CN103011469B - Technology for treating initiating explosive material production waste water - Google Patents
Technology for treating initiating explosive material production waste water Download PDFInfo
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- CN103011469B CN103011469B CN201110284805.XA CN201110284805A CN103011469B CN 103011469 B CN103011469 B CN 103011469B CN 201110284805 A CN201110284805 A CN 201110284805A CN 103011469 B CN103011469 B CN 103011469B
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- waste water
- initiating explosive
- battery lead
- lead plate
- water
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Abstract
The invention relates to a technology for treating initiating explosive material production waste water. The technology is an environmentally friendly key treatment process aiming at waste water pretreatment and nitrophenol waste water in a production process of initiating explosive materials. According to the invention, the process technology has the advantages of clear and complete principles, continuous stable operation of the treatment system, no secondary pollution, COD less than 100mg/l, nitrophenol content less than 1mg/l, the chromaticity nearly zero, and no detectable sulfide. Product water treated by the technology can be directly used for production or greening and has an important meaning to an area with water shortage. A waste water treatment agent cost of the technology is only about 40 yuan per ton of waste water.
Description
Technical field
The present invention relates to the crucial treatment process for Wastewater Pretreatment and nitropheneol waste water in a kind of Loading Materials for Initiating Explosive Devices production process of Loading Materials for Initiating Explosive Devices production wastewater treatment technique, particularly a kind of environmental protection.
Background technology
In the production processes such as Loading Materials for Initiating Explosive Devices dinitrodiazophenol, trinitro-resorcinol, can produce a large amount of waste water, these class waste water principal pollutant are chemical oxygen demand (COD) (COD), colourity, nitropheneol, and nitropheneol contains benzene ring structure and nitryl group, chemical stability is high and have toxicity, is different from general organic waste water completely.The Loading Materials for Initiating Explosive Devices enterprises such as many production dinitrodiazophenol, trinitro-resorcinol are for a long time for COD and nitropheneol can not perplex by qualified discharge.
Loading Materials for Initiating Explosive Devices factory effluent is the difficult problem that domestic and international sewage disposal is faced always, thereby is also the heat subject of domestic and international Recent study.The method that has entered at present productivity application has: active carbon adsorption, electrolytic process, boiler evaporating method, Ozonation, the precipitator method, these methods are all deposited following problem: working cost is high or process water outlet and do not reach " weapon industry pollution discharge standard " requirement (GB14470.2-2002).In addition, people also utilize electricity, ultrasonic wave, UV-light or chemical process,, produce hydroxyl radical free radical under certain condition, make nitropheneol mineralising, become inorganic salt.But these method great majority are processed experimental stage, not yet enter productivity application.
Summary of the invention
The object of this invention is to provide a kind of effectively treatment process of continuous Loading Materials for Initiating Explosive Devices factory effluent, particularly for pretreatment technology, nitropheneol treatment process and the whole waste water treatment process of waste water in this technological process.
Technical scheme of the present invention:
Loading Materials for Initiating Explosive Devices production wastewater treatment technique, is the feature according to waste water, and the wastewater collection that each operation is produced is processed to equalizing tank again, and concrete treatment process steps is as follows:
(1) equalizing tank waste water is quantitatively delivered to after reduction pond regulates PH to be acidity and is added reductive agent through pump;
(2) enter reaction tank 1 through step (1) waste water after treatment, add organic coagulant aids at this;
(3) carry out solid-liquid separation through step (2) waste water after treatment from flowing into settling tank 1;
(4) enter three-phase fluidization oxidation bed through step (3) supernatant liquor after treatment, carbon containing iron filings and porous plastics grain are filled in three-phase fluidization oxidation bed middle part, filler bottom is provided with gas distribution system and is oxidized required oxygen and the required power of three-phase fluidization for waste water provides, and waste water residence time in three-phase fluidized bed is 2～3 hours;
(5) enter electricity through step (4) waste water after treatment and cause Three phase 3 D fluidisation oxidation bed, electricity causes in Three phase 3 D fluidisation oxidation bed and is provided with battery lead plate, battery lead plate is all connected to power supply, electrode packing particles between plates catalyzer, it is that waste water provides oxidation required oxygen and the required power of three-phase fluidization that battery lead plate and beaded catalyst bottom are provided with gas distribution;
(6) through step (5) waste water after treatment from flow into reaction tank 2 adjust PH be alkalescence and add coagulant aids after carry out solid-liquid separation through being pumped into plate-and-frame filter press;
(7) after reaction tank 3 regulates PH to be acidity, enter the logical reaction tower of the electricity charge through step (6) filtrate after treatment, in tower, add H simultaneously
2o
2with catalyzer R.In the logical reaction tower tower of the electricity charge, be provided with battery lead plate, battery lead plate is all connected to power supply, and reaction tower bottom is provided with gas distribution system provides oxygen, and waste water is 6～8 hours at the logical reaction of electricity charge dwell time in the tower;
(8) regulate PH to carry out coagulating sedimentation to alkalescence and after adding coagulant aids at settling tank 2 through step (7) waste water after treatment at reaction tank 4, supernatant liquor enters clean water basin, and a part is back to production, other qualified discharge.
In described step (1), pH value is less than or equal to 2.
In described step (2), organic coagulant aids is PAM.
In described step (4), the volume ratio of carbon containing iron filings and porous plastics grain is 2: 1, and the particle diameter of carbon containing iron filings and plastics is 2～3mm, and gas-water ratio is 5: 1.
In described step (5), battery lead plate is through the A3 of special processing steel plate, and battery lead plate spacing is 25cm～30cm, and access voltage is 5～10V, and electric current is 30～35A, the gac that beaded catalyst is 3mm, and gas-water ratio is 3: 1.
In described step (6), adjusting pH value is 8～9, and the coagulant aids adding is PAM.
In described step (7), adjusting pH value is that 4～5, R is with AI
2o
3for one or more oxide compounds in Ti, the Ni of carrier, Mn, Fe, V
water: M
h2O2:: M
r=1000ml: 2～8g: 2～3g, battery lead plate is that battery lead plate spacing is 20cm～25cm through the A3 steel plate of special passivation processing, and access voltage is 10～12V, and electric current is 25～30A, and gas-water ratio is 3: 1.
In described step (8), adjusting pH value is 8～9, and the coagulant aids adding is PAM.The treatment process principle analysis of Loading Materials for Initiating Explosive Devices factory effluent:
In described treatment process steps, step (2), (3), (6), (8) are well-known conventional treatment method.
The technological principle of step (1): under acidic conditions (pH value is for being less than or equal to 2), under the effect of reductive agent, the polarity of the part contaminant molecule in waste water will change, become hydrophobic molecule from hydrophilic molecule, solubleness in water reduces, and have tiny suspended particle to generate, then add coagulant aids PAM, these tiny suspended particles will be condensed into large alumen ustum.
The technological principle of step (4): three-phase fluidization oxidation bed is taking original battery electrochemistry reaction as basis, has drawn the fluidized technology in chemical industry operation, has formed a kind of efficient wastewater treatment equipment.Essential characteristic is taking carbon containing iron filings, foam grain etc. as carrier, there is a series of physics chemical action in the filler in device and the pollutent of waste water, now can produce the coagulating agent of one or more status nascendis and the oxygenant of status nascendi, carry out multiple physics chemical action such as coagulation, absorption, catalyzed oxidation decomposition, complexing, displacement so simultaneously, the pollutent in waste water is removed rapidly.In addition, the mixed solution of useless water and air from bottom to top makes carrier fluidisation with certain speed during by packing layer, has realized gas-liquid-solid three-phase and has fully contacted, and has improved processing efficiency.
The technological principle of step (5): it is on the basis of catalytic oxidation that electricity causes Three phase 3 D fluidisation oxidation bed, has drawn the fluidized technology of chemical industry operation, and the one of formation is processed high concentrated organic wastewater treatment unit.Its essential characteristic is filler particles gac between two battery lead plates, the Fe in gac and water
2+form a large amount of galvanic cells, have micro-electrolytic action, an additional low-voltage dc voltage between battery lead plate, increases the strength of electric field between battery lead plate, and electric energy increases, the O that outside provides
2the electronics that trapping extra electric field provides, forms oxyradical ion, and this ion generates H after a series of chain reaction
2o
2, H
2o
2add outside under the effect of electronics and metal ion, only this is in the hydroxyl radical free radical of fluorion to excite generation oxidisability, and hydroxyl radical free radical makes organic substance decomposing, mineralising.In addition, the mixed solution of useless water and air from bottom to top makes carrier fluidisation with certain speed during by packing layer, has realized gas-liquid-solid three-phase and has fully contacted, and has improved processing efficiency.
Electricity causes Three phase 3 D fluidisation oxidation bed in whole reaction process, extra electric field is the effect of " safety fuse ", is different from electrolytic process completely, and electrolytic process is that pollutent is in anode and negative electrode generation redox reaction, be converted into innoxious substance and separated, therefore electrolytic process energy consumption is very high.
The technological principle of step (7): under the effect of low pressure Static Electro field energy, having H
2o
2with with AI
2o
3under one or more oxide compound catalytic conditions in Ti, the Ni of carrier, Mn, Fe, will there is radical chain reaction, generate hydroxyl radical free radical, make partial organic substances generate carbonic acid gas and water, make a COD degraded part, remaining organism will acidication.Obviously, this is the degree of depth catalyzed oxidation of (5) step above that continues.
After processing, water outlet can be back to production and discharge by direct part.
Beneficial effect of the present invention
1, this technological principle is clear, complete, and treatment system energy continuous and steady operation, does not produce secondary pollution.
2, treatment effect COD < 100mg/l, nitrophenol < 1mg/l, colourity is almost nil, and sulfide inspection does not measure.
3, process water outlet can direct reuse in producing or greening, be of great importance for the area of water resources anxiety, but process only approximately 30 yuan/ton of waste water of reagent cost of waste water.
Brief description of the drawings
Fig. 1 Loading Materials for Initiating Explosive Devices production wastewater treatment of the present invention process flow sheet.
Embodiment
With reference to figure 1, according to the feature of Loading Materials for Initiating Explosive Devices production technique, the wastewater collection that each operation is produced is processed to equalizing tank again, its concrete treatment process is as follows: the waste water of equalizing tank is pumped into reduction pond, add hydrochloric acid to regulate pH value≤2, and add reductive agent, water outlet is from flowing into reaction tank 1, add coagulant aids PAM at reaction tank 1, water outlet is carried out mud-water separation from flowing into settling tank 1, supernatant liquor is from flowing into pump well, the waste water of pump well is through being pumped to three-phase sulfidation-oxidation bed oxidation 3 hours, water outlet causes Three phase 3 D fluidisation oxidation bed from flowing into electricity, in bed, stop 2.5 hours, water outlet adds Ca (OH)
2regulate PH to 8～9, coagulant aids, water after coagulation is from flowing into transition pond, carry out mud-water separation through sludge pumping to plate-and-frame filter press, filtrate enters pump well, add hydrochloric acid to regulate behind PH to 4～5 through being pumped into reaction tank 3 at pump well, add catalyzer at reaction tank 3, water outlet stops 6～8 hours from flowing into the logical reaction tower of the electricity charge, and water outlet adds Ca (OH)
2regulate PH to 8～9, coagulant aids, the water after coagulation is from flowing into settling tank, and settling tank water outlet is squeezed into more medium filter through pump, and the waste water after filtration, regulating PH adjustment pond to regulate pH value in 6～9, is back to and produces all the other qualified discharges finally by clean water basin part.
Be exactly more than the process of improving of a complete Loading Materials for Initiating Explosive Devices production wastewater treatment, if management is strict, PH and dosage strictly controlled, waste water is incited somebody to action stably qualified discharge after treatment.
Table 1 is for dinitrodiazophenol factory effluent is through the result of laboratory test of aforesaid method water outlet after treatment.Examination criteria is carried out National Standard of the People's Republic of China's " weapon industry pollution discharge standard---Loading Materials for Initiating Explosive Devices " (GB14470.2-2002).
Table 1
As can be seen from Table 1, adopt the inventive method treated water, indices not only all reaches the emission request of national regulation, and far below the maximum emission standard value of national regulation, wherein the clearance of COD reaches 98.95%, the clearance of colourity approaches 100%, and the removal class of nitropheneol reaches 99.97%, and the clearance of sulfide approaches 100%.
The announcement of book and instruction according to the above description, those skilled in the art in the invention can also change and revise above-mentioned embodiment.Therefore, the present invention is not limited to embodiment disclosed and described above, also should fall in the protection domain of claim of the present invention modifications and changes more of the present invention.In addition,, although used some specific terms in this specification sheets, these terms just for convenience of description, do not form any restriction to the present invention.
Claims (8)
1. Loading Materials for Initiating Explosive Devices production wastewater treatment technique, is characterized in that: concrete treatment process steps is:
(1) equalizing tank waste water is quantitatively delivered to after reduction pond regulates pH to be acidity and is added reductive agent through pump;
(2) enter reaction tank 1 through step (1) waste water after treatment, add organic coagulant aids at this;
(3) carry out solid-liquid separation through step (2) waste water after treatment from flowing into settling tank 1;
(4) enter three-phase fluidization oxidation bed through step (3) supernatant liquor after treatment, carbon containing iron filings and porous plastics grain are filled in three-phase fluidization oxidation bed middle part, filler bottom is provided with gas distribution system and is oxidized required oxygen and the required power of three-phase fluidization for waste water provides, and waste water residence time in three-phase fluidized bed is 2～3 hours;
(5) enter electricity through step (4) waste water after treatment and cause Three phase 3 D fluidisation oxidation bed, electricity causes in Three phase 3 D fluidisation oxidation bed and is provided with battery lead plate, battery lead plate is all connected to power supply, electrode packing particles between plates catalyzer, battery lead plate and beaded catalyst bottom are provided with gas distribution system and are oxidized required oxygen and the required power of three-phase fluidization for waste water provides;
(6) through step (5) waste water after treatment from flow into reaction tank 2 adjust pH be alkalescence and add coagulant aids after carry out solid-liquid separation through being pumped into plate-and-frame filter press;
(7) after reaction tank 3 regulates pH to be acidity, enter the logical reaction tower of the electricity charge through step (6) filtrate after treatment, in tower, add H simultaneously
2o
2with catalyzer R, in the logical reaction tower tower of the electricity charge, be provided with battery lead plate, battery lead plate is all connected to power supply, and reaction tower bottom is provided with gas distribution system provides oxygen, and waste water is 6～8 hours at the logical reaction of electricity charge dwell time in the tower; Described catalyzer R is with Al
2o
3for one or more oxide compounds in Ti, the Ni of carrier, Mn, Fe;
(8) regulate pH to carry out coagulating sedimentation to alkalescence and after adding coagulant aids at settling tank 2 through step (7) waste water after treatment at reaction tank 4, supernatant liquor enters clean water basin, and a part is back to production, other qualified discharge.
2. Loading Materials for Initiating Explosive Devices production wastewater treatment technique according to claim 1, is characterized in that: in described step (1), pH value is less than or equal to 2.
3. Loading Materials for Initiating Explosive Devices production wastewater treatment technique according to claim 1, is characterized in that: in described step (2), organic coagulant aids is PAM.
4. Loading Materials for Initiating Explosive Devices production wastewater treatment technique according to claim 1, is characterized in that: in described step (4), the volume ratio of carbon containing iron filings and porous plastics grain is 2: 1, and the particle diameter of carbon containing iron filings and plastics is 2～3mm, and gas-water ratio is 5: 1.
5. Loading Materials for Initiating Explosive Devices production wastewater treatment technique according to claim 1, it is characterized in that: in described step (5), battery lead plate is through the A3 of special processing steel plate, battery lead plate spacing is 25cm～30cm, access voltage is 5～10V, electric current is 30～35A, beaded catalyst is the gac of 3mm, and gas-water ratio is 3: 1.
6. Loading Materials for Initiating Explosive Devices production wastewater treatment technique according to claim 1, is characterized in that: in described step (6), adjust pH is 8～9, and the coagulant aids adding is PAM.
7. Loading Materials for Initiating Explosive Devices production wastewater treatment technique according to claim 1, is characterized in that: in described step (7), adjust pH is 4～5; V
water: MH
2o
2: M
r=1000ml: 2～8g: 2～3g; Battery lead plate is that battery lead plate spacing is 20cm～25cm through the A3 steel plate of special passivation processing, and access voltage is 10～12V, and electric current is 25～30A, and gas-water ratio is 3: 1.
8. Loading Materials for Initiating Explosive Devices production wastewater treatment technique according to claim 1, is characterized in that: in described step (8), adjust pH is 8～9, and the coagulant aids adding is PAM.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110284805.XA CN103011469B (en) | 2011-09-23 | 2011-09-23 | Technology for treating initiating explosive material production waste water |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110284805.XA CN103011469B (en) | 2011-09-23 | 2011-09-23 | Technology for treating initiating explosive material production waste water |
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| Publication Number | Publication Date |
|---|---|
| CN103011469A CN103011469A (en) | 2013-04-03 |
| CN103011469B true CN103011469B (en) | 2014-07-16 |
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| CN201110284805.XA Expired - Fee Related CN103011469B (en) | 2011-09-23 | 2011-09-23 | Technology for treating initiating explosive material production waste water |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1562818A (en) * | 2004-04-01 | 2005-01-12 | 广东省三○九厂 | Method for treating wastewater of dinitrodiazophenol |
| CN101519260A (en) * | 2008-02-28 | 2009-09-02 | 清远市灵捷制造化工有限公司 | Molecular micro-electrolysis treatment method for dinitrodiazophenol wastewater |
| CN101693572A (en) * | 2009-10-28 | 2010-04-14 | 雅化集团绵阳实业有限公司 | Dinitrodiazophenol waste water processing method |
| CN101734817A (en) * | 2009-12-31 | 2010-06-16 | 江苏苏净集团有限公司 | Method for treating organic chemical waste water |
-
2011
- 2011-09-23 CN CN201110284805.XA patent/CN103011469B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1562818A (en) * | 2004-04-01 | 2005-01-12 | 广东省三○九厂 | Method for treating wastewater of dinitrodiazophenol |
| CN101519260A (en) * | 2008-02-28 | 2009-09-02 | 清远市灵捷制造化工有限公司 | Molecular micro-electrolysis treatment method for dinitrodiazophenol wastewater |
| CN101693572A (en) * | 2009-10-28 | 2010-04-14 | 雅化集团绵阳实业有限公司 | Dinitrodiazophenol waste water processing method |
| CN101734817A (en) * | 2009-12-31 | 2010-06-16 | 江苏苏净集团有限公司 | Method for treating organic chemical waste water |
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| CN103011469A (en) | 2013-04-03 |
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