CN102503034A - 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, specifically a kind of method of utilizing materialization-biochemistry to combine is handled the method for the phenolic wastewater that produces in the sebacic acid production process.
Background technology
Domestic sebacic acid working method mainly adopts benzene (first) phenol dilution method, produces a large amount of phenolic wastewater in the production, produces 1 ton of sebacic acid and produces 25 tons of phenolic wastewater approximately; 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 environment is caused serious harm.
The industry treatment of phenolic waste water 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 mud irrigation method, underground water injection method and ocean disposal method etc. in addition.Various treatment technologies are all effective for reducing different starting point concentration phenolic wastewater, but all depositing in deficiency, adopt physisorphtion such as charcoal absorption cost higher, and sorbent material is saturated easily, 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 big.Advantages such as biochemical process has applied range, processing power is big, equipment is simple and both economical, but phenols concentration can suppress microbial growth when big, thereby can not the treatment of high concentration phenolic wastewater.
Present most sebacic acid manufacturer does not have more efficiently treatment process to phenolic wastewater.One Chinese patent application numbers 95109421.1 all adopts the method for resin absorption to handle the sebacic acid phenolic wastewater with 200510038999.x; The phenol of the overwhelming majority can obtain recycling; But this method is handled waste water COD, phenol content is still higher; Contained high-concentration sulfuric acid sodium salt does not separate in the waste water, can not reach discharging or reuse requirement, and regeneration of resin reclaims heavy contamination.One Chinese patent application number 02110255.4 employing extracting process Phenol-Containing Wastewater Treatment; Specifically comprise adjusting, filtration, extraction, dephenolize, five steps of oil removal; 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 SULPHOSUCCINIC 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.One Chinese patent application numbers 200710062541.7 also adopts the extraction process Phenol-Containing Wastewater Treatment, and the extraction agent of employing is a ricinolic acid, and extraction progression is more than 8 grades, and technology 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 the deficiency to 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 the sebacic acid production system and recycles; The sodium sulfate that evaporation is separated out is as sub product, and evaporation condensed water send biochemical system to handle qualified discharge or reuse.
Sebacic acid described in the inventive method is produced phenolic wastewater, is that the sebacate solution that contains phenol in the production process neutralizes, acidifying obtains the sebacic acid mother liquor, again through sedimentation, filter to isolate the phenolic wastewater that obtains behind the sebacic acid solid.
Technical problem to be solved by this invention is the deficiency to prior art, provides a kind of sebacic acid to produce the phenolic wastewater treatment process, is characterized in that its step is following:
(1) extraction: with comparing 1～4 with extraction agent by profit under the phenolic wastewater normal temperature and pressure: water sent evaporization process after 1 thorough mixing, the extracting phase after the layering promptly came together, 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 the above-mentioned extraction phase normal temperature and pressure and the alkali lye thorough mixing; Reextraction adds alkali number and is as the criterion so that the pH end point values is controlled at 8.5～9.5; Phenol sodium solution after the layering is back to the sebacic acid production system, and the extraction agent after the regeneration recycles in extraction, reextraction progression one-level; Described alkali lye is the 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 cut and is not more than 10% sodium sulfate crystal, and further oven dry processing obtains the SODIUM SULPHATE ANHYDROUS 99PCT sub product, 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 adjustings, control pH value 6.5～8.5, and press mass ratio BOD: N: P=100: proportioning added nutritive element in 5: 1; Described nutritive element is sewage, nitrogenous fertilizer or phosphate fertilizer;
(5) anoxic is biochemical: the waste water that equalizing tank is prepared gets into the biochemical system anoxic reacter, carries out anoxic biochemistry earlier, control dissolved oxygen Do < 0.5mg/>l; PH value 6.5～8.5; 20～35 ℃ of temperature, 3～4 hours residence time, mixed solution gets into aerobic reactor again and carries out aerobic biochemical; Add in the biochemical system through domestication, cultured microorganism preparation; In the prior art disclosed can be used for aerobic biochemical, through conventional domestication, cultivate the microbial preparation of processing and all go for the present invention, for example: yeast (Yeast trichosporon), Acinetobacter calcoaceticus (A.calcoaceticus), pseudomonas (pseudomonas.Sp), Alcaligenes eutrophus lcaligenes eutrophus) or the like;
(6) aerobic biochemical: through the mixed solution after the anoxic biochemical treatment, get into the aerobic biochemical reactor drum 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 biochemical is handled is through the sedimentation layering, and the sedimentation sludge part passes back into anoxic reacter, and part effluxes after the press filtration through concentration and settlement, after supernatant adds the processing of flocculation agent flocculation reaction deposition, and water outlet qualified discharge or reuse.
Above-described a kind of sebacic acid is produced in the phenolic wastewater treatment process technical scheme: in step (4), said nitrogenous fertilizer is preferably urea, ammonium chloride or ammonium sulfate; Described phosphate fertilizer is preferably potassium primary phosphate, potassium hydrogenphosphate 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 promptly to reach effect to the processing of phenolic wastewater.2. secondary pollution is little, and extraction agent does not pollute strip liquor (phenol sodium solution), and the phenol sodium 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 the described extracting operation step; Phenolic wastewater is after extracting and demixing, and the upper strata is extraction phase (a load extraction agent), and lower floor is extracting phase (a collection back water); The extraction phase on upper strata (load extraction agent) reclaims aldehydes matter through the operation of stripping, and the extracting phase of lower floor (collection back water) 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 the sebacic acid production system and recycles.Said reextraction operation steps, extraction phase (load extraction agent) is after the reextraction layering, and the upper strata is through the regenerated extraction agent, returns the extracting system recycle, and lower floor is the phenol sodium solution, returns the sebacic acid production system and recycles.
Said vaporization operation step is that extracting phase (collection back water) 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 mikrobe that the evaporation condensed water after regulating is carried out the anoxic biochemical treatment.The biochemical operation of said anoxic is a lipid material high to organic concentration in the waste water, hydrocarbon chain length, to reduce the molecular weight of organic substance, improves the efficient that follow-up aerobic biochemical is handled.
Described aerobic biochemical operation steps is that the mixed solution after utilizing mikrobe 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 handle.Sebacic acid of the prior art is produced phenolic wastewater, pH value about 2～3, the about 20000mg/l of COD, phenol concentration 4000～5000mg/l, sodium sulfate concentration 7%～8%.After the inventive method processing, collection back water pH value about 6, the about 2000mg/l of COD, the about 240mg/l of phenol concentration; Evaporation back water outlet COD is about 1500mg/l; The about 150mg/l of phenol concentration; Sodium sulfate concentration is reduced to below 6000 mg/l, and mikrobe can adapt to through suitable domestication, in the waste water except that phenol; Still have to contain hydrocarbon lipid acid, dimethyl sebacate, dibutylester, USP Kosher etc., all can be through 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 utilizes physico-chemical process to reclaim the aldehydes matter in the waste water earlier, reduces the phenol concentration of waste water; And isolate sodium sulfate salt, reduce the saltiness in the waste water; Further utilize the waste water after domestication, cultured microorganism are to the dephenolize desalination to carry out biochemical treatment again, thereby make discharged wastewater met the national standard or reuse.This method is reasonable in design, and is workable.
Embodiment
Following reference further describes concrete technical scheme of the present invention, so that those skilled in the art understands the present invention further, and does not constitute the restriction to its right.
Embodiment 1, and a kind of sebacic acid is produced the treatment process of phenolic wastewater, and its step is following:
(1) extraction: with comparing 1: 1 thorough mixing with extraction agent by profit under the phenolic wastewater normal temperature and pressure, water sent evaporization process after the extracting phase after the layering promptly came together, 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 the above-mentioned extraction phase normal temperature and pressure and the alkali lye thorough mixing; Reextraction adds alkali number and is as the criterion so that the pH end point values is controlled at 8.5; Phenol sodium solution after the layering is back to the sebacic acid production system, and the extraction agent after the regeneration recycles in extraction, reextraction progression one-level; Described alkali lye is the 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 cut and is not more than 10% sodium sulfate crystal, and further oven dry processing obtains the SODIUM SULPHATE ANHYDROUS 99PCT sub product, 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 adjustings, control pH value 6.5, and press mass ratio BOD: N: P=100: proportioning added nutritive element in 5: 1; Described nutritive element is sewage, nitrogenous fertilizer or phosphate fertilizer;
(5) anoxic is biochemical: the waste water that equalizing tank is prepared gets into the biochemical system anoxic reacter, carries out anoxic biochemistry earlier, control dissolved oxygen Do 0.5mg/l, and pH value 6.5,20 ℃ of temperature, 3 hours residence time, mixed solution gets into aerobic reactor again and carries out aerobic biochemical; Add in the biochemical system through domestication, cultured microorganism preparation;
(6) aerobic biochemical: through the mixed solution after the anoxic biochemical treatment, get into the aerobic biochemical reactor drum 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 biochemical is handled is through the sedimentation layering, and the sedimentation sludge part passes back into anoxic reacter, and part effluxes after the press filtration through concentration and settlement, after supernatant adds the processing of flocculation agent flocculation reaction deposition, 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 following:
(1) extraction: with comparing 4: 1 thorough mixing with extraction agent by profit under the phenolic wastewater normal temperature and pressure, water sent evaporization process after the extracting phase after the layering promptly came together, 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 the above-mentioned extraction phase normal temperature and pressure and the alkali lye thorough mixing; Reextraction adds alkali number and is as the criterion so that the pH end point values is controlled at 9.5; Phenol sodium solution after the layering is back to the sebacic acid production system, and the extraction agent after the regeneration recycles in extraction, reextraction progression one-level; Described alkali lye is the 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 cut and is not more than 10% sodium sulfate crystal, and further oven dry processing obtains the SODIUM SULPHATE ANHYDROUS 99PCT sub product, 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 adjustings, control pH value 8.5, and press mass ratio BOD: N: P=100: proportioning added nutritive element in 5: 1; Described nutritive element is sewage, nitrogenous fertilizer or phosphate fertilizer;
(5) anoxic is biochemical: the waste water that equalizing tank is prepared gets into the biochemical system anoxic reacter, carries out anoxic biochemistry earlier, control dissolved oxygen Do 0.5mg/l, and pH value 8.5,35 ℃ of temperature, 4 hours residence time, mixed solution gets into aerobic reactor again and carries out aerobic biochemical; Add in the biochemical system through domestication, cultured microorganism preparation;
(6) aerobic biochemical: through the mixed solution after the anoxic biochemical treatment, get into the aerobic biochemical reactor drum 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 biochemical is handled is through the sedimentation layering, and the sedimentation sludge part passes back into anoxic reacter, and part effluxes after the press filtration through concentration and settlement, after supernatant adds the processing of flocculation agent flocculation reaction deposition, and water outlet qualified discharge or reuse.
Embodiment 3, and in the step (4) of the treatment process of embodiment 1 or 2 described a kind of sebacic acid production phenolic wastewater, said nitrogenous fertilizer is urea, ammonium chloride or ammonium sulfate; Described phosphate fertilizer is potassium primary phosphate, potassium hydrogenphosphate 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 through homogeneous, after all amount is regulated.
(1) extraction with in pump delivery to the interrupted extraction still, is compared the efficient extraction agent that adds same volume at 1: 1 with the above-mentioned phenolic wastewater of certain volumetrical by profit; Normal temperature stirred 0.5 hour down, and thorough mixing left standstill 0.5 hour again; Lower floor's extracting phase after the layering (collection back water) is discharged and is sent evaporization process, and extraction progression is one-level, phenolic wastewater pH value 3; Extracting operation need not regulated pH value, the waste water ph about 6 after the extraction.The upper strata oil reservoir is extraction phase (a load extraction agent), stays and waits the regeneration of stripping in the still.
(2) strip, open extraction kettle and stir, 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 the still, and control reextraction terminal point pH value is 9.0; Alkali lye adds continued and stirred 20 minutes, leaves standstill layering in 0.5 hour, discharges lower floor's strip liquor (phenol sodium 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 also is one-level.
(3) evaporation; Above-mentioned extracting phase (collection back water), to single-effect evaporator, vacuum-evaporation is concentrated into finite concentration with pump delivery; The SODIUM SULPHATE ANHYDROUS 99PCT crystallization is constantly separated out in beginning; Go out sodium sulfate crystal with whizzer continuous filtration, further oven dry is processed as the SODIUM SULPHATE ANHYDROUS 99PCT sub product, and the evaporation concentration water Returning evaporimeter that filters out continues evaporation concentration.Evaporation condensed water is through being cooled to 35 ℃ down with being pumped into equalizing tank.
(4) regulate, the evaporation condensed water after cooling gets into equalizing tank, carries out homogeneous, all measures, and presses BOD: N: P=100: (mass ratio) proportioning added nutritive elements such as nitrogen, phosphorus in 5: 1, regulated pH value to 7 with 30% NaOH solution.
(5) anoxic is biochemical; Waste water in the equalizing tank after overregulating adds in the reactor drum through domestication, cultured microorganism preparation with pump delivery to sequence bioreactor (SBR), and water inlet is slow simultaneously stirs; 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, control 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, about 1 hour of settling time, the supernatant after the discharge sedimentation, after adding flocculation agent flocculation reaction deposition is handled, water outlet qualified discharge or reuse; Lower floor's sedimentation mud stays in reactor drum the microbiobacterial agent as next operational cycle, and the discharge section excess sludge effluxes after the pressure filter press filtration to sludge thickener simultaneously.
Embodiment chamber 5, continuous operation type sebacic acid produce the treatment process experiment two of phenolic wastewater.
(1) extraction, the sebacic acid behind the impurity such as removal suspended substance is produced phenolic wastewater normal temperature and is used pump delivery with efficient extraction agent down, through spinner-type flowmeter adjusting flow; Compare 2: 1 by profit and deliver to the static mixer thorough mixing, continuously flow into extraction tower, 1 hour residence time; After layering; Lower floor's extracting phase (collection back water) is delivered to evaporization process continuously, and the upper strata oil reservoir is extraction phase (a load extraction agent), is delivered to load extraction agent basin continuously.
(2) strip, the extraction agent normal temperature of load is used pump delivery with a certain amount of 15% NaOH solution down, after spinner-type flowmeter is regulated flow; Through the static mixer thorough mixing, continuously flow into the back extraction tower, 1 hour residence time; After layering, lower floor's strip liquor (phenol sodium solution) is delivered to the strip liquor basin continuously, is back to the sebacic acid production system; The upper strata oil reservoir is a regenerated extraction agent after the back extraction, is delivered to the extraction agent basin continuously, recycles in extracting system.
(3) evaporation is from the extracting phase (collection back water) of extraction process, through heat exchanger heats; With being pumped into the three-effect counter flow vapo(u)rization system, evaporation concentration, the SODIUM SULPHATE ANHYDROUS 99PCT solid is separated out in crystallization; Centrifuging; Obtain water cut less than 10% sodium sulfate, the SODIUM SULPHATE ANHYDROUS 99PCT sub product is processed in oven dry, and the condensed water that filters out is returned vapo(u)rization system and continued evaporation concentration.Evaporation condensed water is cooled to 35 ℃ down with being pumped into equalizing tank through cooling tower.
(4) regulate, get into the evaporation condensed water of equalizing tank, mixes, carry out homogeneous, all amount is regulated, and add 30% NaOH solution adjusting pH value to 7.5 with waste water such as the ground wash-down water of production plant discharging, sewages through cooling.
(5) anoxic is biochemical, and the waste water in the equalizing tank after overregulating is delivered in the anoxic pond with pump continuously, adds in the anoxic pond through domestication, cultured microorganism preparation; Start stirring, control dissolved oxygen (Do) < 0.5mg/>l, pH value 8.0; 25 ℃ of temperature, retention time of sewage 4 hours.Mixed solution flows automatically continuously or squeezes into Aerobic Pond with pump.
(6) aerobic biochemical, after above-mentioned mixed solution continuously flowed into Aerobic Pond, constantly aeration agitation was 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, about 1 hour of settling time, the supernatant liquid continuous overflow goes out second pond to flocculation sedimentation tank; After adding the processing of flocculation agent flocculation reaction deposition, water outlet qualified discharge or reuse; Lower floor's sedimentation sludge part is back to anoxic pond, and part is delivered to sludge thickener, after the pressure filter press filtration, effluxes.
Claims (2)
1. a sebacic acid is produced the treatment process of phenolic wastewater, it is characterized in that its step is following:
(1) extraction: with comparing 1～4 with extraction agent by profit under the phenolic wastewater normal temperature and pressure: water sent evaporization process after 1 thorough mixing, the extracting phase after the layering promptly came together, 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 the above-mentioned extraction phase normal temperature and pressure and the alkali lye thorough mixing; Reextraction adds alkali number and is as the criterion so that the pH end point values is controlled at 8.5～9.5; Phenol sodium solution after the layering is back to the sebacic acid production system, and the extraction agent after the regeneration recycles in extraction, reextraction progression one-level; Described alkali lye is the 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 cut and is not more than 10% sodium sulfate crystal, and further oven dry processing obtains the SODIUM SULPHATE ANHYDROUS 99PCT sub product, 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 adjustings, control pH value 6.5～8.5, and press mass ratio BOD: N: P=100: proportioning added nutritive element in 5: 1; Described nutritive element is sewage, nitrogenous fertilizer or phosphate fertilizer;
(5) anoxic is biochemical: the waste water that equalizing tank is prepared gets into the biochemical system anoxic reacter, carries out anoxic biochemistry earlier, control dissolved oxygen Do < 0.5mg/>l; PH value 6.5～8.5; 20～35 ℃ of temperature, 3～4 hours residence time, mixed solution gets into aerobic reactor again and carries out aerobic biochemical; Add in the biochemical system through domestication, cultured microorganism preparation;
(6) aerobic biochemical: through the mixed solution after the anoxic biochemical treatment, get into the aerobic biochemical reactor drum 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 biochemical is handled is through the sedimentation layering, and the sedimentation sludge part passes back into anoxic reacter, and part effluxes after the press filtration through concentration and settlement, after supernatant adds the processing of flocculation agent flocculation reaction deposition, 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), said nitrogenous fertilizer is urea, ammonium chloride or ammonium sulfate; Described phosphate fertilizer is potassium primary phosphate, potassium hydrogenphosphate 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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