CN1176864C - Method for treating sewage by DSD acid reduction acid bleeding - Google Patents
Method for treating sewage by DSD acid reduction acid bleedingInfo
- Publication number
- CN1176864C CN1176864C CNB021489343A CN02148934A CN1176864C CN 1176864 C CN1176864 C CN 1176864C CN B021489343 A CNB021489343 A CN B021489343A CN 02148934 A CN02148934 A CN 02148934A CN 1176864 C CN1176864 C CN 1176864C
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- China
- Prior art keywords
- acid
- waste water
- dsd
- wastewater treatment
- treatment method
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Abstract
The present invention relates to a method for treating waste water containing DSD acid and reduction acid, which belongs to the field of the purification treatment of industrial sewage. The technological method comprises: a. the pH value of waste water containing reduction acid is from 3 to 4, and hydrogen peroxide and ferrous salt are added for carrying out an oxidation reaction; b. the oxidized waste water enters an electrolytic reactor, and an electrolytic reaction is carried out; c. the pH value of the waste water after the electrolytic reaction is neutralized to 8 to 9; d. mud and water are separated; e. the decalcification treatment is carried out to the separated liquid. The technology has the advantages of low cost of waste water treatment, favorable decoloring effect, simple equipment and technology, easy operation and no generation of secondary pollution, the reactant cost is lower than 3.5 yuan/ton waste water, and the effluent chrominance is smaller than five times without rebound.
Description
Technical field
The present invention relates to a kind of DSD acid reduction acid out wastewater treatment method, belong to the industrial sewage purification process field.
Background technology
DSD acid full name is 4,4 '-diaminobenzil-2,2 '-disulfonic acid, claim Qi Shi acid again, molecular formula C
14H
14N
2O
6S
2Yellow needle-like water absorbability xln, industrial goods are light yellow paste, its production technique is to be raw material with the para-nitrotoluene, must be through the oleum sulfonation to nitro ortho-sulfonic acid base toluene, carry out oxidative condensation again and get 4,4 '-dinitrobenzene toluylene-2,2 '-disulfonic acid, get after iron powder reducing is refining, reduction acid out waste water is meant the waste water that is produced in the acid out process behind iron powder reducing, contain phenyl amines, nitrobenzene class pollutant and the higher colourity of higher concentration, belongs to the poisonous and harmful waste water with strong carinogenicity.At present domesticly be: in acid out waste water, add flocculation agents such as quaternary ammonium salt, molysite, aluminium salt and poly-propionic acid amide and carry out flocculation decoloration for this waste water treatment technology, adopt precipitation, air supporting or press filtration to carry out mud-water separation then, water outlet is discharged after sorbing material such as charcoal absorption.Its main drawback is: (1) wastewater treatment expense height, and flocculation agent, neutralization are 8～14 yuan/ton with alkali and sorbing material expense, production unit is difficult to bear; (2) the phenyl amines pollutants removal rate is low, and chromophoric group destroys not exclusively, and treat effluent is easily returned look, enter water surrounding after, still can cause environmental pollution in various degree.
Summary of the invention
Technical problem to be solved by this invention provides low, the effective DSD acid reduction acid out wastewater treatment method of a kind of expense.
The technical scheme that the present invention takes comprises the steps:
(a), will reduce acid out waste water under PH3～4 conditions, add hydrogen peroxide (30%) and ferrous salt, carry out oxidizing reaction;
(b), make the waste water after the oxidation enter electrolysis reactor, carry out electrolytic reaction;
(c), the waste water after the electrolytic reaction is neutralized to PH8～9;
(d), mud-water separation;
(e), the liquid after will separating carries out decalcification and handles.
The ferrous salt that uses in the described DSD acid reduction acid out wastewater treatment method step (a) is a ferrous sulfate.
Hydrogen peroxide (30%) add-on (w/w) is 1.5 ‰～2.5 ‰ in the described DSD acid reduction acid out wastewater treatment method step (a), and the ferrous salt add-on is 0.2 ‰～2 ‰.
The time of oxidizing reaction is 〉=0.5 hour in the described DSD acid reduction acid out wastewater treatment method step (a), and temperature of reaction is 35～80 ℃.
The electrolytic reaction of described DSD acid reduction acid out wastewater treatment method step (b) is to make the waste water after the oxidation enter the reactor that iron-carbon filling material is housed, and carries out electrolytic reaction.
The iron-carbon filling material that electrolytic reaction is adopted in the described DSD acid reduction acid out wastewater treatment method is that granularity is iron filings and the coke of 2～10mm.
The electrolytic reaction of step (b) is to make the waste water after the oxidation enter the reactor that is provided with the ferroelectric utmost point with technical scheme in addition in the described DSD acid reduction acid out wastewater treatment method, and logical 12V direct current carries out electrolytic reaction.
The reaction times is 〉=0.5 hour in the described DSD acid reduction acid out wastewater treatment method step (b).
Neutralization reaction medicament in the described DSD acid reduction acid out wastewater treatment method step (c) is milk of lime or Calcium Carbide Ash.
Decalcification is to adopt the ordinary elasticity filler to adhere to the calcium sulfate that crystallization is separated out in the water in the described DSD acid reduction acid out wastewater treatment method step (e).
Reaction principle of the present invention is: a, under the catalysis of ferrous ion, and the peroxidation Hydrogen Energy produces two kinds of active hydroxyl free radicals, thereby causes and propagate radical chain reaction, accelerates the oxidation of phenyl amines pollutent, destroys chromophoric group simultaneously; Electrolytic reaction takes place at iron filings filler or ferroelectric extremely surface in b, slightly acidic waste water, produce hydrogen in statu nascendi, nitrobenzene compounds in the waste water is under its effect, at first be reduced into amino benzenes compounds, amino benzenes compounds and other organic substances further decolour under the acting in conjunction of electrolytic oxidation and electrolytic flocculation and remove COD; C, employing milk of lime or Calcium Carbide Ash neutralization can improve the mud-water separation performance, reduce the expense of neutralization with alkali greatly; D, can adopt filter press, air supporting or intermediate processing to carry out mud-water separation; E, employing ordinary elasticity filler adhere to the calcium sulfate that crystallization is separated out in the water, reduce water hardness and go out water suspension, than traditional yellow soda ash medicament decalcification cost saving.
Technical progress effect of the present invention shows following several aspect:
1, wastewater treatment expense is low, and medicament expense is lower than 3.5 yuan of/ton waste water; 2, good decolorizing effect, effluent color dilution does not rebound less than 5 times (seeing Appendix 1); 3, equipment, technology are simple, easy handling; 4, do not produce secondary pollution.
Description of drawings
Fig. 1 is a process flow sheet of the present invention
Embodiment
Embodiment 1:
Reduction acid out waste water is discharged through the workshop, at first entering equalizing tank mixes well, control PH3.5,40 ℃ of temperature, squeeze into reactor I with pump then, add hydrogen peroxide 1.5Kg/ ton waste water in the reactor I, ferrous sulfate 0.2Kg/ ton waste water, reaction times is more than 0.5 hour, time, long-acting more fruit was good more, and reaction back waste water flows automatically to the reactor II that iron-carbon filling material is housed, and iron-carbon filling material is to be the reactor of packing into after the iron filings of 2～10mm and coke mix with granularity, the filling ratio of coke and iron filings can be 1-5: 1-99, ratio is 1-5 preferably: 95-99, and the micro-electrolysis reaction time, the time, long-acting more fruit was good more more than 0.5 hour, squeeze into neutralization tank then and be neutralized to PH8 with milk of lime, after precipitator method mud-water separation, the mud after the separation can be made the building materials raw material, and liquid feeds the decalcification pond, adhere to the calcium sulfate that crystallization is separated out in the water by the ordinary elasticity filler, waste water is chemical oxygen demand (COD) after decalcification, colourity, phenyl amines, nitrobenzene, suspended substance, pH values etc. all reach national secondary discharge standard.
Embodiment 2:
Steps such as its oxidizing reaction, neutralization reaction, mud-water separation and decalcification are all identical with embodiment 1, the different electrolytic reaction of being, be to settle the iron plate electrode in reactor II, logical 12V direct current feeds reactor II with the waste water after the oxidation and carries out electrolytic reaction more than 1 hour.
Claims (10)
1, a kind of DSD acid reduction acid out wastewater treatment method, it is characterized in that: it comprises the steps:
A, will reduce acid out waste water under PH3～4 conditions, add concentration and be 30% hydrogen peroxide and ferrous salt, carry out oxidizing reaction;
B, make the waste water after the oxidation enter electrolysis reactor, carry out electrolytic reaction;
C, the waste water after the electrolytic reaction is neutralized to PH8～9;
D, mud-water separation;
E, the liquid after will separating carry out decalcification to be handled.
2, DSD acid reduction acid out wastewater treatment method according to claim 1, it is characterized in that: the ferrous salt that uses among the step a is a ferrous sulfate.
3, DSD according to claim 1 and 2 acid reduction acid out wastewater treatment method is characterized in that: add concentration among the step a by weight and be 30% hydrogen peroxide 1.5 ‰～2.5 ‰, ferrous salt adds 0.2 ‰～2 ‰ by weight.
4, DSD acid reduction acid out wastewater treatment method according to claim 1, it is characterized in that: the time of oxidizing reaction is 〉=0.5 hour among the step a, temperature of reaction is 35～80 ℃.
5, DSD according to claim 1 acid reduction acid out wastewater treatment method is characterized in that: the electrolytic reaction of step b is to make the waste water after the oxidation enter the reactor that iron-carbon filling material is housed, and carries out micro-electrolysis reaction.
6, DSD acid reduction acid out wastewater treatment method according to claim 5, it is characterized in that: the iron-carbon filling material that electrolytic reaction is adopted is that granularity is iron filings and the coke of 2～10mm.
7, DSD according to claim 1 acid reduction acid out wastewater treatment method is characterized in that: the electrolytic reaction of step b is to make the waste water after the oxidation enter the reactor that is provided with the ferroelectric utmost point, and logical 12V direct current carries out electrolytic reaction.
8, DSD acid reduction acid out wastewater treatment method according to claim 1, it is characterized in that: the reaction times is 〉=0.5 hour among the step b.
9, DSD acid reduction acid out wastewater treatment method according to claim 1, it is characterized in that: the neutralization reaction medicament among the step c is milk of lime or Calcium Carbide Ash.
10. DSD acid reduction acid out wastewater treatment method according to claim 1, it is characterized in that: decalcification is to adopt the ordinary elasticity filler to adhere to the calcium sulfate that crystallization is separated out in the water among the step e.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021489343A CN1176864C (en) | 2002-11-12 | 2002-11-12 | Method for treating sewage by DSD acid reduction acid bleeding |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021489343A CN1176864C (en) | 2002-11-12 | 2002-11-12 | Method for treating sewage by DSD acid reduction acid bleeding |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1405102A CN1405102A (en) | 2003-03-26 |
| CN1176864C true CN1176864C (en) | 2004-11-24 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB021489343A Expired - Fee Related CN1176864C (en) | 2002-11-12 | 2002-11-12 | Method for treating sewage by DSD acid reduction acid bleeding |
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Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1321906C (en) * | 2005-12-29 | 2007-06-20 | 北京科技大学 | Method for treating DSD acid oxidized waste water using electrolytic process |
| CN100431977C (en) * | 2006-07-21 | 2008-11-12 | 中山大学 | Sterilizing method for hospital waste water |
| CN100503461C (en) * | 2006-07-21 | 2009-06-24 | 中山大学 | sterilizing method for waste water of fowl and livestock breeding |
| CN101786740B (en) * | 2010-02-10 | 2012-05-09 | 山东东岳有机硅材料有限公司 | Treatment method for oily waste water in production of organic silicon monomer |
| CN102295393B (en) * | 2011-08-22 | 2012-09-05 | 山西阳煤丰喜肥业(集团)有限责任公司 | Treatment process for production wastewater of DSD acid |
| CN105330102B (en) * | 2015-10-30 | 2018-04-27 | 浙江奇彩环境科技股份有限公司 | A kind of production technology of improved DSD acid |
-
2002
- 2002-11-12 CN CNB021489343A patent/CN1176864C/en not_active Expired - Fee Related
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| Publication number | Publication date |
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| CN1405102A (en) | 2003-03-26 |
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