CN203878019U - Device for treating waste water produced during production of cyclotetramethylene tetranitramine - Google Patents
Device for treating waste water produced during production of cyclotetramethylene tetranitramine Download PDFInfo
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- CN203878019U CN203878019U CN201320812924.2U CN201320812924U CN203878019U CN 203878019 U CN203878019 U CN 203878019U CN 201320812924 U CN201320812924 U CN 201320812924U CN 203878019 U CN203878019 U CN 203878019U
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Abstract
The utility model relates to a device for treating waste water produced during production of cyclotetramethylene tetranitramine and belongs to the field of wastewater treatment. The device for treating the waste water produced during production of the cyclotetramethylene tetranitramine comprises a neutralization tank A, an anaerobic tank, an aerobic tank A, a sedimentation tank A, an acidification tank, an electrocatalytic oxidation tank, a neutralization tank B, a sedimentation tank B, an aerobic tank B, a sedimentation tank C, an intermediate water tank, a mechanical filter and an activated carbon filter. The device for treating the waste water produced during production of the cyclotetramethylene tetranitramine has the advantages that a technology processing effect is good, process cost is low, and indexes of the waste water produced during production of the cyclotetramethylene tetranitramine by adopting the device and method provided by the utility model are optimized, wherein COD (chemical oxygen demand) can be reduced to below 50mg/L, and concentration of the cyclotetramethylene tetranitramine is less than 0.5mg/L.
Description
Technical field
The utility model relates to a kind of device of processing octogen factory effluent, belongs to field of waste water treatment.
Background technology
In waste water after octogen is produced, contain a large amount of nitre amine substances, stable chemical nature, is difficult to carry out biological degradation, and microorganism is had and suppressed or toxic action.At present, the treatment process of octogen factory effluent is mainly contained to Fenton reagent method, active carbon adsorption, Ozonation etc.
Fenton reagent method needs wastewater pH to be adjusted to 3～4 before processing, after oxidation finishes, adds the anti-neutrality that is adjusted to of alkali again, needs to consume a large amount of bronsted lowry acids and bases bronsted lowries in acidifying and N-process.In addition, because waste water COD is high, the consumption of ferrous sulfate and hydrogen peroxide is also very large, and in treating processes, produces a large amount of inorganic mud, is difficult to dispose.Fenton reagent method can be by the difficult biochemical substances oxidation removal of part in waste water, but removal efficiency is not high enough, and in conjunction with biochemical processing process, water outlet COD is difficult to be down to below 100mg/L.
Active carbon adsorption adopts charcoal absorption to remove the pollutent in waste water.The pollutent in waste water can be effectively removed in charcoal absorption, and water outlet indices all can reach emission standard requirement.But the saturated rear difficult regeneration of charcoal absorption, needs frequently more to renew charcoal.One-time investment and running cost are all very high.
Ozone oxidation can improve waste water B/C, and Substance Transformation that can not be biochemical is can biochemical substances.In practical engineering application, there is the shortcoming that power consumption is large, effluent quality is poor in Ozonation.And the pipeline of ozone oxidation system and aerator all need to adopt high standard stainless steel, pond body needs sealing, and one-time investment is very large.
The eighties in 20th century, people proposed the concept of advanced oxidation processes (AOPs), pointed out that by reaction, generating hydroxyl radical free radical [OH] is effectively to carry out the committed step of the harmless treatment of difficult degradation pollutent.Oxygenant stronger by electrochemical method generation oxidisability, non-secondary pollution that scientific worker begins one's study, as [OH], H
2o
2and O
3deng.At the beginning of the nineties, development has formed electrochemistry oxygen metallization processes gradually.Electrochemical oxidation process is by there being the electrode of catalytic activity directly or indirectly to produce hydroxyl radical free radical or strong active oxide material, thus the efficient oxidation difficult degradation pollutent.Because of in electrochemical oxidation process, do not need to add other chemical substance, and can not produce new pollution substance, and be called as " environmental friendliness " technology, the feature that has other advanced oxidation processes not compare with its multiple advantage.Although the applied research of external electrochemical oxidation process in fields such as percolate, leather-making waste water, dyeing waste water, refinery water, paper wastes makes fast progress, but up to now, the research of electrochemical oxidation process on explosive waste water and application are still seldom and have many open questions, as too high in process cost and processing efficiency is on the low side.It is the key that solves electrochemistry cost and efficiency that the step of electrochemicial oxidation is controlled.Feature pollutent (toxicant) in electrochemicial oxidation used water difficult to degradate is first converted into low toxicity intermediate product, and further oxidation generates low molecular organic acids, and permineralization generates CO
2, H
2o and inorganic salts.It is low that oxidation generates the relative organic acid mineralising of organic acid course energy consumption, and reaction is easy to occur, and organic acid mineralising is a very long process.The key that difficult biochemical high concentrated organic wastewater is processed be can be biochemical pre-treatment, different pretreatment processs has certain adaptability and economy to different waste water, adopt rational operational path that the toxicant in used water difficult to degradate is converted into low toxicity intermediate product, then adopt the cheap biochemical process of processing costs to carry out subsequent disposal.
China is increasing to the attention degree of environment protection, and the law of appearance, rules are continually strengthened the management intensity of emission standard.Weapons group strengthens year by year to the financial support of the processing of explosive waste water, and strengthens the management of factory effluent and planning for the needs of the people's livelihood and Sustainable development.Therefore, research and development of the present utility model and application, by effectively promoting the Sustainable development of China fire explosive enterprise, not only have good environmental benefit, and have outstanding economic benefit and social benefit.
Utility model content
The purpose of this utility model is to provide a kind of technique and device thereof of processing octogen factory effluent, reaches emission standard after making to process rear water outlet, and reduces one-time investment and the processing cost of device.
The purpose of this utility model is achieved through the following technical solutions:
A kind of device of processing octogen factory effluent of the present utility model, this device comprises: neutralization tank A, anaerobic pond, Aerobic Pond A, settling tank A, acidification pool, catalytic oxidation pond, neutralization tank B, settling tank B, Aerobic Pond B, settling tank C, intermediate pool, mechanical filter, activated charcoal filter.
Neutralization tank A is used for adjusting wastewater pH.It is acid that octogen factory effluent is, and in neutralization tank A, adds alkali, and wastewater pH is adjusted to neutrality, to meet follow-up biochemical treatment system water inlet requirement.PH real-time monitoring device, alkaline conditioner throwing device and aeration stirrer are set in neutralization tank A; Wherein, alkaline conditioner throwing device is controlled dosage automatically according to the pH pre-determined range of pH real-time monitoring device setting, and the pH of pending waste water is adjusted to pre-determined range.
Anaerobic pond is closed cell body, outer setting thermal insulation layer, heating unit and temperature real time monitoring apparatus, and inside arranges anaerobism filler, and heating unit carries out temperature adjusting to anaerobic pond waste water automatically according to the temperature regulating range of temperature real time monitoring apparatus setting; Biogas blow-down pipe is established on anaerobic pond top.
Aerobic Pond A inside arranges aerobic filler and aerating apparatus, and aerating apparatus adopts type micro-pore aerator.
The water-in of settling tank A is arranged on Chi Ti bottom centre, and water outlet arranges the side of pond body, and the bottom of settling tank is also provided with spoil disposal passage and sludge reflux passage.
Acidification pool is for wastewater pH is adjusted to acidity, and pond inwall adopts Corrosion Protection of Fiber Reinforced Plastics.PH real-time monitoring device, acid regulator throwing device and aeration stirrer are set in acidification pool; Wherein, acid regulator throwing device is controlled dosage automatically according to the pH pre-determined range of pH real-time monitoring device setting, and the pH of pending waste water is adjusted to pre-determined range.
Catalytic oxidation pond is for carrying out electrochemical treatment to waste water.Catalytic oxidation arranges electrochemical apparatus in pond, and aeration stirrer is installed in bottom, pond.Electrochemical apparatus Anodic adopts oxygen evolution potential type titanium base stannic oxide electrode (Ti/SnO
2), this electrode adopts brushes thermal oxidation method preparation, and negative electrode adopts stainless steel plate, fills ceramic particle and iron filings that area load has Sn-Sb-Ag between two pole plates.
Neutralization tank B is used for adjusting the pH of catalytic oxidation pond water outlet.PH real-time monitoring device, alkaline conditioner throwing device, flocculation agent throwing device and aeration stirrer are set in neutralization tank B; Wherein, alkaline conditioner throwing device is controlled dosage automatically according to the pH pre-determined range of pH real-time monitoring device setting, and the pH of pending waste water is adjusted to pre-determined range.
Settling tank B, settling tank C arrange identical with settling tank A.
Aerobic Pond B adopts BAC process.Using biological activated carbon as filler, and aeration adopts single-hole membrane aerator.
Mechanical filter adopts double-layer filter material, and upper strata is thick 0.4-0.5m, the hard coal of particle diameter 0.8-1.8mm; Lower floor is thick 0.4-0.5m, the quartz sand of particle diameter 0.5-1.2mm; Water-in is arranged on the upper end of mechanical filter double-layer filter material, and water outlet is arranged on the lower end of mechanical filter double-layer filter material.
Activated charcoal filter adopts wooden columnar activated carbon, particle diameter 2-5mm.
Intake-outlet between neutralization tank A, anaerobic pond, Aerobic Pond A, settling tank A, acidification pool, catalytic oxidation pond, neutralization tank B, settling tank B, Aerobic Pond B, settling tank C connects by pipeline successively; The water outlet of settling tank C is pipeline connecting machine tool strainer and activated charcoal filter successively; The spoil disposal passage of settling tank A, settling tank B and settling tank C is all connected the water-in of sludge thickener by sludge pump pipeline.
Adopt device of the present utility model to process the method for octogen factory effluent, concrete treatment step is as follows:
1) by adding alkaline conditioner that the pH value of octogen factory effluent is adjusted to 7.5～8.5, carry out aeration agitation, the gas-water ratio of aeration agitation is 2:1 simultaneously;
2) by through the 1st) step pH value regulates the octogen factory effluent after processing to enter anaerobic treatment 12h in anaerobic environment, and temperature maintains between 30～35 ℃;
3) by through the 2nd) octogen factory effluent after step anaerobic treatment enters aerobic treatment 6h in aerobic environment, and sludge concentration maintains 3000mg/L～4500mg/L;
4) will be through the 3rd) more than octogen factory effluent precipitation 1h after step aerobic treatment, by precipitate and separate, removes the suspended substance in water, by lower floor's mud extraction, concentrate successively, processed; By adding acid regulator, make its pH be adjusted to 4.0～4.5 supernatant liquid, the residence time is 10min, passes through aeration agitation in the time of acidification simultaneously;
5) by through the 4th) octogen factory effluent after step acidification carries out electrochemical treatment, and the current density in electrochemical treatment is 10mA/cm
2, the residence time is 2h, carries out aeration agitation in electrochemical treatment, and waste water is mixed;
6) by through the 5th) octogen factory effluent after one-step electrochemistry is processed makes its pH be adjusted to neutrality by adding alkaline conditioner, and add polymerize aluminum chloride and polyacrylamide after regulating pH, dosage is respectively polymerize aluminum chloride 10mg/L, polyacrylamide 2mg/L, again after aeration agitation 5min, more than precipitation process 0.5h, remove the suspended substance in waste water;
7) will be through the 6th) lower floor's mud in octogen factory effluent after step precipitation process extracts out, concentrates successively, processed;
Simultaneously by through the 6th) supernatant liquid in octogen factory effluent after step precipitation process enters in aerobic environment more than aerobic treatment 3h, and wherein the gas-water ratio of aerated reaction is 10:1;
8) will be through the 7th) more than octogen factory effluent precipitation 0.5h after step aerobic treatment, remove the suspended substance in waste water, lower floor's mud is extracted out, concentrate successively, processed; Supernatant liquid is passed through to double-layer filter material and activated carbon filtration successively simultaneously.
Beneficial effect
The utility model is combined materialization with biochemical process, first by anaerobism+aerobic biochemical processing process, remove most pollutents, then by catalytic oxidation processing unit, improve wastewater biodegradability, by aerobic treatment unit, remove most of pollutent again, finally by mechanical filter and activated carbon filtration technique, check on, guarantee water outlet qualified discharge.The utility model has been given full play to the low advantage of the good biochemical process cost of physicochemical techniques treatment effect, when guaranteeing treatment effect, effectively reduces working cost.Adopt device of the present utility model to process the indices after octogen factory effluent, COD (chemical oxygen demand (COD)) can be down to below 50mg/L, octogen is less than 0.5mg/L, meet the requirement of < < weapon industry pollution discharge standard fire explosive > > (GB14470.1-2002), wherein COD index can reach the first discharge standard of < < integrated wastewater discharge standard > > (GB8978-1996).
Accompanying drawing explanation
Fig. 1 is the connection diagram that the utility model is processed octogen factory effluent device.
Embodiment
Below in conjunction with drawings and Examples, content of the present utility model is described further:
Embodiment
The octogen factory effluent that Yi Mou factory discharges is for processing object, and its parameters is: COD=8000 ± 700mg/L, octogen=80～120mg/L, BOD=2800～3200mg/L, B/C=0.35, pH=4.2～5.1.
Adopt the utility model device to carry out Combined Processing to above-mentioned octogen factory effluent; Concrete treatment step is as follows:
1) by octogen factory effluent, the water-in by neutralization tank A enters in neutralization tank A, the pH regulator scope of setting pH real-time monitoring device in neutralization tank A is 8, octogen factory effluent in neutralization tank A is outside this default pH regulator scope, pH real-time monitoring device is controlled alkaline conditioner throwing device and is thrown in alkaline conditioner, until this octogen factory effluent pH is reached to this default pH regulator scope, alkaline conditioner throwing device stops throwing in, and aeration agitation 10min, the gas-water ratio of aeration agitation is 2:1; To regulate the octogen factory effluent after processing to enter anaerobic pond from neutralization tank A through pH value again;
2) by through the 1st) step pH value regulates the octogen factory effluent after processing in anaerobic pond, carrying out anaerobic treatment 12h; According to the monitoring result of temperature real time monitoring apparatus, Controlling System is controlled the running status of warming apparatus automatically, maintains temperature in anaerobic pond between 30～35 ℃; Then octogen factory effluent after anaerobic treatment is entered to Aerobic Pond A, and make the sludge concentration in Aerobic Pond maintain 3000mg/L～4500mg/L, aerobic treatment 6h.
3) will be through the 2nd) octogen factory effluent enters in settling tank A and precipitates 1h from Aerobic Pond A after step aerobic treatment, by precipitate and separate, remove the suspended substance in water, then adopt sludge pump that the lower floor's mud in settling tank A is beaten to sludge thickener from the spoil disposal passage of settling tank A bottom, carry out sludge treatment; Supernatant liquid in settling tank A enters acidification pool;
4) the pH real-time monitoring device in acidification pool is controlled acid regulator throwing device and is thrown in acid regulator, by through the 3rd) octogen factory effluent pH value in acidification pool after step precipitation process is adjusted to 4.0～4.5, and aeration agitation 10min, then the octogen factory effluent in acidification pool is entered to catalytic oxidation pond;
5) by through the 4th) octogen factory effluent after step acidification carries out electrochemical treatment in catalytic oxidation pond, and the current density in electrochemical treatment is 10mA/cm
2, the residence time is 2h, carries out aeration agitation in electrochemical treatment, and waste water is mixed, then the octogen factory effluent after electrochemical treatment is entered to neutralization tank B;
6) the pH real-time monitoring device in neutralization tank B is controlled alkaline conditioner throwing device and is thrown in alkaline conditioner, by through the 5th) octogen factory effluent pH value in neutralization tank B after one-step electrochemistry is processed is adjusted to neutrality; By flocculation agent throwing device, in neutralization tank B, throw in flocculation agent again, and aeration agitation 10min; Flocculation agent is that polymerize aluminum chloride and polyacrylamide dosage are respectively 10mg/L and 2mg/L;
7) by through the 6th) octogen factory effluent after step neutralizing treatment enters precipitation 0.5h in settling tank B, by precipitate and separate, remove the suspended substance in water, then adopt sludge pump that the lower floor's mud in settling tank B is beaten to sludge thickener from the spoil disposal passage of settling tank B bottom, carry out sludge treatment; Supernatant liquid in settling tank B enters Aerobic Pond B;
8) will be through the 7th) supernatant liquid aerobic treatment 3h in Aerobic Pond after step precipitation process, wherein the gas-water ratio of aerated reaction is 10:1;
9) by through the 8th) octogen factory effluent after step aerobic treatment enters precipitation 1.5h in settling tank C, by precipitate and separate, remove the suspended substance in water, then adopt sludge pump just the lower floor's mud in settling tank C extract out, concentrate successively, processed; Supernatant liquid is filtered through mechanical filter and activated charcoal filter successively, further remove pollutent remaining in waste water, wastewater treatment completes;
Wherein, mechanical filter is that upper strata is thick 0.5m, the hard coal of particle diameter 0.8-1.8mm; Lower floor is thick 0.5m, the double-layer filter material of the quartz sand of particle diameter 0.5-1.2mm;
Activated charcoal filter adopts the wooden columnar activated carbon of particle diameter 2-5mm.
Adopt front and back contrast effect that system and method for the present utility model processes octogen factory effluent as following table:
Claims (3)
1. a device of processing octogen factory effluent, is characterized in that: this device comprises: neutralization tank A, anaerobic pond, Aerobic Pond A, settling tank A, acidification pool, catalytic oxidation pond, neutralization tank B, settling tank B, Aerobic Pond B, settling tank C, intermediate pool, mechanical filter, activated charcoal filter;
PH real-time monitoring device, alkaline conditioner throwing device and aeration stirrer are set: wherein in neutralization tank A, alkaline conditioner throwing device is controlled dosage automatically according to the pH pre-determined range of pH real-time monitoring device setting, and the pH of pending waste water is adjusted to pre-determined range;
Anaerobic pond is closed cell body, outer setting thermal insulation layer, heating unit and temperature real time monitoring apparatus, and inside arranges anaerobism filler, and heating unit carries out temperature adjusting to anaerobic pond waste water automatically according to the temperature regulating range of temperature real time monitoring apparatus setting; Biogas blow-down pipe is established on anaerobic pond top;
Aerobic Pond A inside arranges aerobic filler and aerating apparatus, and aerating apparatus adopts type micro-pore aerator;
The water-in of settling tank A is arranged on Chi Ti bottom centre, and water outlet arranges the side of pond body, and the bottom of settling tank is also provided with spoil disposal passage and sludge reflux passage; Settling tank B, settling tank C arrange identical with settling tank A;
PH real-time monitoring device, acid regulator throwing device and aeration stirrer are set in acidification pool; Wherein, acid regulator throwing device is controlled dosage automatically according to the pH pre-determined range of pH real-time monitoring device setting, and the pH of pending waste water is adjusted to pre-determined range;
Catalytic oxidation arranges electrochemical apparatus in pond, and aeration stirrer is installed in bottom, pond; Electrochemical apparatus Anodic adopts oxygen evolution potential type titanium base stannic oxide electrode, and negative electrode adopts stainless steel plate, fills ceramic particle and iron filings that area load has Sn-Sb-Ag between two pole plates;
PH real-time monitoring device, alkaline conditioner throwing device, flocculation agent throwing device and aeration stirrer are set in neutralization tank B; Wherein, alkaline conditioner throwing device is controlled dosage automatically according to the pH pre-determined range of pH real-time monitoring device setting, and the pH of pending waste water is adjusted to pre-determined range;
Aerobic Pond B is usingd biological activated carbon as filler, and aeration adopts single-hole membrane aerator;
Mechanical filter adopts double-layer filter material, and upper strata is thick 0.4-0.5m, the hard coal of particle diameter 0.8-1.8mm; Lower floor is thick 0.4-0.5m, the quartz sand of particle diameter 0.5-1.2mm; Water-in is arranged on the upper end of mechanical filter double-layer filter material, and water outlet is arranged on the lower end of mechanical filter double-layer filter material;
Activated charcoal filter adopts wooden columnar activated carbon, particle diameter 2-5mm;
Intake-outlet between neutralization tank A, anaerobic pond, Aerobic Pond A, settling tank A, acidification pool, catalytic oxidation pond, neutralization tank B, settling tank B, Aerobic Pond B, settling tank C connects by pipeline successively; The water outlet of settling tank C is pipeline connecting machine tool strainer and activated charcoal filter successively; The spoil disposal passage of settling tank A, settling tank B and settling tank C is all connected the water-in of sludge thickener by sludge pump pipeline.
2. a kind of device of processing octogen factory effluent as claimed in claim 1, is characterized in that: the pond inwall of acidification pool adopts Corrosion Protection of Fiber Reinforced Plastics.
3. a kind of device of processing octogen factory effluent as claimed in claim 1, is characterized in that: in electrochemical apparatus oxygen evolution potential type titanium base stannic oxide electrode, adopt and brush thermal oxidation method preparation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320812924.2U CN203878019U (en) | 2013-12-12 | 2013-12-12 | Device for treating waste water produced during production of cyclotetramethylene tetranitramine |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320812924.2U CN203878019U (en) | 2013-12-12 | 2013-12-12 | Device for treating waste water produced during production of cyclotetramethylene tetranitramine |
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| CN203878019U true CN203878019U (en) | 2014-10-15 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320812924.2U Withdrawn - After Issue CN203878019U (en) | 2013-12-12 | 2013-12-12 | Device for treating waste water produced during production of cyclotetramethylene tetranitramine |
Country Status (1)
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| CN (1) | CN203878019U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103723886A (en) * | 2013-12-12 | 2014-04-16 | 北京北方节能环保有限公司 | Cyclotetramethylenete-tranitramine production sewage treatment device and method |
| CN109516641A (en) * | 2018-12-17 | 2019-03-26 | 南通寰宇博新化工环保科技有限公司 | Method for treating high-salt high-concentration organic wastewater by electrocatalytic oxidation-biochemical coupling |
-
2013
- 2013-12-12 CN CN201320812924.2U patent/CN203878019U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103723886A (en) * | 2013-12-12 | 2014-04-16 | 北京北方节能环保有限公司 | Cyclotetramethylenete-tranitramine production sewage treatment device and method |
| CN109516641A (en) * | 2018-12-17 | 2019-03-26 | 南通寰宇博新化工环保科技有限公司 | Method for treating high-salt high-concentration organic wastewater by electrocatalytic oxidation-biochemical coupling |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20141015 Effective date of abandoning: 20150513 |
|
| RGAV | Abandon patent right to avoid regrant |