CN110357357A - A kind of high concentration nonionic surfactant wastewater treatment equipment and method - Google Patents
A kind of high concentration nonionic surfactant wastewater treatment equipment and method Download PDFInfo
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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
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
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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
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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
- C02F1/24—Treatment of water, waste water, or sewage by flotation
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- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
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- 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
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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- 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
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- 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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- 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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- 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
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
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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
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
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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
- C02F3/30—Aerobic and anaerobic processes
Abstract
The present invention relates to surface active agent wastewater process field, especially a kind of high concentration nonionic surfactant wastewater treatment equipment and method.The present invention can effectively remove the nonionic surfactant in waste water, while COD is also greatly reduced by using materializations group technologies such as coagulation chemical precipitation+air-dissolving air-float+three-level light electrolysis+Fenton oxidations, reach the water inlet requirement of biochemistry pool;Subsequent UASB anaerobic mud bed reactor+hydrolysis acidification+aerobic contact oxidation group technology, COD in water body significantly reduce, and reach country and local water quality discharge standard.
Description
Technical field
The present invention relates to surface active agent wastewater process field, especially a kind of high concentration nonionic surfactant waste water
Processing unit and method.
Background technique
Surfactant surface-active with higher can reduce solvent surface tension and transformation solution inner part subgroup
The characteristics such as conjunction are therefore widely used in industrial production so that properties of product and production technology are improved.Wherein, non-
Ionic surface active agent is widely used in the industries such as weaving, papermaking, food, cosmetics, but alkyl phenol in the market simultaneously
The nonionic surfactants such as polyoxyethylene ether, fatty alcohol polyoxyethylene ether and fatty acid methyl ester APEO belong to biology
Hard-degraded substance will cause water surface blistering into water body, and water body self-purification ability reduces, and then water quality is made to degenerate.Therefore to it is non-from
The processing of sub- surfactant increasingly attracts people's attention.
Treating Waste Water Containing Surfactants mainly have micro electrolysis tech, biological oxidation processing technique, coagulating sedimentation at present
Technology, foam separating technology.Adsorption treatment technology etc..But the effect is unsatisfactory for single process, some technique is also deposited
In the problem of subsequent processing difficulty.Chinese patent application CN1644536A passes through at mesh screen coarse filtration-membrane microfiltration-film nanofiltration three-level
Reason reaches water purification purpose, and the process contamination is few, treatment process is without adding medicament, easy to operate;But micro-filtration & nano-filtration unit is all
Pressure pump is needed to provide power, the anti-seepage effect of mechanical performance and equipment to film is more demanding, involves great expense.Chinese patent Shen
Please CN104386852A be directed to concentrated surfactant waste water, at acidolysis-extraction-coagulating sedimentation group technology
Reason, COD removal rate can reach 90% or more;But the acidolysis stage needs for pH to be reduced to 1 or so, and dosage is more, is not suitable for
Large-scale application, and extractant used in extraction stages is chloroform, the light-exposed easy decomposition of chloroform has toxicity and carcinogenicity, behaviour
It is not convenient to make storage, may cause secondary pollution.Chinese patent application CN107935236A is adsorbed by adsorbent material, foam is floating
Surfactant in choosing removal waste water;But the amido modified SiO in adsorbent material particle2、TiO2Or organic resin, system
Standby mode is more complex, not cheap and easy to get, and how the material after absorption handles and do not explain, may cause secondary pollution.
Therefore, for the wastewater containing non-ion surfactants of high concentration, study a kind of high treating effect, it is low in cost,
The stable technique of secondary pollution, operational effect will not be generated, becomes the field of waste water treatment and urgently solves the problems, such as.
Summary of the invention
The object of the present invention is to provide a kind of high concentration nonionic surfactant wastewater treatment equipment and methods, can fill out
The blank for mending the field of waste water treatment reaches environmental protection, economy, safely and steadly handles high concentration nonionic surfactant
Purpose.
The technique combines work by using materializations such as coagulation chemical precipitation+air-dissolving air-float+three-level light electrolysis+Fenton oxidations
Skill can effectively remove the nonionic surfactant in waste water, while COD is also greatly reduced, and has reached the water inlet of biochemistry pool
It is required that;Subsequent UASB anaerobic mud bed reactor+hydrolysis acidification+aerobic contact oxidation group technology, COD in water body significantly drop
It is low, reach country and local water quality discharge standard.
The present invention provides a kind of high concentration nonionic surfactant wastewater treatment equipment, including the adjusting being sequentially communicated
Pond, dosing pond, chemical precipitation pond, air bearing reaction tank, discharge bay, three-level micro cell, Fenton reaction tank, neutralization pond, upstream
It the pond formula anaerobic mud bed reactor UASB, hydrolysis acidification pool, contact-oxidation pool, biochemical sedimentation basin, clear water reserviors and is sequentially connected
Sludge concentration tank and dehydration machine room;The wherein entrance of sludge concentration tank and chemical precipitation pond, neutralization pond and biochemical sedimentation basin
Mud discharging mouth is connected, and biochemical sedimentation basin is connected by sludge return pipe with the pond UASB, hydrolysis acidification pool;Air bearing reaction tank and go out
Pond is successively connected with the water outlet of dissolving and water inlet, three pond circulation connections;It is equipped at the top of air bearing reaction tank useless
Liquid collecting tank;Dissolving is also connect with air compressor machine.
Process flow chart of the invention is as shown in Figure 1, specifically follow these steps to carry out:
(1) water and water quality adjustment are carried out to the waste water containing nonionic surfactant for entering conditioning tank, water outlet enters
Dosing pond;
(2) in dosing pond, dosing coagulant and quick lime, water body and drug stirring are equal under the action of blender in pond
It is even, coagulating is carried out, is then pumped into chemical precipitation pond;
(3) in chemical precipitation pond, after precipitating, sediment is separated with supernatant realization.
(4) in air bearing reaction tank, air compressor machine aeration is sufficiently mixed in dissolving with the water outlet of part discharge bay, after mixing
Air-water mixture from reaction bottom of pond portion release, so that flocs float in water body is formed dross.Bubble trap is floating by what is kept afloat
Slag drains in time, collects and recycles;
(5) water outlet positioned at the lower half position of air bearing reaction tank is connected with discharge bay, the water after air bearing is reacted
Body enters in discharge bay;
(6) water outlet a part of discharge bay and air compressor machine aeration mix, and another part was followed by adding iron carbon filler
The first, second, third micro cell;
(7) sulphur acid for adjusting pH is added in the first, second, third micro cell, the sufficiently rear water body of micro-electrolysis reaction enters
Fenton reaction tank;
(8) pH value that sulfuric acid adjusts water inlet is added in Fenton reaction tank, adds H2O2Solution carries out Fenton oxidation
Reaction, the water body after Fenton reaction enter neutralization pond;
(9) it in neutralization pond, adds after sodium hydroxide solution adjusts pH and is pumped into the pond UASB;
(10) water outlet is sent by pumping to the anaerobic mud bed area of UASB reactor bottom in neutralization pond, organic in waste water
Object is decomposed by anaerobe, and subsequent water body enters hydrolysis acidification pool;
(11) in hydrolysis acidification pool, macromolecular, organic matter degradation difficult to degrade in waste water are by hydrolytic bacteria and acid-producing bacteria
Small organic molecule, and improve the biodegradability of waste water, it creates favorable conditions for subsequent processing;
(12) water body after Anaerobic Treatment enters in aerobic contact oxidation pond, opens underwater aerating system, passes through throwing
Sulfuric acid or sodium hydroxide solution is added to adjust pH, addition nutritive salt makes the microorganism mass propagation on filler, and water body is purified;
(13) water outlet of aerobic tank carries out mud-water separation in biochemical sedimentation basin, and supernatant enters clear water reserviors qualified discharge,
High activity sludge a part in precipitating flows back into the pond UASB and hydrolysis acidification pool, and it is dense that another part excess sludge enters sludge
In contracting pond.
(14) sludge in chemical precipitation pond, neutralization pond and biochemical sedimentation basin is pumped by sludge pump into sludge concentration tank,
The moisture content of sludge by sludge pump is delivered to dehydration machine room after being reduced.
(15) sludge generates mud cake after the dehydration of frame dehydration machine in dehydration machine room, transports outward.
Conditioning tank stirs water body by water pump endless form come regulating water quality in above-mentioned steps (1), controls to adjust pond water outlet
Flow is 10~20m3/ d, COD concentration are no more than 300000mg/L, and nonionic surfactant is alkyl phenol polyoxyethylene ether,
Mass concentration is no more than 1%.
Coagulant is bodied ferric sulfate PFS and polyacrylamide PAM, drug order of adding are as follows: first throw in above-mentioned steps (2)
Add the PFS of 30~60kg/ kiloton water, adding CaO control pH later is 8.0~10.0, finally adds PAM, dosage is 5~
20kg/ kiloton water.
The chemical precipitation pond residence time is 8.0~12.0h in above-mentioned steps (3).
Pressure is 0.2~0.5MPa in dissolving in above-mentioned steps (4), and the residence time is 2~5min, air bearing reaction in tank
The residence time in pond is 1~3h, gas-liquid volume ratio 5:1.
The foam of the water surface is drained and is collected in waste collection tank by bubble trap in above-mentioned steps (4), is carried out to its purity
It examines, concentration can directly recycle use higher than 10g/L's, otherwise be back in conditioning tank.
Addition sulfuric acid solution adjusts pH to 3.0~4.0 in above-mentioned steps (7), in iron carbon filler Fe/C mass ratio be 1:3~
1:5, dosage be 1.0t/ tons of water, the residence time of the first, second, third micro cell be respectively 30min, 60min,
30min。
Addition sulfuric acid solution adjusts pH to 2.0~4.0 in above-mentioned steps (8), and hydrogen peroxide mass fraction used is 20%~
35%, dosage is mass ratio COD:H2O2=1:1~2:1, reaction time are 0.3~1.5h.
Concentration of sodium hydroxide solution is 20%~25% in above-mentioned steps (9), and adjusting pH is 7.
The upflow velocity of above-mentioned steps (10) UASB anaerobic reactor is 0.5~3.0m/h, is conducive to micro- life in sludge
Object comes into full contact with useless Organic substance in water, improves removal rate.
The nutritive salt added in contact-oxidation pool in above-mentioned steps (12) is glucose, urea and/or dipotassium hydrogen phosphate, is made
The BOD that dosage is surveyed according to water body5, ammonia nitrogen and total phosphorus value according to mass ratio BOD5: N:P=100:5:1 is calculated, control water inlet
Temperature is 20~35 DEG C, pH is 6.5~8.5, and the residence time is 4~8h.
High activity sludge concentration is 8000~12000mg/L in above-mentioned steps (13).
In above-mentioned steps (15) sludge cake moisture content be 40%, can agricultural, building materials utilize or be used for thermal power generation,
Realize the purpose of energy-saving and environmental protection.
The present invention has the advantages that
(1) coagulation chemical precipitation+air-dissolving air-float+three-level light electrolysis+Fenton oxidation materialization group technology and UASB are used
Anaerobic mud bed reactor+hydrolysis acidification+aerobic contact oxidation biochemistry combination process, not only nonionic surfactant is had
The removal of effect, COD index also have decreased to national emission standard.
(2) the sequence energy that coagulating sedimentation uses and first adds PFS, adds organic flocculant PAM with CaO adjusting pH, finally again
Significantly reduce surfactant concentration.
(3) different pH, residence time, filler Fe/C is selected to carry out three-level light electrolysis respectively, than simple level-one light electrolysis
Effect is more preferable on removal COD, the Fe that light electrolysis generates2+It can directly utilize, reduce in subsequent Fenton reaction
FeSO4The expense of drug.
(4) waste water after this process, not having to can be with direct emission through subsequent processing, and operational effect is good, treatment scale
Greatly, there is practical reference value.
Specific embodiment
It is the process of a kind of processing high concentration nonionic surfactant waste water system of the present invention and technique as shown in Figure 1
Figure.
The nonionic surfactant waste water COD measured value of certain factory is 250000mg/L, and alkyl phenol polyoxyethylene ether is dense
Degree is 1%, pH 5.6, is handled according to the following steps:
Water body is stirred by water pump endless form to the waste water containing alkyl phenol polyoxyethylene ether for entering conditioning tank first
Carry out regulating water quality, control and regulation pond COD concentration is 230000mg/L, water flow 15m3/ d, nonionic surfactant are dense
Degree is 0.9%.In dosing pond, 45kg/ kiloton water PFS is first added, adding CaO control pH later is 9.0, is finally added
PAM12kg/ kiloton water.In chemical precipitation pond, coagulating sedimentation 10h is carried out.The complete water body of coagulating sedimentation enters air bearing reaction tank
In, the residence time in pond is 2h, gas-liquid volume ratio 5:1;Pressure is 0.4MPa in auxiliary device dissolving, and forced air exists
The residence time is 4min in tank,;During air bearing, bubble trap drains the foam kept afloat in time, examines its alkyl phenol poly-
Ethylene oxide ether concentration recycles it after being 15.8g/L.Water outlet and discharge bay phase positioned at the lower half position of air bearing reaction tank
Even, the water body after air bearing is reacted enters in discharge bay.Water outlet a part of discharge bay is mixed with air compressor machine aeration, another portion
Divide followed by the first, second, third micro cell for adding iron carbon filler.The water outlet of discharge bay enters three-level micro cell
Afterwards, addition sulfuric acid solution adjusts pH to 3.5, and iron carbon filler Fe/C mass ratio used is 1:3, and dosage is 1.0t/ tons of water, the
One, the residence time of second, third micro cell is respectively 30min, 60min, 30min.It adds sulfuric acid solution and adjusts light electrolysis
For the pH value of pond water outlet to 3.0, measuring COD value is 31000mg/L, adds 88.6kg/ tons of water of 35% hydrogen peroxide solution of mass fraction,
Carry out Fenton oxidation reaction, reaction time 0.75h.To the waste water after Fenton reaction, the hydrogen-oxygen that concentration is 20% is added
Change after sodium solution adjusts pH to 7 and enters the pond UASB.It is discharged in neutralization pond and send the anaerobism to UASB reactor bottom dirty by pumping
The area Ni Chuan, control upflow velocity are 0.7m/h, and the microorganism be conducive in sludge comes into full contact with useless Organic substance in water, are improved useless
For organic matter in water by anaerobe decomposition efficiency, subsequent water body enters hydrolysis acidification pool.In hydrolysis acidification pool, hydrolytic bacteria and
Macromolecular, organic matter degradation difficult to degrade in waste water are small organic molecule by acid-producing bacteria, and improve the biodegradability of waste water, are
Subsequent processing creates favorable conditions.Then in aerobic contact oxidation pond, underwater aerating system is opened, measures BOD in water5For
200mg/L, ammonia nitrogen amount are 100mg/L, total phosphorus 17mg/L, add glucose and potassium dihydrogen phosphate 5kg/ tons of water and 6.7g/ respectively
Ton water, control inflow temperature is 25 DEG C, pH 7, makes the microorganism mass propagation on filler, water body is purified after stopping 6h.
The water outlet of aerobic tank carries out mud-water separation in biochemical sedimentation basin, and supernatant enters in clear water reserviors, and COD is 85mg/ in clear water reserviors
L, can be with qualified discharge.
A part of concentration is 9000mg/L high activity sludge reflux into the pond UASB and hydrolysis acidification pool in sedimentation basin, another
Some residual sludge enters in sludge concentration tank.Sludge in chemical precipitation pond, neutralization pond and biochemical sedimentation basin is dense by sludge
The mud cake that moisture content is 40% is generated behind contracting pond, after dehydration, can agricultural, building materials utilize or for thermal power generation, realizes and save
Energy, environmentally friendly purpose.
This example is the description of the invention, is not limitation of the invention, the side after any pair of simple transformation of the present invention
Case all belongs to the scope of protection of the present invention.
Claims (10)
1. a kind of high concentration nonionic surfactant wastewater treatment equipment, which is characterized in that described device includes being sequentially communicated
Conditioning tank, dosing pond, chemical precipitation pond, air bearing reaction tank, discharge bay, three-level micro cell, Fenton reaction tank, neutralize
Pond, the pond upflow anaerobic sludge blanket reactor UASB, hydrolysis acidification pool, contact-oxidation pool, biochemical sedimentation basin, clear water reserviors and according to
Secondary connected sludge concentration tank and dehydration machine room;Wherein the entrance of sludge concentration tank and chemical precipitation pond, neutralization pond and biochemistry are heavy
The mud discharging mouth in shallow lake pond is connected, and biochemical sedimentation basin is connected by sludge return pipe with the pond UASB, hydrolysis acidification pool;Air bearing reaction
Pond and discharge bay are successively connected with the water outlet of dissolving and water inlet, three pond circulation connections;Peace at the top of air bearing reaction tank
Equipped with waste collection tank;Dissolving is also connect with air compressor machine.
2. implementing the method for high concentration nonionic surfactant wastewater treatment using device as claimed in claim, feature exists
In, the specific steps are as follows:
(1) water and water quality adjustment are carried out to the waste water containing nonionic surfactant for entering conditioning tank, water outlet enters dosing
Pond;
(2) in dosing pond, dosing coagulant and quick lime, water body is stirred evenly with drug under the action of blender in pond,
Coagulating is carried out, is then pumped into chemical precipitation pond;
(3) in chemical precipitation pond, after precipitating, sediment is separated with supernatant realization;
(4) in air bearing reaction tank, air compressor machine aeration is sufficiently mixed in dissolving with the water outlet of part discharge bay, mixed gas
Aqueous mixtures make the flocs float in water body form dross from reaction bottom of pond portion release;Bubble trap by the dross kept afloat and
When drain, collect and recycle;
(5) be connected positioned at the water outlet of lower half position of air bearing reaction tank with discharge bay, the water body after air bearing is reacted into
Enter in discharge bay;
(6) water outlet a part of discharge bay and air compressor machine aeration mix, and another part was followed by adding the of iron carbon filler
One, second, third micro cell;
(7) sulphur acid for adjusting pH is added in the first, second, third micro cell, the sufficiently rear water body of micro-electrolysis reaction enters
Fenton reaction tank;
(8) pH value that sulfuric acid adjusts water inlet is added in Fenton reaction tank, adds H2O2Solution carries out Fenton oxidation reaction,
Water body after Fenton reaction enters neutralization pond;
(9) it in neutralization pond, adds after sodium hydroxide solution adjusts pH and is pumped into the pond UASB;
(10) water outlet is sent by pumping to the anaerobic mud bed area of UASB reactor bottom in neutralization pond, the organic matter quilt in waste water
Anaerobe is decomposed, and subsequent water body enters hydrolysis acidification pool;
(11) in hydrolysis acidification pool, macromolecular, organic matter degradation difficult to degrade in waste water are small point by hydrolytic bacteria and acid-producing bacteria
Sub- organic matter, and improve the biodegradability of waste water, it creates favorable conditions for subsequent processing;
(12) water body after Anaerobic Treatment enters in aerobic contact oxidation pond, underwater aerating system is opened, by adding sulphur
Acid or sodium hydroxide solution adjust pH, and addition nutritive salt makes the microorganism mass propagation on filler, and water body is purified;
(13) water outlet of aerobic tank carries out mud-water separation in biochemical sedimentation basin, and supernatant enters clear water reserviors qualified discharge, precipitating
In high activity sludge a part flow back into the pond UASB and hydrolysis acidification pool, another part excess sludge enters sludge concentration tank
In;
(14) sludge in chemical precipitation pond, neutralization pond and biochemical sedimentation basin is pumped by sludge pump into sludge concentration tank, sludge
Moisture content be reduced after dehydration machine room is delivered to by sludge pump;
(15) sludge generates mud cake after the dehydration of frame dehydration machine in dehydration machine room, transports outward.
3. the method as described in claim 1, which is characterized in that in step (1), conditioning tank stirs water by water pump endless form
Body carrys out regulating water quality, and control and regulation pond water flow is 10~20m3/ d, COD concentration are no more than 300000mg/L, nonionic table
Face activating agent is alkyl phenol polyoxyethylene ether, and mass concentration is no more than 1%;In step (2), coagulant is bodied ferric sulfate PFS
With polyacrylamide PAM, drug order of adding are as follows: first add the PFS of 30~60kg/ kiloton water, adding CaO control pH later is
8.0~10.0, PAM is finally added, dosage is 5~20kg/ kiloton water.
4. the method as described in claim 1, which is characterized in that in step (3) the chemical precipitation pond residence time be 8.0~
12.0h。
5. the method as described in claim 1, which is characterized in that in step (4), pressure is 0.2~0.5MPa, tank in dissolving
The interior residence time is 2~5min, and the residence time of air bearing reaction tank is 1~3h, gas-liquid volume ratio 5:1;In step (4), remove
The foam of the water surface is drained and is collected in waste collection tank by bubbler, is tested to its purity, and concentration can be with higher than 10g/L's
Directly recycling uses, and is otherwise back in conditioning tank.
6. the method as described in claim 1, which is characterized in that in step (7), addition sulfuric acid solution adjusting pH to 3.0~
4.0, Fe/C mass ratio is 1:3~1:5 in iron carbon filler, and dosage is 1.0t/ tons of water, in the first, second, third micro cell
Residence time is respectively 30min, 60min, 30min;In step (8), addition sulfuric acid solution adjusts pH to 2.0~4.0, used double
Oxygen water quality score is 20%~35%, and dosage is mass ratio COD:H2O2=1:1~2:1, reaction time are 0.3~1.5h.
7. the method as described in claim 1, which is characterized in that in step (9), concentration of sodium hydroxide solution be 20%~
25%, adjusting pH is 7;In step (10), the upflow velocity of UASB anaerobic reactor is 0.5~3.0m/h, is conducive in sludge
Microorganism come into full contact with useless Organic substance in water, improve removal rate.
8. the method as described in claim 1, which is characterized in that in step (12), the nutritive salt added in contact-oxidation pool is
Glucose, urea and/or dipotassium hydrogen phosphate, the BOD that usage amount is surveyed according to water body5, ammonia nitrogen and total phosphorus value according to mass ratio
BOD5: N:P=100:5:1 is calculated, and control inflow temperature is 20~35 DEG C, pH is 6.5~8.5, and the residence time is 4~8h.
9. the method as described in claim 1, which is characterized in that in step (13), high activity sludge concentration be 8000~
12000mg/L。
10. the method as described in claim 1, which is characterized in that sludge cake moisture content is 40% in step (15), can be with agriculture
It is utilized with, building materials or for thermal power generation, realizes the purpose of energy-saving and environmental protection.
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Cited By (3)
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CN110902963A (en) * | 2019-12-10 | 2020-03-24 | 九江天赐高新材料有限公司 | Treatment method of alkali-soluble polymer-containing wastewater |
CN111470716A (en) * | 2020-04-15 | 2020-07-31 | 河南恒安环保科技有限公司 | Pretreatment method for high-salt high-ammonia nitrogen wastewater in rebamipide production |
CN111620485A (en) * | 2020-06-17 | 2020-09-04 | 河北铭万精细化工有限公司 | Wastewater recycling process |
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