CN103408177A - Method for treating and recycling waste water in anthranilic acid production technology - Google Patents
Method for treating and recycling waste water in anthranilic acid production technology Download PDFInfo
- Publication number
- CN103408177A CN103408177A CN2013103351630A CN201310335163A CN103408177A CN 103408177 A CN103408177 A CN 103408177A CN 2013103351630 A CN2013103351630 A CN 2013103351630A CN 201310335163 A CN201310335163 A CN 201310335163A CN 103408177 A CN103408177 A CN 103408177A
- Authority
- CN
- China
- Prior art keywords
- adsorption column
- desorption
- resin
- waste water
- polymeric adsorbent
- 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.)
- Granted
Links
Landscapes
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Water Treatment By Sorption (AREA)
Abstract
The invention discloses a method for treating and recycling waste water in an anthranilic acid production technology. Through the adoption of the method provided by the invention, waste water in the anthranilic acid production technology can be treated, and recycled organic substances can be directly subjected to cyclic utilization; the CODCr being about 24000 mg/L of waste water before treatment is reduced to 80 mg/L below after treatment to reach the national-level emission standard; coarse sodium chloride salt can be recycled; resin is subjected to desorption and regeneration by using 4-6% of dilute sodium hydroxide solution or dilute hydrochloric acid, and a desorption solution can be taken as raw materials to be input in the acidizing step or degrading step of the original production technology, so that the product quality is not affected, 99% of anthranilic acid and phthalimide in the waste water can be recycled, and distilled effluent can be utilized repeatedly; waste water can be treated while the waste recycling can be realized.
Description
Technical field
The present invention relates to a kind ofly will take Tetra hydro Phthalic anhydride and urea and obtain the processing wastewater (CODc that anthranilic acid was produced as raw material generates phthalic imidine after by degraded, acidifying
rBe 23000～24000mg/L) improvement and reclaim organic circulation utilization method.Particularly, be the organism anthranilic acid in processing wastewater, the recycle of phthalic imidine, realize simultaneously cleansing and recycling or the qualified discharge of waste water, finally realize improvement and the resource utilization thereof of o-amino benzoyl acid production process waste water.
Background technology
The synthetic route that present method was suitable for obtains phthalic imidine for take Tetra hydro Phthalic anhydride and excessive urea as starting raw material carries out amidation, after under alkaline condition, degrading with clorox again, obtain the o-amino benzoyl acid sodium-salt, after hcl acidifying, obtain anthranilic acid, cardinal principle is as follows:
1, amidation
2, degraded
3, acidifying
Adopt above-mentioned production technique, after hcl acidifying, centrifugation, will produce one waste water in technique, after washing, produce one waste water in addition, in two strands of water, all mainly contain unreacted phthalic imidine and product anthranilic acid, sodium chloride salt.Product per ton will produce waste water 15～18m
3, this waste water sorrel, CODc
rBe 23000～24000mg/L, wherein phthalic imidine is 7800～8100mg/L, the content of anthranilic acid is 6000～6500mg/L, sodium chloride content is 100～120g/L, because saltiness in waste water is higher, present treatment process be mainly after this processing wastewater concentrates as dangerous solidification disposal of waste, not only processing costs is higher, has also wasted wherein expensive phthalic imidine, anthranilic acid and sodium-chlor; Or adopt the ethyl acetate extraction method to reclaim, and the rate of recovery is 63% left and right only, and the ethyl acetate losing quantity is larger, and energy consumption is higher, therefore this processing wastewater does not have economic effective improvement method so far.
In the patents of invention such as Zhao Yuming (ZL200610041529.3), adopted weak-base ion-exchange resin or vinylbenzene-strong polar resin of divinylbenzene type, having proposed a kind ofly from mother liquor or waste water, reclaiming the method for anthranilic acid, is a kind ofly will take Tetra hydro Phthalic anhydride and urea and obtain the processing wastewater (CODc that anthranilic acid was produced as raw material generates phthalic imidine after by degraded, acidifying due to what the present invention relates to
rBe 23000～24000mg/L), contain a large amount of inorganic salt, therefore adopt the technique of ion-exchange absorption can't realize the resource utilization of anthranilic acid in waste water, phthalic imidine.
The patent of invention of the applications such as Meng Fanqiu (application number 201110073494.2) relates to a kind of from the methyl esters mother liquor waste water, reclaiming the preparation method of anthranilic acid, be produce the waste acid water that produces in the mother liquor waste water that produces in the methyl o-aminobenzoate process and asccharin production process mantoquita, alkali be molten through preparing, press filtration, decolouring, acid out, suction filtration, drying and obtain anthranilic acid, the method also can't realize a large amount of inorganic salt o-amino benzoyl acid production process waste water that contains the present invention is directed to.
Summary of the invention
The present invention is directed to the deficiencies in the prior art provides a kind of improvement and circulation utilization method of o-amino benzoyl acid production process waste water, and the technical scheme of employing is as follows:
A kind of improvement and circulation utilization method of o-amino benzoyl acid production process waste water comprise the following steps:
A) waste water is sorrel after processing after filtration, after with 1～2% diluted sodium hydroxide solution, regulating pH and be about 8, at 0～40 ℃, through the first adsorption column, obtains faint yellow transparent one-level absorption effluent, CODc with the flow of 1～2BV/h
r12000～14000mg/L, described the first adsorption column is filled with the Hypercrosslinked polystyrene of chemically modified-divinylbenzene polymeric adsorbent, it is standby that the first adsorption column is arranged in parallel the second adsorption column of the Hypercrosslinked polystyrene that another root is filled with chemically modified equally-divinylbenzene polymeric adsorbent, the first adsorption column and the second adsorption column treatment capacity are 18～20BV/ and criticize, and BV is the volume of adsorption column;
B) after the one-level absorption effluent of the first adsorption column in step a is about to 5 with 1～2% dilute hydrochloric acid adjusting pH, at 0～40 ℃, with the flow process of 1～2BV/h, be filled with the 3rd adsorption column of Hypercrosslinked polystyrene-divinylbenzene polymeric adsorbent, obtain water white secondary absorption water outlet, CODc
r800～1000mg/L; Described the 3rd adsorption column is arranged in parallel another root, and to be filled with equally the 4th adsorption column of Hypercrosslinked polystyrene-divinylbenzene polymeric adsorbent standby, and the 3rd adsorption column and the 4th adsorption column adsorption column treatment capacity are that 30～32BV/ criticizes;
C) the first adsorption column adsorb organic compound is near after saturated, replaces the first adsorption column to come into operation the second adsorption column, repeating step a, the first adsorption column after desorption alkali cleaning as standby adsorption column; Desorption alkali washing method are: by adsorb organic compound in described the first adsorption column near saturated polymeric adsorbent with dilute hydrochloric acid 2～3BV desorption and regeneration of 4～6%, by 0.5BV, concentration, be the washing of 1～2wt% diluted sodium hydroxide solution again, the washing water outlet is incorporated in original solution;
D) the 3rd adsorption column adsorb organic compound, near after saturated, replaces the 3rd adsorption column to come into operation the 4th adsorption column, repeating step b; The 3rd adsorption column after desorption alkali cleaning as standby adsorption column; Desorption alkali washing method are: by adsorb organic compound in described the 3rd adsorption column near saturated polymeric adsorbent with diluted sodium hydroxide solution solution 2～3BV desorption and regeneration of 4～6%, then with 0.5BV1～2% dilute hydrochloric acid washing, the washing water outlet is incorporated in original solution;
E) the described secondary absorption water outlet in step b is carried out to triple effect evaporation, concentrated solution is through cooling, centrifugal recovery sodium chloride salt, and the secondary absorption water outlet of mother liquor and other batches mixes, and the distillation water outlet can be overlapped for former technique, or after aerobic treatment CODc
rBe less than 80mg/L, qualified discharge;
F) after the polymeric adsorbent that loads in adsorption column is used 15 batches, process once with methyl alcohol, the methyl alcohol desorption liquid is through Distillation recovery methyl alcohol, the residue burning disposal;
G) the dense desorption liquid of height of step c gained is dropped in the acidification step in original production process.
H) the dense desorption liquid of the height of steps d gained is dropped in the degradation step in original production process.
Described method, the polymeric adsorbent described in step a adopts ZH01, ZH11, one of ZH124, ZH33; Polymeric adsorbent described in step b is one of domestic CHA111 resin, JX101 resin, NDA150 resin and U.S. AmberLiteXAD-4, XAD-2, XAD-7 resin.
Described method, in step a preferably through chemically modified super high cross-linked adsorbing resin ZH01 resin, super high cross-linked adsorbing resin NDA150 resin preferably in step b.
Described method, while in step c, being desorbing agent with 4～6% dilute hydrochloric acid, desorption temperature is 40～60 ℃, the desorbing agent flow is 0.5～1BV/h.
Described method, while in steps d, being desorbing agent with 4～6% diluted sodium hydroxide solution, desorption temperature is 40～60 ℃, the desorbing agent flow is 0.5～1BV/h.
Described method, while in step f, processing with methyl alcohol, treatment temp is 20～45 ℃, flow is 1～1.5BV/h.
Adopt the inventive method that a kind of o-amino benzoyl acid production process waste water is governed and the organism of its recovery can the direct circulation utilization, the COD of waste water before and after processing
CrFrom about 24000mg/L left and right, be down to below 80mg/L, can reach national grade one discharge standard, reclaim thick sodium chloride salt.Resin is with 4～6% diluted sodium hydroxide solutions or dilute hydrochloric acid desorption and regeneration, desorption liquid drops in the acidification step or degraded in original production process as raw material, do not affect quality product, in waste water, 99% anthranilic acid and phthalic imidine are recycled, and the distillation water outlet can reuse.When administering waste water, realized changing waste into resources.
Embodiment
Below in conjunction with specific embodiment, the present invention is described in detail.
Embodiment 1:
20mL (about 15g, dry weight) NDA150 resin and ZH01 resin are filled in respectively in two adsorption columns that insulation jacket arranged, (Φ 20 * 250mm).
After getting the processing wastewater filtration in 1000mL anthranilic acid production russet, drip 1% sodium hydroxide solution 0.5ml, pH is 7.92, upper prop liquid COD
CrFor 24170mg/L, the o-amino benzoyl acid content is 6160mg/L, phthalic imidine content is 7960mg/L, 35 ± 5 ℃ by 640ml upper prop liquid with the flow of 40mL/h by the ZH01 resin column, the one-level water outlet is faint yellow, phthalic imidine content is 12.2mg/L, and phthalic imidine content is 6014mg/L, COD
CrReduce to 13990mg/L, after dripping 1% dilute hydrochloric acid 0.5ml, pH is 5.08,35 ± 5 ℃ by 400ml upper prop liquid with the flow of 40mL/h by the NDA150 resin column, the secondary absorption water outlet is colourless, the phthalic imidine inspection does not measure, COD
CrReduce to 994mg/L, anthranilic acid is 10.6mg/L, by this water distillation, reclaims thick sodium chloride salt 60.4g.Water outlet can reach national grade one discharge standard after aerobic treatment.
ZH01 resin after absorption carries out desorption and regeneration with the dilute hydrochloric acid solution 40mL that temperature is 55 ± 5 ℃ 6%, and flow is 20mL/h.Resin after desorption and regeneration washs through 1% diluted sodium hydroxide solution solution 10ml.The desorption rate of phthalic imidine is 98.1%.It is centrifugation under 7 rear room temperatures that desorption liquid (40mL) adds 30% sodium hydroxide solution to be neutralized to pH, obtains solid phthalic imidine 3.32g (purity 93.9%).
NDA150 resin after absorption carries out desorption and regeneration with the hydrochloric acid soln 40mL that temperature is 55 ± 5 ℃ 6%, and flow is 20mL/h.Resin after desorption and regeneration washs through 1% hydrochloric acid soln 10ml.The desorption rate of anthranilic acid is 97.8%.Desorption liquid (40mL) adds in 30% sodium hydroxide solution and pH is centrifugation under 5 rear room temperatures, obtains solid anthranilic acid 4.02g (purity 95.7%).
Embodiment 2:
200mL (about 150g, dry weight) NDA150 resin and 300mL (about 225g, dry weight) ZH01 resin are filled in respectively in two adsorption columns that insulation jacket arranged, (Φ 35 * 500mm).
After getting the processing wastewater filtration in 10L anthranilic acid production russet, drip 1% sodium hydroxide solution 5ml, pH is 8.04, upper prop liquid COD
CrFor 23960mg/L, the o-amino benzoyl acid content is 6210mg/L, phthalic imidine content is 8026mg/L, 5 ± 5 ℃ by 6400ml upper prop liquid with the flow of 200mL/h by the ZH01 resin column, the one-level water outlet is faint yellow, phthalic imidine content is 14.7mg/L, and the o-amino benzoyl acid content is 6102mg/L, COD
CrReduce to 14160mg/L, after dripping 1% dilute hydrochloric acid 5ml, pH is 4.98,5 ± 5 ℃ by 6400ml upper prop liquid with the flow of 200mL/h by the NDA150 resin column, the secondary absorption water outlet is colourless, anthranilic acid is 15.5mg/L, the phthalic imidine inspection does not measure, COD
CrReduce to 899mg/L, by this water distillation, reclaim thick sodium chloride salt 758g.Water outlet can reach national grade one discharge standard after aerobic treatment.
ZH01 resin after absorption carries out desorption and regeneration with the dilute hydrochloric acid solution 400mL that temperature is 45 ± 5 ℃ 6%, and flow is 600mL/h.Resin after desorption and regeneration washs through 2% diluted sodium hydroxide solution solution 60ml.The desorption rate of phthalic imidine is 96.2%.It is centrifugation under 7 rear room temperatures that desorption liquid (600mL) adds 30% sodium hydroxide solution to be neutralized to pH, obtains solid phthalic imidine 53.1g (purity 92.8%).
NDA150 resin after absorption carries out desorption and regeneration with the hydrochloric acid soln 400mL that temperature is 45 ± 5 ℃ 6%, and flow is 400mL/h.Resin after desorption and regeneration washs through 2% hydrochloric acid soln 60ml.The desorption rate of anthranilic acid is 95.8%.Desorption liquid (400mL) adds in 30% sodium hydroxide solution and pH is centrifugation under 5 rear room temperatures, obtains solid anthranilic acid 41.1g (purity 92.4%).
Embodiment 3:
Change respectively the ZH01 resin in the embodiment 1 and 2 in embodiment 1 and 2 into FZH11, ZH124, ZH33, the NDA150 resin changes respectively JX101 resin, CHA111 resin, AmberLiteXAD-7, XAD-4, XAD-2 resin into, other operational conditions remain unchanged, except every batch processing volume and yield changed, other results were basic identical.
Should be understood that, for those of ordinary skills, can be improved according to the above description or conversion, and all these improve and conversion all should belong to the protection domain of claims of the present invention.
Claims (6)
1. improvement and the circulation utilization method of an o-amino benzoyl acid production process waste water, is characterized in that, comprises the following steps:
A) waste water is sorrel after processing after filtration, after with 1～2% diluted sodium hydroxide solution, regulating pH and be about 8, at 0～40 ℃, through the first adsorption column, obtains faint yellow transparent one-level absorption effluent, CODc with the flow of 1～2BV/h
r12000～14000mg/L, described the first adsorption column is filled with the Hypercrosslinked polystyrene of chemically modified-divinylbenzene polymeric adsorbent, it is standby that the first adsorption column is arranged in parallel the second adsorption column of the Hypercrosslinked polystyrene that another root is filled with chemically modified equally-divinylbenzene polymeric adsorbent, the first adsorption column and the second adsorption column treatment capacity are 18～20BV/ and criticize, and BV is the volume of adsorption column;
B) after the one-level absorption effluent of the first adsorption column in step a is about to 5 with 1～2% dilute hydrochloric acid adjusting pH, at 0～40 ℃, with the flow process of 1～2BV/h, be filled with the 3rd adsorption column of Hypercrosslinked polystyrene-divinylbenzene polymeric adsorbent, obtain water white secondary absorption water outlet, CODc
r800～1000mg/L; Described the 3rd adsorption column is arranged in parallel another root, and to be filled with equally the 4th adsorption column of Hypercrosslinked polystyrene-divinylbenzene polymeric adsorbent standby, and the 3rd adsorption column and the 4th adsorption column adsorption column treatment capacity are that 30～32BV/ criticizes;
C) the first adsorption column adsorb organic compound is near after saturated, replaces the first adsorption column to come into operation the second adsorption column, repeating step a, the first adsorption column after desorption alkali cleaning as standby adsorption column; Desorption alkali washing method are: by adsorb organic compound in described the first adsorption column near saturated polymeric adsorbent with dilute hydrochloric acid 2～3BV desorption and regeneration of 4～6%, by 0.5BV, concentration, be the washing of 1～2wt% diluted sodium hydroxide solution again, the washing water outlet is incorporated in original solution;
D) the 3rd adsorption column adsorb organic compound, near after saturated, replaces the 3rd adsorption column to come into operation the 4th adsorption column, repeating step b; The 3rd adsorption column after desorption alkali cleaning as standby adsorption column; Desorption alkali washing method are: by adsorb organic compound in described the 3rd adsorption column near saturated polymeric adsorbent with diluted sodium hydroxide solution solution 2～3BV desorption and regeneration of 4～6%, then with 0.5BV1～2% dilute hydrochloric acid washing, the washing water outlet is incorporated in original solution;
E) the described secondary absorption water outlet in step b is carried out to triple effect evaporation, concentrated solution is through cooling, centrifugal recovery sodium chloride salt, and the secondary absorption water outlet of mother liquor and other batches mixes, and the distillation water outlet can be overlapped for former technique, or after aerobic treatment CODc
rBe less than 80mg/L, qualified discharge;
F) after the polymeric adsorbent that loads in adsorption column is used 15 batches, process once with methyl alcohol, the methyl alcohol desorption liquid is through Distillation recovery methyl alcohol, the residue burning disposal;
G) the dense desorption liquid of height of step c gained is dropped in the acidification step in original production process;
H) the dense desorption liquid of the height of steps d gained is dropped in the degradation step in original production process.
2. method according to claim 1, is characterized in that, the polymeric adsorbent described in step a adopts ZH01, ZH11, one of ZH124, ZH33; Polymeric adsorbent described in step b is one of domestic CHA111 resin, JX101 resin, NDA150 resin and U.S. AmberLiteXAD-4, XAD-2, XAD-7 resin.
3. method according to claim 2, is characterized in that, in step a preferably through chemically modified super high cross-linked adsorbing resin ZH01 resin, super high cross-linked adsorbing resin NDA150 resin preferably in step b.
4. method according to claim 1, is characterized in that, while in step c, being desorbing agent with 4～6% dilute hydrochloric acid, desorption temperature is 40～60 ℃, and the desorbing agent flow is 0.5～1BV/h.
5. method according to claim 1, is characterized in that, while in steps d, being desorbing agent with 4～6% diluted sodium hydroxide solution, desorption temperature is 40～60 ℃, and the desorbing agent flow is 0.5～1BV/h.
6. method according to claim 1, is characterized in that, while in step f, processing with methyl alcohol, treatment temp is 20～45 ℃, and flow is 1～1.5BV/h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310335163.0A CN103408177B (en) | 2013-08-02 | 2013-08-02 | Method for treating and recycling waste water in anthranilic acid production technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310335163.0A CN103408177B (en) | 2013-08-02 | 2013-08-02 | Method for treating and recycling waste water in anthranilic acid production technology |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103408177A true CN103408177A (en) | 2013-11-27 |
| CN103408177B CN103408177B (en) | 2015-04-08 |
Family
ID=49601237
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310335163.0A Expired - Fee Related CN103408177B (en) | 2013-08-02 | 2013-08-02 | Method for treating and recycling waste water in anthranilic acid production technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103408177B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104986908A (en) * | 2015-06-29 | 2015-10-21 | 盐城师范学院 | Method for treating and recycling process waste water generated during production of 1,2-Benzisothiazolin-3-One |
| CN105110537A (en) * | 2015-08-21 | 2015-12-02 | 山西青山化工有限公司 | DSD acid oxidation waste water treatment and resource recycling method |
| CN105330082A (en) * | 2015-12-09 | 2016-02-17 | 南京环保产业创新中心有限公司 | Treatment method for 4-methyl-2-benzothiazolehydrazine production wastewater |
| CN109319876A (en) * | 2018-12-24 | 2019-02-12 | 安徽国星生物化学有限公司 | A kind of resin adsorption method processing acetic acid waster water process |
| CN110683720A (en) * | 2019-11-21 | 2020-01-14 | 重庆化医长寿化工集团有限公司 | Method for treating sulfanilamide mother liquor |
| US10968466B2 (en) | 2016-12-20 | 2021-04-06 | Covestro Deutschland Ag | Process for preparing aminobenzoic acid or an aminobenzoic acid conversion product |
| CN113277590A (en) * | 2021-02-04 | 2021-08-20 | 中化河北有限公司 | Method for treating 1, 3-cyclohexanedione production wastewater by using adsorption resin |
| CN114804280A (en) * | 2022-05-26 | 2022-07-29 | 西安海润新材料有限公司 | Method for recovering acid, thioxanthone and derivatives thereof from waste acid |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003305465A (en) * | 2002-04-15 | 2003-10-28 | Mitsubishi Electric Corp | System for making pure water and method for monitoring water quality |
| CN1923799A (en) * | 2006-09-12 | 2007-03-07 | 南京大学 | Method of recovering o-aminobenzoic acid from mother liquid or waste water |
| CN102190590A (en) * | 2011-03-25 | 2011-09-21 | 天津市鑫卫化工有限责任公司 | Method for recovering anthranilic acid from mother liquor waste water |
-
2013
- 2013-08-02 CN CN201310335163.0A patent/CN103408177B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003305465A (en) * | 2002-04-15 | 2003-10-28 | Mitsubishi Electric Corp | System for making pure water and method for monitoring water quality |
| CN1923799A (en) * | 2006-09-12 | 2007-03-07 | 南京大学 | Method of recovering o-aminobenzoic acid from mother liquid or waste water |
| CN102190590A (en) * | 2011-03-25 | 2011-09-21 | 天津市鑫卫化工有限责任公司 | Method for recovering anthranilic acid from mother liquor waste water |
Non-Patent Citations (1)
| Title |
|---|
| 王海玲等，: ""对氨基苯甲酸生产废水的树脂吸附预处理"", 《南京工业大学学报》 * |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104986908A (en) * | 2015-06-29 | 2015-10-21 | 盐城师范学院 | Method for treating and recycling process waste water generated during production of 1,2-Benzisothiazolin-3-One |
| CN105110537A (en) * | 2015-08-21 | 2015-12-02 | 山西青山化工有限公司 | DSD acid oxidation waste water treatment and resource recycling method |
| CN105330082A (en) * | 2015-12-09 | 2016-02-17 | 南京环保产业创新中心有限公司 | Treatment method for 4-methyl-2-benzothiazolehydrazine production wastewater |
| US10968466B2 (en) | 2016-12-20 | 2021-04-06 | Covestro Deutschland Ag | Process for preparing aminobenzoic acid or an aminobenzoic acid conversion product |
| CN109319876A (en) * | 2018-12-24 | 2019-02-12 | 安徽国星生物化学有限公司 | A kind of resin adsorption method processing acetic acid waster water process |
| CN110683720A (en) * | 2019-11-21 | 2020-01-14 | 重庆化医长寿化工集团有限公司 | Method for treating sulfanilamide mother liquor |
| CN113277590A (en) * | 2021-02-04 | 2021-08-20 | 中化河北有限公司 | Method for treating 1, 3-cyclohexanedione production wastewater by using adsorption resin |
| CN114804280A (en) * | 2022-05-26 | 2022-07-29 | 西安海润新材料有限公司 | Method for recovering acid, thioxanthone and derivatives thereof from waste acid |
| CN114804280B (en) * | 2022-05-26 | 2024-06-11 | 西安海润新材料有限公司 | Method for recovering acid and thioxanthone and derivatives thereof from waste acid |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103408177B (en) | 2015-04-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103408177B (en) | Method for treating and recycling waste water in anthranilic acid production technology | |
| CN101244877B (en) | Treatment for wastewater of technique for producing spaston and cyclic utilization method for recycled organic matter | |
| CN104986908A (en) | Method for treating and recycling process waste water generated during production of 1,2-Benzisothiazolin-3-One | |
| CN102417162B (en) | Recycling method of hydrochloric acid-acetic acid waste liquid | |
| CN105036222A (en) | High-salinity wastewater recovery treatment method | |
| CN104591464A (en) | Recycling method of high-salinity wastewater | |
| CN101798154A (en) | Method for processing wastewater produced in saponification cyclization step in epoxy chloropropane production method | |
| CN102730721A (en) | Recovering method of by-product sodium chloride in polyphenylene sulfide production | |
| CN106986490A (en) | A kind of recovery processing technique and device of carboxylate industrial production wastewater | |
| CN102126777B (en) | Treatment method of phenol sodium salt waste water | |
| CN103977773A (en) | Preparation method and application of eichhornia crassipes cellulose xanthate calcium salt | |
| CN103880211A (en) | Process for resourceful treatment of high-salt wastewater containing magnesium | |
| CN106397180B (en) | Aspirin raffinate treatment process | |
| CN107311254A (en) | A kind of resource utilization method of thiram waste water | |
| CN111003745A (en) | Method for recycling acetic acid wastewater by utilizing adsorption method resources | |
| CN104628587B (en) | A kind of amoxicillin of reclaiming produces the method for D-pHPG in waste liquid | |
| CN104876245A (en) | Method for separating sodium chloride and calcium chloride in alkali preparation waste solution by crystallization | |
| CN100486903C (en) | Treatment for waste water of benzidine production by two-section adsorbing method an d resource recovery method | |
| CN211620237U (en) | Device for extracting bromine from tetrabromobisphenol A wastewater | |
| CN103012186A (en) | Method for recycling paracetamol from refined mother liquor by using adsorption resin | |
| CN101428926A (en) | Adsorption-evaporation integrated non-waste discharge treatment method for phloroglucine wastewater | |
| CN106277706A (en) | A kind of deeply dehydrating sludge conditioner | |
| CN101284775B (en) | Process for reclaiming 2-keto-L-gulonate by salting out method | |
| CN110922320B (en) | Method for extracting methyl isobutyl ketone and sodium p-toluenesulfonate | |
| CN207537375U (en) | A kind of cyanoacetic acid isolates and purifies device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| DD01 | Delivery of document by public notice |
Addressee: Yancheng Normal College Document name: Notification to Pay the Fees |
|
| DD01 | Delivery of document by public notice | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150408 Termination date: 20180802 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |