CN112811725A - Treatment method of carbon fiber production wastewater - Google Patents
Treatment method of carbon fiber production wastewater Download PDFInfo
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- CN112811725A CN112811725A CN202011634196.1A CN202011634196A CN112811725A CN 112811725 A CN112811725 A CN 112811725A CN 202011634196 A CN202011634196 A CN 202011634196A CN 112811725 A CN112811725 A CN 112811725A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 57
- 229920000049 Carbon (fiber) Polymers 0.000 title claims abstract description 30
- 239000004917 carbon fiber Substances 0.000 title claims abstract description 30
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000007380 fibre production Methods 0.000 title claims abstract description 26
- 230000003647 oxidation Effects 0.000 claims abstract description 36
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 36
- 230000003197 catalytic effect Effects 0.000 claims abstract description 35
- 230000001105 regulatory effect Effects 0.000 claims abstract description 18
- 238000005189 flocculation Methods 0.000 claims abstract description 17
- 230000016615 flocculation Effects 0.000 claims abstract description 17
- 239000010865 sewage Substances 0.000 claims abstract description 17
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 15
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- PJNZPQUBCPKICU-UHFFFAOYSA-N phosphoric acid;potassium Chemical compound [K].OP(O)(O)=O PJNZPQUBCPKICU-UHFFFAOYSA-N 0.000 claims description 2
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- GNSKLFRGEWLPPA-UHFFFAOYSA-M potassium dihydrogen phosphate Chemical compound [K+].OP(O)([O-])=O GNSKLFRGEWLPPA-UHFFFAOYSA-M 0.000 description 3
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- 239000002033 PVDF binder Substances 0.000 description 1
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- 238000010586 diagram Methods 0.000 description 1
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical group [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 1
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Images
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/40—Organic compounds containing sulfur
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Water Treatment By Sorption (AREA)
Abstract
The invention relates to a treatment method of carbon fiber production wastewater, which solves the technical problems in the prior method and comprises the following steps of temporarily storing the carbon fiber production wastewater in wastewater, then entering a pH adjusting tank, adjusting the pH, and then flocculating in a flocculation tank to obtain supernatant; the supernatant enters a catalytic oxidation tank, the pH value is further adjusted, and the supernatant enters a catalytic oxidation device for catalytic oxidation; and (3) conveying the wastewater to a biochemical regulating tank to be converged with domestic sewage, further performing biochemical regulation on the wastewater, regulating COD (chemical oxygen demand), ammonia nitrogen and total phosphorus of the wastewater, introducing the wastewater into a biochemical unit for biochemical treatment, and discharging the wastewater after the wastewater treatment reaches the standard. The invention can be used in the field of treatment of carbon fiber production wastewater.
Description
Technical Field
The invention relates to a method for treating wastewater, in particular to a method for treating carbon fiber production wastewater.
Background
The carbon fiber is an important high polymer material and is widely applied to the fields of aerospace, aviation, wind power blades, sports equipment, buildings, cable cores and the like, the number of derived products is hundreds, acrylonitrile is mainly used as a raw material in the production process, the acrylonitrile is flammable in chemical property, and the steam and the air can form an explosive mixture. It is easy to burn and release toxic gas when exposed to fire and high heat. React with oxidant, strong acid, strong alkali, amine and bromine violently.
In the production process of carbon fiber, a large amount of waste water is generated in which the concentration of acrylonitrile is not so high, but since the solvent used in the spinning process is dimethyl sulfoxide, the discharge concentration thereof is high and has an inhibitory effect on microorganisms, and thus the biodegradability is extremely poor. At the highest, the concentration of dimethyl sulfoxide can reach 0.5%, and aiming at the wastewater, the currently adopted method mostly adopts pretreatment and biochemical cycle treatment to change the structure of biodegradable organic compounds, eliminate or weaken the toxicity of the biodegradable organic compounds and increase the biodegradability of the biodegradable organic compounds. The physical and chemical methods commonly used include adsorption, membrane separation, coagulation and precipitation, chemical oxidation, neutralization, chemical coagulation and precipitation, and electrochemical methods. However, the treatment effects of the treatment technologies are general, and the effluent has a certain concentration of dimethyl sulfoxide, so that the biological substances in the water can be continuously inhibited, and the water body is polluted.
Chinese patent application publication No. CN102951730A discloses a biochemical treatment method of dimethyl sulfoxide (DMSO) in carbon fiber production wastewater; performing sludge discharge and film formation on the combined filler in the reactor by using activated sludge in the aerobic aeration tank, wherein the sludge concentration required by the film formation is 4000-5000 mg/L; continuously feeding carbon fiber production wastewater containing DMSO into a reactor, adding nutrient salt and a co-metabolism substrate, adjusting the pH value of inlet water to maintain the pH value in the reactor at 5.5-6.5, and acclimating a biological membrane; continuously feeding the carbon fiber plant to discharge production wastewater in daily life, and simultaneously adding trace elements and a co-metabolism substrate; the method has narrow DMSO concentration range, and the removal rate is obviously and greatly reduced when the DMSO concentration range is larger than 420 mg/L; the DMSO load impact resistance is poor, so that the unrecoverable system is easy to collapse; the effluent Suspended Substances (SS) are more and finely crushed, and are not easy to precipitate; if the recycled water is used as reclaimed water, further precipitation, filtration and disinfection treatment are needed, and the process is long.
Chinese patent application publication No. CN104512980A discloses a process for treating wastewater from carbon fiber production; carbon fiber production wastewater enters an integrated aerobic membrane bioreactor, a co-metabolism substrate and nutrient salt are added, the pH in the reactor is controlled to be 6.5-5.5 by adding alkali, after aerobic biochemical reaction, effluent passes through a membrane component of the reactor, enters an ozone contact tank, is oxidized by ozone, and then automatically flows into a clean water tank, wherein the addition amount of the co-metabolism substrate and the nutrient salt is 0.10-0.15 time and 0.05-0.15 time of the mass of inlet dimethyl sulfoxide; the temperature is 15-35 ℃; the concentration of dissolved oxygen is 2-4 mg/L; the sludge concentration is 5-6 g/L; the alkali is sodium bicarbonate; the co-metabolism matrix refers to one or any combination of monosaccharide, disaccharide, polysaccharide and waste molasses; the nutritive salt is ammonium phosphate; adopting a polyvinylidene fluoride hollow fiber curtain type membrane component; the DMSO concentration treated by the method can reach 1850 mg/L; the DMSO removal rate is close to 100%.
However, this method mainly has the following problems:
1. when the carbon fiber is used for production, as polymerization liquid is prepared, partial acrylonitrile monomer can be discharged when polymerization degree is not ideal, acrylonitrile has certain toxicity, and the content of the acrylonitrile directly entering a biochemical system is easy to cause poisoning and collapse of the biochemical system;
2. in the aerobic process, the pH value of the system needs to be maintained between 5.5 and 6.5, the system is acidic, acid and alkali need to be added for control, so that the use amount of the acid and alkali is increased, the cost is increased, and the misoperation risk is caused;
3. the MBR membrane module is adopted to treat the effluent, the membrane module has high energy consumption, the treatment cost is increased, the later MBR membrane maintenance cost is high, the membrane needs to be cleaned chemically at regular intervals, the MBR membrane needs to be replaced integrally about every 3-5 years, and the operation cost is greatly increased.
Disclosure of Invention
The invention provides a method for treating carbon fiber production wastewater, aiming at solving the technical problems existing in the prior method.
Therefore, the invention provides a method for treating carbon fiber production wastewater, which comprises the following steps: (1) carbon fiber production wastewater enters a temporary wastewater storage tank, is pumped in to adjust the pH value, is adjusted to 8.0-8.5, then enters a high-efficiency flocculation tank to flocculate, and is subjected to flocculation treatment by adding a certain proportion of flocculant; (2) the flocculated supernatant flows to a catalytic oxidation tank by gravity through a pipeline to further adjust the pH value to between 3.0 and 4.5, and is pumped into an advanced catalytic oxidation device by adopting H2O2Treating the wastewater by gas-phase catalytic oxidation; (3) the effluent of advanced catalytic oxidation treatment is sent to a biochemical regulating reservoir to be converged with domestic sewage, then the biochemical regulation is further carried out on the wastewater, the COD, ammonia nitrogen and total phosphorus of the wastewater are regulated by adding drugs and are pumped into a biochemical unit for biochemical treatment, the biochemical unit is divided into an aerobic unit, a biological filter unit and a deep oxidation unit, and the wastewater is finally discharged into a sewage treatment plant after reaching the standard.
In the step (2), the concentration of AN oxidant needs to be finely controlled in the catalytic oxidation process, the secondary pollution of sewage can be caused by excessive input, the oxidant is not completely consumed and remains in water, the adjustment is carried out according to the concentrations of acrylonitrile (hereinafter referred to as AN) and dimethyl sulfoxide (hereinafter referred to as DMSO) in the inlet water during control, when the concentration of AN is less than or equal to 10mg/L, DMSO and less than or equal to 400mg/L, the adding amount of the oxidant is controlled to be 4-4.5 per thousand of the mass of the sewage, and when the adding concentration of the oxidant is too high and is higher than 1%, microorganisms in a biochemical section are killed by the oxidant, so that the fluctuation of a biochemical system is caused;
in the step (3), the pH and COD need to be adjusted simultaneously during the adjustmentcrThe ammonia nitrogen, the temperature and the total phosphorus are comprehensively regulated, the COD (chemical oxygen demand) of the wastewater is regulated to be 400mg/L, the ammonia nitrogen is regulated to be 15mg/L and the total phosphorus is regulated to be 0.5mg/L by adding drugs, the temperature is regulated according to the weather conditions (the water temperature is controlled to be about 25-30 ℃ in winter), the pH value is regulated to be about 8.3, and the regulated wastewater enters a biochemical system for biochemical treatment.
The biochemical unit is divided into an aerobic unit, a flocculation precipitation unit, a biological filter unit and a deep oxidation unit, when the water body of the biochemical unit is acidic, the flocculation precipitation effect is deteriorated, the biological filter is blocked, and the effluent suspended matter is too high, so that the effluent effect is influenced. Therefore, in the operation process, attention is paid to monitoring the pH in the biochemical system, the pH is kept to be alkalescent, the treatment effect is reduced after the aerobic pool is weakly acidic, and the treatment effect of the biochemical system is very low when the pH reaches about 5.5 generally.
The pretreatment process adopts the advanced catalytic oxidation unit to efficiently reduce the concentration of acrylonitrile and dimethyl sulfoxide in the wastewater, improves the biochemical property of the wastewater by matching with domestic sewage, pumps the wastewater into the biochemical treatment unit, and finally further treats the wastewater through the advanced oxidation unit to an external sewage treatment plant which reaches the standard.
Preferably, the pH adjusting tank in the step (1) adjusts the pH by using an alkaline reagent and an acidic reagent.
Further preferably, the acidic reagent is concentrated sulfuric acid; the alkaline reagent is sodium hydroxide.
Preferably, the specific parameters pumped into the high-efficiency flocculation tank in the step (1) are as follows: the PAC concentration range is 200-250mg/L, and the configuration concentration is 5-6%.
Preferably, the specific parameters pumped into the advanced catalytic oxidation device in the step (2) are as follows: h2O2Concentration controlThe preparation range is 3-5%; the retention time is 250min-500 min; the hydrogen peroxide is of industrial grade, and the mass concentration is 27.5%; the air supply control range of the blower is 100-150L/s; the catalytic oxidation filler is a columnar active carbon filler pressed by a noble metal catalyst.
Preferably, the effluent from the catalytic oxidation in the step (3) is sent to a biochemical regulating tank for regulation, and the specific regulation parameters are as follows: the COD concentration range is controlled to be 400-500 mg/L; controlling the ammonia nitrogen concentration range to be 8-15 mg/L; the total phosphorus concentration range is controlled to be 1-3 mg/L; the concentration of acrylonitrile is less than or equal to 0.1 mg/L; the concentration of dimethyl sulfoxide is less than or equal to 100 mg/L; the pH concentration range is controlled between 7.5 and 8.5; C. n, P the nutrient is glucose (food grade), urea (industrial grade 47% N content), and potassium dihydrogen phosphate (industrial grade 22.7% P content).
Preferably, the specific adjustment parameters of the biochemical treatment unit in the step (3) are as follows: 10% of activated carbon particle filler is adopted in the pool as an attached bed of aerobic bacteria, and the pH control range is between 7.5 and 8.5; the reflux ratio is controlled to be between 1.5 and 2; the rear-end biological filter adopts volcanic rock as filler, and the specification of the volcanic rock is 3-5 centimeters.
Preferably, the specific parameters of the deep oxidation unit in the step (3) are as follows: h2O2The control range of the adding amount accounts for 10-15% of the sewage quality, and the retention time is controlled between 120 and 240 min; the unit is internally provided with adsorption type activated carbon particles, pollutants in water are adsorbed, and the activated carbon is periodically backwashed for regeneration.
The beneficial effects of the invention and the prior art are as follows: by means of H2O2The wastewater is treated by a gas phase/solid phase three-phase catalytic oxidation mode, the concentration of organic matters in the wastewater can be effectively reduced, toxic, harmful and difficultly-degraded organic matters in the wastewater are reduced, the wastewater is basically colorless after biochemical treatment and deep oxidation treatment, the COD (chemical oxygen demand) can be controlled within 50mg/L, the operation is simple, and the operation is stable.
The water distribution system and the biochemical unit are controlled in an interlocking manner, the water distribution system is adjusted according to the water quality feedback condition of the biochemical unit, the biochemical system can cause the change of the pH value of the biochemical system due to the different concentration fluctuation conditions of the DMSO (dimethyl sulfoxide) of the inlet water, when the concentration of the DMSO is higher, the pH value is reduced faster, the pH value of the inlet water is increased through the interlocking adjustment, the pH control range of the biochemical aerobic unit is ensured to be between 8.0 and 8.5, and finally, after the treatment through the biochemical system is finished, the wastewater treatment reaches the standard and is discharged.
Drawings
FIG. 1 is a schematic process flow diagram of a process for treating wastewater from carbon fiber production according to the present invention.
Detailed Description
The present invention will be further described with reference to the following examples.
Example 1
The carbon fiber production wastewater to be treated has the following characteristics: CODcr550mg/L, chroma 5, pH7.8, dimethyl sulfoxide 980mg/L, acrylonitrile 0.8 mg/L.
The specific operation steps are as follows:
adding sodium hydroxide into a pH adjusting tank to adjust the pH to 8.7, introducing the pH into a flocculation precipitation tank, adding 200mg/L of flocculant, adjusting the concentration of the flocculant PAC 5% and PAM1 ‰, sending the supernatant into a catalytic oxidation tank to adjust the pH after the flocculation effect reaches the standard, adjusting the pH to 3.7, pumping the supernatant into an advanced catalytic oxidation tower to perform catalytic oxidation, keeping the pH for 240min, and introducing H during the period2O2The amount is 3 per mill (the adding amount of hydrogen peroxide accounts for the same as the sewage in a thousandth ratio), the air quantity of the blower is 150L/s, the concentration of acrylonitrile in the catalytic effluent is reduced to 0.3mg/L, and the concentration of dimethyl sulfoxide is reduced to 328 mg/L;
2. the catalytic effluent is pumped into a biochemical regulation tank for regulation, the wastewater is regulated to COD450mg/L, ammonia nitrogen 8mg/L, total phosphorus 0.5mg/L and pH8.3 by adding glucose, urea, monopotassium phosphate and an acid-base reagent, the reflux ratio is 2, the aeration in the biochemical tank is uniform, the dissolved oxygen concentration is controlled to be 8mg/L, aerobic system effluent COD75.3mg/L and ammonia nitrogen 4.7mg/L are subjected to flocculation precipitation, the effluent is sent into a biological filter, the biological filter effluent COD33.5mg/L, ammonia nitrogen 0.3mg/L, dimethyl sulfoxide ND and acrylonitrile ND finally reach the national first-level A discharge standard (GB18918-2002) and is discharged into a sewage treatment plant.
Example 2
The carbon fiber production wastewater to be treated has the following characteristics: CODcr450mg/L, chroma 5.3, pH7.6, dimethyl sulfoxide 870mg/L, acrylonitrile 0.9 mg/L.
The specific operation steps are as follows:
adding sodium hydroxide into a pH adjusting tank to adjust the pH to 8.3, introducing the pH into a flocculation precipitation tank, adding 185mg/L of flocculant, adjusting the concentration of the flocculant PAC 5% and PAM1 ‰, after the flocculation effect reaches the standard, delivering the supernatant into a catalytic oxidation tank to adjust the pH, adjusting the pH to 3.5, pumping the supernatant into an advanced catalytic oxidation tower to perform catalytic oxidation, keeping the pH for 200min, and introducing H during the period2O2The amount is 3 per mill (the adding amount of hydrogen peroxide accounts for the weight of the sewage in a thousandth ratio), the air quantity of the blower is 130L/s, the concentration of acrylonitrile in the catalytic effluent is reduced to 0.3mg/L, and the concentration of dimethyl sulfoxide is reduced to 350 mg/L;
2. the catalytic effluent is pumped into a biochemical regulation tank for regulation, the wastewater is regulated to COD350mg/L, ammonia nitrogen 8.5mg/L, total phosphorus 0.55mg/L and pH8.5 by adding glucose, urea, monopotassium phosphate and acid-base reagents, the reflux ratio is 2, aeration in the biochemical tank is uniform, the concentration of dissolved oxygen is controlled to be 9mg/L, the COD of aerobic system effluent is 65mg/L and the ammonia nitrogen 5.0mg/L, the effluent is sent into a biological filter after flocculation and precipitation, the effluent of the biological filter is COD28.5mg/L, the ammonia nitrogen 0.2mg/L, dimethyl sulfoxide below 0.1mg/L and the lower limit of acrylonitrile below the detection limit is less than 0.1mg/L (ND), and the effluent finally reaches the national first-level A discharge standard (1GB 8918-2002) and is discharged into a sewage treatment plant.
Example 3
The carbon fiber production wastewater to be treated has the following characteristics: CODcr520mg/L, chroma 5.5, pH7.9, dimethyl sulfoxide 890mg/L, acrylonitrile 0.93 mg/L.
The specific operation steps are as follows:
adding sodium hydroxide into a pH adjusting tank to adjust the pH to 8.4, introducing the pH into a flocculation precipitation tank, adding 175mg/L of a flocculating agent, adjusting the pH of a supernatant to 3.5, pumping the supernatant into an advanced catalytic oxidation tower to perform catalytic oxidation, wherein the concentration of the flocculating agent is PAC 5% and PAM1 ‰, and after the flocculation effect reaches the standard, the pH is adjusted to 1800min, and introducing H during the period2O2The amount is 3 per mill (the adding amount of hydrogen peroxide accounts for the weight of the sewage in a thousandth ratio), the air quantity of the blower is 100L/s, the concentration of acrylonitrile in the catalytic effluent is reduced to 0.45mg/L, and the concentration of dimethyl sulfoxide is reduced to 390 mg/L;
2. the catalytic effluent is pumped into a biochemical regulation tank for regulation, the wastewater is regulated to COD390mg/L, ammonia nitrogen 8.8mg/L, total phosphorus 0.57mg/L and pH8.5 by adding glucose, urea, monopotassium phosphate and acid-base reagents, the reflux ratio is 2, the aeration in the biochemical tank is uniform, the dissolved oxygen concentration is controlled to be 9.5mg/L, the aerobic system effluent COD73mg/L and ammonia nitrogen 6.0mg/L are subjected to flocculation precipitation, the effluent is sent into a biological filter, the biological filter effluent COD35.5mg/L, ammonia nitrogen 0.33mg/L, dimethyl sulfoxide below 0.15mg/L and acrylonitrile below the detection lower limit of less than 0.1mg/L (ND) finally reaches the national first-grade A discharge standard (GB18918-2002) and is discharged into a sewage treatment plant.
However, the above description is only exemplary of the present invention, and the scope of the present invention should not be limited thereby, and the replacement of the equivalent components or the equivalent changes and modifications made according to the protection scope of the present invention should be covered by the claims of the present invention.
Claims (8)
1. A treatment method of carbon fiber production wastewater is characterized by comprising the following steps:
(1) temporarily storing the carbon fiber production wastewater in wastewater, then entering a pH adjusting tank, adjusting the pH of the wastewater to 8.0-8.5, and then flocculating in a flocculation tank to obtain a supernatant;
(2) the supernatant obtained in the step (1) enters a catalytic oxidation tank, the pH value is further adjusted to be 3.0-4.5, and the supernatant enters a catalytic oxidation device and adopts H2O2Gas phase catalytic oxidation, treating the waste water;
in the catalytic oxidation process, the concentration of the oxidant is adjusted according to the concentrations of acrylonitrile and dimethyl sulfoxide in inlet water during control, and when the concentration of acrylonitrile is less than or equal to 10mg/L and the concentration of dimethyl sulfoxide is less than or equal to 400mg/L, the adding amount of the oxidant is controlled to be 4-4.5 per mill of the mass of the sewage;
(3) delivering the effluent after the catalytic oxidation treatment in the step (2) to a biochemical regulating tank to be merged with domestic sewage, and further performing biochemical regulation on the wastewater, wherein the pH and COD need to be regulated simultaneously during regulationcrAmmonia nitrogen, temperature and total phosphorus are comprehensively regulated; the water distribution system and the biochemical unit are controlled in an interlocking way, and the water quality passing through the biochemical unitAnd (3) adjusting the water distribution system by the feedback condition, controlling the pH range of the biochemical aerobic unit to be 7.5-8.5, and finally discharging the wastewater after the wastewater is treated by the biochemical system.
2. The method for treating carbon fiber production wastewater according to claim 1, wherein the pH adjusting tank in the step (1) adjusts the pH using an alkaline agent and an acidic agent.
3. The method for treating carbon fiber production wastewater according to claim 2, wherein the acidic reagent is concentrated sulfuric acid; the alkaline reagent is sodium hydroxide.
4. The treatment method of carbon fiber production wastewater according to claim 1, wherein the specific parameters entering the flocculation tank in the step (1) are as follows: the PAC concentration range is 200-250mg/L, and the configuration concentration is 5-6%.
5. The method for treating carbon fiber production wastewater according to claim 1, wherein the specific parameters entering the catalytic oxidation device in the step (2) are as follows: h2O2The concentration control range is 3-5 per mill; the retention time is 250min-500 min; the hydrogen peroxide is of industrial grade, and the mass concentration is 27.5%; the air supply control range of the blower is 100-150L/s; the catalytic oxidation filler is a columnar active carbon filler pressed by a noble metal catalyst.
6. The carbon fiber production wastewater treatment method according to claim 1, wherein in the step (3), the effluent of the catalytic oxidation is adjusted to a biochemical adjusting tank, and the specific adjusting parameters are as follows: the COD concentration range is controlled to be 400-500 mg/L; controlling the ammonia nitrogen concentration range to be 8-15 mg/L; the total phosphorus concentration range is controlled to be 1-3 mg/L; the concentration of acrylonitrile is less than or equal to 0.1 mg/L; the concentration of dimethyl sulfoxide is less than or equal to 100 mg/L; C. n, P the nutrient is glucose, urea, and potassium dihydrogen phosphate.
7. The carbon fiber production wastewater treatment method according to claim 1, wherein in the step (3), the biochemical treatment unit specifically adjusts parameters as follows: 10% of activated carbon particle filler is adopted in the pool as an attached bed of aerobic bacteria, and the pH control range is between 7.5 and 8.5; the reflux ratio is controlled to be between 1.5 and 2; the rear-end biological filter adopts volcanic rock as filler, and the specification of the volcanic rock is 3-5 centimeters.
8. The carbon fiber production wastewater treatment method according to claim 1, wherein in the step (3), the specific parameters of the deep oxidation unit are as follows: h2O2The adding amount accounts for 10-15% of the sewage amount, and the retention time is controlled between 120 and 240 min; the unit is internally provided with adsorption type activated carbon particles, pollutants in water are adsorbed, and the activated carbon is periodically backwashed for regeneration.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102010097A (en) * | 2010-10-22 | 2011-04-13 | 蓝星环境工程有限公司 | Method for recycling carbon fiber wastewater |
| CN103102045A (en) * | 2013-01-16 | 2013-05-15 | 武汉千水环境工程技术有限公司 | System for treating waste water from production of carbon fiber |
| CN105174644A (en) * | 2015-10-13 | 2015-12-23 | 辽宁石油化工大学 | Efficient treatment combination process of acrylonitrile wastewater |
| CN106007221A (en) * | 2016-07-12 | 2016-10-12 | 浙江环耀环境建设有限公司 | Pharmaceutical wastewater treatment process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102010097A (en) * | 2010-10-22 | 2011-04-13 | 蓝星环境工程有限公司 | Method for recycling carbon fiber wastewater |
| CN103102045A (en) * | 2013-01-16 | 2013-05-15 | 武汉千水环境工程技术有限公司 | System for treating waste water from production of carbon fiber |
| CN105174644A (en) * | 2015-10-13 | 2015-12-23 | 辽宁石油化工大学 | Efficient treatment combination process of acrylonitrile wastewater |
| CN106007221A (en) * | 2016-07-12 | 2016-10-12 | 浙江环耀环境建设有限公司 | Pharmaceutical wastewater treatment process |
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Application publication date: 20210518 |