CN102503034B - Treatment method of phenol-containing liquid waste in sebacic acid production - Google Patents
Treatment method of phenol-containing liquid waste in sebacic acid production Download PDFInfo
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Abstract
The invention discloses a treatment method of phenol-containing liquid waste in sebacic acid production, specifically comprising the steps of extraction, back extraction, evaporation, regulation, anoxic biochemical reaction and aerobic biochemical reaction, and the like. The phenol-containing liquid waste is filtered to remove the insoluble substance, the phenol substance in the liquid waste is extracted by a specially selected extracting agent, the extract phase is back extracted by alkaline liquor and is regenerated to be recycled, and the back extraction solution is returned to a sebacic acid production system. The raffinate is transferred into an evaporation system to be evaporated and separated to obtain a sodium sulfate by-product, the evaporation condensed water is homogenized and equalized after being cooled, the pH value is regulated, and the evaporation condensed water is performed with anoxic biochemical reaction by acclimated and cultured microorganisms in a biochemical reaction system in the presence of nutrient elements. The method provided by the invention is a method combining materialization and biochemical reaction, and the method has the advantages of reasonable design and strong maneuverability; furthermore, the treated liquid waste can satisfy the discharge standard to be discharged or recycled.
Description
Technical field
The present invention relates to a kind of Chemicals production wastewater treatment method, the method for the phenolic wastewater that specifically produces in a kind of method processing sebacic acid production process of utilizing materialization-biochemistry to combine.
Background technology
Domestic sebacic acid production method mainly adopts benzene (first) phenol dilution method, produce a large amount of phenolic wastewater in production, produce 1 ton of sebacic acid and approximately produce 25 tons of phenolic wastewater, pH value is 2～3, phenol mass concentration 4000～5000mg/l, COD reaches 20000mg/l, also contains 7%～8% the sodium sulfate salt of having an appointment, belong to high slat-containing wastewater, do not add the improvement meeting to the environment harm.
The treatment technology of industry phenolic wastewater mainly contains chemical method (chemical oxidization method, photochemical catalytic oxidation), physico-chemical processes (burning method, steam stripped method, solvent extration and absorption method), biochemical process (activated sludge process, Biological fitler method, emulsion liquid membrane etc.), also has in addition mud irrigation method, underground water injection method and ocean disposal method etc.Various treatment technologies are all effective for reducing different starting point concentration phenolic wastewater, but all depositing in deficiency, adopt physisorphtion as higher in the charcoal absorption cost, sorbent material easily saturated, be difficult to regeneration; Burning method exists secondary pollution, problem that energy consumption is high; Chemical method exists the problem that investment is high, cost is large.The advantages such as biochemical process has applied range, processing power is large, equipment is simple and both economical, but phenols concentration can suppress microbial growth when larger, thereby can not process high-concentration phenolic wastewater.
Present most sebacic acid manufacturer does not have more efficiently treatment process to phenolic wastewater.Chinese patent application numbers 95109421.1 and 200510038999.x all adopt the method for resin absorption to process the sebacic acid phenolic wastewater, the phenol of the overwhelming majority can be recycled utilization, but this method is processed waste water COD, phenol content is still higher, in waste water, contained high-concentration sulfuric acid sodium salt does not separate, can not reach discharging or reuse requirement, and heavy contamination is reclaimed in the regeneration of resin.Chinese patent application number 02110255.4 employing extracting process Phenol-Containing Wastewater Treatment, specifically comprise adjusting, filtration, extraction, dephenolize, oil removal five steps, the two-stage extraction process is adopted in extraction, and the first step adopts higher alcohols to make extraction agent, and the second stage adopts phosphoric acid ester and kerosene mixture to make extraction agent.The higher alcohols extraction agent reclaims and must adopt distillation procedure, and energy consumption is higher, and this method processing waste water COD and phenol content are still higher.Chinese patent application numbers 200710062541.7 also adopts the extraction process Phenol-Containing Wastewater Treatment, and the extraction agent of employing is ricinolic acid, and extraction progression is more than 8 grades, and technique is loaded down with trivial details, and water outlet must be for further processing.
Summary of the invention
Technical problem to be solved by this invention is for the deficiencies in the prior art, a kind of technological design treatment process that rational sebacic acid is produced phenolic wastewater is provided, the aldehydes matter that extraction obtains returns to the sebacic acid production system and recycles, the sodium sulfate that evaporation is separated out is as byproduct, and evaporation condensed water send biochemical system to process qualified discharge or reuse.
Sebacic acid described in the inventive method is produced phenolic wastewater, is that the sebacate solution that contains phenol in production process neutralizes, acidifying obtains the sebacic acid mother liquor, then through sedimentation, filter to isolate the phenolic wastewater that obtains after the sebacic acid solid.
Technical problem to be solved by this invention is for the deficiencies in the prior art, provides a kind of sebacic acid to produce the phenolic wastewater treatment process, is characterized in, its step is as follows:
(1) extraction: will compare 1～4 with extraction agent by profit under the phenolic wastewater normal temperature and pressure: 1 fully mixes, and the extracting phase after layering namely extracts rear water and send evaporization process, and extraction phase is that the load extraction agent send the regeneration of reextraction operation; The pH value 2～3 of extraction agent and waste water mixture, extraction progression one-level; Described extraction agent is for being selected from phosphoric acid ester, alkyl amine, kerosene or diesel oil;
(2) strip: get under above-mentioned extraction phase normal temperature and pressure and fully mix with alkali lye, reextraction adds alkali number and is as the criterion so that the pH end point values is controlled at 8.5～9.5, sodium phenolate solution after layering is back to the sebacic acid production system, and the extraction agent after regeneration recycles in extraction, reextraction progression one-level; Described alkali lye is NaOH or the KOH solution of mass concentration 5～30%;
(3) evaporation: extracting phase is through the vapo(u)rization system evaporation concentration, and filtration obtains water content and is not more than 10% sodium sulfate crystal, and further oven dry processing obtains the anhydrous sodium sulphate byproduct, and the evaporation condensed water of removing sodium sulfate salt send biochemical system;
(4) regulate: evaporation condensed water is cooled to sends into the biochemical system equalizing tank below 35 ℃, carries out homogeneous, all amount is regulated, and controls pH value 6.5～8.5, and BOD: N: P=100 in mass ratio: proportioning added nutritive element in 5: 1; Described nutritive element is sanitary sewage, nitrogenous fertilizer or phosphate fertilizer;
(5) anoxic is biochemical: the waste water that equalizing tank is prepared enters the biochemical system anoxic reacter, first carries out anoxic biochemistry, controls dissolved oxygen Do＜0.5mg/l, pH value 6.5～8.5,20～35 ℃ of temperature, 3～4 hours residence time, mixed solution enters aerobic reactor again and carries out aerobic biochemical; Add the microbial preparation through domestication, cultivation in biochemical system; In prior art disclosed can be used for aerobic biochemical, through conventional domestication, cultivate the microbial preparation of making and all go for the present invention, for example: yeast (Yeast trichosporon), Acinetobacter calcoaceticus (A.calcoaceticus), pseudomonas (pseudomonas.Sp), Alcaligenes eutrophus lcaligenes eutrophus) etc.;
(6) aerobic biochemical: through the mixed solution after the anoxic biochemical treatment, enter the aerobic biochemical reactor and carry out the blast aeration stirring, control dissolved oxygen (Do) 2～4mg/l, pH value 6.5～8.5,20～35 ℃ of temperature; 5～8 hours mixed solution residence time; Mixed solution after aerobic treatment is through the sedimentation layering, and the sedimentation sludge part passes back into anoxic reacter, and part effluxes after press filtration through concentration and settlement, after supernatant liquor adds the flocculation agent flocculation reaction deposition to process, and water outlet qualified discharge or reuse.
Above-described a kind of sebacic acid is produced in phenolic wastewater treatment process technical scheme: in step (4), described nitrogenous fertilizer is preferably urea, ammonium chloride or ammonium sulfate; Described phosphate fertilizer is preferably potassium primary phosphate, dipotassium hydrogen phosphate or ammonium phosphate, and regulating the preferred employing of pH value mass concentration is 30%NaOH or KOH solution, or adopts solid soda ash.
Extraction agent of the present invention and extracting process have the following advantages: 1. extraction efficiency is high, has highly selective, and is high to the partition ratio of phenol, only needs the one-level extraction namely to reach effect to the processing of phenolic wastewater.2. secondary pollution is little, and extraction agent does not pollute strip liquor (sodium phenolate solution), and sodium phenolate solution can be back to sebacic acid production.3. extraction agent is easy to regeneration, and back extraction ratio is high, and stripping does not have emulsion, and reextraction process interface is clear, the solvent-free phenomenon of carrying secretly.4. extraction is easy to carry out with the operation of stripping, all operations at normal temperatures, and cost is low.
In described extracting operation step, phenolic wastewater is after extracting and demixing, and the upper strata is extraction phase (load extraction agent), and lower floor is extracting phase (water after extraction), the extraction phase on upper strata (load extraction agent) reclaims aldehydes matter through the operation of stripping, and the extracting phase of lower floor (water after extraction) send evaporation operation.
Described reextraction operation steps is to utilize alkali lye that extraction phase (load extraction agent) is stripped, and the aldehydes matter of recovery returns to the sebacic acid production system and recycles.Described reextraction operation steps, extraction phase (load extraction agent) are after the reextraction layering, and the upper strata is through the extraction agent of regeneration, returns to the extracting system recycle, and lower floor is sodium phenolate solution, returns to the sebacic acid production system and recycles.
Described vaporization operation step is that extracting phase (water after extraction) is carried out evaporation concentration, and the vaporizer of employing can be single-action or multiple-effect, and pressure can adopt normal pressure or decompression.
The biochemical operation steps of described anoxic is to utilize microorganism to carry out the anoxic biochemical treatment to the evaporation condensed water after regulating.The biochemical operation of described anoxic is lipid material high for organic concentration in waste water, hydrocarbon chain length, to reduce the molecular weight of organic substance, improves the efficient of follow-up aerobic treatment.
Described aerobic biochemical operation steps is that the mixed solution after utilizing microorganism to the anoxic biochemical treatment carries out aerobic biochemical, further reduces the pollutent such as COD, phenol of waste water.
The method of the invention can adopt the mode of periodical operation or operate continuously to process.Sebacic acid of the prior art is produced phenolic wastewater, pH value 2～3 left and right, and COD is 20000mg/l approximately, phenol concentration 4000～5000mg/l, sodium sulfate concentration 7%～8%.After processing through the inventive method, water pH value 6 left and right after extraction, COD is 2000mg/l approximately, and phenol concentration is 240mg/l approximately; After evaporation, water outlet COD is about 1500mg/l, phenol concentration is 150mg/l approximately, sodium sulfate concentration is down to below 6000 mg/l, microorganism can adapt to through suitable domestication, in waste water except phenol, still have to contain hydrocarbon lipid acid, dimethyl sebacate, dibutylester, glycerol etc., all can be by microbiological deterioration.Water outlet COD is lower than 30mg/l after biochemical treatment, and phenol concentration is less than 0.5mg/l.
Compared with prior art, the inventive method is a kind of method that adopts materialization-biochemistry to combine, and first utilizes the aldehydes matter in physico-chemical process recovery waste water, reduces the phenol concentration of waste water; And isolate sodium sulfate salt, reduce the saltiness in waste water; Further utilize again the waste water after domestication, the microorganism cultivated are to the dephenolize desalination to carry out biochemical treatment, thereby make discharged wastewater met the national standard or reuse.The method is reasonable in design, and is workable.
Embodiment
Referring to further describing concrete technical scheme of the present invention, so that those skilled in the art understands the present invention further, and do not consist of its Copyright law.
Embodiment 1, and a kind of sebacic acid is produced the treatment process of phenolic wastewater, and its step is as follows:
(1) extraction: fully mix comparing 1: 1 with extraction agent by profit under the phenolic wastewater normal temperature and pressure, the extracting phase after layering namely extracts rear water and send evaporization process, and extraction phase is that the load extraction agent send the regeneration of reextraction operation; The pH value 2 of extraction agent and waste water mixture, extraction progression one-level; Described extraction agent is for being selected from phosphoric acid ester, alkyl amine, kerosene or diesel oil;
(2) strip: get under above-mentioned extraction phase normal temperature and pressure and fully mix with alkali lye, reextraction adds alkali number and is as the criterion so that the pH end point values is controlled at 8.5, sodium phenolate solution after layering is back to the sebacic acid production system, and the extraction agent after regeneration recycles in extraction, reextraction progression one-level; Described alkali lye is NaOH or the KOH solution of mass concentration 5%;
(3) evaporation: extracting phase is through the vapo(u)rization system evaporation concentration, and filtration obtains water content and is not more than 10% sodium sulfate crystal, and further oven dry processing obtains the anhydrous sodium sulphate byproduct, and the evaporation condensed water of removing sodium sulfate salt send biochemical system;
(4) regulate: evaporation condensed water is cooled to sends into the biochemical system equalizing tank below 35 ℃, carries out homogeneous, all amount is regulated, and controls pH value 6.5, and BOD: N: P=100 in mass ratio: proportioning added nutritive element in 5: 1; Described nutritive element is sanitary sewage, nitrogenous fertilizer or phosphate fertilizer;
(5) anoxic is biochemical: the waste water that equalizing tank is prepared enters the biochemical system anoxic reacter, first carries out anoxic biochemistry, controls dissolved oxygen Do＜0.5mg/l, pH value 6.5,20 ℃ of temperature, 3 hours residence time, mixed solution enters aerobic reactor again and carries out aerobic biochemical; Add the microbial preparation through domestication, cultivation in biochemical system;
(6) aerobic biochemical: through the mixed solution after the anoxic biochemical treatment, enter the aerobic biochemical reactor and carry out the blast aeration stirring, control dissolved oxygen Do to 2mg/l, pH value 6.5,20 ℃ of temperature; 5 hours mixed solution residence time; Mixed solution after aerobic treatment is through the sedimentation layering, and the sedimentation sludge part passes back into anoxic reacter, and part effluxes after press filtration through concentration and settlement, after supernatant liquor adds the flocculation agent flocculation reaction deposition to process, and water outlet qualified discharge or reuse.
Embodiment 2, and a kind of sebacic acid is produced the treatment process of phenolic wastewater, and its step is as follows:
(1) extraction: fully mix comparing 4: 1 with extraction agent by profit under the phenolic wastewater normal temperature and pressure, the extracting phase after layering namely extracts rear water and send evaporization process, and extraction phase is that the load extraction agent send the regeneration of reextraction operation; The pH value 3 of extraction agent and waste water mixture, extraction progression one-level; Described extraction agent is for being selected from phosphoric acid ester, alkyl amine, kerosene or diesel oil;
(2) strip: get under above-mentioned extraction phase normal temperature and pressure and fully mix with alkali lye, reextraction adds alkali number and is as the criterion so that the pH end point values is controlled at 9.5, sodium phenolate solution after layering is back to the sebacic acid production system, and the extraction agent after regeneration recycles in extraction, reextraction progression one-level; Described alkali lye is NaOH or the KOH solution of mass concentration 30%;
(3) evaporation: extracting phase is through the vapo(u)rization system evaporation concentration, and filtration obtains water content and is not more than 10% sodium sulfate crystal, and further oven dry processing obtains the anhydrous sodium sulphate byproduct, and the evaporation condensed water of removing sodium sulfate salt send biochemical system;
(4) regulate: evaporation condensed water is cooled to sends into the biochemical system equalizing tank below 35 ℃, carries out homogeneous, all amount is regulated, and controls pH value 8.5, and BOD: N: P=100 in mass ratio: proportioning added nutritive element in 5: 1; Described nutritive element is sanitary sewage, nitrogenous fertilizer or phosphate fertilizer;
(5) anoxic is biochemical: the waste water that equalizing tank is prepared enters the biochemical system anoxic reacter, first carries out anoxic biochemistry, controls dissolved oxygen Do＜0.5mg/l, pH value 8.5,35 ℃ of temperature, 4 hours residence time, mixed solution enters aerobic reactor again and carries out aerobic biochemical; Add the microbial preparation through domestication, cultivation in biochemical system;
(6) aerobic biochemical: through the mixed solution after the anoxic biochemical treatment, enter the aerobic biochemical reactor and carry out the blast aeration stirring, control dissolved oxygen Do to 4mg/l, pH value 8.5,35 ℃ of temperature; 8 hours mixed solution residence time; Mixed solution after aerobic treatment is through the sedimentation layering, and the sedimentation sludge part passes back into anoxic reacter, and part effluxes after press filtration through concentration and settlement, after supernatant liquor adds the flocculation agent flocculation reaction deposition to process, and water outlet qualified discharge or reuse.
Embodiment 3, and in the step (4) of the treatment process of the described a kind of sebacic acid production phenolic wastewater of embodiment 1 or 2, described nitrogenous fertilizer is urea, ammonium chloride or ammonium sulfate; Described phosphate fertilizer is potassium primary phosphate, dipotassium hydrogen phosphate or ammonium phosphate, and regulating pH value employing mass concentration is 30%NaOH or KOH solution, or adopts solid soda ash.
Embodiment 4, and periodical operation formula sebacic acid is produced the treatment process experiment one of phenolic wastewater.
The sebacic acid mother liquor through sedimentation, filter to isolate the sebacic acid solid, the clear liquid that filters out is sebacic acid and produces phenolic wastewater.Send extraction process by homogeneous, after all amount is regulated.
(1) extraction, with the above-mentioned phenolic wastewater of a constant volume with pump delivery to the interrupted extraction still, compare the efficient extraction agent that adds same volume at 1: 1 by profit, stirred 0.5 hour under normal temperature, fully mix, standing 0.5 hour again, lower floor's extracting phase after layering (water after extraction) is discharged and is sent evaporization process, and extraction progression is one-level, phenolic wastewater pH value 3, extracting operation does not need to regulate pH value, waste water ph 6 left and right after extraction.The upper strata oil reservoir is extraction phase (load extraction agent), stays and waits the regeneration of stripping in still.
(2) strip, the unlatching extraction kettle stirs, stir above-mentioned extraction phase (load extraction agent), slowly add 10% NaOH solution simultaneously, the alkali lye dosage is as the criterion with pH value in still, control reextraction terminal point pH value 9.0, alkali lye adds rear continuation and stirred 20 minutes, and standing 0.5 little layered is discharged lower floor's strip liquor (sodium phenolate solution) and is back to the sebacic acid production system, the upper strata oil reservoir recycles in next extracting operation for the extraction agent after regenerating.Reextraction progression is also one-level.
(3) evaporation, above-mentioned extracting phase (water after extraction), with pump delivery to single-effect evaporator, vacuum evaporation is to finite concentration, the anhydrous sodium sulphate crystallization is constantly separated out in beginning, go out sodium sulfate crystal with whizzer continuous filtration, further oven dry is processed as the anhydrous sodium sulphate byproduct, and the evaporation concentration water Returning evaporimeter that filters out continues evaporation concentration.Evaporation condensed water is through being cooled under 35 ℃ with being pumped into equalizing tank.
(4) regulate, the evaporation condensed water after cooling enters equalizing tank, carries out homogeneous, equal amounts, and by BOD: N: P=100: 5: the 1(mass ratio) proportioning adds the nutritive elements such as nitrogen, phosphorus, with 30% NaOH solution adjusting pH value to 7.
(5) anoxic is biochemical, waste water in equalizing tank after overregulating with pump delivery to sequence bioreactor (SBR), add the microbial preparation through domestication, cultivation in reactor, water inlet is slow the stirring simultaneously, control dissolved oxygen (Do)＜0.5mg/l, pH value 7.5,25 ℃ of temperature, 3 hours residence time.
(6) aerobic biochemical after the biochemical end of anoxic, is opened the aerator blast aeration and is stirred, and controls dissolved oxygen (Do) 3mg/l, pH value 7.5,25 ℃ of temperature.5 hours mixed solution residence time.
(7) sedimentation, draining, aerobic biochemical finishes, and stops aeration, standing sedimentation, approximately 1 hour settling time, the supernatant liquor after the discharge sedimentation, after adding the flocculation agent flocculation reaction deposition to process, water outlet qualified discharge or reuse; Lower floor's sedimentation mud stays in reactor the microbiobacterial agent as next operational cycle, and the discharge section excess sludge to sludge thickener, effluxes after the pressure filter press filtration simultaneously.
Embodiment chamber 5, continuous operation type sebacic acid produce the treatment process experiment two of phenolic wastewater.
(1) extraction, sebacic acid after the impurity such as removal suspended substance is produced under phenolic wastewater normal temperature and efficient extraction agent pump delivery, through the spinner-type flowmeter adjust flux, compare 2: 1 and deliver to static mixer by profit and fully mix, continuously flow into extraction tower, 1 hour residence time, after layering, lower floor's extracting phase (water after extraction) is delivered to evaporization process continuously, and the upper strata oil reservoir is extraction phase (load extraction agent), is delivered to continuously load extraction agent basin.
(2) strip, with a certain amount of 15% NaOH solution pump delivery, after the spinner-type flowmeter adjust flux, fully mix through static mixer under the extraction agent normal temperature of load, continuously flow into the back extraction tower, 1 hour residence time, after layering, lower floor's strip liquor (sodium phenolate solution) is delivered to the strip liquor basin continuously, be back to the sebacic acid production system, the upper strata oil reservoir is the extraction agent of regenerating after back extraction, is delivered to continuously the extraction agent basin, recycles in extracting system.
(3) evaporation, extracting phase (water after extraction) from extraction process, through heat exchanger heats, with being pumped into the technique in three-effect countercurrent evaporation system, evaporation concentration, crystallization anhydrous sodium sulphate solid, centrifuging, obtain water content less than 10% sodium sulfate, the anhydrous sodium sulphate byproduct is processed in oven dry, and the condensed water that filters out is returned to vapo(u)rization system and continued evaporation concentration.Evaporation condensed water is cooled under 35 ℃ with being pumped into equalizing tank through cooling tower.
(4) regulate, enter the evaporation condensed water of equalizing tank through cooling, mixes with waste water such as the ground flushing water of production plant discharging, sanitary sewages, carry out homogeneous, all amount is regulated, and add 30% NaOH solution adjusting pH value to 7.5.
(5) anoxic is biochemical, and the waste water in equalizing tank after overregulating is delivered in anoxic pond continuously with pump, adds the microbial preparation through domestication, cultivation in anoxic pond, start stirring, control dissolved oxygen (Do)＜0.5mg/l, pH value 8.0,25 ℃ of temperature, retention time of sewage 4 hours.Mixed solution continuous self-flowing or squeeze into Aerobic Pond with pump.
(6) aerobic biochemical, after above-mentioned mixed solution continuously flowed into Aerobic Pond, constantly aeration agitation, controlled dissolved oxygen (Do) 2～4mg/l, pH value 8.0,25 ℃ of temperature.5 hours mixed solution residence time.
(7) sedimentation, draining, aerobic biochemical finishes, and mixed solution continuously flows into second pond, standing sedimentation, approximately 1 hour settling time, the supernatant liquid continuous overflow goes out second pond to flocculation sedimentation tank, after adding the flocculation agent flocculation reaction deposition to process, water outlet qualified discharge or reuse; Lower floor's sedimentation sludge part is back to anoxic pond, and part is delivered to sludge thickener, effluxes after the pressure filter press filtration.
Claims (2)
1. the treatment process that sebacic acid is produced phenolic wastewater, is characterized in that, its step is as follows:
(1) extraction: will compare 1～4 with extraction agent by profit under the phenolic wastewater normal temperature and pressure: 1 fully mixes, and the extracting phase after layering namely extracts rear water and send evaporization process, and extraction phase is that the load extraction agent send the regeneration of reextraction operation; The pH value 2～3 of extraction agent and waste water mixture, extraction progression one-level; Described extraction agent is for being selected from phosphoric acid ester, alkyl amine, kerosene or diesel oil;
(2) strip: get under above-mentioned extraction phase normal temperature and pressure and fully mix with alkali lye, reextraction adds alkali number and is as the criterion so that the pH end point values is controlled at 8.5～9.5, sodium phenolate solution after layering is back to the sebacic acid production system, and the extraction agent after regeneration recycles in extraction, reextraction progression one-level; Described alkali lye is NaOH or the KOH solution of mass concentration 5～30%;
(3) evaporation: extracting phase is through the vapo(u)rization system evaporation concentration, and filtration obtains water content and is not more than 10% sodium sulfate crystal, and further oven dry processing obtains the anhydrous sodium sulphate byproduct, and the evaporation condensed water of removing sodium sulfate salt send biochemical system;
(4) regulate: evaporation condensed water is cooled to sends into the biochemical system equalizing tank below 35 ℃, carries out homogeneous, all amount is regulated, and controls pH value 6.5～8.5, and BOD: N: P=100 in mass ratio: proportioning added nutritive element in 5: 1; Described nutritive element is sanitary sewage, nitrogenous fertilizer or phosphate fertilizer;
(5) anoxic is biochemical: the waste water that equalizing tank is prepared enters the biochemical system anoxic reacter, first carries out anoxic biochemistry, controls dissolved oxygen DO＜0.5mg/l, pH value 6.5～8.5,20～35 ℃ of temperature, 3～4 hours residence time, mixed solution enters aerobic reactor again and carries out aerobic biochemical; Add the microbial preparation through domestication, cultivation in biochemical system;
(6) aerobic biochemical: through the mixed solution after the anoxic biochemical treatment, enter the aerobic biochemical reactor and carry out the blast aeration stirring, control dissolved oxygen DO to 2～4mg/l, pH value 6.5～8.5,20～35 ℃ of temperature; 5～8 hours mixed solution residence time; Mixed solution after aerobic treatment is through the sedimentation layering, and the sedimentation sludge part passes back into anoxic reacter, and part effluxes after press filtration through concentration and settlement, after supernatant liquor adds the flocculation agent flocculation reaction deposition to process, and water outlet qualified discharge or reuse.
2. a kind of sebacic acid according to claim 1 is produced the treatment process of phenolic wastewater, and it is characterized in that: in step (4), described nitrogenous fertilizer is urea, ammonium chloride or ammonium sulfate; Described phosphate fertilizer is potassium primary phosphate, dipotassium hydrogen phosphate or ammonium phosphate, and regulating pH value employing mass concentration is 30%NaOH or KOH solution, or adopts solid soda ash.
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