CN104591435A - Treatment method for industrial wastewater - Google Patents
Treatment method for industrial wastewater Download PDFInfo
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- CN104591435A CN104591435A CN201510001370.1A CN201510001370A CN104591435A CN 104591435 A CN104591435 A CN 104591435A CN 201510001370 A CN201510001370 A CN 201510001370A CN 104591435 A CN104591435 A CN 104591435A
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- trade effluent
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Abstract
The invention belongs to the field of sewage treatment, and relates to a treatment method for industrial wastewater. The method comprises steps of primary precipitation, replacement reaction, secondary precipitation, ammonia stripping and ammonia recycling; removal rate to sulfate radicals in industrial wastewater is up to 80%, removal rate to ammonia nitrogen is up to 90%; the method is particularly applicable to treatment of high-concentration ammonium sulfate wastewater, meanwhile, solves the difficult problem that calcium sulphate scaling blocks equipment and pipelines and increases operation load in the conventional precipitation methods.
Description
Technical field
The invention belongs to sewage treatment area, relate to a kind for the treatment of process of trade effluent, be specifically related to a kind for the treatment of process of ammonium sulfate waste water.
Background technology
A large amount of high-concentration sulfuric acid ammonia waste waters can be produced in the Industrial processes such as chemical industry, medicine, papermaking, such waste water sulfate radical and ammonia nitrogen concentration too high, enter water body if deal with improperly and must cause severe contamination to environment.High-concentration sulfuric acid ammonium waste water because of its sulfate concentration and ammonia nitrogen concentration too high and be unsuitable for Biochemical method,
At present, the pretreatment process for high-concentration sulfuric acid ammonium waste water has evaporative crystallization, decrease temperature crystalline, conventional precipitation method, ammonia aeration.Wherein evaporation crystallization equipment investment is high, energy consumption large, and conditional request is comparatively harsh; Lowering temperature crystallization needs cold operation, and must through repeating repeatedly decrease temperature crystalline, complex steps; Conventional precipitation method in waste water, adds excessive lime form calcium sulfate precipitation, causes remaining a large amount of calcium ion in waste water; Ammonia aeration is the common method processing high ammonia-nitrogen wastewater at present, but often because of the calcium sulfate scaling blocking ammonia aeration e-quipment and pipe that remaining excessive calcium ion during removal sulfate radical is formed, causes resistance to mass transfer, increase operating load.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, a kind for the treatment of process of the trade effluent containing high-concentration sulfuric acid ammonium waste water is provided, effective reduction sulfate radical in waste water concentration and ammonia nitrogen concentration, the introducing of sodium carbonate is simultaneously conducive to removing a large amount of calcium ions remaining in waste water, thus solve the calcium sulfate scaling blocking ammonia aeration e-quipment and pipe that conventional precipitation method faces, cause resistance to mass transfer, increase a difficult problem for operating load.
To achieve these goals, the technical solution used in the present invention is:
A treatment process for trade effluent, comprises the steps: primary precipitation, replacement(metathesis)reaction, two-stage precipitation, ammonia aeration, recovery ammonia.
Preferably, in described primary precipitation, add precipitation agent, in described replacement(metathesis)reaction, add displacer.
Preferably, described precipitation agent is calcium lime powder or milk of lime, and described displacer is sodium carbonate, magnesiumcarbonate, the one of zinc carbonate or its combination.
Preferably, described precipitation agent is calcium lime powder, and described displacer is sodium carbonate.
Preferably, a kind for the treatment of process of trade effluent, comprises the steps:
(1) trade effluent enters primary clarifier through sewer line, adds calcium lime powder, opens stirring and reacts, react after 10-30 minute and close stirring, staticly settle 1 ~ 2 hour, the calcium sulfate precipitation of generation is sunken at the bottom of pond, and supernatant liquor enters replacement(metathesis)reaction pond through sewer line.
In above-mentioned steps, the dosage of calcium lime powder looks SO in waste water
4 2-mass concentration and determine, SO in calcium lime powder and waste water
4 2-mass concentration ratio be 1.10-1.80.
(2) trade effluent processed through step (1) enters replacement(metathesis)reaction pond, sodium carbonate is added in replacement(metathesis)reaction pond, open stirring and carry out replacement(metathesis)reaction, react after 15-40 minute and close stirring, trade effluent enters second-level settling pond through sewer line.
In above-mentioned steps, the dosage of the sodium carbonate mass concentration of calcium lime powder depending on adding, the mass concentration ratio of sodium carbonate and calcium lime powder is 0.5-1.0.
(3) trade effluent processed through step (2) staticly settles 1-2 hour in second-level settling pond, and the precipitation of calcium carbonate of generation is sunken at the bottom of pond, and supernatant liquor enters Ammonia blowing-out tower through sewer line.
(4) after the trade effluent liquid adjusting PH with base that step (3) processes, enter Ammonia blowing-out tower through sewer line, react after 3-8 hour, stripping ammonia out enters recovery ammonia tower after pipeline is collected.
In above-mentioned steps, regulate pH to 10 ~ 12, stripping temperature 40 ~ 50 DEG C.
(5) trade effluent processed through step (4) enters subsequent wastewater treatment system, and ammonia enters recovery ammonia tower, take dilute sulphuric acid as ammonia absorption liquid, reclaim(ed) sulfuric acid ammonium.
Trade effluent of the present invention is preferably the ammonium sulfate waste water of high density.
Technical solution of the present invention significantly can reduce sulfate radical and ammonia nitrogen concentration in trade effluent, is particularly useful for the trade effluent containing high concentration sulphate and ammonia nitrogen.The introducing of carbonate of the present invention achieves following unforeseeable effect:
1, compared with conventional precipitation method, lime consumption is few, avoid a large amount of feeding lime cause remaining a large amount of calcium ion in waste water thus solve the calcium sulfate scaling blocking subsequent processing device and pipeline that conventional precipitation method faces, cause resistance to mass transfer, increase a difficult problem for operating load.
2, the introducing of carbonate, because carbonate and calcium ion can in conjunction with the precipitation of calcium carbonate generating more indissoluble, therefore substantially reduce the number calcium ion concn residual in waste water, simultaneously, carbonate and the calcium sulfate generation replacement(metathesis)reaction of part in slightly soluble state, reduce calcium ion concn residual in waste water further.
3, the sulfate radical intermediate processing by improving, fill up the blank of ammonium sulfate wastewater treatment, make should not carry out Biochemical method because of excessive concentration, and not easily use because concentration is too low the sulfate of ammoniac waste water of the recovery process process such as evaporation, decrease temperature crystalline to be able to effective process.
4, ammonia aeration efficiency is improved, because calcium ion concn remaining in waste water reduces greatly, the fouling and clogging problem of ammonia aeration e-quipment and pipe is solved, and therefore the carbonated drink resistance to mass transfer of ammonia aeration reduces, power consumption and heat exhaustion reduce, and running cost reduces.
5, the dosage of calcium lime powder looks SO in waste water
4 2-mass concentration and determine, the dosage of the sodium carbonate mass concentration of calcium lime powder depending on adding, suitable dosage and the use cost added than not only saving medicament, and be more conducive to generating calcium sulfate precipitation and this precipitation of carbonic acid, avoid equipment pipe fouling and clogging problem while maximized reduction sulfate radical in waste water concentration.
6, process for treating industrial waste water of the present invention, can be used for the process modification that existing use conventional precipitation method removes the sewage work of sulfate radical, only need increase replacement(metathesis)reaction pond and can improve wastewater treatment and solve scale problems, therefore have broad application prospects.
In order to the treatment process of the present invention to trade effluent is intuitively described, with reference to accompanying drawing 1, be process flow diagram of the present invention.
Accompanying drawing explanation
Accompanying drawing 1 industrial wastewater treatment scheme of the present invention
Embodiment:
Below will further illustrate the present invention by specific embodiment, but it should be appreciated by those skilled in the art that the specific embodiment of the invention and do not limit the present invention in any way, and take up an official post on basis of the present invention and how all fall within scope with replacement.
The simultaneous test of the conventional precipitation treatment method of embodiment 1 and treatment process of the present invention
The ammonium sulfate waste water produced with certain pharmacy corporation is subjects, test is divided into two groups, be respectively control group and test group, control group employing " conventional precipitation, ammonia aeration, recovery ammonia " treatment process, test group adopts " primary precipitation, replacement(metathesis)reaction, two-stage precipitation, ammonia aeration, recovery ammonia " of the present invention treatment process, and comparative test result is in table 1
Table 1: comparative test result contrasts
By table 1 data, can draw the following conclusions:
Under the prerequisite that the added amount of chemical total mass of two groups is identical, namely control group calcium lime powder consumption is and SO in waste water
4 2-mass concentration ratio be 1.93, experimental group calcium lime powder consumption is and SO in waste water
4 2-mass concentration ratio be 1.28, sodium carbonate amount is be 0.5 with the mass concentration ratio of calcium lime powder, and experimental group is to SO
4 2-clearance higher than control group 15.2%, experimental group is to NH
3-N clearance is higher than control group 3.2%.Therefore, experimental group is better to the treatment effect of ammonium sulfate waste water under the prerequisite not increasing medicament usage quantity.
The pilot plant test of embodiment 2 the method for the invention process ammonium sulfate waste water
Get certain chemical enterprise ammonium sulfate waste water and carry out pilot plant test, this waste water SO
4 2-concentration is 5500mg/L, NH
3-N concentration is 2650mg/L, COD concentration be 4232mg/L, pH is 3.0, and process of the test is as follows:
Ammonium sulfate waste water enters primary clarifier, adds calcium lime powder 6.5g/L, opens stirring and reacts, and react after 20 minutes and close stirring, staticly settle 1 hour, the calcium sulfate precipitation of generation is sunken at the bottom of pond, and supernatant liquor enters replacement(metathesis)reaction pond; In replacement(metathesis)reaction pond, add sodium carbonate 3.5g/L, open stirring and carry out replacement(metathesis)reaction, react after 30 minutes and close stirring, waste water enters second-level settling pond, staticly settle 1 hour, the precipitation of calcium carbonate of generation is sunken at the bottom of pond, enters Ammonia blowing-out tower after supernatant liquor liquid adjusting PH with base to 11; Stripping temperature is 50 DEG C, and after stripping reacts 4 hours, stripping ammonia out enters recovery ammonia tower reclaim(ed) sulfuric acid ammonium after pipeline is collected, and the trade effluent of process detects.SO is carried out in the water outlet of getting each processing unit
4 2-concentration, NH
3the detection of-N concentration and COD concentration, result is as follows:
Claims (10)
1. a treatment process for trade effluent, is characterized in that comprising the steps: primary precipitation, replacement(metathesis)reaction, two-stage precipitation, ammonia aeration, recovery ammonia.
2. the treatment process of trade effluent as claimed in claim 1, is characterized in that adding precipitation agent in described primary precipitation, adds displacer in described replacement(metathesis)reaction.
3. the treatment process of trade effluent as claimed in claim 2, is characterized in that described precipitation agent is calcium lime powder or milk of lime, and described displacer is sodium carbonate, magnesiumcarbonate, the one of zinc carbonate or its combination.
4. the treatment process of trade effluent as claimed in claim 3, it is characterized in that described precipitation agent is calcium lime powder, described displacer is sodium carbonate.
5. the treatment process of the trade effluent as described in as arbitrary in claim 1-4, is characterized in that the device of the treatment process implementing described trade effluent is made up of primary clarifier, replacement(metathesis)reaction pond, second-level settling pond, Ammonia blowing-out tower, recovery ammonia tower.
6. the treatment process of trade effluent as claimed in claim 5, is characterized in that comprising the following steps:
(1) trade effluent enters primary clarifier through sewer line, adds calcium lime powder, opens stirring and reacts, react after 10-30 minute and close stirring, staticly settle 1 ~ 2 hour, the calcium sulfate precipitation of generation is sunken at the bottom of pond, and supernatant liquor enters replacement(metathesis)reaction pond through sewer line;
(2) trade effluent processed through step (1) enters replacement(metathesis)reaction pond, sodium carbonate is added in replacement(metathesis)reaction pond, open stirring and carry out replacement(metathesis)reaction, react after 15-40 minute and close stirring, trade effluent enters second-level settling pond through sewer line;
(3) trade effluent processed through step (2) staticly settles 1-2 hour in second-level settling pond, and the precipitation of calcium carbonate of generation is sunken at the bottom of pond, and supernatant liquor enters Ammonia blowing-out tower through sewer line;
(4) after the trade effluent liquid adjusting PH with base that step (3) processes, enter Ammonia blowing-out tower through sewer line, react after 3-8 hour, stripping ammonia out enters recovery ammonia tower after pipeline is collected;
(5) trade effluent processed through step (4) enters subsequent wastewater treatment system, and ammonia enters recovery ammonia tower, take dilute sulphuric acid as ammonia absorption liquid, reclaim(ed) sulfuric acid ammonium.
7. the treatment process of trade effluent as claimed in claim 6, is characterized in that the dosage of calcium lime powder in step (1) looks SO in waste water
4 2-mass concentration and determine, SO in calcium lime powder and waste water
4 2-mass concentration ratio be 1.10-1.80.
8. the treatment process of trade effluent as claimed in claim 6, it is characterized in that the mass concentration of calcium lime powder of the dosage of sodium carbonate in step (2) depending on adding, the mass concentration ratio of sodium carbonate and calcium lime powder is 0.5-1.0.
9. the treatment process of trade effluent as claimed in claim 6, is characterized in that regulating pH to 10 ~ 12, stripping temperature 40 ~ 50 DEG C in step (4).
10. the treatment process of the trade effluent as described in as arbitrary in claim 1-9, is characterized in that trade effluent is ammonium sulfate waste water.
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| CN201510001370.1A CN104591435B (en) | 2015-01-04 | 2015-01-04 | A kind of processing method of industrial wastewater |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105174287A (en) * | 2015-09-09 | 2015-12-23 | 江西玛德精细化学工业有限公司 | Method for recovering ammonia and coproducing calcium sulfate through lime neutralization of T acid mother liquid |
| CN105541672A (en) * | 2015-12-15 | 2016-05-04 | 浙江闰土研究院有限公司 | Clean production process of dye dispersant MF |
| CN108328789A (en) * | 2018-01-30 | 2018-07-27 | 成都信息工程大学 | A kind of synchronous method for removing sulfate and ammonia nitrogen in smelting wastewater |
| CN111423025A (en) * | 2020-05-22 | 2020-07-17 | 河南心连心化学工业集团股份有限公司 | Treatment device and treatment method for shift condensate decarburization and by-product ammonium sulfate |
| CN112225228A (en) * | 2020-09-29 | 2021-01-15 | 长沙中硅环保科技有限公司 | Method and system for preparing ammonium sulfate by using cement kiln tail waste gas and phosphogypsum |
| CN112777707A (en) * | 2019-11-06 | 2021-05-11 | 江苏普源化工有限公司 | Treatment method of wastewater containing sodium sulfate |
| CN112777708A (en) * | 2019-11-06 | 2021-05-11 | 江苏普源化工有限公司 | Treatment method of salicylic acid production wastewater |
| CN114195290A (en) * | 2021-12-13 | 2022-03-18 | 唐山三友集团兴达化纤有限公司 | Method for retarding scaling in viscose fiber wastewater treatment process by using purified sodium hydrosulfide byproduct |
| CN115259500A (en) * | 2022-08-18 | 2022-11-01 | 中原环保股份有限公司 | Method for treating ammonium nitrate industrial wastewater |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105174287A (en) * | 2015-09-09 | 2015-12-23 | 江西玛德精细化学工业有限公司 | Method for recovering ammonia and coproducing calcium sulfate through lime neutralization of T acid mother liquid |
| CN105541672A (en) * | 2015-12-15 | 2016-05-04 | 浙江闰土研究院有限公司 | Clean production process of dye dispersant MF |
| CN105541672B (en) * | 2015-12-15 | 2017-06-20 | 浙江闰土研究院有限公司 | A kind of process for cleanly preparing of dye dispersant MF |
| CN108328789A (en) * | 2018-01-30 | 2018-07-27 | 成都信息工程大学 | A kind of synchronous method for removing sulfate and ammonia nitrogen in smelting wastewater |
| CN112777707A (en) * | 2019-11-06 | 2021-05-11 | 江苏普源化工有限公司 | Treatment method of wastewater containing sodium sulfate |
| CN112777708A (en) * | 2019-11-06 | 2021-05-11 | 江苏普源化工有限公司 | Treatment method of salicylic acid production wastewater |
| CN111423025A (en) * | 2020-05-22 | 2020-07-17 | 河南心连心化学工业集团股份有限公司 | Treatment device and treatment method for shift condensate decarburization and by-product ammonium sulfate |
| CN111423025B (en) * | 2020-05-22 | 2023-07-28 | 河南心连心化学工业集团股份有限公司 | Treatment device and treatment method for by-product ammonium sulfate in condensate decarburization |
| CN112225228A (en) * | 2020-09-29 | 2021-01-15 | 长沙中硅环保科技有限公司 | Method and system for preparing ammonium sulfate by using cement kiln tail waste gas and phosphogypsum |
| CN114195290A (en) * | 2021-12-13 | 2022-03-18 | 唐山三友集团兴达化纤有限公司 | Method for retarding scaling in viscose fiber wastewater treatment process by using purified sodium hydrosulfide byproduct |
| CN115259500A (en) * | 2022-08-18 | 2022-11-01 | 中原环保股份有限公司 | Method for treating ammonium nitrate industrial wastewater |
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| CN104591435B (en) | 2016-08-17 |
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