the cyclohexane ring α-or beta-position two keys are arranged, 3. two keys at C-2 place are cis.The trans ABA of 2-just has activity after the isomerizing in light.The free acid that ester compound produces after the hydrolysis of ester chain also has activity.PBI 58 is a white crystalline powder, is soluble in methyl alcohol, ethanol, acetone, chloroform, ETHYLE ACETATE and trichloromethane etc., is insoluble in ether, benzene etc., water solubility 3-5g/L (20 ℃).The stability of dormin is better, normal temperature held 2 years, and active constituent content is constant basically, but should preserve in dry, shady and cool, the sealing of lucifuge place.The dormin aqueous solution belongs to the high light decomposition compound to photaesthesia.
It is one of four big plant growth hormoness that dormin and growth hormone, Plant hormones regulators,gibberellins, phytokinin are listed as, and dormin is present in the leaf, statoblast, mature seed of plant.Usually many than in the tender part of children of the content in the organ or tissue of aging.Its effect is to suppress RNA and proteinic synthetic, thereby suppresses stem and lateral bud growth, is a kind of growth inhibitor therefore, helps cell volume and increases.It and Plant hormones regulators,gibberellins have antagonistic action.Dormin promotes coming off of petiole through the formation that promotes absciss layer, is that it can make the activity of the acidifying of cell walls environment, lytic enzyme increase, and can also promote bud and seed dormancy.Higher dormin content is seed dormant major cause in the seed.Seeds such as the peach of handling through lamination, Korean pine are easy to sprouting because of wherein dormin content reduces, and dormin is also relevant with the switching of blade pore.During the wheat leaf blade arid, dormin content increases in the stomata guard cell, and pore is just closed, thereby can reduce rising dehydration.The gravity property motion of the tip of a root is relevant with the distribution of dormin.
The S-abscisic acid produce by: fermentation workshop section, extraction and reextraction workshop section, refining workshop section form.Fermentation workshop section uses the sub product of grain or grain processing to be the master, makes fermention medium, and the microbe inoculation bacterial classification carries out shake-flask culture, first order seed cultivation, secondary seed cultivation, fermentation culture; Extract workshop section and comprise Plate Filtration, micro-filtration (MF), ultrafiltration (UF), nanofiltration (NF), acid out, spinning, extraction, primary crystallization, filtration; Reextraction workshop section comprises mixing, reextraction, spraying drying; Refining workshop section comprises: dissolving, recrystallization, filtration, washing, oven dry.(this production technique is enterprise's security information, receives related patent U.S. Patent No. protection)
The composite waste that produces in the S-abscisic acid production process is mainly by 7 kinds of waste water compositions such as fermentor tank rinse water, sheet frame washing water, film rinse water, MF debris, UF debris, nanofiltration (NF) waste liquid, extraction wastewater, and a day sewage effluent amount is 600: 1～1200: 1 with respect to the target compound rate ratio.The CODcr and the ammonia nitrogen content of composite waste are high; Extraction wastewater wherein more so; Its CODcr concentration between 100,000～150,000 mg/l, ammonia nitrogen concentration between 500～2500mg/l, pH=0.4～2; Belong to the high concentrated acid property extraction wastewater that is difficult to handle, before research the present invention, do not see have report such waste water to be carried out the effective system treatment project case of success.
Summary of the invention
The purpose of this invention is to provide the dormin production wastewater treatment process method that a kind of water outlet reaches GB (GB8978-1996) primary standard, to solve the difficult problem of the ultrahigh concentration wastewater treatment of handling the biological fermentation generation.
The objective of the invention is to realize like this: a kind of dormin production wastewater treatment process method; This factory effluent is formed has the fermentor tank rinse water, 8 kinds of sheet frame washing water, film rinse water, MF debris, UF debris, nanofiltration waste liquid, extraction wastewater and sanitary wastewaters, carries out in order according to the following steps:
A), extraction wastewater is handled:
Adopt high concentrated acid property extraction wastewater toxicity total system that extraction wastewater is carried out pre-treatment, to regulate the pH value and to remove sulfate ion
B) concentration step water distribution:
Pretreated extraction wastewater is mixed with said all the other 7 kinds of factory effluents, carry out the ladder water distribution by concentration during mixing, water distribution first is with this composite waste CODcr concentration adjustment to 10,000～20,000mg/L;
C) two-stage UASB anaerobic treatment:
Waste water after the water distribution is carried out anaerobic treatment in two-stage UASB pond; Carry out mud-water separation through deposition again; The water distribution once more of waste water after the mud-water separation, with waste water COD cr concentration adjustment to 500～800mg/L, the mud after the mud-water separation passes back into respectively in the anaerobic reaction district in two-stage UASB pond;
D) mud backflow biochemical treatment:
In the active sludge aerobic pond, the waste water after the UASB anaerobic treatment being carried out active sludge aerobic handles; Waste water after the active sludge aerobic settling tank precipitate and separate is sent into biological contact Aerobic Pond and is carried out biology contact aerobic treatment; Waste water after biological contacting sedimentation tank precipitate and separate is sent into the advanced treatment operation again; And the isolating mud of active sludge aerobic settling tank passes back into the active sludge aerobic pond, and the isolating mud of biological contacting sedimentation tank passes back into biological contact Aerobic Pond;
E) advanced treatment:
The waste water that is come by the biochemical treatment operation gets into clean water basin after sand filtration is handled, the waste water COD cr that gets into clean water basin reduces to 90～100mg/L, and ammonia nitrogen is 8～12mg/L;
Above-mentioned a is in the step, and the extraction wastewater treatment step is following:
A1) high concentrated acid property extraction wastewater is added excess amount of Ca (OH) in the conditioning tower 2, press H +Concentration is calculated, and is excessive 3%～4%, regulates waste water ph to pH value 9～11, sulfate ion in the waste water and Ca 2+The reaction back generates CaSO 4Deposition is through accomplishing SO after the precipitate and separate 4 2-Remove;
A2) remove SO 4 2-After waste water through being pumped into neutralizing tower, and add the excessive waste water of handling without the conditioning tower at neutralizing tower, press OH -Concentration is calculated, and waste water is excessive 1%～2%, the SO in the waste water 4 2-With dissolved Ca in the waste water 2+The reaction back generates CaSO for the second time 4Deposition is accomplished Ca through precipitate and separate 2+Remove, reduce subsequent handling equipment scaling incidence;
A3) waste water of handling through alkali and excessive acid in the neutralizing tower adds excessive NaOH simultaneously by being pumped into knockout tower, presses H +Concentration is calculated, and NaOH is excessive 10%～20%, regulates between waste water ph to 9～10 for the second time; Use steam indirect heating waste water then, make wastewater temperature near its boiling point, keep this temperature; In waste water, blast pressurized air through tower inner bottom part air feeder; Make the extraction solvent in the waste water bring gas phase into by air by a certain percentage, the part extraction solvent is separated from waste water, the gas that contains extraction solvent imports boiler house gas blower pipeline; Send in the boiler and use, when blasting air, use waste water to spray through the spray equipment in the knockout tower as combustion-supporting gas.
Above-mentioned high concentrated acid property extraction wastewater is by being produced in the biological fermented product production process, this wastewater pH=0.4～2.0, and CODcr concentration is 100,000～150,000 mg/L, ammonia nitrogen concentration is 2000～7000mg/L, SO 4 2-Concentration is 480～38000mg/L, contains part by weight simultaneously and be 2%～4% extraction solvent; This extraction solvent is mainly sherwood oil, ETHYLE ACETATE, butylacetate; After knockout tower was handled, the CODcr of waste water was reduced to 80,000～100,000 mg/L, and ammonia nitrogen is reduced to 1500～5000mg/L.
Above-mentioned b step concentration step water distribution concrete steps are: the film rinse water flows into high pH pond, and one batch film rinse water is utilized the hydrochloric acid dispensing slot after all mixing, and adds HCl solution, regulates pH 9～10, pumps into the water distribution equalizing tank; Sheet frame washing water, MF debris, UF debris and nanofiltration waste liquid pump into the water distribution equalizing tank after getting into high dense mixed pond mixing; Sanitary wastewater mixes with the fermentor tank rinse water after after the artificial fine fack processing of artificial coarse rack (10) of one-level and two-stage, get into low dense mixed pond;
Above-mentioned a step extraction wastewater is handled concrete steps and is: every batch of extraction wastewater 20m 3/～40m 3The disposable extraction wastewater container for storing liquid that enters is stored, and pumps into high concentrated acid property extraction wastewater toxicity total system and handles, and waste water after treatment mixes with above-mentioned other waste water that has got in the pond from flowing into the water distribution equalizing tank; The waste water that perhaps will hang down dense mixed pond again pumps into the water distribution equalizing tank and carries out water distribution; Water distribution equalizing tank CODcr concentration is controlled at 10,000～20 the most at last, in the 000mg/L technic index;
Above-mentioned c step two-stage UASB anaerobic treatment concrete steps are: adopt lift pump will be stored in the waste water that allotment is good in the water distribution equalizing tank and pump into two-stage UASB pond; Add dispenser through alkali and add NaOH solution; Regulate between the waste water ph 9～10, waste water provides upflow velocity in the pond through recycle pump in the pond in, and mud is suspended state and floats in the water in the maintenance pond; Waste water is from flowing into the UASB settling tank; Waste water COD cr concentration is reduced to 5000～8000mg/L in the UASB settling tank, and the mud of UASB settling tank bottom is partly refluxed to two-stage UASB pond through sludge pump, and part pumps into storage basin; Waste water in the UASB settling tank is from flowing into aerobic water distribution equalizing tank; Simultaneously, waste water and the waste water in the clean water basin in the low dense mixed pond are pumped into aerobic water distribution equalizing tank, and mix stirring through the blower fan air-supply; To keep in the aerobic water distribution equalizing tank waste water COD cr at 500～800mg/L; And add dispenser through alkali and add NaOH solution, to regulate waste water ph 8～9, ammonia nitrogen 40～50mg/L.
Above-mentioned mud backflow biochemical treatment concrete steps are: waste water from flowing into the active sludge aerobic pond, through blower fan air-supply oxygen supply, produces Water purification from aerobic water distribution equalizing tank under the aerobic microbiological effect; Waste water COD cr concentration is reduced to 150～300mg/L, and ammonia nitrogen is reduced to 20～30mg/L, and the mud waste water that contains after the processing flows into the active sludge aerobic settling tank; After the solid-liquid separation, mud is partly refluxed to the active sludge aerobic pond through sludge pump, and part pumps into storage basin; Waste water through blower fan aerating wastewater oxygenation in the pond, produces Water purification from flowing into biological contact Aerobic Pond under the microbial process in the pond on the microbial film; Waste water COD cr concentration is reduced to 90～110mg/L, and ammonia nitrogen is reduced to 10～15mg/L, and the mud waste water that contains after the processing flows into contacting sedimentation tank; After the solid-liquid separation, mud is partly refluxed to the active sludge aerobic settling tank through sludge pump, and part pumps into storage basin; Waste water flows into sand filter certainly from biological contacting sedimentation tank; Processed waste water CODcr reduces to 90～100mg/L, and ammonia nitrogen is reduced to 8～12mg/L, and mud enters storage basin.
Above-mentioned active sludge aerobic pond is equipped with sprinkling system, the foam that produces when eliminating aeration with biological the contact in the Aerobic Pond.
The recoil that above-mentioned sand filter also adopts recoil blower fan and recoil pump to carry out regular G&W is cleaned.
Waste water after above-mentioned sand filter is handled is also from flowing into clean water basin, the waste water of clean water basin or be used for the water distribution reuse of water distribution equalizing tank, or the water that cleans as recoil; The waste water of clean water basin is from flowing into stabilization pond, the biological toxicity test pool before stabilization pond effluxes as waste water.
Also have the mud discharging step: the mud in the storage basin pumps into the extraction mud pipe road by slush pump; The line mixer that on the extraction mud pipe road, is provided with adds and adds the PAM solution that dispenser configures through PAM; Send into pressure filter after mixing with mud again and handle, the dewatered sludge after the processing is delivered to sludge landfill.
The invention has the beneficial effects as follows:
1) this technology has merged the theory of modular design, mainly divides three modules: (1) high concentrated acid property extraction wastewater toxicity is removed module; (2) composite waste water distribution adjustment module; (3) multi-stage countercurrent load control biological method biochemical treatment module; Three module independent operatings have very high capacity of resisting impact load and waste water regulating power.
2) waste water that this technology can effectively be handled this type of biological fermentation waste water ultrahigh concentration, contains the difficult degradation macromole, impact load is high; Dormin (S-abscisic acid) is produced composite waste through handling; Water outlet can reach (GB8978-1996) primary standard, has solved the unmanageable difficult problem of present domestic biological fermentation ultrahigh concentration waste water.This technology treatment facility treatment effects at different levels are as shown in table 1:
Table 1 dormin (S-abscisic acid) is produced composite waste treatment process effect (water yield is a reference value in the table)
3) the present invention carries out classification processing according to the waste water composition, changes according to waste strength and carries out corresponding water distribution processing.Kind of waste water is many for handling, complicated component, composite waste that fluctuation of concentration is big have practical extending application value.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
Fig. 2, Fig. 3 are respectively the enlarged views of Fig. 1 left part and right part.
Fig. 4 is Fig. 1 left part enlarged view (with a literal in the clear demonstration arrow).
Embodiment
Below in conjunction with accompanying drawing and instance the present invention is further specified.
Fig. 1 form by: 101: the extraction wastewater container for storing liquid; 102: high concentrated acid property extraction wastewater toxicity total system is (in the square frame of Fig. 1 upper left side.Three towers among Fig. 1 are followed successively by from left to right: conditioning tower, neutralizing tower, knockout tower); 103: the water distribution equalizing tank; 104: two-stage UASB pond; The 105:UASB settling tank; 106: aerobic water distribution equalizing tank; 127: multi-stage countercurrent load control biological system (comprises 107 active sludge aerobic ponds; 108: the active sludge aerobic settling tank; 109: biological contact Aerobic Pond; 110: biological contacting sedimentation tank); 111: sand filter; 112: clean water basin; 113: stabilization pond constitutes main flow.Auxiliary unit comprises: 114: storage basin; 115: accident pool; 116: frame trough; 117: low dense mixed pond; 118: high dense mixed pond; 119: high PH pond.Auxiliary auxiliary facility has: 120 lime add dispenser; 121: caustic soda adds dispenser; 122: the hydrochloric acid dispenser; 123: alkali adds dispenser; 124: molysite adds dispenser; 125:PAM adds dispenser; 126: composite waste water distribution regulation system; Off-set facility such as relevant WT-MSR, lifting, backflow, comprising: 1: lift pump; 2: multifunctional pump; The 3:UASB lift pump; 4: recycle pump; 5: the accident pump; 6: sludge pump; 7: recoil pump; 8: blower fan; 9: the recoil blower fan; 10: coarse rack; 11: fine fack; 12: pressure filter; 13: slush pump; 14,15: triphase separator; 16,18: sprinkling system; 17,19: aeration head; 20: the back flushing air system; 21: the recoil water system; 22,23,24,25,26:pH probe; 27,28,29,30,31,32: under meter; 33: line mixer.
Various pipelines are following among Fig. 1: WW: the water treatment management; WN: mud pipeline; A: compressed-air line; GS: contain the solvent waste line; LW: condensate piping; SW: water supply line; SA: vapour line; BCa: add the CaOH pipeline; BNa: add the NaOH pipeline; HCL: add the HCL pipeline; FE: add the molysite pipeline; PAM: add the PAM pipeline; SG: reuse water pipeline; FC: recoil water pipeline.
The present invention is primarily aimed at the composite waste of 7 kinds of waste water compositions that produced in dormin (S abscisic acid) production process; And can suitably handle a certain amount of sanitary wastewater; The characteristics of this waste water are following: 1, kind of waste water is many, complicated component, and the Pollutant levels fluctuation is bigger; All kinds of waste water COD cr fluctuation of concentrations are 100mg/L～150,000 mg/L, NH 3-N fluctuation of concentration is 1mg/L～7000mg/L, and the impact load of waste water is high; 2, wastewater pH=0.4～11, the PH fluctuation is bigger; 3, the extraction wastewater in the composite waste contains a large amount of larger molecular organicses (being greater than or less than fermentation target compound molecular weight); Form by organic solvents such as sherwood oil, ETHYLE ACETATE, butylacetates; The tradition biochemical process can't effectively be handled, and contains a large amount of salts substances simultaneously, has certain bio-toxicity; If directly get into the biochemical treatment operation; Can have a strong impact on biochemical effect, cause biochemical system collapse, extraction wastewater must pass through toxicity remove and improve the pre-treatment of biochemical after could get into degree of depth materialization, biochemical treatment with other waste water; 4, because water quality often fluctuates, cause each workshop section's processing power of conventional process flow unstable, the effluent quality fluctuation is big; 5, conventional process flow is to the variation water quality bad adaptability of this type composite waste, and minimum accident also can be destroyed biochemical system after taking place, and biochemical system is difficult for recovering.
S-abscisic acid factory effluent involved in the present invention is mainly by fermentor tank rinse water, sheet frame washing water, film rinse water, MF debris, UF debris, r-o-, extraction wastewater and 8 kinds of waste water compositions of sanitary wastewater, and except that sanitary wastewater, factory effluent is all by the disposable discharging of production batch; The annual work of factory 300 days; Produce 100 batches altogether, by producing 10t per year, 95% pure concentration xln calculates; Be scaled a day processing load, it is following that all kinds of waste water constitute situation:
1) extraction wastewater: quantity discharged is 20～40m 3/ batch, CODcr concentration is 100,000～150,000 mg/L, NH 3-N concentration is 2000～7000mg/L, SO 4 2-Concentration is 480～38000mg/L, pH=0.4～2.0;
2) fermentor tank rinse water: quantity discharged is 2～6m 3/ batch, CODcr concentration 100～300mg/l, pH=7～8, ammonia nitrogen 0.5～2mg/l;
3) sheet frame washing water: quantity discharged is 1～6m 3/ batch, CODcr concentration 1000～3000mg/l, pH=7～8, ammonia nitrogen 1～4mg/l;
4) film rinse water: quantity discharged is 20～82m 3/ batch, CODcr concentration 100～1000mg/l adopts NaOH solution and HCl solution to clean respectively during cleaning, and the mixed solution after the cleaning is alkalescence, and pH ≈ about 11, ammonia nitrogen 0.2～60mg/l;
5) micro-filtration (MF) debris: quantity discharged is 10～47m 3/ batch, CODcr concentration 0.2～0.8 ten thousand mg/l, pH=5～6, ammonia nitrogen 8～35mg/l;
6) ultrafiltration (UF) debris: quantity discharged is 5～20m 3/ batch, CODcr concentration 0.5～20,000 mg/l, pH=4～5, ammonia nitrogen 7.5～80mg/l;
7) nanofiltration (NF) waste liquid: quantity discharged is 20～81m 3/ batch, CODcr concentration 0.05～0.25 ten thousand mg/l, pH=5～6, ammonia nitrogen 1～5mg/l;
Above factory effluent day quantity discharged conversion is about 78m 3/ d.
8) sewage: headcount is about 100 people in the factory, and the sewage quantity discharged is 160L for each person every day, and then a day quantity discharged is 16m 3/ day, CODcr concentration is at 200～300mg/l, ammonia nitrogen 25mg/l.Composite waste water quantity and quality and treatment scale are as shown in table 2:
Table 2 waste water water quantity and quality and treatment scale table
The present invention has adopted " high concentrated acid property extraction wastewater toxicity is removed technology and support equipment ", " multi-stage countercurrent load control biological method " (patent No.: the 200810045465.3) combination of two kinds of patented technologies; Newly-increased UASB anaerobic treatment workshop section, concentration step water distribution workshop section; And press waste strength and change (pollutant load gradient and variation); Adopt the high density, the difficult degradation macromole that are produced in three grades of clear water of three grades of mud backflows (handling back water) Treatment for Reuse dormin (S-abscisic acid) production process, the composite waste that impact load is high.
Description of Related Art is following:
High concentrated acid property extraction wastewater toxicity is removed process method, the steps include:
A1) high concentrated acid property extraction wastewater is added excess amount of Ca (OH) in the conditioning tower 2, press H +Concentration is calculated, and is excessive 3%～4%, regulates waste water ph to pH value 9～11, sulfate ion in the waste water and Ca 2+The reaction back generates CaSO 4Deposition is through accomplishing SO after the precipitate and separate 4 2-Remove;
A2) remove SO 4 2-After waste water through being pumped into neutralizing tower, and add the excessive waste water of handling without the conditioning tower at neutralizing tower, press OH -Concentration is calculated, and waste water is excessive 1%～2%, the SO in the waste water 4 2-With dissolved Ca in the waste water 2+The reaction back generates CaSO for the second time 4Deposition is accomplished Ca through precipitate and separate 2+Remove, reduce subsequent handling equipment scaling incidence;
A3) waste water of handling through alkali and excessive acid in the neutralizing tower adds excessive NaOH simultaneously by being pumped into knockout tower, presses H +Concentration is calculated, and NaOH is excessive 10%～20%, regulates between waste water ph to 9～10 for the second time; Use steam indirect heating waste water then, make wastewater temperature near its boiling point, keep this temperature; In waste water, blast pressurized air through tower inner bottom part air feeder; Make the extraction solvent in the waste water bring gas phase into by air by a certain percentage, the part extraction solvent is separated from waste water, the gas that contains extraction solvent imports boiler house gas blower pipeline; Send in the boiler and use, when blasting air, use waste water to spray through the spray equipment in the knockout tower as combustion-supporting gas;
In the above-mentioned conditioning tower whipping appts and mud discharging device are arranged, neutralising arrangement, whipping appts and mud reflux are arranged in the neutralizing tower, tripping device, chemicals dosing plant, settler, aerating apparatus, mud reflux etc. are arranged in the knockout tower.
The UASB anaerobic treatment: the anaerobic biological treatment process is a successive microbiological process, from biological chemistry and microbiology angular divisions, can simply be divided into: produce acid phase and produce methane phase.Producing the acid phase biota mainly is fermenting bacterial, and this bacterioid can be hydrolyzed to the larger molecular organics of complicacy small organic molecule and further generate organic acid and alcohol through the acidogenic fermentation effect, produces CO simultaneously 2And H 2The main purpose of producing acid phase is to be micromolecular organism with macromolecular organic matter degradation, thereby helps the subsequent biological treatment process.Therefore, in this stage, the CODcr clearance generally is merely about 20%, and promptly the clearance of CODcr is not the purpose in this stage.Such bacterial species is many, and metabolic capacity is strong, and reproduction speed is fast, and the doubling time only lacks most needs tens minutes.In producing methane phase, methanogen is reduced to CH with one-carbon compound (CO, methyl alcohol, formic acid, methylamine etc.) and acetate 4Exist hydrogen transference between kind between non-methanogen and the methanogen, i.e. the H that the former metabolism produces 2Can be by The latter, with CO 2Be reduced to CH 4Reaction formula is following:
CH 3COOH+2H 2O→2CO 2+4H 2
4H 2+CO 2→CH 4+2H 2O
Total formula: CH 3COOH → CH 4+ 2H 2O
Compare with fermenting bacterial, the methanogen kind is few, utilizes substrate limited, and reproduction speed is slow, and the time in epoch, length can reach 4～6 days, and very responsive to environmental factors such as temperature, pH value, toxic substance influence.
Filter and the dual characteristics of anaerobic activated sludge method by anaerobism owing to having for UASB (upflow anaerobic sludge blanket process Up-flow Anaerobic Sludge Bed) technology, as can pollutants in sewage being changed into the regeneration clean energy---and a technology of biogas.UASB is made up of sludge reaction district, gas-liquid-solid three-phase separator (comprising the settling region) and air chamber three parts.In bottom anaerobic reaction district, retain a large amount of anaerobic sludges, the mud with good sedimentation function and cohesion performance forms sludge blanket in the bottom.The sewage of handling from anaerobic mud bed bottom flow into sludge blanket mud mix and contact, the organism in the microbiological degradation sewage in the mud is converted into biogas to it.Biogas is constantly emitted with the micro-bubble form, and micro-bubble constantly merges in uphill process; Form bigger bubble gradually, on Sludge Bed top because the stirring of biogas forms biogas, the muddy water mixolimnion that sludge concentration is thinner, mud and the water entering triphase separator that rises together; When biogas is run into the reflector of separator bottom, be folded to reflector around, pass water layer then and get into air chamber; The biogas that concentrates on air chamber is derived with conduit, and the solid-liquid mixed solution is through the settling region of reflection entering triphase separator, and the mud in the sewage flocculates; Particle increases gradually, and sedimentation under action of gravity.The mud that is precipitated on the skew wall is slided back in the anaerobic reaction district along skew wall, makes a large amount of mud of accumulation in the reaction zone, overflows on overflow weir top from the settling region with the treat effluent after mud separates, and discharges Sludge Bed then.
Waste water gets into two-stage UASB pond and carries out anaerobic treatment; The biogas that UASB pond (being upflow anaerobic sludge blanket process) produces causes the boiler burning or uses the energy as life; Processed waste water gets into active sludge aerobic settling tank 108 and carries out solid-liquid separation, and the sludge part under the deposition is back to two-stage UASB pond, and part is delivered to storage basin and concentrated; The storage basin supernatant returns the water distribution equalizing tank, and waste water flows into aerobic water distribution equalizing tank; Sewage with after final processing the in the waste water in the mixed pond and clean water basin and the stabilization pond carries out water distribution to the waste water in the aerobic water distribution equalizing tank, and CODcr is between 500～800mg/l in control; Waste water flows into multi-stage countercurrent load control biological system by distribution reservoir and handles.
The water distribution of concentration step: this method that the present invention adopts is carried out categorised collection according to the contaminated wastewater substrate concentration, disposes respectively.According to the water distribution of being correlated with of the situation of each wastewater treatment working section.Other waste water that high quintessence is got in waste water and the mixed pond dilutes in proportion, and control water distribution equalizing tank COD concentration is at 10000～20000mg/L.This moment, waste water got into two-stage UASB processing; The vertical sedimentation tank of UASB configure dedicated (being called for short the UASB settling tank); Water outlet flows into aerobic water distribution equalizing tank after getting into UASB settling tank mud-water separation again, with the sewage that disposes in waste water in the mixed pond and the stabilization pond waste water in the distribution reservoir is diluted, and thinning ratio is 8～12 times; COD is between 500～800mg/l in control, and waste water entering this moment multi-stage countercurrent load control biological system further disposes.
Concentration step water distribution mode mixes high-concentration waste water and low concentration wastewater, has reduced the concentration of composite waste, has alleviated the impact load of wastewater biochemical treatment facility, has utilized the processing power of biochemical treatment facilities at different levels to greatest extent.
Three grades of mud reflux: the mud that this technology produced refluxes respectively in each workshop section, does not change this corresponding workshop section treatment effect of assurance of ability maximum efficiency to guarantee the returned sluge quality.Mud after UASB settling tank mud-water separation passes back into two-stage UASB; The isolating mud of activated sludge settling tank passes back into the active sludge aerobic pond; The isolating mud of biological contacting sedimentation tank passes back into biological contact Aerobic Pond.
Three grades of clear water (handling back water) reuse: a part of processed waste water is circulated to the water distribution equalizing tank, in order to control this pond average water outlet CODcr concentration between 10000～20000mg/l, guarantees the UASB treatment effect; Part clear water is back to aerobic water distribution equalizing tank, controls this pond average water outlet CODcr concentration between 500～800mg/l, guarantees multi-stage countercurrent load control biological system handles effect; Part clear water is back to sand filter, as sand filter recoil water.
High concentrated acid property extraction wastewater toxicity is removed technology and support equipment (patent of invention is applied for): a kind of to producing process method and the support equipment that high concentrated acid property extraction wastewater toxicity is removed in the biological fermentation production of articles process; Excessive acid method of secondary base excess (being called for short the BAB method) is combined with vaporizing extract process; In BAB method operation; The potential of hydrogen of waste water has obtained adjusting, and pH is by 0.4～2 left and right adjusting to 9～10, SO 4 2-Be reduced to about 2mg/L by 4800mg/L, in the vaporizing extract process operation, the CODcr of waste water is reduced to 80,000～100,000 mg/L by 100,000～150,000 mg/L, and ammonia nitrogen is reduced to 1500～5000mg/L by 2000～7000mg/L.This technology is adjusted to weakly alkaline with waste water by strongly-acid, has removed the SO of waste water middle and high concentration 4 2-The sherwood oil that is difficult to biochemical degradation in a large number, part ETHYLE ACETATE, butylacetate class material make the toxicity of waste water obtain removal, and biodegradability is improved, for condition has been created in follow-up degree of depth materialization, biochemical treatment.
Multi-stage countercurrent load control biological method (patent No.: 200810045465.3): a kind of multi-stage refluxing load control biological process and matched facilities, form by postprocessing working procedures such as pretreatment procedures such as coagulating sedimentation, the multistage reflux duty control treatment process operation of mud and air supportings.In the multistage reflux duty control of mud treatment process; Handle in the integral biological pond that waste water is formed through three sections nine grades of biological treatment tanks: promptly first and second level contacts anaerobic treatment; Third stage intermediate sedimentation, fourth, fifth grade of catalytic oxidation handled the 6th grade of gap aeration; Seven, eight grades of catalytic oxidations and add the basic nutrition thing, the 9th grade of aeration and sedimentation.According to load condition, the mud in the pond is back to the previous stages biological tank, with biological processes such as microbic activity, breeding and variation in the control pond.Modular design concept is introduced in the integrated pond of this invention, has to take up an area of little, easy construction, regulation and control are flexible, construction cost is low advantage.The present invention has adopted the part principle of this patented technology; Be mainly the multistage backflow principle of mud; And according to the difference of wastewater property part workshop section in the technology is adjusted, the contact anaerobic treatment of first and second grade is adjusted into the UASB anaerobic treatment improving the anaerobism effect, fourth, fifth grade of catalytic oxidation handled being adjusted into active sludge aerobic and handling; The 6th grade of gap aeration is adjusted into intermediate sedimentation, with the characteristic of better adaptation dormin (S-abscisic acid) factory effluent.
The object of the invention is by following method: composite waste is formed has the fermentor tank rinse water, 8 kinds of sheet frame washing water, film rinse water, MF debris, UF debris, nanofiltration (NF) waste liquid, extraction wastewater and sanitary wastewaters.Invention adopt " high concentrated acid property extraction wastewater toxicity is removed technology " that extraction wastewater is carried out detoxification and improve the pre-treatment of biodegradability after mix with all the other 7 kinds of waste water; Carry out the ladder water distribution by concentration; Water distribution first is with waste water COD cr concentration adjustment to 10000～20000mg/l; Waste water gets into the water distribution once more after anaerobic treatment of anaerobic treatment workshop section, and with waste water COD cr concentration adjustment to 500～800mg/l, waste water gets into the biochemical treatment workshop section that adopts " multi-stage countercurrent load control biological method " principle to carry out sending into the sand filter processing after the advanced treatment; Waste water part qualified discharge after the processing, part can be used as the dilution water reuse.
In the water distribution regulation system of the composite waste of Fig. 1:
The film rinse water flows into high pH pond, and one batch film rinse water utilizes hydrochloric acid to add the dispenser device for formulating after all mixing, and adds HCl solution, regulates pH after about 9, squeezes into the water distribution equalizing tank.
Sheet frame washing water, MF debris, UF debris and nanofiltration (NF) waste liquid are squeezed into the water distribution equalizing tank after getting into high dense mixed pond mixing.
Sanitary wastewater mixes with the fermentor tank rinse water after artificial coarse rack of one-level and the artificial fine fack processing of two-stage, gets into low dense mixed pond.
According to processing requirement, squeeze into the water distribution equalizing tank respectively and mix with extraction wastewater with aerobic water distribution equalizing tank and mix with two-stage UASB pond water outlet, play diluting effect.
Every batch of extraction wastewater (20m 3/ batch) the disposable extraction liquid storage pond that enters stores, and pumps into high concentrated acid property extraction wastewater toxicity total system, every day, flooding quantity was 6～18m 3, after extraction wastewater got into total system, waste water got into the water distribution equalizing tank after total system is removed toxicity (regulate the pH value, remove sulfate ion).
With mixing the clear water that other waste water, lower concentration in the pond mix after handling in pond and the stabilization pond extraction wastewater of removing after the toxicity is carried out water distribution; Water distribution equalizing tank CODcr concentration is controlled at 10000～20000mg/l; The waste water for preparing is pumped into the UASB pond carry out anaerobic treatment, the biogas that the UASB pond produces causes the boiler burning or uses the energy as life, and processed waste water gets into medium sediment pool and carries out solid-liquid separation; Sludge part under the deposition is back to the UASB pond; Part is delivered to storage basin and is concentrated, and the storage basin supernatant returns the water distribution equalizing tank, and waste water flows into aerobic water distribution equalizing tank.
Sewage with after final processing the in waste water in the mixed pond and the stabilization pond carries out water distribution to the waste water in the aerobic water distribution equalizing tank, and CODcr is between 500～800mg/l in control.Waste water flows into multi-stage countercurrent load control biological system by distribution reservoir and handles.
Waste water inflow sand filter carries out advanced treatment after multi-stage countercurrent load control biological system handles, and the waste water after the processing gets into clean water basin, and after the qualified discharge part, all the other get into stabilization pond, as the dilution water reuse in clean water basin.
Embodiment: process step is following:
1) in view of the extraction wastewater characteristic, its single collection is stored in extraction wastewater container for storing liquid 101, about waste water PH=0.4～2, SO 4 2-Content is 5000mg/L, and CODcr concentration is 100,000～150,000 mg/L, NH 3-N concentration is 2000～7000mg/L, SO 4 2-Concentration is the extraction agents such as sherwood oil, ETHYLE ACETATE and butylacetate that 480～38000mg/L contains bio-refractory simultaneously; Start high concentrated acid property extraction wastewater toxicity total system (this treatment system adopts " high concentrated acid property extraction wastewater toxicity is removed technology and support equipment " a complete set of Processes and apparatus of applying for patent of invention); Extraction wastewater is squeezed into this total system from extraction wastewater container for storing liquid 101; Being aided with lime adds dispenser 120, caustic soda and adds dispenser 121 and regulate waste water pH value to 9～10; Remove toxicity, mud pumps into the SO of storage basin more than 114,99.6%～99.9% 4 2-Obtained removal with the larger molecular organics of 20% above difficult degradation, biochemical is improved, and can get into follow-up biochemical treatment.This moment, the CODcr of extraction wastewater was that ammonia nitrogen is reduced to 1500～5000mg/L about 8～100,000 mg/L, and the pH value is about 9～10, SO 4 2-Content is about 2mg/L; In total system, utilize the stripping principle, with pressurized air materials such as the part ETHYLE ACETATE in the extraction wastewater, sherwood oil being blown out (about 20%) again after the steam heating extraction wastewater, air causes in the boiler and burns.
2) extraction wastewater after total system is handled waits pending next step biochemical treatment from flowing into water distribution equalizing tank 103.
3) sheet frame washing water, micro-filtration debris, ultrafiltration debris, nanofiltration debris are combined in high dense mixed pond 118 through the waste water pipe network.
4) fermentor tank rinse water, the sanitary wastewater after will being compiled by the waste water pipe network sent into coarse rack 10 in the frame trough 116, fine fack 11 combines in low dense mixed pond 117 after removing slags.
5) the film rinse water is combined in high pH pond 119 through the waste water pipe network.
6) add dispenser 122 fine settings through hydrochloric acid and be stored in the high pH waste water in the high pH pond, observe pH probe 22, regulate waste water ph to 9～10.(low dense high pH waste water does not directly mix with hc effluent, alleviates the load of front end UASB and handles the water yield)
7) will combine in waste water in low dense mixed pond 117, high dense mixed pond 118, the high pH pond 119 through multifunctional pump 02 and handle afterwards with clean water basin or stabilization pond 113 that clear water carry out pumping into water distribution equalizing tank 103 behind the thorough mixing; Mix stirring through blower fan 08 air-supply simultaneously; Add dispenser 123 through alkali and add NaOH solution, observe pH probe 23, regulate about wastewater pH to 9～10; Water distribution equalizing tank CODcr concentration is controlled at 10000～20000mg/L, and ammonia nitrogen is about 300mg/L.
The waste water that 8) will be stored in after allocating well in the water distribution equalizing tank through UASB lift pump 03 pumps into two-stage UASB pond 104.UASB pond 104 has been concentrated anaerobic mud bed and the advantage anaerobism bed of packings, can effectively degrade to organic pollutant, and pollutant in water content is reduced greatly, helps next step aerobic treatment.Observe pH probe 24,25, add dispenser 123 through alkali and add little amount of N aOH solution, keep between waste water PH to 9～10; Waste water provides upflow velocity in the pond through recycle pump 04 in the pond; Keep in the pond mud to be suspended state and float in the water, waste water is from flowing into UASB settling tank 105, and this moment, waste water COD cr concentration was about 5000～8000mg/L; The mud of UASB settling tank 105 bottoms is partly refluxed to UASB pond 104 through sludge pump 06, and part pumps into storage basin 114.
9) waste water flows into aerobic water distribution equalizing tank 106 certainly from UASB settling tank 105; The waste water that will be stored in low dense mixed pond 117 through control multifunctional pump 02 valve and accident pump 05 valve is squeezed into aerobic water distribution equalizing tank 106 in proportion with the clear water that the processing back flows into stabilization pond; Mix stirring through blower fan 08 air-supply simultaneously; Keep in the 106 aerobic water distribution equalizing tanks waste water COD cr between 500～800mg/L, observe pH probe 26, add dispenser 123 through alkali and add little amount of N aOH solution; Keep between waste water PH to 8～9, this moment, ammonia nitrogen in waste water was about 40～50mg/L.
10) waste water flows into multi-stage countercurrent load control biological system (this treatment system adopts the part technology and the principle of patent of invention " ZL 200810045465.3 multi-stage countercurrent load control biological methods ") certainly from aerobic water distribution equalizing tank 106.Concrete technology is following: waste water flows into active sludge aerobic pond 107, and the aerobic microbiological after domestication is arranged in the pond, through the abundant oxygen supply of gas blower 08 air-supply; Under the effect of aerobic microbiological, sewage is purified, and waste water COD cr concentration is reduced to about 150～300mg/L; Ammonia nitrogen is reduced to about 20～30mg/L; Carry sprinkling system in the pond, the mud waste water that contains behind abundant aeration flows into active sludge aerobic settling tank 108, after the solid-liquid separation; Mud is partly refluxed to active sludge aerobic pond 107 through sludge pump 06, and part is squeezed into storage basin 114; Waste water from flowing into biological contact Aerobic Pond 109, through blower fan 08 aeration aerating, is provided with biofilm packing from active sludge aerobic settling tank 108 in the pond; Sewage contacts with microbial film on the filler, and under the microbial process on the microbial film, sewage is purified; Waste water COD cr concentration is reduced to about 90～110mg/L, and ammonia nitrogen is reduced to about 10～15mg/L, carries sprinkling system in the pond; Waste water flows into contacting sedimentation tank 110; After the solid-liquid separation, mud is partly refluxed to activated sludge settling tank 108 through sludge pump 06, and part is squeezed into storage basin 114);
11) from flowing into sand filter 111, waste water COD cr reduces to about 90～100mg/L waste water from contacting sedimentation tank 110, and ammonia nitrogen is about 8～12mg/L, and mud enters storage basin 114.With the back flushing air system 20 that has disposed recoil blower fan 09 and the recoil water system 21 that has disposed recoil pump 07 regularly to recoil cleaning of sand filter 111.
12) processed waste water flows into clean water basin 112 certainly, but qualified discharge; A water part up to standard here is used for leading portion water distribution reuse, and backwashing water is used; Be provided with molysite and add inlet, can be as required add dispenser 124 and add molysite and waste water recycling to leading portion is handled through molysite.
13) this technology is provided with stabilization pond 113, and from flowing into stabilization pond 113, waste water carries out natural purification to waste water in stabilization pond, further guarantee discharged wastewater met the national standard through clean water basin 112.Put the part fish in the pond in a suitable place to breed, the biological toxicity test pool before effluxing as waste water.
14) mud that is stored in storage basin 114 pumps into the extraction mud pipe road by slush pump 13; The line mixer 33 that on the extraction mud pipe road, is provided with adds and adds the PAM solution that dispenser 125 configures through PAM; Send into pressure filter 12 after mixing with mud again and handle, handle the back dewatered sludge to sludge landfill.
PAM full name is SEPIGEL 305, and the molecular energy of this product and the suspended particles bridge formation absorption that is scattered in the solution have extremely strong throwing out.
Main application: this product has a macromolecular compound water-soluble with and main chain on active acyl group; Thereby have widely in industries such as oil production, water treatment, textile printing and dyeing, papermaking, ore dressing, coal washing, medicine, sugaring, breed, building materials, agriculturals and to use, the title of " all trades auxiliary agent ", " omnipotent product " is arranged.
The application of PAM in water treatment industry mainly comprises aspect 3 of former water treatment, WWT and the Treatment of Industrial Water.In former water treatment, PAM and gac etc. is used, and can be used for the cohesion and the clarification of suspended particle in the life water; In WWT.PAM can be used for sludge dewatering; In Treatment of Industrial Water, mainly as prescription medicament.In former water treatment, replace inorganic flocculating agent with organic floculant PAM, even do not transform settling bowl, the water purification ability also can improve more than 20%.So present many big and medium-sized cities when water supply gets or water quality are relatively poor, all adopt PAM as replenishing.In WWT, adopt PAM can increase water reuse round-robin rate of utilization.

Claims (7)

1. dormin production wastewater treatment process method; This factory effluent is formed has the fermentor tank rinse water, 8 kinds of sheet frame washing water, film rinse water, MF debris, UF debris, nanofiltration waste liquid, extraction wastewater and sanitary wastewaters, it is characterized in that: carry out in order according to the following steps:
A) extraction wastewater is handled:
Adopt high concentrated acid property extraction wastewater toxicity total system that extraction wastewater is carried out pre-treatment, to regulate the pH value and to remove sulfate ion;
B) concentration step water distribution:
Pretreated extraction wastewater is mixed with said all the other 7 kinds of factory effluents, carry out the ladder water distribution by concentration during mixing, water distribution first is with this composite waste CODcr concentration adjustment to 10,000～20,000mg/L;
C) two-stage UASB anaerobic treatment:
Waste water after the water distribution is carried out anaerobic treatment in two-stage UASB pond; Carry out mud-water separation through deposition again; The water distribution once more of waste water after the mud-water separation, with waste water COD cr concentration adjustment to 500～800mg/L, the mud after the mud-water separation passes back into respectively in the anaerobic reaction district in two-stage UASB pond;
D) mud backflow biochemical treatment:
In active sludge aerobic pond (107), the waste water after the UASB anaerobic treatment being carried out active sludge aerobic handles; Waste water after active sludge aerobic settling tank (108) precipitate and separate is sent into biological contact Aerobic Pond (109) and is carried out biology contact aerobic treatment; Waste water after biological contacting sedimentation tank (110) precipitate and separate is sent into the advanced treatment operation again; And the isolating mud of active sludge aerobic settling tank (108) passes back into active sludge aerobic pond (107), and the isolating mud of biological contacting sedimentation tank (110) passes back into biological contact Aerobic Pond (109);
E) advanced treatment:
The waste water that is come by the biochemical treatment operation gets into clean water basin after sand filtration is handled, the waste water COD cr that gets into clean water basin reduces to 90～100mg/L, and ammonia nitrogen is 8～12mg/L;
Above-mentioned a is in the step, and the extraction wastewater treatment step is following:
A1) high concentrated acid property extraction wastewater is added excess amount of Ca (OH) in the conditioning tower 2, press H +Concentration is calculated, and is excessive 3%～4%, regulates waste water ph to pH value 9～11, sulfate ion in the waste water and Ca 2+The reaction back generates CaSO 4Deposition is through accomplishing SO after the precipitate and separate 4 2-Remove;
A2) remove SO 4 2-After waste water through being pumped into neutralizing tower, and add the excessive waste water of handling without the conditioning tower at neutralizing tower, press OH -Concentration is calculated, and waste water is excessive 1%～2%, the SO in the waste water 4 2-With dissolved Ca in the waste water 2+The reaction back generates CaSO for the second time 4Deposition is accomplished Ca through precipitate and separate 2+Remove, reduce subsequent handling equipment scaling incidence;
A3) waste water of handling through alkali and excessive acid in the neutralizing tower adds excessive NaOH simultaneously by being pumped into knockout tower, presses H +Concentration is calculated, and NaOH is excessive 10%～20%, regulates between waste water ph to 9～10 for the second time; Use steam indirect heating waste water then, make wastewater temperature near its boiling point, keep this temperature; In waste water, blast pressurized air through tower inner bottom part air feeder; Make the extraction solvent in the waste water bring gas phase into by air by a certain percentage, the part extraction solvent is separated from waste water, the gas that contains extraction solvent imports boiler house gas blower pipeline; Send in the boiler and use, when blasting air, use waste water to spray through the spray equipment in the knockout tower as combustion-supporting gas;
Above-mentioned high concentrated acid property extraction wastewater is by being produced in the biological fermented product production process, this wastewater pH=0.4～2.0, and CODcr concentration is 100,000～150,000 mg/L, ammonia nitrogen concentration is 2000～7000mg/L, SO 4 2-Concentration is 480～38000mg/L, contains part by weight simultaneously and be 2%～4% extraction solvent; This extraction solvent is mainly sherwood oil, ETHYLE ACETATE, butylacetate; After knockout tower was handled, the CODcr of waste water was reduced to 80,000～100,000 mg/L, and ammonia nitrogen is reduced to 1500～5000mg/L.
2. dormin production wastewater treatment process method according to claim 1; It is characterized in that: said b step concentration step water distribution concrete steps are: the film rinse water flows into high pH pond (119); One batch film rinse water is utilized hydrochloric acid dispensing slot (122) after all mixing, and adds HCl solution; Regulate pH 9～10, pump into water distribution equalizing tank (103); Sheet frame washing water, MF debris, UF debris and nanofiltration waste liquid pump into water distribution equalizing tank (103) after getting into high dense mixed pond (118) mixing; Sanitary wastewater mixes with the fermentor tank rinse water after after artificial coarse rack (10) of one-level and the artificial fine fack of two-stage (11) processing, get into low dense mixed pond (117);
Said a step extraction wastewater is handled concrete steps and is: every batch of extraction wastewater 20m 3/～40m 3The disposable extraction wastewater container for storing liquid (101) that enters is stored, and pumps into high concentrated acid property extraction wastewater toxicity total system and handles, and waste water after treatment mixes with above-mentioned other waste water that has got in the pond from flowing into the water distribution equalizing tank; The waste water that perhaps will hang down dense mixed pond (117) again pumps into the water distribution equalizing tank and carries out water distribution; Water distribution equalizing tank CODcr concentration is controlled at 10,000～20 the most at last, in the 000mg/L technic index;
Said c step two-stage UASB anaerobic treatment concrete steps are: adopt lift pump will be stored in the waste water that allotment is good in the water distribution equalizing tank (103) and pump into two-stage UASB pond (104); Add dispenser (123) through alkali and add NaOH solution; Regulate between the waste water ph 9～10; Waste water provides upflow velocity in the pond through recycle pump (04) in the pond; Keep in the pond mud to be suspended state and float in the water, waste water is from flowing into UASB settling tank (105), and the interior waste water COD cr of UASB settling tank (105) concentration is reduced to 5000～8000mg/L; The mud of UASB settling tank (105) bottom is partly refluxed to two-stage UASB pond (104) through sludge pump (06), and part pumps into storage basin (114); Waste water in the UASB settling tank (105) is from flowing into aerobic water distribution equalizing tank (106); Simultaneously, the waste water and the interior waste water of clean water basin (112) that will hang down in the dense mixed pond (117) pump into aerobic water distribution equalizing tank (106), and mix stirring through blower fan (08) air-supply; To keep in the aerobic water distribution equalizing tank waste water COD cr at 500～800mg/L; And add dispenser (123) through alkali and add NaOH solution, to regulate waste water ph 8～9, ammonia nitrogen 40～50mg/L.
3. dormin production wastewater treatment process method according to claim 2 is characterized in that: said mud backflow biochemical treatment concrete steps are: waste water flows into active sludge aerobic pond (107) certainly from aerobic water distribution equalizing tank (106), through blower fan (08) air-supply oxygen supply; Under the aerobic microbiological effect, produce Water purification, waste water COD cr concentration is reduced to 150～300mg/L, and ammonia nitrogen is reduced to 20～30mg/L; The mud waste water that contains after the processing flows into active sludge aerobic settling tank (108), and after the solid-liquid separation, mud is partly refluxed to active sludge aerobic pond (107) through sludge pump (06); Part pumps into storage basin (114), and waste water is from flowing into biological contact Aerobic Pond (109), through blower fan (08) aerating wastewater oxygenation in the pond; Produce Water purification under the microbial process in the pond on the microbial film, waste water COD cr concentration is reduced to 90～110mg/L, and ammonia nitrogen is reduced to 10～15mg/L; The mud waste water that contains after the processing flows into biological contacting sedimentation tank (110); After the solid-liquid separation, mud is partly refluxed to active sludge aerobic settling tank (108) through sludge pump (06), and part pumps into storage basin (114); Waste water flows into sand filter (111) certainly from biological contacting sedimentation tank (110); Processed waste water CODcr reduces to 90～100mg/L, and ammonia nitrogen is reduced to 8～12mg/L, and mud enters storage basin (114).
4. dormin production wastewater treatment process method according to claim 3 is characterized in that: said active sludge aerobic pond (107) is equipped with sprinkling system with biological the contact in the Aerobic Pond (109).
5. dormin production wastewater treatment process method according to claim 4 is characterized in that: the recoil that said sand filter (111) also adopts recoil blower fan (09) and recoil pump (07) to carry out regular G&W is cleaned.
6. dormin production wastewater treatment process method according to claim 5; It is characterized in that: the waste water after said sand filter (111) is handled is also from flowing into clean water basin (112); The waste water of clean water basin or be used for the water distribution reuse of water distribution equalizing tank (103), or the water that cleans as recoil; The waste water of clean water basin (112) is from flowing into stabilization pond (113), and stabilization pond is as the biological toxicity test pool before effluxing.
7. dormin production wastewater treatment process method according to claim 6; It is characterized in that: also have the mud discharging step: the mud in the storage basin (114) pumps into the extraction mud pipe road by slush pump (13); The line mixer that on the extraction mud pipe road, is provided with (33) adds and adds the PAM solution that dispenser (125) configures through PAM; Send into pressure filter (12) after mixing with mud again and handle, the dewatered sludge after the processing is delivered to sludge landfill.
CN201110095687A 2011-04-15 2011-04-15 Treatment process method for wastewater from abscisic acid production Active CN102198997B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201110095687A CN102198997B (en) 2011-04-15 2011-04-15 Treatment process method for wastewater from abscisic acid production

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201110095687A CN102198997B (en) 2011-04-15 2011-04-15 Treatment process method for wastewater from abscisic acid production

Publications (2)

Publication Number Publication Date
CN102198997A CN102198997A (en) 2011-09-28
CN102198997B true CN102198997B (en) 2012-10-10

Family

ID=44660025

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201110095687A Active CN102198997B (en) 2011-04-15 2011-04-15 Treatment process method for wastewater from abscisic acid production

Country Status (1)

Country Link
CN (1) CN102198997B (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102923917B (en) * 2012-11-20 2014-04-23 利尔化学股份有限公司 Method and system for treating wastewater containing pyridine and pyridine derivatives
CN102923920A (en) * 2012-11-28 2013-02-13 四川省环保科技工程有限责任公司 Traditional Chinese medicine wastewater treatment process
CN103663616A (en) * 2013-11-29 2014-03-26 福建省沃特宝环保科技有限公司 Printing and dyeing wastewater recycling device
CN106915817A (en) * 2017-04-24 2017-07-04 奥为（天津）环保科技有限公司 A kind of vehicular efficient water repair system

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5792355A (en) * 1995-09-15 1998-08-11 Desjardins; Gaetan Process for treating waste water
WO1998055402A1 (en) * 1997-06-04 1998-12-10 Ulrich Braun Method and device for sewage treatment
CN1485287A (en) * 2002-09-28 2004-03-31 财团法人工业技术研究院 System and method for removing organic oxide from waste water
CN1589239A (en) * 2001-10-17 2005-03-02 先进环境技术有限公司 Organic waste treatment
CN1621364A (en) * 2003-11-30 2005-06-01 魏军 Organic waste water treatment process

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5792355A (en) * 1995-09-15 1998-08-11 Desjardins; Gaetan Process for treating waste water
WO1998055402A1 (en) * 1997-06-04 1998-12-10 Ulrich Braun Method and device for sewage treatment
CN1589239A (en) * 2001-10-17 2005-03-02 先进环境技术有限公司 Organic waste treatment
CN1485287A (en) * 2002-09-28 2004-03-31 财团法人工业技术研究院 System and method for removing organic oxide from waste water
CN1621364A (en) * 2003-11-30 2005-06-01 魏军 Organic waste water treatment process

Also Published As

Publication number Publication date
CN102198997A (en) 2011-09-28

Similar Documents

Publication Publication Date Title
CN100406399C (en) Method and system for harnessing consumer waste landfill percolate
CN101234836B (en) Garbage percolate treatment technique
CN1208262C (en) High concentration oxganic effluent treatment composite process and its equipment
CN102557359B (en) Device for treating wastewater during production of pentaerythritol
CN204079710U (en) Less energy-consumption rural domestic sewage treatment system
CN101565261A (en) Treatment process for medical intermediate production waste water
CN101698556A (en) Treatment method and treatment device of wastewater from middle stage of wheat straw pulp paper-making
CN102198997B (en) Treatment process method for wastewater from abscisic acid production
CN105417843A (en) Treatment method achieving zero release of leachate in municipal domestic garbage incineration plant
CN108314255A (en) A kind of efficient Chinese herbal medicine extraction sewage treatment process
CN103304093A (en) Device and method for advanced denitrification and phosphorous removal of municipal wastewater
CN103183446A (en) Treatment device for piggery wastewater
CN202829786U (en) Advanced and efficient culture and slaughter wastewater treatment device
CN206767868U (en) A kind of garbage percolation liquid treating system
CN104445841A (en) Treatment device and treatment process for surfactant waste water
CN100500599C (en) Treatment method and device of rice lees wastewater
CN202543002U (en) Sewage treatment system
CN204417278U (en) Culturing wastewater processing system
CN202658051U (en) Aquaculture wastewater biochemical treatment system
CN203904167U (en) Biochemical sludge treatment system
CN205258241U (en) Printing and dyeing wastewater treatment system
CN103373783B (en) Zero discharging process for nitrogenous wastewater generated by photovoltaic industry and dedicated system of zero discharging process
CN204434424U (en) A kind for the treatment of unit of surface active agent wastewater
CN204434436U (en) A kind of extensive mud oxidation dehydration fertilizer producing equipment
CN202594916U (en) Pentaerythritol producing wastewater treatment device

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
GR01 Patent grant
C14 Grant of patent or utility model
TR01 Transfer of patent right

Effective date of registration: 20130613

Address after: 610041, No. four, 18 South Renmin Road, Chengdu, Wuhou District, attached to the 2-4 floor of the administrative building of No. 10 hospital, Sichuan

Patentee after: Sichuan Environmental Protection Science and Technology Engineering Co., Ltd.

Patentee after: Longmang Fusheng Science &. Technology Co., Ltd., Sichuan Prov.

Address before: 610041, No. four, 18 South Renmin Road, Chengdu, Wuhou District, attached to the 2-4 floor of the administrative building of No. 10 hospital, Sichuan

Patentee before: Sichuan Environmental Protection Science and Technology Engineering Co., Ltd.

ASS Succession or assignment of patent right

Owner name: LONGMANG FUSHENG SCIENCE +. TECHNOLOGY CO., LTD.,

Effective date: 20130613

C41 Transfer of patent application or patent right or utility model