CN105923869A - Pretreatment method for chemical industry wastewater - Google Patents
Pretreatment method for chemical industry wastewater Download PDFInfo
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- CN105923869A CN105923869A CN201610294582.8A CN201610294582A CN105923869A CN 105923869 A CN105923869 A CN 105923869A CN 201610294582 A CN201610294582 A CN 201610294582A CN 105923869 A CN105923869 A CN 105923869A
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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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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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
- C02F1/46—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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- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
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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
- C02F1/52—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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- 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
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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
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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)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention relates to a pretreatment method for chemical industry wastewater with high salt, high ammonia nitrogen, high organic solvent and high toxicity. According to the technical scheme, the chemical industry wastewater is subjected to coagulating reaction sedimentation treatment, microelectrolysis reaction treatment, Fenton reaction treatment and MVR evaporation treatment in sequence. By means of the pretreatment method, the content of fine suspended matter and low-boiling-point organic matter in the chemical industry wastewater can be effectively reduced, the phenomenon that foam is formed in the operation process of an MVR evaporator is reduced, and thus normal operation of the MVR evaporator is guaranteed; as the chemical industry wastewater is subjected to microelectrolysis reaction treatment and Fenton reaction treatment, organic nitrogen can be converted into ammonia nitrogen before the chemical industry wastewater is subjected to MVR evaporation treatment, the existing form of nitrogen in the wastewater is controlled, most ammonia nitrogen is crystallized out of the system in the form of ammonium chloride, and thus the ammonia nitrogen load in subsequent condensate biochemical treatment is reduced. Compared with a conventional treatment process, the pretreatment method has an unexpected treatment effect on the chemical industry wastewater, and the operation stability of the whole system is guaranteed.
Description
Technical field
The invention belongs to chemical wastewater treatment field, be specifically related to a kind of high salt, high ammonia nitrogen, high organic
Solvent, high toxicity wastewater from chemical industry preprocess method.
Background technology
Conventional to " high salt, high ammonia nitrogen, high organic solvent, high toxicity " class wastewater from chemical industry, first
It is evaporated desalination, except organic solvent, further according to feature increase " light electrolysis or the sweet smell of the condensed water discharged
Oxidation " etc. processing unit, concrete technology flow process is: wastewater from chemical industry-evaporimeter-micro-electrolysis reactor-
Fenton reactor-coagulating sedimentation reaction-supernatant biochemical treatment.Wherein evaporimeter is used for removing wastewater from chemical industry
In salt and part organic solvent, described micro-electrolysis reactor-Fenton reactor is used for steaming of degrading
Sending out the organic matter in the condensed water that device is discharged, described coagulating precipitation is used for removing the suspension in water,
Conventional flowsheet often occurs following problem to cause the system cannot be properly functioning in actual moving process:
1, wastewater from chemical industry complicated component, the low boiling point organic solvent containing Various Complex, in evaporation process
Bubble-related issues are serious, have a strong impact on the properly functioning of evaporimeter；
2, such wastewater from chemical industry is after steamer desalination, and condensed water is again through light electrolysis, Fenton's reaction
After the processing units such as device, coagulating precipitation, the total salt quantity in waste water can increase, and increments is general and throws
Chemical feeding quantity is relevant, and the total salt quantity increased in waste water in actual motion can process generation to subsequent biochemical and press down
System；
3, in the condensed water that waste water is discharged after evaporimeter processes, low boiling organic components is complicated, organic nitrogen
Content is high, then after the processing units such as light electrolysis, Fenton reactor, coagulating precipitation, in waste water
Ammonia nitrogen and the content of total nitrogen can increase, increase subsequent biochemical system loading.
Summary of the invention
In order to solve above-mentioned technical problem, the present invention provide a kind of high salt, high ammonia nitrogen, high organic solvent,
High toxicity wastewater from chemical industry preprocess method.
In order to realize the purpose of the present invention, present invention employs techniques below scheme:
A kind of wastewater from chemical industry preprocess method, described wastewater from chemical industry sequentially pass through coagulating precipitation process,
Micro-electrolysis reaction processes, Fenton's reaction processes, MVR evaporation process.
Optimal technical scheme, described coagulating precipitation process uses PAC as coagulant, PAM conduct
Flocculation aid, described PAC dosage is 98-102mg/L, and described PAM dosage is 9-11mg/L, institute
The pH value stating coagulating precipitation is controlled at 6-9 by sulfuric acid regulation.
Further technical scheme, described micro-electrolysis reaction processes and uses up-flow contact reactor, described liter
Stream contact reactor is bucket body structure, set gradually from bottom to top in described staving water distributing area, reaction zone,
Disengagement zone, the bucket wall at place, described water distributing area is provided with water inlet, compressed air inlet, described reaction zone
Inside be filled with micro-electrolysis stuffing, described wastewater from chemical industry by water distributing area even in reaction zone again by Disengagement zone
Separate, 1.2-1.4 times of a diameter of described reaction zone diameter in described Disengagement zone；At described micro-electrolysis reaction
During reason, control ph is at 2.8-3.2.
Further technical scheme, H in described Fenton's reaction processing procedure2O2Dosage 9-10g/L, FeSO4
Dosage 180-220g/L, PAM dosage is 4-6mg/L, and is existed by sulfuric acid regulation control ph
2.8-3.2。
Further technical scheme, during described MVR evaporation process, control ph is at 5-6.
The beneficial effects of the present invention is:
(1) coagulating precipitation process of the present invention is for removing the suspension in described wastewater from chemical industry
Thing, the light electrolysis that this processing procedure can be prevented effectively from the suspended particle clogging subsequent technique in wastewater from chemical industry is anti-
Answer device, the consumption of follow-up Fenton's reaction medicament can be reduced simultaneously；Described micro-electrolysis reaction processes, sweet smell
Reaction treatment of pausing can make the organic matter of the difficult degradation in described wastewater from chemical industry be degraded, and makes described chemical industry
A large amount of oxidized decomposition of low-boiling-point organic compound in waste water, the stable operation for follow-up MVR evaporation process is created
Condition, it is to avoid bubble in evaporation process；MVR evaporation process of the present invention can be by described wastewater from chemical industry
Sodium salt, sylvite, the salt such as ammonium salt remove, this operation is last one work before condensate liquid biochemical treatment
Sequence, it can be ensured that enter the total salt quantity of subsequent condensation liquid biochemical treatment system, chloride ion content in control range
In.
The present invention processes the fine suspension that technique is effectively reduced in wastewater from chemical industry, low boiling organic matter contains
Amount, effectively reduces MVR evaporimeter and occurs the phenomenon of foam in running, so that it is guaranteed that MVR evaporation
Device is properly functioning；Described wastewater from chemical industry processes through micro-electrolysis reaction, Fenton's reaction processes and can enter MVR
Before evaporimeter, organic nitrogen is converted into ammonia nitrogen, controls nitrogen form present in the waste water, most ammonia-nitrogen with
The form of ammonium chloride crystallizes out system, thus ammonia nitrogen loading when reducing subsequent condensation liquid biochemical treatment.
In processing method of the present invention, the sequencing of each processing step is the most constantly to grope and summary obtains
, compare the conventional treatment process present invention and the result of wastewater from chemical industry is had unexpected process effect
Really, the stability of the operation of whole system have also been obtained guarantee, and the maintenance times of relevant device greatly reduces,
Pharmacy response addition is substantially reduced, evaporate required thermal source demand is substantially reduced.
(2) medicament PAC, PAM of adding during coagulating precipitation process of the present invention and throwing
The selection of dosage, the control of pH value in reaction, common effect makes suspended substance removal in described wastewater from chemical industry
Rate is more than 80%, and CODcr clearance is more than 30%.
(3) micro-electrolysis reaction of the present invention processes up-flow contact reactor used so that wastewater from chemical industry
Entered by bottom up-flow contact reactor, discharge from upper end, This structure increases wastewater from chemical industry and reaction zone
The time of contact of interior micro-electrolysis stuffing and reaction time.Can be to useless by described compressed air inlet
Water ventilated and increases water oxygen level, being beneficial to follow-up Fenton's reaction is processed the Fe in water outlet2+It is oxidized to
Fe3+, increase the sedimentation effect that Fenton water outlet is follow-up.The a diameter of described reaction zone diameter in described Disengagement zone
1.2-1.4 times, the rate of climb that this structure makes autoreaction district ascend into the waste water in Disengagement zone is dropped
Low, so it is beneficial to the decline of micro-electrolysis stuffing carbon granules in waste water, using the Disengagement zone expanded to design can be effective
Separation water outlet in carbon granules, reduce the loss of micro-electrolysis stuffing in micro-electrolysis reaction district, improve effluent quality.
(4) present invention makes high slat-containing wastewater be regulated by acid adding during described MVR evaporation process
PH value is to 5-6, it is ensured that in evaporation process, ammonium salt will not hydrolyze and be concentrated and separate, thus by sodium
Salt, sylvite, ammonium salt are all removed.
(5) setting of each process sequence of the present invention, and the selection of parameter in each operation, including
Medicament kind, added amount of chemical, the control of pH and the selection of equipment, all to described wastewater from chemical industry
Final process result produce extremely important impact, the present invention to high salt, high ammonia nitrogen, high organic solvent,
High toxicity wastewater from chemical industry carries out pretreatment and compares conventional treatment process, and after process, water quality indices is the most more
Excellent, system is run the most more stable.
Accompanying drawing explanation
Fig. 1 is the structural representation of up-flow contact reactor of the present invention.
In accompanying drawing, the implication of mark is as follows:
10-up-flow contact reactor 11-water distributing area 111-water inlet 112-compressed air inlet
12-reaction zone 13-Disengagement zone 131-outlet canal
Detailed description of the invention
Micro-electrolysis reaction treatment technology of the present invention is a kind of reason processing high concentrated organic wastewater at present
Think technique, also known as internal electrolysis.It is in the case of cold, utilizes the micro-electricity being filled in waste water
Solve filler self generation 1.2V potential difference and waste water is carried out electrolysis process, to reach degradable organic pollutant
Purpose.
Described Fenton's reaction treatment technology is with ferrous ion (Fe2+) it is catalyst hydrogen peroxide (H2O2)
Carry out the method for wastewater treatment of chemical oxidation.The system being made up of ferrous ion and hydrogen peroxide, is referred to as sweet smell
Pause reagent, and it can generate the hydroxyl radical free radical of strong oxidizing property, generates with hardly degraded organic substance in aqueous
Organic free radical is allowed to structural deterioration, final oxidation Decomposition.
The general principle of described MVR evaporation process is: in MVR evaporator system, at certain pressure
Under, utilize the fixed gas in vapour compression machine heat exchanger (when starting to preheat) and water vapour (to start evaporation
Time) be compressed, thus produce steam, discharge heat energy simultaneously.The indirect steam produced is through mechanical type
After heat energy compressor effect, and in evaporator system, the heat of produced indirect steam is used repeatedly
Amount, make intrasystem temperature promote 5～20 DEG C, heat can being utilized with continuous several times, live steam
It is only used for supplemental heat loss and is supplemented in discharging heat content, significantly lowering evaporimeter to external live steam
Consume, improve the thermal efficiency, reduce energy consumption, it is to avoid use external steam and boiler.
Described micro-electrolysis reaction processes and uses up-flow contact reactor 10, as it is shown in figure 1, described up-flow connects
Touching reactor 10 is bucket body structure, sets gradually water distributing area 11, reaction zone in described staving from bottom to top
12, Disengagement zone 13, the bucket wall at place, described water distributing area 11 is provided with water inlet 111, compressed air is entered
Mouth 112, is filled with micro-electrolysis stuffing in described reaction zone 12, described wastewater from chemical industry is equal by water distributing area 11
Separated by Disengagement zone 13 again in even entrance reaction zone 12, a diameter of described reaction zone in described Disengagement zone 13
1.2-1.4 times of 12 diameters.Micro-electrolysis reaction the most of the present invention processes up-flow contact reactor used
10 so that wastewater from chemical industry is entered by flowing up water distributing area 11 bottom contact reactor 10, from Disengagement zone, upper end
13 discharge, This structure increases in wastewater from chemical industry and reaction zone 12 time of contact of micro-electrolysis stuffing, with
And the reaction time.Described compressed air inlet 112 can be ventilated in waste water and increase water oxygen level,
It is beneficial to follow-up Fenton's reaction is processed the Fe in water outlet2+It is oxidized to Fe3+, increase follow-up the sinking of Fenton water outlet
Shallow lake effect.1.2-1.4 times of a diameter of described reaction zone 12 diameter in described Disengagement zone 13, this structure makes
Derive from reaction zone 12 to ascend into the rate of climb of the waste water in Disengagement zone 13 and be reduced, be so beneficial to
The decline of micro-electrolysis stuffing carbon granules in waste water, uses the Disengagement zone 13 expanded design to efficiently separate out
Carbon granules in water, in minimizing micro-electrolysis reaction district 12, the loss of micro-electrolysis stuffing, improves effluent quality.
Below in conjunction with embodiment technical solution of the present invention made more specific detail:
Embodiment 1
Select high salt, high ammonia nitrogen, high organic solvent, high toxicity wastewater from chemical industry to sequentially pass through coagulating to sink
Shallow lake process, micro-electrolysis reaction process, Fenton's reaction process, MVR evaporation process, condensate liquid biochemical treatment；
Wherein said coagulating precipitation process uses PAC as coagulant, and PAM is as flocculation aid, institute
Stating PAC dosage is 98mg/L, and described PAM dosage is 11mg/L, described coagulating precipitation
PH value is controlled 6 by sulfuric acid regulation；
In described micro-electrolysis reaction processing procedure, control ph is 2.8；
H in described Fenton's reaction processing procedure2O2Dosage 9g/L, FeSO4Dosage 180g/L, PAM
Dosage is 4mg/L, and by sulfuric acid regulation control ph 2.8；
During described MVR evaporation process, control ph is 5.
Embodiment 2
This embodiment is identical with embodiment 1 preprocess method, simply makes an adjustment corresponding process parameters,
Specifically:
Described in wherein said coagulating precipitation process, PAC dosage is 102mg/L, and described PAM throws
Dosage is 9mg/L, and the pH value of described coagulating precipitation is controlled 9 by sulfuric acid regulation；
In described micro-electrolysis reaction processing procedure, control ph is 3.2；
H in described Fenton's reaction processing procedure2O2Dosage 10g/L, FeSO4Dosage 220g/L, PAM
Dosage is 6mg/L, and by sulfuric acid regulation control ph 3.2；
During described MVR evaporation process, control ph is 6.
Embodiment 3
This embodiment is identical with embodiment 1 preprocess method, simply makes an adjustment corresponding process parameters,
Specifically:
Described in wherein said coagulating precipitation process, PAC dosage is 100mg/L, and described PAM throws
Dosage is 10mg/L, and the pH value of described coagulating precipitation is controlled 7 by sulfuric acid regulation；
In described micro-electrolysis reaction processing procedure, control ph is 3；
H in described Fenton's reaction processing procedure2O2Dosage 9.6g/L, FeSO4Dosage 200g/L, PAM
Dosage is 5mg/L, and by sulfuric acid regulation control ph 3；
During described MVR evaporation process, control ph is 5.5.
Preprocess method of the present invention uses first in Laian County listed company chemical wastewater treatment project,
This preprocess method flow process is before application produces, through repeatedly lab scale and pilot scale, and success the most aborning
Application, table 1 below is the treatment effect of each processing unit.
Table 1:
Same employing Laian County listed company wastewater from chemical industry, following table processes describedization for using common process
The treatment effect of work waste water:
Table 2:
Integrated comparative table 1 and the clearance of whole pretreatment system in table 2, it is known that processing method of the present invention
Every treatment effect is significantly better than that conventional preprocess method.
Claims (5)
1. a wastewater from chemical industry preprocess method, it is characterised in that: described wastewater from chemical industry sequentially passes through mixed
Solidifying reaction precipitation processes, micro-electrolysis reaction processes, Fenton's reaction processes, MVR evaporation process.
2. wastewater from chemical industry preprocess method as claimed in claim 1, it is characterised in that: described coagulation
Reaction precipitation processes and uses PAC as coagulant, and PAM is as flocculation aid, and described PAC dosage is
98-102mg/L, described PAM dosage is 9-11mg/L, and the pH value of described coagulating precipitation is passed through
Sulfuric acid regulation controls at 6-9.
3. wastewater from chemical industry preprocess method as claimed in claim 1, it is characterised in that: described micro-electricity
Solving reaction treatment and use up-flow contact reactor (10), described up-flow contact reactor (10) is staving
Structure, sets gradually water distributing area (11), reaction zone (12), Disengagement zone from bottom to top in described staving
(13), the bucket wall at described water distributing area (11) place is provided with water inlet (111), compressed air is entered
Mouth (112), is filled with micro-electrolysis stuffing in described reaction zone (12), described wastewater from chemical industry is by water distribution
District (11) is separated by Disengagement zone (13) even in reaction zone (12) again, described Disengagement zone (13)
1.2-1.4 times of a diameter of described reaction zone (12) diameter；Described micro-electrolysis reaction processing procedure is controlled
PH value processed is at 2.8-3.2.
4. wastewater from chemical industry preprocess method as claimed in claim 1, it is characterised in that: described Fenton
H during reaction treatment2O2Dosage 9-10g/L, FeSO4Dosage 180-220g/L, PAM dosage
For 4-6mg/L, and by sulfuric acid regulation control ph at 2.8-3.2.
5. wastewater from chemical industry preprocess method as claimed in claim 1, it is characterised in that: described MVR
During evaporation process, control ph is at 5-6.
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| CN201610294582.8A CN105923869A (en) | 2016-05-03 | 2016-05-03 | Pretreatment method for chemical industry wastewater |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107082521A (en) * | 2017-04-25 | 2017-08-22 | 杭州盛景环保工程有限公司 | A kind of pretreatment system for handling high salt high concentrated organic wastewater |
| CN108726773A (en) * | 2017-10-23 | 2018-11-02 | 科迈化工股份有限公司 | A kind of chemical wastewater treatment technique |
| CN108793552A (en) * | 2018-06-07 | 2018-11-13 | 浙江奇彩环境科技股份有限公司 | A kind of processing method of nigrosine production waste water |
| CN109574401A (en) * | 2018-12-28 | 2019-04-05 | 苏州南风优联环保工程有限公司 | Textile auxiliary produces waste water zero discharge treatment process and equipment |
| CN110066077A (en) * | 2019-06-11 | 2019-07-30 | 泉州南京大学环保产业研究院 | A kind of processing method of cymoxanil agricultural chemicals waste water |
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| US20150191370A1 (en) * | 2012-05-29 | 2015-07-09 | Jmy Invest Aps | Device for treating a liquid |
| CN105000734A (en) * | 2015-06-18 | 2015-10-28 | 四川珍福堂商贸有限公司 | Pharmaceutical wastewater treating system and method |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107082521A (en) * | 2017-04-25 | 2017-08-22 | 杭州盛景环保工程有限公司 | A kind of pretreatment system for handling high salt high concentrated organic wastewater |
| CN107082521B (en) * | 2017-04-25 | 2020-08-25 | 杭州盛景环保工程有限公司 | Pretreatment system for treating high-salt high-concentration organic wastewater |
| CN108726773A (en) * | 2017-10-23 | 2018-11-02 | 科迈化工股份有限公司 | A kind of chemical wastewater treatment technique |
| CN108793552A (en) * | 2018-06-07 | 2018-11-13 | 浙江奇彩环境科技股份有限公司 | A kind of processing method of nigrosine production waste water |
| CN109574401A (en) * | 2018-12-28 | 2019-04-05 | 苏州南风优联环保工程有限公司 | Textile auxiliary produces waste water zero discharge treatment process and equipment |
| CN110066077A (en) * | 2019-06-11 | 2019-07-30 | 泉州南京大学环保产业研究院 | A kind of processing method of cymoxanil agricultural chemicals waste water |
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