CN102329048A - Method for treating wastewater produced during chemical synthesis of vitamin B6 - Google Patents
Method for treating wastewater produced during chemical synthesis of vitamin B6 Download PDFInfo
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- CN102329048A CN102329048A CN201110229203A CN201110229203A CN102329048A CN 102329048 A CN102329048 A CN 102329048A CN 201110229203 A CN201110229203 A CN 201110229203A CN 201110229203 A CN201110229203 A CN 201110229203A CN 102329048 A CN102329048 A CN 102329048A
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- treatment
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- waste water
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Abstract
The invention provides a method for treating wastewater produced during chemical synthesis of vitamin B6, which comprises the following steps that: A) the wastewater is subject to three-effect pressure-reducing evaporator desalting - iron carbon micro electrolysis oxidation treatment; B) the wastewater enters an upflow anaerobic sludge blanket (UASB) reactor for anaerobic biochemical treatment; and C) the wastewater enters a jet aeration basin for aerobic biochemical treatment, sludge and water are separated through a sedimentation basin and then supernatant liquid which satisfies standards is discharged. Since a multi-effect evaporation - iron cabin micro electrolysis - UASB - jet aerator process is designed to treat the wastewater produced during the production of the vitamin B6, the process is simple, the treatment effect is good, the method is suitable for the treatment of the wastewater produced during the production of the vitamin B6, and the chemical oxygen demand (COD), the chromaticity and other indexes of the treated wastewater satisfy the Discharge Standards of Water Pollutants for Pharmaceutical Industry - Chemical Synthesis Products Category (GB21904-2008).
Description
Technical field
The present invention relates to the treatment process of medical chemistry synthetic wastewater, particularly relate to the chemosynthesis vitamins B
6Wastewater treatment method.
Background technology
The general Cai Yong of Guang oxazole chemical synthesis is produced vitamins B both at home and abroad
6, building-up process is complicated, and its key step is that L-Ala prepares N-ethoxalyl alanine ethyl ester with oxalic acid, the synchronous esterification of oxalic acid diethyl ester; The latter makes synthetic 4-methyl-5-Yi Yang Ji oxazole through cyclization, basic hydrolysis, acidifying, decarboxylation in POCl3, triethylamine, toluene system; After Diels-Alder, aromizing, hydrolysis, make vitamins B with n-propyl seven rings again
6Thisly make the coloured machine group and the inorganic salinity of a large amount of difficult degradations get into factory effluent, brought great difficulty to wastewater treatment through repeatedly condensation, hydrolysis, acidifying synthesis technique.
Vitamins B
6Factory effluent organic cod concentration is generally 5000～50000mg/L, and BOD5 is 1000～4200mg/L, saltiness 5～12%.Contain organic substances such as being difficult to biodegradable benzene, toluene, ester in a large number in the waste water; And salinity (like sodium-chlor, sodium phosphate etc.) concentration is high; Colour difference, biodegradability is poor, adopts the high and low concentration waste water of traditional waste water treatment process requirement pre-treatment to mix; So just increase a large amount of water, very traditional technology is administered vitamins B simultaneously
6The factory effluent difficulty reaches emission standard.
Summary of the invention
The present invention is directed to vitamins B
6The characteristics of factory effluent provide a kind of method of wastewater treatment, and the rate of removing of pollutents such as this method salinity, COD, colourity is higher, and the waste water after the processing can reach national specified discharge standard.
The present invention provides a kind of chemosynthesis vitamins B
6Wastewater treatment method comprises the steps:
A waste water carries out triple effect decompression evaporator desalination-iron-carbon micro-electrolysis oxidative treatment,
B gets into the UASB anaerobic reactor and carries out the anaerobic biological processing,
C gets into the jet-flow aeration pond and carries out aerobic biochemical processing, supernatant qualified discharge after the settling tank mud-water separation.
Iron-carbon micro-electrolysis oxidation, the waste water residence time in the pond is 1.0～4.0 hours, 20～35 ℃ of temperature, and the pH value is controlled at 5.0～6.5, iron-carbon ratio (volume ratio) 1:1～2:1.
UASB anaerobic reactor hydraulic detention time is 15～24 hours, 20～35 ℃ of temperature.
The jet aerator aeration is cultivated, hydraulic detention time 24 hours.
The water outlet that aerobic biochemical is handled gets into settling tank and carries out mud-water separation, and a part of mud in the settling tank is back to the aeration tank, and reflux ratio 0.7 enters network of drains after supernatant is up to standard.
Vitamins B
6Factory effluent contains a large amount of inorganic salt, like sodium-chlor, sodium phosphate etc.Be difficult to biodegradable characteristics in view of waste water contains a large amount of salts,, remove the salinity in the waste water, reduce organic concentration, improve the biodegradability of waste water so this technology is at first carried out triple effect reduction vaporization desalination pre-treatment to waste water.The triple effect decompression evaporator, the organism that is partially soluble in water is understood and inorganic salt crystallization together.
Contain part through the pretreated waste water of desalination and be difficult to biodegradable organism; Like benzene, toluene, organic ester etc., after the iron-carbon micro-electrolysis oxidation, oxidation-reduction reaction takes place under the effect of nascent state Fe with hydrochloric acid adjust pH 5.0～6.5; Destroy its chemical structure; Make the color development of coloring matter or help organic macromolecule group generation chain-scission degradations such as look, improved wastewater biodegradability, reduced the colourity of waste water.Owing to produce the Fe (OH) of nascent state in the reaction process
2And Fe (OH)
3Generally all have positive charge; Have extremely strong surfactivity and adsorptive power; Have deposition, flocculation and adsorption; Can adsorb effectively, the suspension in parcel and the copolymerization deposition waste water or the molecule and the organic polymer of colloidal attitude, can further reduce the colourity of waste water, remove the part organic pollution materials simultaneously waste water be purified.
Iron-carbon micro-electrolysis of the present invention is handled the colourity that the waste water worker further reduces waste water, removes the part organic pollution materials simultaneously waste water is purified.Iron-carbon micro-electrolysis oxidation, the waste water residence time in the pond is 1.0-4.0 hour, and temperature 20-35 ℃, the pH value is controlled at 5.0～6.5, iron-carbon ratio (volume ratio) 1:1～2:1.The skill principle: micro-electrolysis method is to utilize Principles of Metal Erosion, forms the good process that galvanic cell is handled waste water.It is under cold situation, utilizes the micro-electrolysis material self that is filled in the waste water to produce high low potential difference waste water is carried out electrolysis treatment, to reach the purpose of degradable organic pollutant.When sewage passed through the filler of iron content and carbon, iron became anode, and carbon becomes negative electrode, and had little electric current to flow, and had formed thousands upon thousands small batteries, produced " interior electrolysis ", corroded, just redox reaction:
Anodic reaction: Fe-2e → Fe
2+E
0(Fe
2+/ Fe)=-0.44V
Cathodic reaction: 2H
++ 2e → H
2↑ E
0(H
+/ H
2)=0.00V
When oxygen: O
2+ 4H
++ 4e → 2H
2O E0 (O
2)=1.23V
O
2+2H
2O+4e→40H
- E0(O
2/OH
-)=0.40V
Following reaction further takes place in Fe in electrolyte solution:
4Fe
2+?+?80H→4Fe(OH)
2?
4Fe
2+?+?80H?+?O
2 +?2H
2O?→4Fe(OH)
3
In the environment of neutrality or slant acidity, fine electrolyser itself and the nascent state [H], the Fe that produce
2+Have strong reducing property, can with the organic pollutant generation oxidation-reduction reaction of difficult degradation in the waste water, destroy its chemical structure; Such as color development that can destroy the coloring matter in the waste water or auxochrome group, even chain rupture, can decolour; Reduce COD; Improve biodegradability, all right oxidized metal ion reduces its toxicity.Gac is except that participating in also having the effect of reduction absorption the electrode reaction as the negative electrode of galvanic cell.In addition, owing to have electrical effect around the electrode of battery, charged colloidal particles and impurity attach collection, cohesion through the effect of electrostatic attraction and surface energy in the waste water, and waste water is purified.
Waste water after the iron-carbon micro-electrolysis oxidation gets into the UASB anaerobic reactor; Utilizing hydrolytic bacteria, fermenting bacterial and acid-producing bacteria (comprise and produce the hydrogen acetogen), under anaerobic, is small molecules, dissolved organic matter with the macromole of complicacy, insoluble hydrolysis of organic matter; When COD of sewage concentration is further reduced; Effectively improve the biodegradability of sewage,, improve the efficient of biochemical reaction the load that reduces the postorder biochemical reaction stage greatly.
The hydraulic detention time of UASB anaerobic reactor is 15～24 hours, 20～35 ℃ of temperature.
The waste water of handling through anaerobic biological gets into the aerobic biochemical processing, and aerobic biochemical system is cultivated for the jet aerator aeration, utilizes the effects such as metabolism of aerobic bacteria, further reduces organism.Water outlet after aerobic treatment gets into settling tank and carries out mud-water separation, and a part of mud in the settling tank is back to the aeration tank, and reflux ratio 0.7 enters network of drains after supernatant is up to standard.Traditional aeration mode at present still usefulness be blast aeration, but aeration head easy blocking, damage cause aeration decrease in efficiency, aeration inhomogeneous, directly have influence on the treatment effect of Sewage treatment systems.
Jet aerator utilizes the negative inspiratory pressure principle; Adopt heavy caliber water conservancy shower nozzle; Under water pump drives, self produce the negative pressure absorbing air, air gets into the air water reaction chamber simultaneously with the current that pass through at a high speed, and oxygen is dissolved in the water body rapidly through the high pressure principle in the air water reaction chamber.No moving part, no consumable accessory does not have the possibility of stopping up.
Beneficial effect of the present invention: the present invention has designed multiple-effect evaporation-iron-carbon micro-electrolysis-upflow anaerobic sludge blanket process UASB-jet aerator art breading vitamins B
6Factory effluent, technology is simple, and treatment effect is good, is applicable to vitamins B
6Production wastewater treatment, index concentration such as the waste water COD after the processing, colourity reach " chemosynthesis class pharmaceutical industry pollution discharge standard " (GB21904-2008).Below be the waste water leading indicator COD the treatment stage of passing through each, the content of colourity:
Embodiment
Embodiment 1
Vitamins B
6COD concentration in the factory effluent is 35000mg/L, saltiness 8.0%.At first get into the triple effect decompression evaporator and carry out evaporation concentration, evaporation back water of condensation COD concentration is 5500mg/L, saltiness 0.6%, and colourity is 35.Crystallisate cooling back spinning after the evaporation concentration obtains white sodium-chlor and sodium phosphate crystallization.
Water of condensation after the evaporation gets into the iron-carbon micro-electrolysis oxidation pond, with hydrochloric acid adjust pH 5.5, and iron-carbon micro-electrolysis oxidation, oxidization time 1.9 hours, 28 ℃ of temperature, iron-carbon ratio (volume ratio) 1.5:1.Waste water COD concentration behind little electrolytic oxidation is 3600mg/L, and colourity is 9.
Supernatant behind little electrolytic oxidation gets into the UASB anaerobic reation pool, and waste water is 19 hours in the residence time of anaerobic stages, 25 ℃ of temperature, and the waste water COD concentration after anaerobic biological treatment is 730mg/L, colourity is 8.Sediment behind little electrolytic oxidation is through filter press, gained waste residue burning disposal.
Water behind the anaerobic biological gets into the aeration tank, adopts the jet aerator aeration to cultivate hydraulic detention time 24 hours.Water outlet after aerobic treatment gets into settling tank and carries out mud-water separation, and a part of mud in the settling tank is back to the aeration tank, and reflux ratio 0.7 enters network of drains after supernatant is up to standard.COD concentration and colourity in the waste water after the anaerobic biological system handles are respectively 101mg/L and 8, reach " chemosynthesis class pharmaceutical industry pollution discharge standard " (GB21904-2008).
Embodiment 2
Vitamins B
6COD concentration in the factory effluent is 50000mg/L, saltiness 5.0%.At first get into the triple effect decompression evaporator and carry out evaporation concentration, evaporation back water of condensation COD concentration is 5000mg/L, saltiness 0.5%, and colourity is 30.Crystallisate cooling back spinning after the evaporation concentration obtains white sodium-chlor and sodium phosphate crystallization.
Water of condensation after the evaporation gets into the iron-carbon micro-electrolysis oxidation pond, with hydrochloric acid adjust pH 5.0, and iron-carbon micro-electrolysis oxidation, oxidization time 1.0 hours, 25 ℃ of temperature, iron-carbon ratio (volume ratio) 1:1.Waste water COD concentration behind little electrolytic oxidation is 3500mg/L, and colourity is 8.
Supernatant behind little electrolytic oxidation gets into the UASB anaerobic reation pool, and waste water is 15 hours in the residence time of anaerobic stages, 25 ℃ of temperature, and the waste water COD concentration after anaerobic biological treatment is 700mg/L, colourity is 7.Sediment behind little electrolytic oxidation is through filter press, gained waste residue burning disposal.
Water behind the anaerobic biological gets into the aeration tank, adopts the jet aerator aeration to cultivate hydraulic detention time 24 hours.Water outlet after aerobic treatment gets into settling tank and carries out mud-water separation, and a part of mud in the settling tank is back to the aeration tank, and reflux ratio 0.7 enters network of drains after supernatant is up to standard.COD concentration and colourity in the waste water after the anaerobic biological system handles are respectively 95mg/L and 7, reach " chemosynthesis class pharmaceutical industry pollution discharge standard " (GB21904-2008).
Embodiment 3
Vitamins B
6COD concentration in the factory effluent is 42000mg/L, saltiness 12.0%.At first get into the triple effect decompression evaporator and carry out evaporation concentration, evaporation back water of condensation COD concentration is 6000mg/L, saltiness 0.7%, and colourity is 40.Crystallisate cooling back spinning after the evaporation concentration obtains white sodium-chlor and sodium phosphate crystallization.
Water of condensation after the evaporation gets into the iron-carbon micro-electrolysis oxidation pond, with hydrochloric acid adjust pH 6.0, and iron-carbon micro-electrolysis oxidation, oxidization time 4 hours, 30 ℃ of temperature, iron-carbon ratio (volume ratio) 2:1.Waste water COD concentration behind little electrolytic oxidation is 3692mg/L, and colourity is 9.
Supernatant behind little electrolytic oxidation gets into the UASB anaerobic reation pool, and waste water is 24 hours in the residence time of anaerobic stages, 35 ℃ of temperature, and the waste water COD concentration after anaerobic biological treatment is 750mg/L, colourity is 9.Sediment behind little electrolytic oxidation is through filter press, gained waste residue burning disposal.
Water behind the anaerobic biological gets into the aeration tank, adopts the jet aerator aeration to cultivate hydraulic detention time 24 hours.Water outlet after aerobic treatment gets into settling tank and carries out mud-water separation, and a part of mud in the settling tank is back to the aeration tank, and reflux ratio 0.7 enters network of drains after supernatant is up to standard.COD concentration and colourity in the waste water after the anaerobic biological system handles are respectively 105mg/L and 9, reach " chemosynthesis class pharmaceutical industry pollution discharge standard " (GB21904-2008).
Claims (5)
1. chemosynthesis vitamins B
6Wastewater treatment method comprises the steps:
A waste water carries out triple effect decompression evaporator desalination-iron-carbon micro-electrolysis oxidative treatment,
B gets into the UASB anaerobic reactor and carries out the anaerobic biological processing,
C gets into the jet aerator pond and carries out aerobic biochemical processing, supernatant qualified discharge after the settling tank mud-water separation.
2. treatment process as claimed in claim 1 is characterized in that described iron-carbon micro-electrolysis oxidation, and waste water residence time in the pond is 1.0～4.0 hours, 20～35 ℃ of temperature, and the pH value is controlled at 5.0～6.5, iron carbon volume ratio 1:1～2:1.
3. according to claim 1 or claim 2 treatment process is characterized in that described UASB anaerobic reactor hydraulic detention time is 15～24 hours, 20～35 ℃ of temperature.
4. according to claim 1 or claim 2 treatment process is characterized in that settling tank that described aerobic biochemical is handled comprises that the jet aerator aeration cultivates hydraulic detention time 24 hours.
5. treatment process as claimed in claim 4 is characterized in that the water outlet entering settling tank that described aerobic biochemical is handled carries out mud-water separation, and a part of mud in the settling tank is back to the aeration tank, and reflux ratio 0.7 enters network of drains after supernatant is up to standard.
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|---|---|---|---|
| CN201110229203A CN102329048B (en) | 2011-08-11 | 2011-08-11 | Method for treating wastewater produced during chemical synthesis of vitamin B6 |
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| CN102329048B CN102329048B (en) | 2012-10-03 |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102826721A (en) * | 2012-09-20 | 2012-12-19 | 艾特克控股集团有限公司 | Method for treating wastewater being generated during vitamin C production |
| CN103833180A (en) * | 2013-11-19 | 2014-06-04 | 华中药业股份有限公司 | Method for treating waste water obtained during synthesis of vitamin B6 through oxazole method |
| CN106430793A (en) * | 2016-11-24 | 2017-02-22 | 江苏九天高科技股份有限公司 | Zero discharging method and device for vitamin B2 production waste water |
| CN109231664A (en) * | 2018-09-19 | 2019-01-18 | 河南慧锦药业有限公司 | A kind of comprehensive processing technique of high salinity and high COD pharmacy waste water |
| CN111499101A (en) * | 2020-04-27 | 2020-08-07 | 中南林业科技大学 | Complicated organic sewage step purifier |
| CN114262121A (en) * | 2021-12-22 | 2022-04-01 | 新疆新环工程技术有限公司 | Process for treating wastewater of fine chemical and pharmaceutical intermediate |
| CN114315041A (en) * | 2021-12-31 | 2022-04-12 | 宁夏万博生物科技有限公司 | Process system for efficiently treating wastewater |
| CN114262121B (en) * | 2021-12-22 | 2024-04-16 | 新疆新环工程技术有限公司 | Process for treating fine chemical medical intermediate wastewater |
Citations (1)
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|---|---|---|---|---|
| CN101973659A (en) * | 2010-10-12 | 2011-02-16 | 北京科技大学 | Device and method for refining waste water by treating vitamin B12 by means of co-use of micro-electrolysis and physicochemical method |
-
2011
- 2011-08-11 CN CN201110229203A patent/CN102329048B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101973659A (en) * | 2010-10-12 | 2011-02-16 | 北京科技大学 | Device and method for refining waste water by treating vitamin B12 by means of co-use of micro-electrolysis and physicochemical method |
Non-Patent Citations (1)
| Title |
|---|
| 《水处理技术》 20100131 郗金娥等 "蒸发/UASB/生化/高级氧化处理高盐难生化制药废水" 第128-131页 1-5 第36卷, 第1期 * |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102826721A (en) * | 2012-09-20 | 2012-12-19 | 艾特克控股集团有限公司 | Method for treating wastewater being generated during vitamin C production |
| CN103833180A (en) * | 2013-11-19 | 2014-06-04 | 华中药业股份有限公司 | Method for treating waste water obtained during synthesis of vitamin B6 through oxazole method |
| CN103833180B (en) * | 2013-11-19 | 2015-09-30 | 华中药业股份有限公司 | The treatment process of Yi Zhong oxazole method synthesise vitamins B6 waste water |
| CN106430793A (en) * | 2016-11-24 | 2017-02-22 | 江苏九天高科技股份有限公司 | Zero discharging method and device for vitamin B2 production waste water |
| CN109231664A (en) * | 2018-09-19 | 2019-01-18 | 河南慧锦药业有限公司 | A kind of comprehensive processing technique of high salinity and high COD pharmacy waste water |
| CN111499101A (en) * | 2020-04-27 | 2020-08-07 | 中南林业科技大学 | Complicated organic sewage step purifier |
| CN111499101B (en) * | 2020-04-27 | 2021-08-24 | 中南林业科技大学 | Organic sewage step purifier |
| CN114262121A (en) * | 2021-12-22 | 2022-04-01 | 新疆新环工程技术有限公司 | Process for treating wastewater of fine chemical and pharmaceutical intermediate |
| CN114262121B (en) * | 2021-12-22 | 2024-04-16 | 新疆新环工程技术有限公司 | Process for treating fine chemical medical intermediate wastewater |
| CN114315041A (en) * | 2021-12-31 | 2022-04-12 | 宁夏万博生物科技有限公司 | Process system for efficiently treating wastewater |
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|---|---|
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