CN105366862A - Treatment method of sulfur acid-containing dye wastewater - Google Patents
Treatment method of sulfur acid-containing dye wastewater Download PDFInfo
- Publication number
- CN105366862A CN105366862A CN201510799342.9A CN201510799342A CN105366862A CN 105366862 A CN105366862 A CN 105366862A CN 201510799342 A CN201510799342 A CN 201510799342A CN 105366862 A CN105366862 A CN 105366862A
- Authority
- CN
- China
- Prior art keywords
- treatment
- ammonium sulfate
- treatment process
- value
- treatment solution
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Abstract
The present invention discloses a treatment method of sulfur acid-containing dye wastewater, high-quality and stable-storage ammonium sulfate can be obtained by ammonia treatment, active carbon decoloration and impurity removal, pH adjustment with an acid, concentration and crystallization, separation and a series of means of wastewater, the processed wastewater is low in chromaticity, and small in TOC (total organic carbon) value, and can be recycled, and zero discharge of the wastewater can be achieved.
Description
Technical field
The present invention relates to a kind for the treatment of process of sulfur acid waste water from dyestuff.
Background technology
The sulfur acid waste water of a large amount of high COD produced in DYE PRODUCTION process, high toxicity and potential carinogenicity adopts traditional treatment process usually, namely adopts the method for lime or carbide slag neutralization precipitation, but can produce a large amount of dangerous solid waste, influence ecological environment.And the harmless treatment to calcium sulfate, a series of problems such as current ubiquity investment is large, cost is high, technology is difficult.
CN102826673A discloses the cleaning method to a kind of dyestuffs industries acid waste water, this method solves calcium sulfate waste residues handling problems.But the ammonium sulfate long-term exposure that the method obtains can cause degradation in atmosphere, be unfavorable for storage or strict to condition of storage requirement.
Summary of the invention
The invention provides a kind for the treatment of process of sulfur acid waste water from dyestuff, comprise: sulfur acid waste water from dyestuff is adjusted a series of means such as pH, condensing crystal, separation through ammonia treatment, decolorization and impurity removal by active carbon, acid, obtain that quality is high, the ammonium sulfate of storage-stable, and treated waste water from dyestuff colourity is low, TOC value is little, reusable edible, realizes wastewater zero discharge.
The treatment process of sulfur acid waste water from dyestuff of the present invention comprises:
(1) ammonia treatment: collect vitriolated waste water from dyestuff, under agitation adds ammonia adjust ph to 8.5 ~ 12, obtains treatment solution;
(2) decolorization and impurity removal by active carbon: add decolorization and impurity removal by active carbon in step (1) described treatment solution, filters and removes gac, obtain ammonium sulfate filtrate;
(3) pH is regulated: in step (2) described ammonium sulfate filtrate, add sulfuric acid adjust ph to 2 ~ 7, obtain treatment solution;
(4) condensing crystal: the described treatment solution of step (3), through concentrated, crystallization, separation, obtains ammonium sulfate.
In order to reduce processing cost, improve treatment effect, oxidation treatment step can be increased: add oxidizing in step (3) gained treatment solution in above-mentioned steps (3) and step (4), then pH to 5 ~ 7 are adjusted with ammonia, gained oxidation solution after filtration, obtain ammonium sulfate filtrate, and then carry out the step of step (4).
More specifically, described method comprises:
(A) ammonia treatment: collect vitriolated waste water from dyestuff, under agitation adds ammonia adjust ph to 8.5 ~ 12, obtains treatment solution;
(B) decolorization and impurity removal by active carbon: add gac in step (A) described treatment solution, filters and removes gac, obtain ammonium sulfate filtrate;
(C) pH is regulated: in step (B) described ammonium sulfate filtrate, add sulfuric acid adjust ph to 2 ~ 7, obtain treatment solution;
(D) removing impurities by oxidation: add oxygenant and be oxidized 1 ~ 6 hour in step (C) described treatment solution at 20 ~ 70 DEG C, then adjusts pH to 5 ~ 7 with ammonia, filters to obtain ammonium sulfate filtrate;
(E) concentrated, crystallization: the described ammonium sulfate filtrate of step (D), through concentrated, crystallization, separation, obtains ammonium sulfate.
In above-mentioned steps (1) or (A) described acid waste water, sulfuric acid content is preferably 1 ~ 40%.
The pH value of above-mentioned steps (1) or (A) described treatment solution is preferably adjusted to 8.5 ~ 9.
The quality consumption of above-mentioned steps (2) or (B) described gac is preferably 0.05 ~ 2% for the treatment of solution quality.
Above-mentioned steps (2) or (B) middle bleaching temperature are preferably 20 ~ 70 DEG C, more preferably 25-45 DEG C, more preferably 35-40 DEG C.
Above-mentioned steps (2) or (B) middle decolorization and impurity removal by active carbon time are preferably more than 0.25 hour, are more preferably 2 ~ 4 hours.
Above-mentioned steps (3) or (C) described sulfuric acid can be the low COD Waste Sulfuric Acid in DYE PRODUCTION, or dilute sulphuric acid.
The pH value of above-mentioned steps (3) described treatment solution is preferably adjusted to 5 ~ 7.
The pH value of above-mentioned steps (C) described treatment solution is preferably 2 ~ 5.
Above-mentioned steps (D) described oxygenant be preferably in clorox, hydrogen peroxide, dioxide peroxide, ozone, sodium chlorate, Fenton reagent one or more, its quality consumption is preferably 0.02 ~ 1% of neutralizer quality.
In above-mentioned steps (2) or step (D), after filtering, the colourity of gained filtrate is preferably less than 20 times of (extension rate method measured value), total organic carbon (TOC) values and is preferably less than 60mg/L.
In above-mentioned steps (4) or step (E), the concentrated water of condensation produced can be back in DYE PRODUCTION, the crystalline mother solution produced after isolation of crystalline in crystallisation step can be got back in concentrated, Crystallization Procedure and go, see Fig. 1, Fig. 3, or get back to the impurity going to remove enrichment in decolorization and impurity removal by active carbon operation, see Fig. 2, Fig. 4, crystallization gained ammonium sulfate wet product directly as product, also drying can obtain the lower product of water content further.
Described sulfur acid waste water from dyestuff can be sulfur acid waste water from dyestuff in waste water from dyestuff storage tank after the water yield homogenizes, also can be mother liquid coming in DYE PRODUCTION and washing water etc.
In concentrated, crystallisation step of the present invention, concentratedly can adopt that conventional single-action is concentrated, Multi-effect concentration, the mode that vapor recompression also can be adopted concentrated is as MVR etc., and concentrated water of condensation can be back to use in DYE PRODUCTION further and go.
Method of the present invention, its advantage is mainly reflected in: the circulation comprehensive that present invention achieves waste water from dyestuff utilizes, waste water adjusts a series of means such as pH, (be optionally oxidized), concentrated, crystallization, separation through ammonia treatment, decolorization and impurity removal by active carbon, acid, the recycling condensing water that concentration produces is in DYE PRODUCTION, not only avoid the secondary pollution of calcium sulfate waste residues, but also achieve the cleaner production of energy-saving and emission-reduction, environmental protection.Gained ammonium sulfate quality meets national standard, can directly as commodity, and it is high to expose aerial stability, requires low to condition of storage, saves storage cost.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of a kind of embodiment of the treatment process of sulfur acid waste water from dyestuff of the present invention.
Fig. 2 is the schematic flow sheet of the another kind of embodiment of the treatment process of sulfur acid waste water from dyestuff of the present invention.
Fig. 3 is the schematic flow sheet of the another kind of embodiment of the treatment process of sulfur acid waste water from dyestuff of the present invention.
Fig. 4 is the schematic flow sheet of the another kind of embodiment of the treatment process of sulfur acid waste water from dyestuff of the present invention.
Embodiment
Below in conjunction with specific embodiment, the present invention is conducted further description, but protection scope of the present invention is not limited in this.
Embodiment 1
Technical process is see Fig. 1, in aftertreatment pot, drop into sulfur acid waste water from dyestuff (detect data: sulfuric acid content 8%, colourity 400 times, TOC value 1500mg/L), under agitation add liquefied ammonia adjust ph to 8.5 ~ 9, the gac adding 0.5% weight relative to waste water from dyestuff total amount carries out decolouring removal of impurities, bleaching temperature 35 ~ 40 DEG C, stir 2.5 hours, sampling filtering detects, and detects data: colourity 4 times, TOC value 30mg/L, decolouring terminates, filtering separation gac waste residue, active breeze directly burns and carries out harmless treatment, obtains ammonium sulfate filtrate.Ammonium sulfate filtrate sulfuric acid adjust ph to 6 ~ 7, then concentrate, the concentrated recycling condensing water produced is in DYE PRODUCTION, crystallization, filtration, obtain wet product ammonium sulfate, the crystalline mother solution that filtration produces is got back in enrichment process and is gone, and wet product ammonium sulfate carries out drying further, and the ammonium sulfate product obtained meets national standard.
Embodiment 2
Technical process is see Fig. 3, in aftertreatment pot, drop into 63 DISPERSE Violet 63 93:1 waste water (detect data: sulfuric acid content 10%, colourity 800 times, TOC value 2000mg/L), under agitation add liquefied ammonia to process, adjust ph 8.5 ~ 9, the gac adding 0.5% weight relative to waste water from dyestuff total amount carries out decolouring removal of impurities, bleaching temperature 40 ~ 45 DEG C, stirs 2.5 hours, and sampling filtering detects, detect data: colourity 10 times, TOC value 65mg/L, decolouring terminates, and filtering separation gac waste residue, active breeze directly burns and carries out harmless treatment.Obtain ammonium sulfate filtrate.Ammonium sulfate filtrate sulfuric acid adjust ph to 3 ~ 5, then add the hydrogen peroxide of 0.2% weight relative to ammonium sulfate filtrate, oxidizing temperature controls at 40 ~ 50 DEG C, oxidization time 2.5 hours, after oxidation terminates, and sampling analysis, colourity 4 times, TOC value 20mg/L.Then use liquefied ammonia adjust ph to 6 ~ 7, filter, gained filtrate concentrates.The concentrated recycling condensing water produced is in DYE PRODUCTION, and crystallization, filtration, obtain wet product ammonium sulfate.The crystalline mother solution that filtration produces is got back in enrichment process and is gone, and the wet product ammonium sulfate obtained carries out drying further, and the ammonium sulfate product obtained meets national standard.
Embodiment 3
Technical process is see Fig. 1, in aftertreatment pot, drop into DISPERSE ORANGE 30 200 288 waste water (detect data: sulfuric acid content 13%, colourity 800 times, TOC value 1400mg/L), under agitation add liquefied ammonia to process, adjust ph 8.5 ~ 9, add the gac of 0.5% weight relative to waste water from dyestuff total amount, carry out decolouring removal of impurities, bleaching temperature 40 ~ 45 DEG C, stir 2.5 hours, sampling filtering detects, and detects data: colourity 8 times, TOC value 43mg/L, and decolouring terminates, filtering separation gac waste residue, active breeze directly burns and carries out harmless treatment.Obtain ammonium sulfate filtrate.Ammonium sulfate filtrate sulfuric acid adjust ph to 6 ~ 7, then concentrate.The concentrated recycling condensing water produced is in DYE PRODUCTION.Crystallization, filtration, obtain wet product ammonium sulfate.The crystalline mother solution that filtration produces is got back in enrichment process and is gone, and the wet product ammonium sulfate obtained carries out drying further, and the ammonium sulfate product obtained meets national standard.
Embodiment 4
Technical process is see Fig. 1, in aftertreatment pot, drop into Disperse Blue-60 waste water (detect data: sulfuric acid content 36%, colourity 500 times, TOC value 200mg/L), under agitation add liquefied ammonia to process, adjust ph to 8.5 ~ 9, the gac adding 0.2% weight relative to waste water from dyestuff total amount carries out decolouring removal of impurities, bleaching temperature 40 ~ 45 DEG C, stirs 2.5 hours, and sampling filtering detects, detect data: colourity 4 times, TOC value 23mg/L, decolouring terminates, and filtering separation gac waste residue, active breeze directly burns and carries out harmless treatment.Obtain ammonium sulfate filtrate.Ammonium sulfate filtrate sulfuric acid adjust ph to 6 ~ 7, then concentrate.The concentrated recycling condensing water produced is in DYE PRODUCTION.Crystallization, filtration, obtain wet product ammonium sulfate.The crystalline mother solution that filtration produces is got back in enrichment process and is gone, and the wet product ammonium sulfate obtained carries out drying further, and the ammonium sulfate product obtained meets national standard.
Detect data
According to standard GB/T 535-1995, carry out mass analysis to the ammonium sulfate product that embodiment 1 ~ 4 obtains respectively, result is as following table 1:
Table 1
As seen from the above table, the ammonium sulfate product obtained according to embodiment 1 ~ 4 meets national standard.
Embodiment 5
Technical process is see Fig. 1, in aftertreatment pot, drop into waste water from dyestuff (detect data: sulfuric acid content 8%, colourity 1000 times, TOC value 1500mg/L), under agitation add liquefied ammonia to process, adjust ph 8.5 ~ 9.0, the gac adding 0.5% weight relative to waste water from dyestuff total amount carries out decolouring removal of impurities, bleaching temperature 45 ~ 50 DEG C, stir 2.5 hours, sampling filtering detects, detect data: colourity 8 times, TOC value 25mg/L (the results are shown in table 3), decolouring terminates, filtering separation gac waste residue, active breeze directly burns and carries out harmless treatment.Obtain ammonium sulfate filtrate.Ammonium sulfate filtrate sulfuric acid adjust ph 6.0 ~ 7.0, then concentrates, and the concentrated recycling condensing water produced is in DYE PRODUCTION.Crystallization, filtration, obtain wet product ammonium sulfate, and the crystalline mother solution that filtration produces is got back in enrichment process and gone, and the wet product ammonium sulfate obtained carries out drying further, and the ammonium sulfate product obtained meets national standard.
Comparative example 1
In and still in insert waste water from dyestuff (detect data: sulfuric acid content 8%, colourity 400 times, TOC value 1500mg/L), under agitation, add liquefied ammonia and carry out neutralization reaction to pH value 6.0 ~ 7.0, the gac of 0.5% weight is added relative to waste water from dyestuff total amount, carry out decolouring removal of impurities, bleaching temperature 45 ~ 50 DEG C, stir 2.5 hours, sampling filtering detects, detect data: colourity 64 times, TOC value 150mg/L, continue to add gac 0.25% and carry out decolouring insulation 1 hour, detected result is: colourity 16 times, TOC value is 80mg/L, decolouring terminates, filtering separation gac waste residue, obtain ammonium sulfate filtrate.Ammonium sulfate filtrate is through concentrated, crystallization, the concentrated recycling condensing water produced makes water at the bottom of Dyestuff synthesis or filter cake washing water, as finished product after the further drying of ammonium sulfate wet product, the crystalline mother solution that filtration produces then returns concentration systems or partly returning decolouring system carries out circular treatment, and the active breeze of filtering directly can burn and carry out harmless treatment.
Detect data
According to standard GB/T 535-1995, carry out mass analysis to the ammonium sulfate product that embodiment 5 and comparative example 1 obtain respectively, result is as following table 2:
Table 2
As seen from the above table, product in comparative example 1 exposes for a long time and causes degradation in atmosphere, and the ammonium sulfate quality adopting processing method provided by the invention to obtain meets national standard, and it is higher to expose aerial stability, require low to condition of storage, save storage cost.
Comparative example 2
Keep other conditions in embodiment 5 constant, in ammonia treating step, regulate pH to be respectively 4 ~ 5,5 ~ 6,7 ~ 8,9 ~ 10, after charcoal absorption decolouring, detect colourity and TOC value.Result is as following table 3:
Table 3
| PH | 4～5 | 6～7 | 7～8 | 8.5～9 | 9～10 |
| Colourity/doubly | 64 | 32 | 16 | 8 | 8 |
| TOC mg/L | 218 | 122 | 75 | 25 | 22 |
As can be seen from the above table, along with the increase of pH value, the colourity of ammoniumsulphate soln and TOC value decline.PH value has very excellent effect when being more than 8.5.
Claims (10)
1. a treatment process for sulfur acid waste water from dyestuff, described method comprises:
(1) ammonia treatment: collect vitriolated waste water from dyestuff, under agitation adds ammonia adjust ph to 8.5 ~ 12, obtains treatment solution;
(2) decolorization and impurity removal by active carbon: add decolorization and impurity removal by active carbon in step (1) treatment solution, filters and removes gac, obtain ammonium sulfate filtrate;
(3) pH is regulated: in step (2) ammonium sulfate filtrate, add sulfuric acid adjust ph to 2 ~ 7, obtain treatment solution;
(4) condensing crystal: step (3) treatment solution, through concentrated, crystallization, separation, obtains ammonium sulfate.
2. treatment process as claimed in claim 1, it is characterized in that also comprising oxide treatment between step (3) and step (4): add oxidizing in step (3) gained treatment solution, then ammonia adjust ph to 5 ~ 7 are used, filter to obtain ammonium sulfate filtrate, then carry out the step of step (4).
3. treatment process as claimed in claim 1, is characterized in that the pH value of step (3) treatment solution is adjusted to 5 ~ 7.
4. treatment process as claimed in claim 1 or 2, is characterized in that the pH value of step (1) treatment solution is adjusted to 8.5 ~ 9.
5. treatment process as claimed in claim 1 or 2, is characterized in that step (2) bleaching time is 2 ~ 4 hours.
6. treatment process as claimed in claim 1 or 2, is characterized in that the sulfuric acid that the adjust ph in step (3) uses is the low COD Waste Sulfuric Acid in DYE PRODUCTION, or dilute sulphuric acid.
7. treatment process as claimed in claim 1 or 2, is characterized in that the crystalline mother solution obtained in step (4) turns back in concentration crystallization step or decolorization and impurity removal by active carbon step.
8. the method for claim 1, is characterized in that: the extension rate method measured value of the colourity of ammonium sulfate filtrate described in step (2) is less than 20 times, total organic carbon TOC value is less than 60mg/L.
9. treatment process as claimed in claim 2, is characterized in that: the extension rate method measured value of filtering the colourity of the ammonium sulfate filtrate of gained after oxide treatment is less than 20 times, total organic carbon TOC value is less than 60mg/L.
10. treatment process as claimed in claim 2, is characterized in that the pH value of step (3) treatment solution is 2 ~ 5; Preferably, described oxygenant be selected from clorox, hydrogen peroxide, dioxide peroxide, ozone, sodium chlorate, Fenton reagent one or more.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510799342.9A CN105366862A (en) | 2015-11-18 | 2015-11-18 | Treatment method of sulfur acid-containing dye wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510799342.9A CN105366862A (en) | 2015-11-18 | 2015-11-18 | Treatment method of sulfur acid-containing dye wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105366862A true CN105366862A (en) | 2016-03-02 |
Family
ID=55369573
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510799342.9A Pending CN105366862A (en) | 2015-11-18 | 2015-11-18 | Treatment method of sulfur acid-containing dye wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105366862A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107382411A (en) * | 2017-07-07 | 2017-11-24 | 湖北得力新材料有限公司 | A kind of method of the comprehensive utilization of spent acid containing potassium caused by sulfonation para-ester or the production of G salt |
| CN112158975A (en) * | 2020-08-19 | 2021-01-01 | 九江富达实业有限公司 | Recycling method of anthraquinone dye and intermediate wastewater |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0396790A1 (en) * | 1989-05-09 | 1990-11-14 | Bayer Antwerpen N.V. | Process for the removal of nitrate and organic pollutants from effluents |
| CN101177284A (en) * | 2007-11-02 | 2008-05-14 | 北京化工大学 | Method for reclaiming sulfuric ammonium and ferric oxide from sulfuric acid pickling waste fluid |
| CN102826673A (en) * | 2011-06-15 | 2012-12-19 | 浙江龙盛化工研究有限公司 | Cleaning treatment method of dying industrial acidic wastewater |
| CN103130370A (en) * | 2013-03-12 | 2013-06-05 | 浙江迪邦化工有限公司 | Dye acidic waste water treatment method and device |
| CN103214116A (en) * | 2013-03-15 | 2013-07-24 | 浙江闰土股份有限公司 | Recycling method of sulfuric acid-containing wastewater from disperse dye production |
-
2015
- 2015-11-18 CN CN201510799342.9A patent/CN105366862A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0396790A1 (en) * | 1989-05-09 | 1990-11-14 | Bayer Antwerpen N.V. | Process for the removal of nitrate and organic pollutants from effluents |
| CN101177284A (en) * | 2007-11-02 | 2008-05-14 | 北京化工大学 | Method for reclaiming sulfuric ammonium and ferric oxide from sulfuric acid pickling waste fluid |
| CN102826673A (en) * | 2011-06-15 | 2012-12-19 | 浙江龙盛化工研究有限公司 | Cleaning treatment method of dying industrial acidic wastewater |
| CN103130370A (en) * | 2013-03-12 | 2013-06-05 | 浙江迪邦化工有限公司 | Dye acidic waste water treatment method and device |
| CN103214116A (en) * | 2013-03-15 | 2013-07-24 | 浙江闰土股份有限公司 | Recycling method of sulfuric acid-containing wastewater from disperse dye production |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107382411A (en) * | 2017-07-07 | 2017-11-24 | 湖北得力新材料有限公司 | A kind of method of the comprehensive utilization of spent acid containing potassium caused by sulfonation para-ester or the production of G salt |
| CN112158975A (en) * | 2020-08-19 | 2021-01-01 | 九江富达实业有限公司 | Recycling method of anthraquinone dye and intermediate wastewater |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104355443B (en) | A kind for the treatment of process of the waste water containing unsymmetrical dimethyl hydrazine | |
| CN105130854B (en) | A kind of improved H acid production processes | |
| CN106495404A (en) | A kind of processing method of the high salinity cupric organic wastewater of highly acidity | |
| CN110835199A (en) | Electroplating wastewater zero-discharge treatment system and treatment process thereof | |
| CN108249707B (en) | Treatment system and treatment method for fluorine-containing nitrate nitrogen-containing industrial wastewater | |
| CN103979705B (en) | Method for recovering potassium nitrate from anthraquinone dye alkali wastewater | |
| CN111807589A (en) | Method for recycling high-grade ammonium chloride from high-ammonia nitrogen wastewater in coal chemical industry | |
| CN105366862A (en) | Treatment method of sulfur acid-containing dye wastewater | |
| CN105565566B (en) | A kind of method of Fenton processing 6- nitro -1,2,4- acid oxysome waste water co-production sodium sulphate | |
| CN105110515B (en) | A kind of processing method of DSD acid waste water | |
| WO2016042901A1 (en) | Biological treatment method and biological treatment device | |
| CN110590074A (en) | High-concentration pickle wastewater treatment process | |
| CN101955230B (en) | Preparation method of potassium ferrate | |
| CN104860455A (en) | Methylene dithiocyanate wastewater treatment method | |
| CN102001721B (en) | Method for treating ammonia nitrogen wastewater | |
| CN107381877B (en) | Nitromethane high-salinity wastewater treatment method | |
| CN111204924B (en) | Zero-discharge treatment method for production wastewater of ethyl chloride | |
| CN109607945B (en) | Method for improving biochemical efficiency of wastewater in photovoltaic and electronic industries | |
| CN109336330B (en) | Efficient treatment method of rubber accelerator wastewater | |
| CN107473488B (en) | Treatment method of para-ester production wastewater | |
| CN113562913A (en) | Treatment method of hydrazine hydrate production wastewater | |
| CN108275846B (en) | Anthraquinone wastewater treatment method | |
| CN108911415A (en) | Recycling processing method containing Vulkacit M wastewater | |
| CN111362487A (en) | Sewage treatment method | |
| CN104609640B (en) | Comprehensive treatment method of sebacic acid production wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160302 |
|
| RJ01 | Rejection of invention patent application after publication |