CN104291532A - Treatment method and equipment of beta-naphthol production wastewater - Google Patents
Treatment method and equipment of beta-naphthol production wastewater Download PDFInfo
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- CN104291532A CN104291532A CN201410580957.8A CN201410580957A CN104291532A CN 104291532 A CN104291532 A CN 104291532A CN 201410580957 A CN201410580957 A CN 201410580957A CN 104291532 A CN104291532 A CN 104291532A
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- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C02F3/02—Aerobic processes
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- C02F3/30—Aerobic and anaerobic processes
Abstract
The invention provides treatment method and equipment of a beta-naphthol production wastewater. The equipment comprises a collecting tank, a high-efficiency air-flotation reactor, an acidification tank, a micro-electrolysis tower, a pipeline mixer, a Fenton reactor, a neutralization coagulation reaction pool, a compound sedimentation pool, an adjusting and cooling pool, a hydrolysis acidification pool, a mobile bed biofilm reaction tank, a contact oxidation tank, a secondary sedimentation tank, an intermediate tank, a prefilter, a catalytic oxidation tower and a biological aerated filter. Through an application method of the equipment, the problem that the beta-naphthol production wastewater is high in COD, high in chromaticity and difficult to degrade is solved, and long-period stable emission on standard of the beta-naphthol production wastewater is ensured.
Description
Technical field
The present invention relates to the treatment process of 2-Naphthol factory effluent, belong to technical field of waste water processing, is more specifically a kind of method and apparatus adopting physical chemistry method process 2-Naphthol factory effluent.
Background technology
β-naphthols has another name called 2-naphthols, ethyl naphthol, 2-hydroxyl naphthalene, is one of naphthalene series dye intermediate typical products.Be mainly used in the production of dyestuff and dyestuff intermediate, be also widely used in medicine, agricultural chemicals, rubber ingredients, spices, leather tanning, textile auxiliary and dressing agent raw material etc.
Due to the singularity that 2-Naphthol is produced, its environmental protection impact extremely both at home and abroad environmental administration is paid attention to.In 20 end of the centurys, the U.S. and European Union member countries are classified as naphthols as priority pollutant, and the production of corresponding 2-Naphthol also marries again developing country.At present, the nations of China and India is the main product ground of 2-naphthols.On the Chinese side, 2-Naphthol year overall throughput be approximately 8-9 ten thousand tons, account for 50% of whole world ultimate production, export volume accounts for 35%.The wastewater through organic matter content discharged in its production process is high, acidity large, and saliferous is high, toxic to microorganism, has teratogenesis, carcinogenesis to human body, is difficult to degraded in the environment, belongs to one of organic industrial sewage of pole refractory reason.
At present, the sulfonation-alkali fusion of the main naphthalene by Technical comparing maturation both at home and abroad, the method take naphthalene as raw material, obtains 2-Naphthol through the process such as sulfonation, hydrolysis, neutralization, alkali fusion, acidifying, refining (distillation).Discharge in 2-Naphthol production process that waste water water temperature high (50-60 DEG C) color and luster is dark, soda acid resiliency is strong, COD is up to 30000 ~ 40000 mg/L, wherein containing a large amount of inorganicss (content is up to 10% ~ 15%) such as sodium sulfate, S-WAT, and be separated the organic intermediate products such as incomplete naphthene sulfonic acid.Therefore, in waste water, COD causes primarily of the oxidation of inferior sulfate radical and naphthene sulfonic acid root, and the high-concentration naphthalene sulfonic acid (17 ~ 18 g/L) especially contained is maximum to COD contribution.In addition, due to the conjugatedπbond of the delocalization that naphthalene nucleus is made up of 10 carbon atoms, structure quite stable, is difficult to degraded, belongs to the wastewater from chemical industry of high salt, high COD high chroma.The BOD5/COD of this kind of waste water is extremely low, and biodegradability is poor, and toxic to microorganism, is difficult to general biochemical method process.
At present, the main methods of 2-Naphthol factory effluent has: method of enrichment, absorption method, chemical oxidization method, biochemical process.Method of enrichment utilizes sulfonated alkali fusion method to synthesize a large amount of Na contained in the factory effluent of 2-Naphthol
2sO4, by salting out, can make sodiumβ-naphthalenesulfonate wherein separate out.Although method of enrichment has certain environmental benefit, and simple to operate, technical maturity.But the energy consumption of method of enrichment is high, and the factory effluent qualified discharge of 2-Naphthol cannot be guaranteed.Absorption method is the common method of process naphthols waste water, but treatment effect is not satisfactory, and cost is higher, if sorbing material recycling is improper, also can cause secondary pollution.Chemical oxidization method mainly adds the naphthalene nucleus that oxygenant is mainly used in destroying naphthene sulfonic acid in waste water, resolve into small organic molecule, and then remove COD, but oxidation style running cost is high, and technical difficulty is comparatively large, is used alone oxidation style and is difficult to complete qualified discharge.For biochemical process, the factory effluent biodegradability of 2-Naphthol is poor, and bio-toxicity is higher, needs to carry out pre-treatment before biochemistry.The factory effluent harm of 2-Naphthol is large, and single art breading effect is poor, and therefore, employing combination process is the development trend of the production wastewater treatment research of 2-Naphthol.
Summary of the invention
For above-mentioned prior art Problems existing, the invention provides a kind of 2-Naphthol production wastewater treatment method and apparatus, solve 2-Naphthol factory effluent height COD, high chroma, be difficult to the problem of degrading, realize guaranteeing the qualified discharge that 2-Naphthol factory effluent long period is stable.
For solving prior art Problems existing, the technical scheme that the present invention takes is: a kind of 2-Naphthol production wastewater treatment method, comprises the steps:
(1) 2-Naphthol factory effluent enters efficient air-floating reactor by water collecting basin through pump lifting, removes the wet goods impurity of suspended substance, oil slick and the solubilised state in waste water, and the waste gas that air supporting reaction produces enters absorption tower and passes through alkali liquor absorption;
(2) water outlet of efficient air-floating reactor enters souring tank, adds acid for adjusting pH to 1, and the inferior sulfate radical acidifying in 2-Naphthol factory effluent is changed into SO
2, adopt blower fan aeration, promote the SO produced in waste water
2gas overflowing, the waste gas of generation enters absorption tower and passes through alkali liquor absorption;
(3) 2-Naphthol factory effluent is removed after inferior sulfate radical through step (2) acidifying, waste water ph is about 3, water outlet directly enters light electrolysis tower carry out micro-electrolysis reaction process without the need to regulating, the hydroxyl radical free radical of strong oxidizing property is produced by electrochemical reaction, the larger molecular organics of 2-Naphthol factory effluent is oxidized to small organic molecule, improves the biodegradability of waste water;
(4) waste water ph after microelectrolysis processing is about 4.5, directly carries out Fenton's reaction, adds hydrogen peroxide and iron powder, carries out oxide treatment further to the larger molecular organics in 2-Naphthol factory effluent;
(5) Fenton's reaction water outlet enter in and coagulation reaction tank carry out in and coagulating, pH to 6-8 is regulated by adding CaO, add flocculation agent PAC, coagulant aids PAM removes the suspended substance in waste water, in and water outlet after coagulation enter compound settling bowl and carry out sedimentation;
(6) waste water of the water outlet of compound settling bowl and lower concentration enters and regulates cooling tank to lower the temperature, and is partly refluxed to adjustment cooling tank adjustment waste water quality by effluent of aeration biological filter, carries out biochemical condition to meet waste water;
(7) cooling tank water outlet is regulated to enter hydrolysis acidification pool, the non-solubility organism in waste water is changed into dissolved organic matter by the characteristic of microorganism, mainly the organism of wherein difficult for biological degradation is changed into the organism of readily biodegradable, improve the biodegradability of waste water, be beneficial to follow-up oxygen consumption process;
(8) after acidication, water outlet enters fluid bed biological film reaction tank, by thermopnore aerobe method process 2-Naphthol factory effluent, carries out advanced treatment by the respiration of aerobic microbiological to the organism in waste water;
(9) water outlet of fluid bed biological film reaction tank enters contact-oxidation pool, by thermopnore aerobe method process 2-Naphthol factory effluent, carries out advanced treatment by the respiration of aerobic microbiological to the organism in waste water;
(10) contact-oxidation pool water outlet enters second pond, and second pond supernatant liquor enters intermediate pool, and intermediate pool water outlet is removed suspended substance through fore filter and entered catalyzed oxidation tower, by catalytic ozonation reaction depth process 2-Naphthol factory effluent;
(11) catalytic ozonation water outlet enters BAF, is further removed SS, COD in waste water by biomembrance process, guarantees that 2-Naphthol factory effluent can qualified discharge or reuse.SS refers to suspended substance.
Step (2) described souring tank, step (3) described micro-electrolysis reaction, step (7) described hydrolysis acidification pool, the described fluid bed biological film reaction tank of step (8), step (9) described contact-oxidation pool, step (11) described BAF all carries out aeration by blower fan.The optional common acid of acid that in step (2), souring tank adds, as: sulfuric acid, hydrochloric acid, nitric acid, preferably sulfuric acid of the present invention.
The mud that efficient air-floating reactor, compound settling bowl and second pond produce enters sludge thickener, and the sludge reflux in sludge thickener is to regulating cooling tank, hydrolysis acidification pool fluid bed biological film reaction tank and contact-oxidation pool.
The described light electrolysis tower of step (3) adopts iron carbon compounded mix.
It is 30%(massfraction that step (4) described Fenton's reaction adds hydrogen peroxide concentration), dosage is account for influent waste water volume 5 ‰.
During step (5) is described and coagulation reaction tank to add PAC dosage be 1%, the PAM dosage accounting for influent waste water volume is account for influent waste water volume 1 ‰.
The waste water quality that the described adjustment cooling tank of step (6) carries out after cooling adjustment is COD<2000mg/L, specific conductivity <0.7ms/cm.
Present invention also offers a kind of 2-Naphthol production wastewater treatment device, comprising: water collecting basin, efficient air-floating reactor, souring tank, light electrolysis tower, line mixer, Fenton reactor, in and coagulation reaction tank, compound settling bowl, regulate cooling tank, hydrolysis acidification pool, fluid bed biological film reaction tank, contact-oxidation pool, second pond, intermediate pool, fore filter, catalyzed oxidation tower, BAF, described water collecting basin connects efficient air-floating reactor, described efficient air-floating reactor connects souring tank, described souring tank connects light electrolysis tower, described light electrolysis tower is connected with Fenton reactor by line mixer, during described Fenton reactor connects and coagulation reaction tank, compound settling bowl is connected with coagulation reaction tank in described, described compound settling bowl connects adjustment cooling tank, described adjustment cooling tank connects hydrolysis acidification pool, described hydrolysis acidification pool connects fluid bed biological film reaction tank, fluid bed biological film reaction tank connects contact-oxidation pool, described contact-oxidation pool connects second pond, described second pond connects intermediate pool, described intermediate pool connects fore filter, described fore filter connects catalyzed oxidation tower, described catalyzed oxidation tower connects BAF, described BAF connects cooling equalizing tank, effluent of aeration biological filter is partly refluxed to adjustment cooling tank, the backflow water yield is regulated according to biochemical inflow requirement.
Described efficient air-floating reactor is connected with absorption tower with souring tank top, and described absorption tower connects aiutage.
Described Fenton reactor connects hydrogen peroxide grug feeding jar.
PAC grug feeding jar and PAM grug feeding jar is connected with coagulation reaction tank in described.
Described cooling equalizing tank connects circulating cooling tower.
Described efficient air-floating reactor, compound settling bowl are connected sludge thickener with bottom second pond, and the mud of generation enters sludge thickener.Described sludge thickener is also connected with adjustment cooling tank, hydrolysis acidification pool, fluid bed biological film reaction tank and contact-oxidation pool, for regulating cooling tank, hydrolysis acidification pool, fluid bed biological film reaction tank and contact-oxidation pool to provide mud, supplements mud loss.
Described catalyzed oxidation tower connects ozonizer.
Described souring tank, light electrolysis tower, hydrolysis acidification pool, fluid bed biological film reaction tank, contact-oxidation pool and the equal connecting fan of BAF.
Beneficial effect of the present invention is:
(1) guarantee 2-Naphthol factory effluent qualified discharge after treatment, and can reuse be met, rinse, for the adjustment water of biochemistry water inlet for ground and equipment.
(2) remove inferior sulfate radical by adding sulfuric acid, and adopt air aeration, better make the SO produced in waste water
2overflow.
(3) first the pre-treatment of 2-Naphthol factory effluent carries out acidifying removal inferior sulfate radical, water outlet pH directly can meet the condition of iron-carbon micro-electrolysis reaction, pH value after micro-electrolysis reaction directly can meet the condition of Fenton's reaction, technical process arrangement is reasonable, pH value progressively raises, without the need to carrying out pH regulator, reduce soda acid consumption in technique, for enterprise reduces running cost.
(4) rail carbon micro-electrolytic processes and Fenton technology coupling is adopted, naphthalene nucleus is can be good to open, larger molecular organics is changed into small organic molecule, improve the biodegradability of 2-Naphthol factory effluent, greatly reduced the bio-toxicity of 2-Naphthol factory effluent by Fenton technology process, meet the condition that waste water carries out biochemical treatment.
(5) effluent of aeration biological filter may be used for device ground wash-down water, also can be used for the adjustment water regulating biochemical water inlet, achieves the resource recycling of 2-Naphthol factory effluent, and decrease the quantity discharged of waste water.
Accompanying drawing explanation
Fig. 1 is the schema of the treatment process of 2-Naphthol factory effluent of the present invention;
Fig. 2 is the treatment unit schematic diagram of 2-Naphthol factory effluent of the present invention;
Wherein: 1-water collecting basin, 2-efficient air-floating reactor, 3-souring tank, 4-absorption tower, 5-aiutage, 6-light electrolysis tower, 7-Fenton reactor, 8-line mixer, 9-hydrogen peroxide grug feeding jar, 10-PAC grug feeding jar, 11-PAM grug feeding jar, in 12-and coagulation reaction tank, 13-compound settling bowl, 14-regulates cooling tank, 15-hydrolysis acidification pool, 16-fluid bed biological film reaction tank, 17-contact-oxidation pool, 18-second pond, 19-intermediate pool, 20-fore filter, 21-catalyzed oxidation tower, 22-BAF, 23 ozonizers, 24 sludge thickeners, 25 circulating cooling towers, 26 blower fans.
Embodiment
Below in conjunction with embodiment, the present invention is described in detail.
Embodiment 1
As shown in Figure 1-2, a kind of 2-Naphthol production wastewater treatment method, comprises the steps:
(1) 2-Naphthol factory effluent enters efficient air-floating reactor 2 by water collecting basin 1 through pump lifting, removes the wet goods impurity of suspended substance, oil slick and the solubilised state in waste water, and the waste gas that air supporting reaction produces enters absorption tower 4 and passes through alkali liquor absorption;
(2) efficient air-floating reactor 2 water outlet enters souring tank 3, adds acid for adjusting pH to 1, and the inferior sulfate radical acidifying in 2-Naphthol factory effluent is changed into SO
2, adopt blower fan 26 aeration, promote the SO produced in waste water
2gas overflowing, the waste gas of generation enters absorption tower 4 and passes through alkali liquor absorption;
(3) 2-Naphthol factory effluent is removed after inferior sulfate radical through step (2) acidifying, waste water ph is about 3, water outlet directly enters light electrolysis tower 6 carry out micro-electrolysis reaction process without the need to regulating, the hydroxyl radical free radical of strong oxidizing property is produced by electrochemical reaction, the larger molecular organics of 2-Naphthol factory effluent is oxidized to small organic molecule, improves the biodegradability of waste water;
(4) waste water ph after microelectrolysis processing is about 4.5, directly carries out Fenton's reaction, adds hydrogen peroxide and iron powder, carries out oxide treatment further to the larger molecular organics in 2-Naphthol factory effluent;
(5) Fenton's reaction water outlet enter in and coagulation reaction tank 12 carry out in and coagulating, pH to 6-8 is regulated by adding CaO, add flocculation agent PAC, coagulant aids PAM removes the suspended substance in waste water, in and water outlet after coagulation enter compound settling bowl 13 and carry out sedimentation;
(6) waste water of compound settling bowl 13 water outlet and lower concentration enters and regulates cooling tank 14 to lower the temperature, and by BAF 22 water part be back to regulate cooling tank 14 regulate waste water quality, BAF 22 regulates cooling tank 14 to regulate the backflow water yield according to biochemical inflow requirement, carries out biochemical condition to meet waste water;
(7) cooling tank 14 water outlet is regulated to enter hydrolysis acidification pool 15, the non-solubility organism in waste water is changed into dissolved organic matter by the characteristic of microorganism, mainly the organism of wherein difficult for biological degradation is changed into the organism of readily biodegradable, improve the biodegradability of waste water, be beneficial to follow-up oxygen consumption process;
(8) after acidication, water outlet enters fluid bed biological film reaction tank 16, by thermopnore aerobe method process 2-Naphthol factory effluent, carries out advanced treatment by the respiration of aerobic microbiological to the organism in waste water;
(9) fluid bed biological film reaction tank 16 water outlet enters contact-oxidation pool 17, by thermopnore aerobe method process 2-Naphthol factory effluent, carries out advanced treatment by the respiration of aerobic microbiological to the organism in waste water;
(10) contact-oxidation pool 17 water outlet enters second pond 18, second pond 18 supernatant liquor enters intermediate pool 19, intermediate pool 19 water outlet is removed suspended substance through fore filter 20 and is entered catalyzed oxidation tower 21, by catalytic ozonation reaction depth process 2-Naphthol factory effluent;
(11) catalytic ozonation water outlet enters BAF 22, is further removed SS, COD in waste water by biomembrance process, guarantees that 2-Naphthol factory effluent can qualified discharge or reuse;
The described souring tank 3 of step (2), step (3) described micro-electrolysis reaction, the described hydrolysis acidification pool 15 of step (7), the described fluid bed biological film reaction tank 16 of step (8), the described contact-oxidation pool 17 of step (9), the described BAF 22 of step (11) all carries out aeration by blower fan 26; The mud that efficient air-floating reactor 2, compound settling bowl 13 and second pond 18 produce enters sludge thickener 24, and the sludge reflux in sludge thickener 24 is to regulating cooling tank 14, hydrolysis acidification pool 15 fluid bed biological film reaction tank 16 and contact-oxidation pool 17; The described light electrolysis tower 6 of step (3) adopts iron carbon compounded mix; The concentration that step (4) described Fenton's reaction adds hydrogen peroxide is 30%, and dosage is account for influent waste water volume 5 ‰; During step (5) is described and coagulation reaction tank 12 to add PAC dosage be 1%, the PAM dosage accounting for influent waste water volume is account for influent waste water volume 1 ‰; The waste water quality that the described adjustment cooling tank 14 of step (6) carries out after cooling adjustment is COD<2000mg/L, specific conductivity <0.7ms/cm.
Embodiment 2
As shown in Figure 1-2, a kind of 2-Naphthol production wastewater treatment device, comprising: water collecting basin 1, efficient air-floating reactor 2, souring tank 3, light electrolysis tower 6, line mixer 8, Fenton reactor 7, in and coagulation reaction tank 12, compound settling bowl 13, regulate cooling tank 14, hydrolysis acidification pool 15, fluid bed biological film reaction tank 16, contact-oxidation pool 17, second pond 18, intermediate pool 19, fore filter 20, catalyzed oxidation tower 21, BAF 22, described water collecting basin 1 connects efficient air-floating reactor 2, described efficient air-floating reactor 2 connects souring tank 3, described souring tank 3 connects light electrolysis tower 6, described light electrolysis tower 6 is connected with Fenton reactor 7 by line mixer 8, with coagulation reaction tank 12 during described Fenton reactor 7 connects, compound settling bowl 13 is connected with coagulation reaction tank 12 in described, described compound settling bowl 13 connects adjustment cooling tank 14, described adjustment cooling tank 14 connects hydrolysis acidification pool 15, described hydrolysis acidification pool 15 connects fluid bed biological film reaction tank 16, fluid bed biological film reaction tank 16 connects contact-oxidation pool 17, described contact-oxidation pool 17 connects second pond 18, described second pond 18 connects intermediate pool 19, described intermediate pool 19 connects fore filter 20, described fore filter 20 connects catalyzed oxidation tower 21, described catalyzed oxidation tower 21 connects BAF 22, described BAF 22 connects cooling equalizing tank, the backflow water yield is regulated according to biochemical inflow requirement.
Efficient air-floating reactor 2 is connected with absorption tower 4 with souring tank 3 top, and described absorption tower 4 connects aiutage 5; Described Fenton reactor 7 connects hydrogen peroxide grug feeding jar 9; PAC grug feeding jar 10 and PAM grug feeding jar 11 is connected with coagulation reaction tank 12 in described; Described cooling equalizing tank connects circulating cooling tower 25; Described efficient air-floating reactor 2, compound settling bowl 13 are connected sludge thickener 24 with bottom second pond 18, and the mud of generation enters sludge thickener 24.Described sludge thickener 24 is also connected with adjustment cooling tank 14, hydrolysis acidification pool 15, fluid bed biological film reaction tank 16 and contact-oxidation pool 17, for regulating cooling tank 14, hydrolysis acidification pool 15, fluid bed biological film reaction tank 16 and contact-oxidation pool 17 to provide mud, supplement mud loss; Described catalyzed oxidation tower 21 connects ozonizer 23; Described souring tank 3, light electrolysis tower 6, hydrolysis acidification pool 15, fluid bed biological film reaction tank 16, contact-oxidation pool 17 and BAF 22 be connecting fan 26 all.
Embodiment 3
Certain factory's 2-Naphthol factory effluent, COD is 42620mg/L, pH is 5.61, flow 20m
3/ h, waste water B/C are 0.091.
(1) 2-Naphthol factory effluent enters efficient air-floating reactor 2 by water collecting basin 1 through pump lifting, removes the wet goods impurity of suspended substance, oil slick and the solubilised state in waste water, and the waste gas that air supporting reaction produces enters absorption tower 4 and passes through alkali liquor absorption;
(2) efficient air-floating reactor 2 water outlet enters souring tank 3, adds the sulphur acid for adjusting pH to 1.22 of 98%, and the inferior sulfate radical acidifying in 2-Naphthol factory effluent is changed into SO
2, adopt blower fan 26 aeration, promote the SO produced in waste water
2gas overflowing, the waste gas of generation enters absorption tower 4 and passes through alkali liquor absorption;
(3) 2-Naphthol factory effluent is removed after inferior sulfate radical through step (2) acidifying, and waste water ph is about 3.06, directly enters light electrolysis tower 6 and carries out micro-electrolysis reaction process;
(4) waste water ph after microelectrolysis processing is about 4.62, directly carries out Fenton's reaction, adds the hydrogen peroxide 0.1m that massfraction is 30%
3/ h and 9.2kg/h iron powder, carry out oxide treatment to the larger molecular organics in 2-Naphthol factory effluent further, and water outlet COD is that to be about 47.9%, B/C be 0.48 to 22180mg/L, COD clearance;
(5) during Fenton's reaction water outlet enters and coagulation reaction tank 12 carry out in and coagulating, regulating pH to 7.21 by adding CaO, adding flocculation agent PAC and measuring as 0.1m
3the amount of/h, coagulant aids PAM is 0.01m
3/ h removes the suspended substance in waste water, in and water outlet after coagulation enter compound settling bowl 13 and carry out sedimentation;
(6) waste water of compound settling bowl 13 water outlet and lower concentration enters and regulates cooling tank 14 to lower the temperature, and regulates waste water quality, and after regulating, waste water COD is 2360mg/L, and BAF 22 is back to and regulates cooling tank 14 water yield to be 60m
3/ h;
(7) cooling tank 14 water outlet is regulated to enter hydrolysis acidification pool 15, the non-solubility organism in waste water is changed into dissolved organic matter by the characteristic of microorganism, mainly the organism of wherein difficult for biological degradation is changed into the organism of readily biodegradable, improve the biodegradability of waste water, be beneficial to follow-up oxygen consumption process;
(8) after acidication, water outlet enters fluid bed biological film reaction tank 16, by thermopnore aerobe method process 2-Naphthol factory effluent, carries out advanced treatment by the respiration of aerobic microbiological to the organism in waste water;
(9) fluid bed biological film reaction tank 16 water outlet enters contact-oxidation pool 17, by thermopnore aerobe method process 2-Naphthol factory effluent, by the respiration of aerobic microbiological, advanced treatment is carried out to the organism in waste water, after process, water outlet COD is 196mg/L, it is 7.44 that COD clearance is about 91.7%, pH;
(10) contact-oxidation pool 17 water outlet enters second pond 18, second pond 18 supernatant liquor enters intermediate pool 19, intermediate pool 19 water outlet is removed suspended substance through fore filter 20 and is entered catalyzed oxidation tower 21, by catalytic ozonation reaction depth process 2-Naphthol factory effluent, water outlet COD is 112mg/L, pH value is that 7.6, COD clearance is about 42.9%;
(11) catalytic ozonation water outlet enters BAF 22, is further removed SS, COD in waste water by biomembrance process, and water outlet COD is 75mg/L, pH is 7.33, guarantees that 2-Naphthol factory effluent can qualified discharge or reuse.
To sum up, after treatment, water outlet COD75mg/L, COD clearance is about 99.8% to 2-Naphthol factory effluent, and pH value is 7.33, SS is 45mg/L, and waste water meets plant area's reuse water requirement.
Claims (8)
1. a 2-Naphthol production wastewater treatment method, is characterized in that, comprises the steps:
(1) 2-Naphthol factory effluent enters efficient air-floating reactor by water collecting basin through pump lifting, removes the wet goods impurity of suspended substance, oil slick and the solubilised state in waste water, and the waste gas that air supporting reaction produces enters absorption tower and passes through alkali liquor absorption;
(2) water outlet of efficient air-floating reactor enters souring tank, adds acid for adjusting pH to 1, and the inferior sulfate radical acidifying in 2-Naphthol factory effluent is changed into SO
2, adopt blower fan aeration, promote the SO produced in waste water
2gas overflowing, the waste gas of generation enters absorption tower and passes through alkali liquor absorption;
(3) 2-Naphthol factory effluent is removed after inferior sulfate radical through step (2) acidifying, waste water ph is about 3, water outlet directly enters light electrolysis tower carry out micro-electrolysis reaction process without the need to regulating, the hydroxyl radical free radical of strong oxidizing property is produced by electrochemical reaction, the larger molecular organics of 2-Naphthol factory effluent is oxidized to small organic molecule, improves the biodegradability of waste water;
(4) waste water ph after microelectrolysis processing is about 4.5, directly carries out Fenton's reaction, adds hydrogen peroxide and iron powder, carries out oxide treatment further to the larger molecular organics in 2-Naphthol factory effluent;
(5) Fenton's reaction water outlet enter in and coagulation reaction tank carry out in and coagulating, pH to 6-8 is regulated by adding CaO, add flocculation agent PAC, coagulant aids PAM removes the suspended substance in waste water, in and water outlet after coagulation enter compound settling bowl and carry out sedimentation;
(6) waste water of the water outlet of compound settling bowl and lower concentration enters and regulates cooling tank to lower the temperature, and is partly refluxed to adjustment cooling tank adjustment waste water quality by effluent of aeration biological filter, carries out biochemical condition to meet waste water;
(7) cooling tank water outlet is regulated to enter hydrolysis acidification pool, the non-solubility organism in waste water is changed into dissolved organic matter by the characteristic of microorganism, mainly the organism of wherein difficult for biological degradation is changed into the organism of readily biodegradable, improve the biodegradability of waste water, be beneficial to follow-up oxygen consumption process;
(8) after acidication, water outlet enters fluid bed biological film reaction tank, by thermopnore aerobe method process 2-Naphthol factory effluent, carries out advanced treatment by the respiration of aerobic microbiological to the organism in waste water;
(9) water outlet of fluid bed biological film reaction tank enters contact-oxidation pool, by thermopnore aerobe method process 2-Naphthol factory effluent, carries out advanced treatment by the respiration of aerobic microbiological to the organism in waste water;
(10) contact-oxidation pool water outlet enters second pond, and second pond supernatant liquor enters intermediate pool, and intermediate pool water outlet is removed suspended substance through fore filter and entered catalyzed oxidation tower, by catalytic ozonation reaction depth process 2-Naphthol factory effluent;
(11) catalytic ozonation water outlet enters BAF, is further removed SS, COD in waste water by biomembrance process, guarantees that 2-Naphthol factory effluent can qualified discharge or reuse.
2. a kind of 2-Naphthol production wastewater treatment method according to claim 1, it is characterized in that, step (2) described souring tank, step (3) described micro-electrolysis reaction, step (7) described hydrolysis acidification pool, the described fluid bed biological film reaction tank of step (8), step (9) described contact-oxidation pool, step (11) described BAF all carries out aeration by blower fan.
3. a kind of 2-Naphthol production wastewater treatment method according to claim 1, it is characterized in that, the mud that efficient air-floating reactor, compound settling bowl and second pond produce enters sludge thickener, and the sludge reflux in sludge thickener is to regulating cooling tank, hydrolysis acidification pool fluid bed biological film reaction tank and contact-oxidation pool.
4. a kind of 2-Naphthol production wastewater treatment method according to claim 1, is characterized in that, the described light electrolysis tower of step (3) adopts iron carbon compounded mix.
5. a kind of 2-Naphthol production wastewater treatment method according to claim 1, is characterized in that, the concentration that step (4) described Fenton's reaction adds hydrogen peroxide is 30%, and dosage is account for influent waste water volume 5 ‰.
6. a kind of 2-Naphthol production wastewater treatment method according to claim 1, is characterized in that, during step (5) is described and coagulation reaction tank to add PAC dosage be 1%, the PAM dosage accounting for influent waste water volume is account for influent waste water volume 1 ‰.
7. a kind of 2-Naphthol production wastewater treatment method according to claim 1, it is characterized in that, the waste water quality that the described adjustment cooling tank of step (6) carries out after cooling adjustment is COD<2000mg/L, specific conductivity <0.7ms/cm.
8. a 2-Naphthol production wastewater treatment device, it is characterized in that, comprising: water collecting basin, efficient air-floating reactor, souring tank, light electrolysis tower, line mixer, Fenton reactor, in and coagulation reaction tank, compound settling bowl, regulate cooling tank, hydrolysis acidification pool, fluid bed biological film reaction tank, contact-oxidation pool, second pond, intermediate pool, fore filter, catalyzed oxidation tower, BAF, described water collecting basin connects efficient air-floating reactor, described efficient air-floating reactor connects souring tank, described souring tank connects light electrolysis tower, described light electrolysis tower is connected with Fenton reactor by line mixer, during described Fenton reactor connects and coagulation reaction tank, compound settling bowl is connected with coagulation reaction tank in described, described compound settling bowl connects adjustment cooling tank, described adjustment cooling tank connects hydrolysis acidification pool, described hydrolysis acidification pool connects fluid bed biological film reaction tank, fluid bed biological film reaction tank connects contact-oxidation pool, described contact-oxidation pool connects second pond, described second pond connects intermediate pool, described intermediate pool connects fore filter, described fore filter connects catalyzed oxidation tower, described catalyzed oxidation tower connects BAF, described BAF connects cooling equalizing tank,
Described efficient air-floating reactor is connected with absorption tower with souring tank top, and described absorption tower connects aiutage;
Described Fenton reactor connects hydrogen peroxide grug feeding jar;
PAC grug feeding jar and PAM grug feeding jar is connected with coagulation reaction tank in described;
Described cooling equalizing tank connects circulating cooling tower;
Described efficient air-floating reactor, compound settling bowl are connected sludge thickener with bottom second pond, and described sludge thickener is also connected with adjustment cooling tank, hydrolysis acidification pool, fluid bed biological film reaction tank and contact-oxidation pool;
Described catalyzed oxidation tower connects ozonizer;
Described souring tank, light electrolysis tower, hydrolysis acidification pool, fluid bed biological film reaction tank, contact-oxidation pool and the equal connecting fan of BAF.
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